Method for producing decolorized internal olefin sulfonate composition

Abstract

The present invention provides a method for producing a decolorized internal olefin sulfonate composition which has a weak smell and good storage stability. A method for producing a decolorized internal olefin sulfonate composition according to the present invention includes a decolorizing step (A) for performing: an adjustment step (a1) for adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition that contains an internal olefin sulfonate is present; and a mixing step (a2) for mixing a decolorizing agent with the internal olefin sulfonate composition present in the system. The adjustment step (a1) is a step for adjusting the concentration of the alkali compound in the decolorizing step (A) so that the concentration of the alkali compound after mixing the decolorizing agent with the internal olefin sulfonate composition present in the system is 0.004 mmol to 0.26 mmol inclusive with respect to 1 g of the internal olefin sulfonate.

Description

Method for producing bleaching internal olefin sulfonate composition

[0001] The present invention relates to a method for producing a bleaching internal olefin sulfonate composition.

[0002]

[0003] Conventionally, anionic surfactants, particularly alkyl sulfates and polyoxyalkylene alkyl ether sulfates, have been widely used as cleaning ingredients for household and industrial use due to their excellent detergency and foaming power. Furthermore, as one type of anionic surfactant, olefin sulfonates, particularly internal olefin sulfonates obtained from an internal olefin having a double bond not at the terminal but inside the olefin, have been reported.

[0003] The internal olefin sulfonate is generally obtained by reacting an internal olefin with sulfur trioxide to sulfonate it, neutralizing the resulting sulfonated product, and then hydrolyzing it.

[0004] The internal olefin sulfonate is usually obtained as an aqueous solution containing the internal olefin sulfonate (internal olefin sulfonate composition). However, the internal olefin sulfonate composition is colored, and such coloration is inconvenient when used as a cleaning agent.

[0005] Regarding the decolorization of an internal olefin sulfonate composition, for example, Patent Document 1 proposes a technique of decolorizing an internal olefin sulfonate composition with hydrogen peroxide.

[0006] JP 2015-178467 A

[0007] However, it has been newly discovered that an internal olefin sulfonate composition bleached with hydrogen peroxide may have a strong odor or may have reduced storage stability.

[0008] The problems (odor and storage stability) of internal olefin sulfonate compositions bleached with a bleaching agent such as hydrogen peroxide have not been sufficiently investigated in the past, and the present invention provides a method for producing a bleached internal olefin sulfonate composition that has a weak odor and good storage stability.

[0009] The present invention relates to a method for producing a bleached internal olefin sulfonate composition, the method comprising: a bleaching step (A) of performing, in a system where an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjusting step (a1) of adjusting the concentration of an alkali compound in the system; and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, wherein the adjusting step (a1) is a step of adjusting the concentration of the alkali compound in the bleaching step (A) so that the concentration of the alkali compound after mixing the bleaching agent with the internal olefin sulfonate composition present in the system is 0.004 mmol or more and 0.26 mmol or less per 1 g of the internal olefin sulfonate.

[0010] According to the manufacturing method of the present invention, by adjusting the concentration of the alkaline compound in the system to a specific range when mixing the bleaching agent and the internal olefin sulfonate composition, a bleached internal olefin sulfonate composition that exhibits good color fading, a weak odor, and good storage stability can be obtained.

[0011] The present invention will be described in detail below.

[0012] The method for producing a bleached internal olefin sulfonate composition of the present invention includes a bleaching step (A) of performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjusting step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, wherein the adjusting step (a1) is a step of adjusting the concentration of the alkali compound in the bleaching step (A) so that the concentration of the alkali compound after mixing the bleaching agent with the internal olefin sulfonate composition present in the system is 0.004 mmol or more and 0.26 mmol or less per 1 g of the internal olefin sulfonate.

[0013] In the present invention, internal olefin sulfonate is a sulfonate obtained by sulfonating, neutralizing, and hydrolyzing an internal olefin. That is, when an internal olefin is sulfonated, it is converted into β-sultone, γ-sultone, and olefin sulfonic acid. These are further converted into hydroxysulfonate and olefin sulfonate in the neutralization and hydrolysis steps. The obtained product is mainly a mixture of these. In the present invention, these products and their mixture are collectively referred to as internal olefin sulfonate.

[0014] The internal olefin sulfonate composition is an aqueous solution containing the internal olefin sulfonate, and is obtained through the following sulfonation step, neutralization step, and optional hydrolysis step.

[0015] <Sulfonation Step> The sulfonation step is a step in which an internal olefin is reacted with sulfur trioxide gas to obtain a sulfonated product.

[0016] An internal olefin is an olefin having a double bond at a position other than the terminal of the olefin chain, i.e., an olefin having a double bond at position 2 or higher of the carbon chain. The internal olefin may contain a trace amount of so-called α-olefin, in which the double bond is at position 1 of the carbon chain.

[0017] From the viewpoint of cleaning performance when the internal olefin sulfonate is used as a cleaning agent, the number of carbon atoms of the internal olefin is preferably 10 or more, more preferably 12 or more, even more preferably 14 or more, and still more preferably 16 or more, and is preferably 22 or less, more preferably 18 or less.

[0018] The internal olefin may be used alone or in combination of two or more. The internal olefin is at least one selected from the group consisting of an internal olefin having 16 carbon atoms and an internal olefin having 18 carbon atoms, from the viewpoint of cleaning performance when the internal olefin sulfonate is used in a cleaning agent. When two or more internal olefins are used in combination, an internal olefin having 16 carbon atoms and an internal olefin having 18 carbon atoms are preferably used in combination, from the viewpoint of cleaning performance when the internal olefin sulfonate is used in a cleaning agent.

[0019] The internal olefin can be produced by a known method, for example, the method described in WO 2011 / 052732.

[0020] The sulfur trioxide gas is not particularly limited, but is preferably diluted with air, nitrogen, or another inert gas. The concentration of sulfur trioxide gas is preferably 0.5% by volume or more, more preferably 1.0% by volume or more, from the viewpoint of reducing the reactor volume by efficiently reacting the internal olefin with the sulfur trioxide gas and thereby improving economic efficiency, and is preferably 10% by volume or less, more preferably 6.0% by volume or less, from the viewpoint of obtaining a sulfonated product with a good color by appropriately controlling the reaction rate.

[0021] The amount of sulfur trioxide gas used is preferably 0.8 mol or more, more preferably 0.9 mol or more, and even more preferably 0.95 mol or more, per mol of internal olefin from the viewpoint of improving the yield of the sulfonated product, and is preferably 1.2 mol or less, more preferably 1.10 mol or less, and even more preferably 1.05 mol or less, from the viewpoint of improving economic efficiency and suppressing coloration of the sulfonated product.

[0022] The sulfonation reactor used in the sulfonation step is not particularly limited, but is preferably equipped with an external jacket from the viewpoint of controlling the reaction temperature and obtaining a high-quality sulfonated product. Furthermore, from the viewpoint of efficiently reacting a liquid internal olefin with gaseous sulfur trioxide, a falling film sulfonation reactor is preferred, in which the internal olefin is allowed to flow downward in the form of a thin film and react with sulfur trioxide. Examples of such sulfonation reactors include the reactors described in JP-A-11-315061, JP-B-49-48409, IT-1248079A, and U.S. Pat. No. 3,257,175A.

[0023] The treatment temperature in the sulfonation step is preferably 0° C. or higher from the viewpoint of preventing solidification of sulfur trioxide and the sulfonated product, and is preferably 50° C. or lower from the viewpoint of suppressing coloration of the sulfonated product.

[0024] Since the sulfonation reaction is an exothermic reaction, it is preferable to provide an external jacket for the sulfonation reactor and pass cooling water through it for cooling. The temperature of the cooling water passed through the external jacket of the sulfonation reactor is preferably 0°C or higher from the viewpoint of improving the reaction rate, and is preferably 30°C or lower, more preferably 20°C or lower, from the viewpoint of suppressing side reactions and reducing impurities such as internal olefins and inorganic salts in the finally obtained internal olefin sulfonate.

[0025] In order to control the reaction rate and prevent deterioration in the quality of the sulfonated product, an inert gas may be introduced between the internal olefin and sulfur trioxide gas. Examples of such a reactor include the reactors described in JP-A-11-315061 and JP-B-49-48409.

[0026] The reaction rate of the internal olefin in the sulfonation reaction is preferably 95% or more, more preferably 96% or more, and even more preferably 97% or more, from the viewpoint of improving the yield of the sulfonated product, and is preferably 99.8% or less, from the viewpoint of suppressing coloration of the sulfonated product due to excess sulfur trioxide.

[0027] <Neutralization Step> The neutralization step is a step of neutralizing the sulfonated product obtained in the sulfonation step to obtain a neutralized product.

[0028] The alkali compound used for neutralization may be either an inorganic alkali compound or an organic alkali compound. Examples of inorganic alkali compounds that can be used include alkali metal hydroxides such as sodium hydroxide and potassium hydroxide, and alkali metal carbonates such as sodium carbonate and potassium carbonate. Examples of organic alkali compounds that can be used include ammonia and amine compounds having 1 to 6 carbon atoms, such as 2-aminoethanol.

[0029] The alkali compound used for neutralization is preferably an inorganic alkali compound, more preferably an alkali metal hydroxide, and even more preferably at least one selected from sodium hydroxide and potassium hydroxide, from the viewpoints of availability and economic efficiency.

[0030] The alkaline compound used for neutralization is preferably used as an aqueous alkaline solution from the viewpoint of ease of handling. In the neutralization, the sulfonated product may be mixed with an aqueous alkaline solution, or the sulfonated product may be mixed with an aqueous alkaline solution and water. When the sulfonated product is mixed with an aqueous alkaline solution and water, a high-concentration aqueous alkaline solution can be used. The concentration of the aqueous alkaline solution, or the concentration of the mixed solution when the aqueous alkaline solution and water are mixed, is preferably 1% by mass or more, more preferably 4.5% by mass or more, even more preferably 7% by mass or more, still more preferably 10% by mass or more, and even more preferably 12% by mass or more from the viewpoint of improving economic efficiency and suppressing the formation of impurities such as internal olefins and inorganic salts. Furthermore, from the viewpoint of improving productivity in the hydrolysis step, the concentration is preferably 50% by mass or less, more preferably 32% by mass or less, even more preferably 23% by mass or less, still more preferably 20% by mass or less, and even more preferably 18% by mass or less.

[0031] In the present invention, it is preferable to control the concentration of the alkali compound in the internal olefin sulfonate composition after the hydrolysis step by adjusting the amount of the alkali compound used in the neutralization step. The amount of the alkali compound used in the neutralization step is preferably 1 molar or more, more preferably 1.02 molar or more, and even more preferably 1.030 molar or more, relative to the sulfonic acid groups, from the viewpoints of suppressing the generation of impurities such as internal olefins and inorganic salts and improving reactivity; more preferably 1.034 molar or more, more preferably 1.035 molar or more, and even more preferably 1.04 molar or more, from the viewpoints of suppressing deterioration of odor after bleaching; and from the viewpoints of improving economic efficiency and storage stability, preferably 1.13 molar or less, more preferably 1.12 molar or less, even more preferably 1.110 molar or less, still more preferably 1.105 molar or less, still more preferably 1.10 molar or less, still more preferably 1.09 molar or less, still more preferably 1.08 molar or less, still more preferably 1.07 molar or less, and still more preferably 1.06 molar or less.

[0032] In the neutralization step, the temperature when mixing the sulfonated product with the aqueous alkaline solution and the temperature during the neutralization reaction are preferably 40° C. or lower, more preferably 35° C. or lower, even more preferably 30° C. or lower, and still more preferably 25° C. or lower, from the viewpoint of suppressing the generation of impurities such as internal olefins and inorganic salts due to side reactions; and are preferably 0° C. or higher, more preferably 10° C. or higher, even more preferably 15° C. or higher, and still more preferably 20° C. or higher, from the viewpoint of improving reactivity.

[0033] In the neutralization step, any type of mixer may be used as long as it can efficiently mix the sulfonated product and the aqueous alkaline solution and apply shear force to the oily material. Examples of such mixers include static mixers, collision mixers, impeller mixers, and vibration mixers. Examples of static mixers include a static mixer manufactured by Noritake Co., Ltd. Examples of impingement mixers include a high-pressure emulsifier manufactured by Nanomizer Co., Ltd. Examples of impeller mixers include a Milder manufactured by Pacific Machinery Works Co., Ltd. and a Homomixer manufactured by Primix Corporation. Among these, impeller mixers are preferred from the viewpoint of equipment cost.

[0034] When a stirring blade type mixer is used, the stirring speed of the stirrer is preferably 5 m / s or more, more preferably 10 m / s or more, and even more preferably 20 m / s or more from the viewpoint of suppressing the generation of impurities such as internal olefins and inorganic salts, and is preferably 200 m / s or less, more preferably 100 m / s or less, even more preferably 50 m / s or less, still more preferably 30 m / s or less, still more preferably 27.5 m / s or less, and still more preferably 25 m / s or less from the viewpoint of suppressing heat generation. Here, the stirring speed is the speed of the tip of the stirring blade and is expressed as 2 × (pi) × (radius of the stirring blade) × (number of rotations per unit time).

[0035] The neutralization step may be carried out by a continuous system, a batch system, or the like. From the viewpoint of suppressing the formation of by-products and improving productivity, it is preferable to carry out the neutralization step by a so-called continuous system in which the sulfonated product and an aqueous alkaline solution are added while circulating the reaction solution using a loop reactor, and the reaction solution is simultaneously withdrawn. Here, the "batch system" refers to a process in which raw materials are charged into a reactor, the reaction is initiated and allowed to proceed, and the product is recovered after completion. The "continuous system" refers to a process in which both raw material charging and product recovery are carried out simultaneously during the reaction. The "semi-batch system" described below refers to a process in which either raw material charging or product recovery is carried out simultaneously during the reaction.

[0036] In the neutralization step, the mixing time when mixing the sulfonated product with the alkaline aqueous solution is preferably 10 minutes or more, more preferably 20 minutes or more, and even more preferably 30 minutes or more, from the viewpoint of reducing impurities, and is preferably 120 minutes or less, more preferably 90 minutes or less, even more preferably 60 minutes or less, and still more preferably 50 minutes or less, from the viewpoint of improving economic efficiency.

[0037] The concentration of the internal olefin sulfonate in the neutralization product is preferably 40% by mass or more, more preferably 45% by mass or more, and even more preferably 48% by mass or more, from the viewpoint of obtaining a high-concentration internal olefin sulfonate composition, and is preferably 65% ​​by mass or less, more preferably 60% by mass or less, from the viewpoint of suppressing an increase in viscosity of the neutralization product. The concentration of the internal olefin sulfonate in the neutralization product is a value calculated by adding the concentration of the internal olefin sulfonate to the concentration of γ-sultone × (the molecular weight of the 3-hydroxysulfonate salt / the molecular weight of the γ-sultone).

[0038] <Hydrolysis Step> The hydrolysis step is a step in which the neutralized product obtained in the neutralization step is hydrolyzed by heating to obtain a hydrolysate.

[0039] In the hydrolysis step, the temperature during hydrolysis is preferably 120°C or higher, more preferably 140°C or higher, and even more preferably 160°C or higher, from the viewpoint of improving reactivity, and is preferably 220°C or lower, more preferably 200°C or lower, from the viewpoint of suppressing decomposition of the product.

[0040] The hydrolysis reaction may be carried out in a batch reactor or a continuous reactor. When a batch reactor is used, it is preferable to mix the components with a stirrer or the like.

[0041] The treatment time for the hydrolysis step is preferably 30 minutes or more, more preferably 45 minutes or more, and even more preferably 1 hour or more from the viewpoint of completing the reaction, and is preferably 4 hours or less, more preferably 3 hours or less from the viewpoint of improving productivity.

[0042] The average double bond positions of the raw material olefins for the internal olefin sulfonate is preferably 3 or more, more preferably 3.5 or more, and even more preferably 3.8 or more, from the viewpoints of the color of the sulfonate composition obtained by the reaction and the color of the sulfonate composition obtained after bleaching. In addition, from the viewpoints of suppressing contamination by by-products and reducing the peroxide value of the sulfonate composition obtained after bleaching, the average double bond positions of the raw material olefins for the internal olefin sulfonate is preferably 5 or less, more preferably 4.5 or less, even more preferably 4.4 or less, and even more preferably 4.3 or less.

[0043] From the viewpoint of cleaning performance when a decolorized internal olefin sulfonate composition (bleached internal olefin sulfonate composition) obtained through the decolorization step (A) described below is used as a cleaning agent, the internal olefin sulfonate preferably contains one or more internal olefin sulfonates selected from the group consisting of internal olefin sulfonates having a carbon number of 16 and internal olefin sulfonates having a carbon number of 18. Here, the number of carbon atoms in the internal olefin sulfonate is derived from the carbon chain of the internal olefin.

[0044] The concentration of the alkali compound in the internal olefin sulfonate composition obtained in the hydrolysis step is, from the viewpoint of suppressing deterioration of the odor of the internal olefin sulfonate composition after the bleaching step (A) and from the viewpoint of reducing the peroxide value of the internal olefin sulfonate composition after the bleaching step (A), preferably 0.010 mmol or more, more preferably 0.015 mmol, even more preferably 0.020 mmol or more, still more preferably 0.025 mmol or more, and still more preferably 0.029 mmol or more, relative to 1 g of the internal olefin sulfonate in the internal olefin sulfonate composition. Furthermore, from the viewpoint of suppressing a decrease in storage stability, it is preferably 0.27 mmol or less, more preferably 0.240 mmol or less, and even more preferably 0.210 mmol or less; and from the viewpoint of increasing the fading rate, it is preferably 0.27 mmol or less, more preferably 0.240 mmol or less, even more preferably 0.220 mmol or less, even more preferably 0.210 mmol or less, even more preferably 0.20 mmol or less, even more preferably 0.18 mmol or less, even more preferably 0.16 mmol or less, even more preferably 0.10 mmol or less, and even more preferably 0.08 mmol or less.

[0045] The hydrolysis step is not limited to the step of obtaining a hydrolysate by hydrolysis, and the concentration of the alkali compound in the internal olefin sulfonate composition may be controlled by adjusting the amount of the alkali compound.

[0046] From the viewpoint of reducing the amount of impurities in the internal olefin sulfonate composition, the internal olefin sulfonate composition is preferably produced by a production method in which the concentration of the alkali compound in the internal olefin sulfonate composition after the hydrolysis step is controlled within the above-mentioned preferred range by an adjustment method selected from a method of adjusting the amount of the alkali compound used in the neutralization step and a method of adjusting the amount of the alkali compound in the hydrolysis step. From the same viewpoint, the internal olefin sulfonate composition is more preferably produced by a production method in which the concentration of the alkali compound in the internal olefin sulfonate composition after the hydrolysis step is controlled within the above-mentioned preferred range by a method of adjusting the amount of the alkali compound used in the neutralization step. The preferred range of the amount of the alkali compound used in the neutralization step is as described above.

[0047] <Bleaching Step (A)> The bleaching step (A) is a step of carrying out, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjusting step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, wherein the adjusting step (a1) is a step of adjusting the concentration of the alkali compound in the bleaching step (A) so that the concentration of the alkali compound after mixing the bleaching agent with the internal olefin sulfonate composition present in the system is 0.004 mmol or more and 0.26 mmol or less per 1 g of the internal olefin sulfonate.

[0048] Here, in the present invention, the term "reactor" refers to the reaction tank itself used in a batch or semi-batch system, and the term "reactor" refers to the entire unit involved in the reaction, including the reaction tank, piping, etc., and the reaction apparatus in a continuous system may not include the reaction tank.

[0049] The system in which the internal olefin sulfonate composition is present may be a liquid (liquid composition) in which the internal olefin sulfonate composition is present.

[0050] The order in which the adjusting step (a1) and the mixing step (a2) are performed is not particularly limited, and the adjusting step (a1) may be performed after the mixing step (a2), or the mixing step (a2) may be performed after the adjusting step (a1). The mixing step (a2) and the adjusting step (a1) may also be performed in parallel. However, since the bleaching treatment (bleaching reaction) is initiated by mixing (contacting) the bleaching agent with the internal olefin sulfonate composition, when the adjusting step (a1) is performed after the mixing step (a2), it is preferable to perform the adjusting step (a1) immediately after the mixing step (a2) from the viewpoint of suppressing deterioration of the odor. In the present invention, it is preferable to perform the mixing step (a2) and the adjusting step (a1) in parallel from the viewpoint of suppressing deterioration of the odor and improving economic efficiency.

[0051] The bleaching treatment (bleaching reaction) refers to a state in which the bleaching agent and the internal olefin sulfonate composition coexist, and includes the mixing step (a2) and the aging step (b) described below. Here, the aging step (b) is a process of maintaining a state in which the bleaching agent and the internal olefin sulfonate composition coexist after mixing the bleaching agent.

[0052] The decolorization step (A) may be carried out at any stage after the internal olefin sulfonate composition is formed in the production process of the internal olefin sulfonate composition. However, it is preferably carried out after the neutralization step or the hydrolysis step, and more preferably after the hydrolysis step from the viewpoint of suppressing the generation of by-products.

[0053] A preferred embodiment of the concentration of the alkali compound in the internal olefin sulfonate composition before carrying out the decolorization step (A) is the same as a preferred embodiment of the concentration of the alkali compound in the internal olefin sulfonate composition obtained in the hydrolysis step.

[0054] The system in which the internal olefin sulfonate composition containing the internal olefin sulfonate is present is a system containing the internal olefin sulfonate composition before the bleaching treatment, and specifically includes a system containing the internal olefin sulfonate composition after the neutralization step and a system containing the internal olefin sulfonate composition after the hydrolysis step. Each step will be described below.

[0055] [Adjusting Step (a1)] In the adjusting step (a1), the concentration of the alkali compound is adjusted so that the concentration of the alkali compound after mixing the bleaching agent with the internal olefin sulfonate composition present in the system in the decolorizing process (A) is 0.004 mmol to 0.26 mmol per 1 g of the internal olefin sulfonate. By mixing the bleaching agent with the internal olefin sulfonate composition and carrying out the decolorizing reaction, the concentration of the alkali compound in the reaction system decreases, and therefore the adjusting step (a1) controls (adjusts) the concentration of the alkali compound in the system. In the present invention, it is preferable to adjust the concentration of the alkali compound in the system immediately after the mixing step (a2) to be within the above-mentioned range.

[0056] In the adjusting step (a1), the concentration of the alkali compound in the system is adjusted to 0.004 mmol or more and 0.26 mmol or less per gram of the internal olefin sulfonate after the mixing step (a2). By adjusting the alkali compound to such a concentration, a bleached internal olefin sulfonate composition having good color fading, a weak odor, and good storage stability can be obtained. The concentration of the alkali compound is preferably 0.005 mmol or more from the viewpoint of suppressing deterioration of the odor and reducing the peroxide value, and is more preferably 0.010 mmol or more, even more preferably 0.015 mmol or more, even more preferably 0.020 mmol or more, and even more preferably 0.030 mmol or more from the viewpoint of reducing the peroxide value. The concentration of the alkali compound is preferably 0.23 mmol or less, more preferably 0.215 mmol or less, and even more preferably 0.20 mmol or less, from the viewpoint of suppressing a decrease in the storage stability of the bleached internal olefin sulfonate composition. Furthermore, from the viewpoint of increasing the fading rate, the concentration is preferably 0.23 mmol or less, more preferably 0.215 mmol or less, even more preferably 0.20 mmol or less, even more preferably 0.15 mmol or less, even more preferably 0.10 mmol or less, even more preferably 0.08 mmol or less, and even more preferably 0.06 mmol or less. Because the concentration of the alkali compound decreases during the bleaching treatment, it is preferable to adjust the concentration of the alkali compound immediately after the bleaching treatment (i.e., immediately after the mixing step (a2)). The adjusting step (a1) is a step for adjusting the concentration of the alkali compound. If the concentration of the alkali compound is already within a suitable range, there is no need to change the concentration of the alkali compound. Such cases where adjustment of the concentration of the alkali compound is not required are also included in the "adjusting step (a1)" of the present invention.

[0057] When the adjusting step (a1) is performed after the mixing step (a2), the concentration of the alkali compound may be adjusted to the above-mentioned level in the adjusting step (a1), but when the adjusting step (a1) is performed before the mixing step (a2), it is preferable to adjust the concentration of the alkali compound taking into account the concentration of the alkali compound that decreases during the bleaching treatment. Specifically, from the viewpoints of suppressing deterioration of the odor and reducing the peroxide value, the concentration of the alkali compound in the adjusting step (a1) is preferably 0.010 mmol or more, more preferably 0.015 mmol, more preferably 0.020 mmol or more, still more preferably 0.025 mmol or more, still more preferably 0.030 mmol or more, and still more preferably 0.035 mmol or more, per gram of the internal olefin sulfonate. Furthermore, from the viewpoint of suppressing a decrease in storage stability, it is preferably 0.270 mmol or less, more preferably 0.240 mmol or less, more preferably 0.210 mmol or less, and from the viewpoint of increasing the fading rate, it is even more preferably 0.240 mmol or less, even more preferably 0.220 mmol or less, even more preferably 0.210 mmol or less, even more preferably 0.20 mmol or less, even more preferably 0.18 mmol or less, even more preferably 0.16 mmol or less, even more preferably 0.10 mmol or less, more preferably 0.08 mmol or less.

[0058] The adjustment method is not particularly limited, but can be carried out by withdrawing the liquid from the system and quickly analyzing the concentration of the alkali compound in the withdrawn liquid at room temperature. If the analysis results in a concentration lower than the preferred concentration range, such as less than 0.004 mmol per 1 g of the internal olefin sulfonate, the alkali compound can be added to the system to adjust the alkali compound concentration after the mixing step to the preferred alkali compound concentration.

[0059] The alkali compound may be an inorganic alkali compound or an organic alkali compound. Examples of inorganic alkali compounds include alkali metal hydroxides such as sodium hydroxide and potassium hydroxide, and alkali metal carbonates such as sodium carbonate and potassium carbonate. Examples of organic alkali compounds include ammonia and amine compounds having 1 to 6 carbon atoms, such as 2-aminoethanol.

[0060] From the viewpoints of availability and economic efficiency, the alkaline compound is preferably an inorganic alkaline compound, more preferably an alkali metal hydroxide, and even more preferably at least one selected from the group consisting of sodium hydroxide and potassium hydroxide.

[0061] The alkaline compound is preferably used in the form of an alkaline aqueous solution from the viewpoint of ease of handling.

[0062] The adjusting step (a1) can be carried out in a batch system, a semi-batch system, or a continuous system, and from the viewpoint of improving productivity, a continuous system is preferred.

[0063] The adjusting step (a1) is preferable, for example, when the loop reactor is used, because the liquid in the system can be extracted and the extracted mixed liquid can be quickly analyzed for the concentration of the alkaline compound at room temperature.

[0064] In the preparation step (a1), from the viewpoint of odor reduction, it is preferable to carry out the preparation continuously using a circulation system. For example, it is preferable to carry out the preparation continuously while circulating the internal olefin sulfonate composition using the above-mentioned loop reactor or the like. From the viewpoint of odor reduction, the circulation ratio is preferably more than 0, more preferably 1 or more, more preferably 2 or more, even more preferably 3 or more, and even more preferably 4 or more. From the viewpoint of improving economic efficiency, it is preferably 20 or less, more preferably 10 or less, and even more preferably 8 or less. Here, the circulation ratio is the ratio of the flow rate circulating in the reactor to the flow rate introduced into the reactor, and is expressed as ((flow rate in the reactor) / (flow rate introduced into the reactor))-1. Here, the flow rate in the reactor refers to the flow rate immediately after merging with the fluid introduced into the reactor.

[0065] In the preparation step (a1), any type of mixer may be used as long as it can efficiently mix the internal olefin sulfonate composition and the bleaching agent (aqueous solution of the bleaching agent). Examples of such mixers include impellers, static mixers, impingement mixers, impeller mixers, and vibration mixers. Impingers include small and large impingers, and examples of small impingers include flat paddle impingers, inclined paddle impingers, and propeller impingers. Examples of large impingers include anchor impingers, helical ribbon impingers, screw impingers, Max Blend, Supermix impingers (MR205 (product name, manufactured by Satake Multimix Co., Ltd.)), and Fullzone. Examples of static mixers include static mixers manufactured by Noritake Co., Ltd. Examples of impingement mixers include high-pressure emulsifiers manufactured by Nanomizer Co., Ltd. Examples of impingement mixers include Milder manufactured by Pacific Machinery & Engineering Co., Ltd., Cavitron manufactured by Pacific Machinery & Engineering Co., Ltd., and pipeline homomixer manufactured by Primix Corporation. Among these, from the viewpoint of improving colorfastness, agitating blades and agitating blade-type mixers are preferred, large blades and agitating blade-type mixers are more preferred, and agitating blade-type mixers are even more preferred.

[0066] In the adjusting step (a1), when a reaction vessel having an agitator blade or an agitator-type mixer is used, the peripheral speed of the agitator blade is, from the viewpoint of the decolorizing effect (discoloration rate) and improving mixability, preferably 0.01 m / s or more, more preferably 0.05 m / s or more, even more preferably 0.1 m / s or more, still more preferably 0.3 m / s or more, still more preferably 0.9 m / s or more, still more preferably 4.7 m / s or more, still more preferably 7.0 m / s or more, and still more preferably 9.0 m / s or more, and from the viewpoint of improving economic efficiency, preferably 50 m / s or less, more preferably 40 m / s or less, still more preferably 26 m / s or less, and still more preferably 15 m / s or less. When the adjustment step (a1) is carried out continuously, the peripheral speed of the stirring blade is preferably 0.1 m / s or more, more preferably 0.3 m / s or more, even more preferably 4 m / s or more, still more preferably 7.0 m / s or more, and even more preferably 9.0 m / s or more, from the viewpoint of increasing the fading rate, and is preferably 50 m / s or less, more preferably 40 m / s or less, more preferably 26 m / s or less, and even more preferably 15 m / s or less, from the viewpoint of reducing odor deterioration and improving economic efficiency. When the preparation step (a1) is carried out in a semi-batch manner, the peripheral speed of the stirring blade is preferably 0.1 m / s or more, more preferably 0.3 m / s or more, even more preferably 0.5 m / s or more, and even more preferably 0.7 m / s or more, from the viewpoint of increasing the fading rate, and is preferably 50 m / s or less, more preferably 40 m / s or less, even more preferably 26 m / s or less, even more preferably 15 m / s or less, even more preferably 10 m / s or less, and even more preferably 8 m / s or less, from the viewpoint of reducing odor deterioration and improving economic efficiency. When the preparation step (a1) is carried out batchwise, the peripheral speed of the stirring blade is preferably 0.1 m / s or more, more preferably 0.3 m / s or more, even more preferably 0.9 m / s or more, still more preferably 1.0 m / s or more, and even more preferably 1.5 m / s or more, from the viewpoint of increasing the fading rate, and is preferably 50 m / s or less, more preferably 40 m / s or less, still more preferably 26 m / s or less, still more preferably 15 m / s or less, still more preferably 10 m / s or less, still more preferably 5 m / s or less, and even more preferably 3 m / s or less, from the viewpoint of reducing odor deterioration and improving economy.

[0067] In the adjusting step (a1), when a reaction vessel having an agitating blade or an agitating blade type mixer is used, the ratio of the agitating blade diameter d to the vessel diameter D (d / D) is preferably 0.01 or more, more preferably 0.05 or more, even more preferably 0.1 or more, even more preferably 0.3 or more, even more preferably 0.4 or more, even more preferably 0.5 or more, even more preferably 0.55 or more, from the viewpoint of improving production capacity, improving mixability, and increasing the fading rate. Also, from the viewpoint of improving economy, it is preferably less than 1, more preferably 0.9 or less, even more preferably 0.8 or less, even more preferably 0.7 or less. Also, from the viewpoint of improving mixability, it is preferably 0.7 or more, more preferably 0.8 or more, even more preferably 0.9 or more, and also preferably less than 1.

[0068] In the adjusting step (a1), when a reaction vessel having an impeller or an impeller-type mixer is used, the ratio of the impeller height h to the vessel height H (h / H) is preferably 0.01 or more, more preferably 0.05 or more, even more preferably 0.1 or more, still more preferably 0.3 or more, and even more preferably 0.4 or more from the viewpoint of improving mixability and increasing the fading rate, and is preferably less than 1, more preferably 0.9 or less, even more preferably 0.8 or less, and still more preferably 0.7 or less from the viewpoint of suppressing foaming. Furthermore, from the viewpoint of improving mixability, it is preferably 0.7 or more, more preferably 0.8 or more, even more preferably 0.9 or more, and is preferably less than 1.

[0069] In the adjusting step (a1), when a reaction vessel having stirring blades or a stirring blade-type mixer is used, the number of stages of the stirring blades is preferably one or more, more preferably two or more, and even more preferably three or more, from the viewpoint of improving mixability, and is preferably ten or less, more preferably nine or less, and even more preferably eight or less, from the viewpoint of improving economy.

[0070] In the adjusting step (a1), when the adjustment is carried out batchwise using a reaction vessel having stirring blades, the d / D, h / H and the number of stages of stirring blades are preferably within the above-mentioned suitable ranges.

[0071] The adjusting step (a1) is preferably carried out under shear conditions. From the viewpoint of improving mixability, the shear rate is preferably 5 / s or more, more preferably 10 / s or more, even more preferably 100 / s or more, still more preferably 500 / s or more, even more preferably 1000 / s or more, still more preferably 1500 / s or more, and from the viewpoint of reducing odor deterioration and improving economic efficiency, it is preferably 100000 / s or less, more preferably 50000 / s or less, even more preferably 30000 / s or less, still more preferably 20000 / s or less. When the preparation step (a1) is carried out continuously, the shear rate is preferably 100 / s or more, more preferably 500 / s or more, even more preferably 1000 / s or more, and even more preferably 1500 / s or more, from the viewpoint of increasing the fading rate, and is preferably 100,000 / s or less, more preferably 50,000 / s or less, even more preferably 30,000 / s or less, and even more preferably 20,000 / s or less, from the viewpoint of reducing odor deterioration and improving economic efficiency. When the preparation step (a1) is carried out in a semi-batch manner, the shear rate is preferably 10 / s or more, more preferably 100 / s or more, even more preferably 500 / s or more, still more preferably 1000 / s or more, and even more preferably 1500 / s or more, from the viewpoint of increasing the fading rate, and is preferably 100,000 / s or less, more preferably 50,000 / s or less, even more preferably 40,000 / s or less, still more preferably 30,000 / s or less, still more preferably 20,000 / s or less, still more preferably 10,000 / s or less, and even more preferably 8,000 / s or less, from the viewpoint of reducing odor deterioration and improving economic efficiency. When the preparation step (a1) is carried out batchwise, the shear rate is preferably 5 / s or more, more preferably 8 / s or more, even more preferably 10 / s or more, and even more preferably 12 / s or more from the viewpoint of increasing the fading rate, and from the viewpoint of reducing odor deterioration and improving economic efficiency, it is preferably 5000 / s or less, more preferably 1000 / s or less, even more preferably 500 / s or less, even more preferably 100 / s or less, and even more preferably 50 / s or less. Here, the shear rate (1 / s) = the rotation speed of the stirring blade (rpm) × pi × stirring blade diameter (m) / (30 × (reaction vessel inner diameter (m) - stirring blade diameter (m))).

[0072] The stirring power (Pv) required per unit liquid volume of the mixer used in the adjusting step (a1) is preferably 0.1 kW / m from the viewpoint of improving the mixing property. ３ More preferably, 0.2 kW / m ３ More preferably, 0.3 kW / m ３ From the viewpoint of improving economic efficiency, it is preferably 100 kW / m ３ Less than 50 kW / m, more preferably ３ More preferably, 30 kW / m or less ３ More preferably, 10 kW / m or less ３ More preferably, 5 kW / m or less ３ More preferably, 1 kW / m or less ３ The required stirring power (Pv) per unit liquid volume (kW / m ３ ) = required mixing power P (kW) / liquid volume (m ３ Here, the stirring power P is the value obtained by subtracting the idling power from the power required for the actual liquid.

[0073] The pressure in the system in the adjusting step (a1) is preferably 0 MPaG or more, more preferably 0.01 MPaG or more, more preferably 0.05 MPaG or more, even more preferably 0.1 MPaG or more, and even more preferably 0.2 MPaG or more from the viewpoint of improving pH controllability, mixability, and foaming suppression, and is preferably 10 MPaG or less, more preferably 5 MPaG or less, even more preferably 1 MPaG or less, and even more preferably 0.5 MPaG or less from the viewpoint of improving economic efficiency. Here, G in MPaG indicates gauge pressure.

[0074] [Mixing step (a2)] The decolorizing agent is not particularly limited, but an oxidizing agent is preferred. Examples of the oxidizing agent include hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate. These may be used alone or in combination of two or more. Of these, hydrogen peroxide is preferred from the viewpoint of preventing impurities from being mixed in.

[0075] The amount of the bleaching agent mixed is, from the viewpoint of increasing the bleaching effect (fading rate), preferably 1 mg or more, more preferably 5 mg or more, even more preferably 10 mg or more, still more preferably 15 mg or more, and still more preferably 20 mg or more, relative to 1 g of the internal olefin sulfonate in the internal olefin sulfonate composition; and, from the viewpoint of improving economic efficiency and suppressing the peroxide value, preferably 300 mg or less, more preferably 100 mg or less, still more preferably 40 mg or less, and still more preferably 30 mg or less, relative to 1 g of the internal olefin sulfonate in the internal olefin sulfonate composition.

[0076] In the mixing step (a2), the bleaching agent may be mixed in one batch or in multiple batches, and the number of batches is not limited.

[0077] The decolorizing agent is preferably used as an aqueous solution of the decolorizing agent from the viewpoint of ease of handling. The concentration of the decolorizing agent in the aqueous solution is not particularly limited, but from the viewpoint of improving economy by reducing the size of the decolorizing agent storage tank, it is preferably 5% or more, more preferably 10% or more, and even more preferably 30% or more, and from the viewpoint of ease of handling, it is preferably 70% or less, more preferably 60% or less, and even more preferably 50% or less.

[0078] The temperature in the mixing step (a2) is preferably 40° C. or higher, more preferably 60° C. or higher, even more preferably 70° C. or higher, and even more preferably 80° C. or higher, from the viewpoint of increasing the bleaching effect (fading rate) and reducing the peroxide value, and is preferably 100° C. or lower, more preferably 90° C. or lower, and even more preferably 85° C. or lower, from the viewpoint of economy. As described above, the bleaching reaction starts by mixing the internal olefin sulfonate composition with the bleaching agent, and therefore the temperature in the mixing step (a2) refers to the temperature during the bleaching reaction.

[0079] The pH of the solution in the system in the mixing step (a2) is preferably 9.3 or more, more preferably 9.5, from the viewpoint of suppressing deterioration of the odor and reducing the peroxide value. Also, from the viewpoint of reducing the peroxide value, it is even more preferably 9.8 or more, and even more preferably 10.0 or more. Furthermore, from the viewpoint of suppressing deterioration of storage stability, it is preferably 11.4 or less, more preferably 11.3 or less. Also, from the viewpoint of increasing the fading rate, it is even more preferably 11.0 or less, even more preferably 10.8 or less, and even more preferably 10.5 or less. The pH can be a value measured with a pH meter installed in the loop reactor. It is preferable that the pH be set within an appropriate range depending on the characteristics of the type of alkaline compound.

[0080] The mixing step (a2) can be carried out in a batchwise, semi-batchwise, or continuous manner, but from the viewpoint of improving productivity, it is preferable to carry out the mixing step (a2) in a so-called continuous manner, in which the internal olefin sulfonate composition before decolorization treatment and the bleaching agent (aqueous solution of the bleaching agent) are added while circulating the mixed liquid using a loop reactor, and simultaneously the decolorized mixed liquid is withdrawn. In the decolorization step (A), the concentration of the alkali compound is reduced by the reaction between the internal olefin sulfonate composition and the bleaching agent, and therefore the concentration of the alkali compound is controlled in the adjusting step (a1).

[0081] In the mixing step (a2), any type of mixer may be used as long as it can efficiently mix the internal olefin sulfonate composition and the bleaching agent (aqueous solution of the bleaching agent). Examples of such mixers include impellers, static mixers, impingement mixers, impeller mixers, and vibration mixers. Impingers include small and large impingers, and examples of small impingers include flat paddle impingers, inclined paddle impingers, and propeller impingers. Examples of large impingers include anchor impingers, helical ribbon impingers, screw impingers, Max Blend, Supermix impingers (MR205 (product name, manufactured by Satake Multimix Co., Ltd.)), and Fullzone. Examples of static mixers include static mixers manufactured by Noritake Co., Ltd. Examples of impingement mixers include high-pressure emulsifiers manufactured by Nanomizer Co., Ltd. Examples of impingement mixers include Milder manufactured by Pacific Machinery & Engineering Co., Ltd., Cavitron manufactured by Pacific Machinery & Engineering Co., Ltd., and Homomixer manufactured by Primix Corporation. Among these, from the viewpoint of increasing the stirring efficiency and the fading rate, a stirring blade or a stirring blade type mixer is preferable, a large blade or a stirring blade type mixer is more preferable, and a stirring blade type mixer is even more preferable.

[0082] In the mixing step (a2), when a reaction vessel having an impeller or an impeller-type mixer is used, the peripheral speed of the impeller is, from the viewpoint of enhancing the decolorizing effect (discoloration rate), preferably 0.01 m / s or more, more preferably 0.05 m / s or more, even more preferably 0.1 m / s or more, still more preferably 0.3 m / s or more, still more preferably 0.9 m / s or more, still more preferably 4.7 m / s or more, still more preferably 7.0 m / s or more, and still more preferably 9.0 m / s or more, and from the viewpoint of reducing odor deterioration and improving economy, is preferably 50 m / s or less, more preferably 40 m / s, still more preferably 26 m / s or less, and still more preferably 15 m / s or less. When the mixing step (a2) is carried out continuously, the peripheral speed of the stirring blade is preferably 0.3 m / s or more, more preferably 0.9 m / s or more, even more preferably 4.7 m / s or more, still more preferably 7.0 m / s or more, and even more preferably 9.0 m / s or more, from the viewpoint of increasing the fading rate, and is preferably 50 m / s or less, more preferably 40 m / s, even more preferably 26 m / s or less, and even more preferably 15 m / s or less, from the viewpoint of reducing odor deterioration and improving economy. When the mixing step (a2) is carried out in a semi-batch manner, the peripheral speed of the stirring blade is preferably 0.01 m / s or more, more preferably 0.1 m / s or more, even more preferably 0.3 m / s or more, and even more preferably 0.9 m / s or more, from the viewpoint of increasing the fading rate, and is preferably 50 m / s or less, more preferably 40 m / s, even more preferably 26 m / s or less, even more preferably 15 m / s or less, and even more preferably 10 m / s or less, from the viewpoint of reducing odor deterioration and improving economic efficiency. When the mixing step (a2) is carried out batchwise, the peripheral speed of the stirring blade is preferably 0.01 m / s or more, more preferably 0.1 m / s or more, even more preferably 0.3 m / s or more, still more preferably 0.9 m / s or more, and even more preferably 1.5 m / s or more, from the viewpoint of increasing the fading rate, and is preferably 50 m / s or less, more preferably 40 m / s, even more preferably 26 m / s or less, still more preferably 15 m / s or less, still more preferably 10 m / s or less, still more preferably 5 m / s or less, and even more preferably 3 m / s or less, from the viewpoint of reducing odor deterioration and improving economy.

[0083] In the mixing step (a2), when a reaction vessel having an impeller or an impeller-type mixer is used, the ratio of the impeller diameter d to the vessel diameter D (d / D) is preferably 0.01 or more, more preferably 0.05 or more, even more preferably 0.1 or more, still more preferably 0.3 or more, still more preferably 0.4 or more, still more preferably 0.5 or more, and still more preferably 0.55 or more from the viewpoint of improving mixability, and is preferably less than 1, more preferably 0.9 or less, even more preferably 0.8 or less, and still more preferably 0.7 or less from the viewpoint of improving mixability. Furthermore, it is preferably 0.7 or more, more preferably 0.8 or more, even more preferably 0.9 or more, and is preferably less than 1.

[0084] In the mixing step (a2), when a reaction vessel having an impeller or an impeller-type mixer is used, the ratio of the impeller height h to the vessel height H (h / H) is preferably 0.01 or more, more preferably 0.05 or more, even more preferably 0.1 or more, still more preferably 0.3 or more, still more preferably 0.4 or more, still more preferably 0.5 or more, and still more preferably 0.55 or more from the viewpoint of improving mixability, and is preferably less than 1, more preferably 0.9 or less, even more preferably 0.8 or less, and still more preferably 0.7 or less from the viewpoint of suppressing foaming. Furthermore, from the viewpoint of improving mixability, it is preferably 0.7 or more, more preferably 0.8 or more, and still more preferably 0.9 or more, and is preferably less than 1.

[0085] In the mixing step (a2), when a reaction vessel having stirring blades or a stirring blade-type mixer is used, the number of stages of the stirring blades is preferably one or more, more preferably two or more, and even more preferably three or more, from the viewpoint of improving mixability, and is preferably ten or less, more preferably nine or less, and even more preferably eight or less, from the viewpoint of improving economy.

[0086] In the mixing step (a2), when the preparation is carried out batchwise using a reaction vessel having stirring blades, the d / D, h / H and number of stirring blade stages are preferably within the above-mentioned suitable ranges.

[0087] The shear rate in the mixing step (a2) is preferably 5 / s or more, more preferably 10 / s or more, even more preferably 100 / s or more, still more preferably 500 / s or more, still more preferably 1000 / s or more, and still more preferably 1500 / s or more, from the viewpoint of increasing the fading rate, and is preferably 100,000 / s or less, more preferably 80,000 / s or less, even more preferably 70,000 / s or less, still more preferably 50,000 / s or less, still more preferably 40,000 / s or less, still more preferably 30,000 / s or less, and still more preferably 20,000 / s or less, from the viewpoint of reducing odor deterioration and improving economic efficiency. When the mixing step (a2) is carried out continuously, the shear rate is preferably 100 / s or more, more preferably 500 / s or more, even more preferably 1000 / s or more, and even more preferably 1500 / s or more, from the viewpoint of increasing the fading rate, and is preferably 100,000 / s or less, more preferably 80,000 / s or less, even more preferably 70,000 / s or less, even more preferably 50,000 / s or less, even more preferably 40,000 / s or less, even more preferably 30,000 / s or less, and even more preferably 20,000 / s or less, from the viewpoint of reducing odor deterioration and improving economic efficiency. When the mixing step (a2) is carried out in a semi-batch manner, the shear rate is preferably 10 / s or more, more preferably 100 / s or more, even more preferably 500 / s or more, still more preferably 1000 / s or more, and even more preferably 1500 / s or more, from the viewpoint of increasing the fading rate, and from the viewpoint of reducing odor deterioration and improving economic efficiency, it is preferably 100,000 / s or less, more preferably 80,000 / s or less, even more preferably 70,000 / s or less, still more preferably 50,000 / s or less, still more preferably 40,000 / s or less, still more preferably 30,000 / s or less, and even more preferably 20,000 / s or less.When the mixing step (a2) is carried out batchwise, the shear rate is preferably 5 / s or more, more preferably 8 / s or more, even more preferably 10 / s or more, and even more preferably 12 / s or more, from the viewpoint of increasing the fading rate, and is preferably 5000 / s or less, more preferably 1000 / s or less, even more preferably 500 / s or less, even more preferably 100 / s or less, and even more preferably 30 / s or less, from the viewpoint of reducing odor deterioration and improving economic efficiency.

[0088] The stirring power (Pv) required per unit liquid volume of the mixer used in the mixing step (a2) is preferably 0.1 kW / m from the viewpoint of increasing the fading rate. ３ More preferably, 0.2 kW / m ３ More preferably, 0.3 kW / m ３ From the viewpoint of reducing odor degradation and improving economic efficiency, it is preferably 100 kW / m ３ Less than 50 kW / m, more preferably ３ More preferably, 30 kW / m or less ３ More preferably, 10 kW / m or less ３ More preferably, 5 kW / m or less ３ More preferably, 1 kW / m or less ３ The following is the result.

[0089] The pressure in the system in the mixing step (a2) is preferably 0 MPaG or more, more preferably 0.01 MPaG or more, more preferably 0.05 MPaG or more, even more preferably 0.1 MPaG or more, and even more preferably 0.2 MPaG or more from the viewpoint of reducing the volume of the apparatus and reducing the peroxide value, and from the viewpoint of improving economic efficiency, it is preferably 10 MPaG or less, more preferably 5 MPaG or less, even more preferably 1 MPaG or less, and even more preferably 0.5 MPaG or less. Here, G in MPaG indicates gauge pressure.

[0090] When the adjusting step (a1) is carried out after the mixing step (a2), or when the adjusting step (a1) is carried out simultaneously with the mixing step (a2), the pressure in the adjusting step is, from the viewpoint of ease of control of the concentration of the alkaline compound, preferably 0 MPaG or more, more preferably 0.01 MPaG or more, even more preferably 0.05 MPaG or more, still more preferably 0.1 MPaG or more, and still more preferably 0.2 MPaG or more, and from the viewpoint of improving economic efficiency, preferably 10 MPaG or less, more preferably 5 MPaG or less, even more preferably 1 MPaG or less, and still more preferably 0.5 MPaG or less.

[0091] The decolorizing step (A) includes the mixing step (a2) and the adjusting step (a1), but may also include other steps, and preferably includes, for example, an aging step (b).

[0092] [Aging Step (b)] The aging step (b) is a process of maintaining a state in which the bleaching agent and the internal olefin sulfonate composition coexist without adding a new bleaching agent after the mixing step (a2), and there is no need to mix them using a mixer, etc. In the present invention, it is preferable to carry out the aging step (b) from the viewpoint of reducing the peroxide value.

[0093] The preferred temperature range for the aging step (b) may be the same as the preferred temperature range for the mixing step (a2) from the viewpoint of economic efficiency. However, for example, from the viewpoint of economic efficiency and reduction of the peroxide value, the preferred temperature range for the aging step (b) is preferably 40°C or higher, more preferably 50°C or higher, and even more preferably 60°C or higher, and from the viewpoint of improving economic efficiency, the preferred temperature range for the aging step (b) is preferably 120°C or lower, more preferably 110°C or lower, and even more preferably 100°C or lower.

[0094] The reaction apparatus for carrying out the aging step (b) is not particularly limited, and in the case of a batch system, a thermostatic bath or a tank-type reactor can be used. In addition, in the case of a semi-batch system or a continuous system, a tank-type reactor can be used. The tank shape of the tank-type reactor can be cylindrical, angular, spherical, etc., and from the viewpoint of improving economic efficiency, a cylindrical reactor is preferred. In addition, tank-type reactors having a cylindrical tank include horizontal cylindrical reactors and vertical cylindrical reactors, and from the viewpoint of improving reaction efficiency, a vertical cylindrical reactor is preferred. In addition, in order to improve reaction efficiency, a dispersion mechanism such as a perforated plate or a dispersion plate may be provided in the reactor as necessary.

[0095] When the aging step (b) is carried out using the vertical cylindrical reactor, the height H of the vertical cylindrical reactor １ and reactor inner diameter D １ The ratio (H １ / D １ ) is preferably 0.1 or more, more preferably 1 or more, and even more preferably 1.5 or more from the viewpoint of improving reaction efficiency, and is preferably 300 or less, more preferably 200 or less, even more preferably 100 or less, still more preferably 50 or less, still more preferably 30 or less, still more preferably 10 or less, and still more preferably 5 or less from the viewpoint of suppressing pressure loss and improving economic efficiency.

[0096] The residence time in the aging step (b) is, from the viewpoint of reducing the peroxide value, preferably 10 minutes or more, more preferably 20 minutes or more, even more preferably 30 minutes or more, still more preferably 45 minutes or more, and still more preferably 60 minutes or more, and, from the viewpoint of improving economic efficiency, is preferably 500 minutes or less, more preferably 400 minutes or less, even more preferably 300 minutes or less, and still more preferably 200 minutes or less.

[0097] The pressure in the aging step (b) is preferably 0 MPaG or more, more preferably 0.01 MPaG or more, more preferably 0.05 MPaG or more, even more preferably 0.1 MPaG or more, and even more preferably 0.2 MPaG or more from the viewpoint of reducing the volume of the apparatus and reducing the peroxide value, and is preferably 10 MPaG or less, more preferably 5 MPaG or less, even more preferably 1 MPaG or less, and even more preferably 0.5 MPaG or less from the viewpoint of improving economic efficiency.

[0098] The aging step (b) may be carried out in a continuous, semi-batch or batch manner. From the viewpoint of reaction efficiency, the batch or semi-batch manner is preferred, and from the viewpoint of improving productivity, the continuous manner is preferred.

[0099] When the aging step (b) is carried out continuously, the linear speed of the internal olefin sulfonate composition is preferably 0.001 mm / s or more, more preferably 0.005 mm / s or more, even more preferably 0.01 mm / s or more, and still more preferably 0.1 mm / s or more, from the viewpoint of maintaining the uniformity of the composition of the internal olefin sulfonate composition, and is preferably 1000 mm / s or less, more preferably 800 mm / s or less, even more preferably 500 mm / s or less, still more preferably 300 mm / s or less, still more preferably 100 mm / s or less, still more preferably 50 mm / s or less, still more preferably 10 mm / s or less, still more preferably 5 mm / s or less, and still more preferably 1 mm / s or less, from the viewpoint of reducing the peroxide value.

[0100] The discoloration rate of the discolored internal olefin sulfonate composition obtained in the discoloration step (A) relative to the internal olefin sulfonate composition before discoloration is preferably 50% or more, more preferably 60% or more, more preferably 63% or more, and even more preferably 65% ​​or more. Here, the discoloration rate can be measured by the method described in the Examples.

[0101] From the viewpoint of the stability of the bleached internal olefin sulfonate composition, the peroxide value of the bleached internal olefin sulfonate composition obtained in the bleaching step (A) is preferably 37.0 meq or less, more preferably 30.0 meq or less, more preferably 20.0 meq or less, more preferably 10 meq or less, still more preferably 7 meq or less, and still more preferably 5 meq or less, per 1 kg of the internal olefin sulfonate in the internal olefin sulfonate composition. Furthermore, the above-mentioned concentration can also be achieved by subjecting the remaining bleaching agent such as an oxidizing agent to reduction treatment and decomposing it. Here, the peroxide value can be measured by the method described in the Examples.

[0102] The decolorized internal olefin sulfonate composition obtained by the production method of the present invention can be used for various applications as it is, but may further be subjected to a degassing step or a pH adjustment step, or may be subjected to purification such as desalting. Furthermore, the concentration of the active ingredient may be adjusted by operations such as adding water or concentrating, and the composition may be used by mixing with other surfactants or solvents.

[0103] Each of the above steps (adjustment step, mixing step, aging step) may be combined with a degassing step.

[0104] <pH Adjustment Step> After the bleaching step (A), a pH adjustment step may be carried out to adjust the pH of the internal olefin sulfonate composition after the bleaching treatment.

[0105] When the pH adjustment step is carried out, the pH of the internal olefin sulfonate composition after the pH adjustment is preferably 8.5 or more, more preferably 9.0 or more, from the viewpoint of suppressing an increase in the amount of impurities in the bleached internal olefin sulfonate composition, and is preferably 12.0 or less, more preferably 11.4 or less, even more preferably 11.0 or less, and still more preferably 10.5 or less, from the viewpoint of ease of handling. Here, the pH is the pH at 25°C when measured after adjusting the concentration of the internal olefin sulfonate in the internal olefin sulfonate composition after the bleaching treatment to 10 mass%.

[0106] The acid used for pH adjustment is not particularly limited, and examples thereof include inorganic acids such as sulfuric acid, hydrochloric acid, phosphoric acid, and boric acid; and organic acids such as citric acid, malic acid, maleic acid, fumaric acid, and succinic acid. These may be used alone or in combination of two or more. Among these, preferably one or more selected from the group consisting of citric acid and phosphoric acid, more preferably citric acid. Furthermore, one or more pH buffers may be used or combined to improve pH controllability. The pH buffer is not particularly limited, and examples thereof include acetic acid, citric acid, phosphoric acid, EDTA, and sodium carbonate.

[0107] The acid is preferably used in the form of an aqueous acid solution from the viewpoint of ease of handling.

[0108] The decolorized internal olefin sulfonate composition obtained by the production method of the present invention exhibits good colorfastness, a weak odor, and good storage stability, and is therefore suitable for use in a variety of applications, such as body cleansers, shampoos, laundry detergents, and dishwashing detergents.

[0109] In addition to the above, the present invention and preferred embodiments thereof are described below. <1> A method for producing a bleached internal olefin sulfonate composition, comprising a bleaching step (A) of performing, in a system where an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjusting step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, wherein the adjusting step (a1) is a step of adjusting the concentration of the alkali compound in the bleaching step (A) so that the concentration of the alkali compound after mixing the bleaching agent with the internal olefin sulfonate composition present in the system is 0.004 mmol to 0.26 mmol per 1 g of the internal olefin sulfonate. <2> A method for producing a bleached internal olefin sulfonate composition according to <1>, in which the adjusting step (a1) is performed after the mixing step (a2). <3> A method for producing a bleached internal olefin sulfonate composition according to <1>, in which the mixing step (a2) is performed after the adjusting step (a1). <4> The method for producing a bleached internal olefin sulfonate composition according to <1>, wherein the adjusting step (a1) and the mixing step (a2) are carried out in parallel. <5> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <4>, wherein the bleaching step (A) is carried out after the neutralization step or after the hydrolysis step, preferably after the hydrolysis step.<6> The method for producing a bleaching internal olefin sulfonate composition according to any one of <1> to <5>, wherein the concentration of the alkali compound in the system solution after adjusting the concentration of the alkali compound in the adjusting step (a1) is preferably 0.005 mmol or more, more preferably 0.010 mmol or more, even more preferably 0.015 mmol or more, still more preferably 0.020 mmol or more, still more preferably 0.030 mmol or more, and is preferably 0.23 mmol or less, more preferably 0.215 mmol or less, even more preferably 0.20 mmol or less, still more preferably 0.15 mmol or less, still more preferably 0.10 mmol or less, still more preferably 0.08 mmol or less, and still more preferably 0.06 mmol or less, relative to 1 g of the internal olefin sulfonate. <7> The method for producing a bleaching internal olefin sulfonate composition according to any one of <1> to <5>, wherein the concentration of the alkali compound in the system solution after adjusting the concentration of the alkali compound in the adjusting step (a1) is preferably 0.010 mmol or more, more preferably 0.015 mmol, even more preferably 0.020 mmol or more, still more preferably 0.025 mmol or more, still more preferably 0.030 mmol or more, still more preferably 0.035 mmol or more, and preferably 0.270 mmol or less, more preferably 0.240 mmol or less, even more preferably 0.210 mmol or less, still more preferably 0.240 mmol or less, still more preferably 0.220 mmol or less, still more preferably 0.210 mmol or less, still more preferably 0.20 mmol or less, still more preferably 0.18 mmol or less, still more preferably 0.16 mmol or less, still more preferably 0.10 mmol or less, and more preferably 0.08 mmol or less, relative to 1 g of the internal olefin sulfonate. <8> The method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <7>, wherein the adjustment method comprises withdrawing a liquid from the system and immediately analyzing the concentration of the alkali compound in the withdrawn liquid at room temperature.<9> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <8>, wherein the alkali compound is preferably an inorganic alkali compound, more preferably an alkali metal hydroxide, and even more preferably at least one selected from the group consisting of sodium hydroxide and potassium hydroxide. <10> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <9>, wherein the preparing step (a1) is preferably carried out in a batchwise, semi-batchwise, or continuous manner, more preferably in a continuous manner. <11> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <10>, wherein the preparing step (a1) is carried out using a loop reactor. <12> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <11>, wherein the preparing step (a1) is carried out in a continuous manner having a circulation system. <13> The method for producing a bleached internal olefin sulfonate composition according to <12>, wherein the circulation rate of the circulation system is preferably more than 0, more preferably at least 1, more preferably at least 2, even more preferably at least 3, even more preferably at least 4, and is preferably at most 20, more preferably at most 10, even more preferably at most 8. <14> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <13>, wherein the adjusting step (a1) is carried out using a reaction vessel having an impeller or an impeller-type mixer, and the peripheral speed of the impeller is 0.01 m / s or more and 50 m / s or less. <15> The method for producing a bleached internal olefin sulfonate composition according to <14>, wherein the peripheral speed of the stirring blade in the adjusting step (a1) is preferably 0.01 m / s or more, more preferably 0.05 m / s or more, even more preferably 0.1 m / s or more, still more preferably 0.3 m / s or more, still more preferably 0.9 m / s or more, still more preferably 4.7 m / s or more, still more preferably 7.0 m / s or more, still more preferably 9.0 m / s or more, and is preferably 50 m / s or less, more preferably 40 m / s or less, still more preferably 26 m / s or less, and still more preferably 15 m / s or less.<16> The method for producing a decolorized internal olefin sulfonate composition according to <14>, wherein the adjusting step (a1) is carried out continuously, and the peripheral speed of the stirring blade is preferably 0.1 m / s or more, more preferably 0.3 m / s or more, even more preferably 4 m / s or more, still more preferably 7.0 m / s or more, still more preferably 9.0 m / s or more, and is preferably 50 m / s or less, more preferably 40 m / s or less, more preferably 26 m / s or less, even more preferably 15 m / s or less. <17> The method for producing a decolorized internal olefin sulfonate composition according to <14>, wherein the adjusting step (a1) is carried out in a semi-batch manner, and the peripheral speed of the stirring blade is preferably 0.1 m / s or more, more preferably 0.3 m / s or more, even more preferably 0.5 m / s or more, still more preferably 0.7 m / s or more, and is preferably 50 m / s or less, more preferably 40 m / s or less, even more preferably 26 m / s or less, still more preferably 15 m / s or less, still more preferably 10 m / s or less, and still more preferably 8 m / s or less. <18> The method for producing a decolorized internal olefin sulfonate composition according to <14>, wherein the adjusting step (a1) is carried out batchwise, and the peripheral speed of the stirring blade is preferably 0.1 m / s or more, more preferably 0.3 m / s or more, even more preferably 0.9 m / s or more, still more preferably 1.0 m / s or more, still more preferably 1.5 m / s or more, and is preferably 50 m / s or less, more preferably 40 m / s or less, still more preferably 26 m / s or less, still more preferably 15 m / s or less, still more preferably 10 m / s or less, still more preferably 5 m / s or less, still more preferably 3 m / s or less.<19> The method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <18>, wherein the adjusting step (a1) is carried out using a reaction vessel having an impeller or an impeller-type mixer, and the ratio of the impeller diameter d to the vessel diameter D (d / D) is preferably 0.01 or more, more preferably 0.05 or more, even more preferably 0.1 or more, still more preferably 0.3 or more, still more preferably 0.4 or more, still more preferably 0.5 or more, still more preferably 0.55 or more, and is preferably less than 1, more preferably 0.9 or less, even more preferably 0.8 or less, and still more preferably 0.7 or less, and from the viewpoint of improving mixability, is preferably 0.7 or more, more preferably 0.8 or more, even more preferably 0.9 or more, and is preferably less than 1. <20> The method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <19>, wherein the adjusting step (a1) is carried out using a reaction vessel having an agitating blade or an agitating blade-type mixer, and the ratio of the agitating blade height h to the vessel height H (h / H) is preferably 0.01 or more, more preferably 0.05 or more, even more preferably 0.1 or more, still more preferably 0.3 or more, still more preferably 0.4 or more, still more preferably 0.5 or more, still more preferably 0.55 or more, and is preferably less than 1, more preferably 0.9 or less, even more preferably 0.8 or less, and still more preferably 0.7 or less, and from the viewpoint of improving mixability, is preferably 0.7 or more, more preferably 0.8 or more, even more preferably 0.9 or more, and is preferably less than 1. <21> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <20>, wherein the adjusting step (a1) is carried out using a reaction vessel having an impeller or an impeller-type mixer, and the number of impeller stages is preferably 1 or more, more preferably 2 or more, even more preferably 3 or more, and preferably 10 or less, more preferably 9 or less, even more preferably 8 or less. <22> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <21>, wherein the adjusting step (a1) is carried out under shear conditions.<23> The method for producing a bleached internal olefin sulfonate composition according to <22>, wherein the shear rate is preferably 5 / s or more, more preferably 10 / s or more, even more preferably 100 / s or more, still more preferably 500 / s or more, still more preferably 1000 / s or more, still more preferably 1500 / s or more, and preferably 100,000 / s or less, more preferably 50,000 / s or less, even more preferably 30,000 / s or less, and still more preferably 20,000 / s or less. <24> The method for producing a bleached internal olefin sulfonate composition according to <22>, wherein the adjusting step (a1) is carried out continuously, and the shear rate is preferably 100 / s or more, more preferably 500 / s or more, even more preferably 1000 / s or more, still more preferably 1500 / s or more, and preferably 100,000 / s or less, more preferably 50,000 / s or less, even more preferably 10,000 / s or less, and still more preferably 8,000 / s or less. <25> The method for producing a bleached internal olefin sulfonate composition according to <22>, wherein the adjusting step (a1) is carried out in a semi-batch manner, and the shear rate is preferably 10 / s or more, more preferably 100 / s or more, even more preferably 500 / s or more, still more preferably 1000 / s or more, still more preferably 1500 / s or more, and preferably 100000 / s or less, more preferably 50000 / s or less, even more preferably 40000 / s or less, still more preferably 30000 / s or less, still more preferably 20000 / s or less, still more preferably 10000 / s or less, still more preferably 8000 / s or less. <26> The method for producing a bleached internal olefin sulfonate composition according to <22>, wherein the adjusting step (a1) is carried out batchwise, and the shear rate is preferably 5 / s or more, more preferably 8 / s or more, even more preferably 10 / s or more, still more preferably 12 / s or more, and preferably 5000 / s or less, more preferably 1000 / s or less, even more preferably 500 / s or less, still more preferably 100 / s or less, and still more preferably 50 / s or less. <27> The stirring power (Pv) per unit liquid volume of the mixer used in the adjusting step (a1) is preferably 0.1 kW / m. ３More preferably, 0.2 kW / m ３ More preferably, 0.3 kW / m ３ or more, preferably 100 kW / m ３ Less than 50 kW / m, more preferably ３ More preferably, 30 kW / m or less ３ More preferably, 10 kW / m or less ３ More preferably, 5 kW / m or less ３ More preferably, 1 kW / m or less ３<28> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <27>, wherein the system pressure in the adjusting step (a1) is preferably 0 MPaG or more, more preferably 0.01 MPaG or more, more preferably 0.05 MPaG or more, even more preferably 0.1 MPaG or more, even more preferably 0.2 MPaG or more, and is preferably 10 MPaG or less, more preferably 5 MPaG or less, even more preferably 1 MPaG or less, and even more preferably 0.5 MPaG or less. <29> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <28>, wherein the bleaching agent is an oxidizing agent. <30> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <29>, wherein the bleaching agent is preferably at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and more preferably hydrogen peroxide. <31> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <30>, wherein the amount of the bleaching agent mixed is preferably 1 mg or more, more preferably 5 mg or more, even more preferably 10 mg or more, still more preferably 15 mg or more, still more preferably 20 mg or more, and preferably 300 mg or less, more preferably 100 mg or less, even more preferably 40 mg or less, and still more preferably 30 mg or less, relative to 1 g of internal olefin sulfonate in the internal olefin sulfonate composition. <32> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <31>, wherein the amount of the bleaching agent mixed is preferably 1 mg or more and 300 mg or less, more preferably 5 mg or more and 100 mg or less, even more preferably 10 mg or more and 40 mg or less, still more preferably 15 mg or more and 30 mg or less, and still more preferably 20 mg or more and 30 mg or less, relative to 1 g of the internal olefin sulfonate in the internal olefin sulfonate composition.<33> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <32>, wherein the bleaching agent is an aqueous solution of the bleaching agent, and the concentration of the bleaching agent in the aqueous solution is preferably 5% or more, more preferably 10% or more, even more preferably 30% or more, and preferably 70% or less, more preferably 60% or less, and even more preferably 50% or less. <34> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <33>, wherein the temperature in the mixing step (a2) is preferably 40°C or more, more preferably 60°C or more, even more preferably 70°C or more, still more preferably 80°C or more, and preferably 100°C or less, more preferably 90°C or less, and even more preferably 85°C or less. <35> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <34>, wherein the temperature in the mixing step (a2) is preferably 40° C. or higher and 100° C. or lower, more preferably 60° C. or higher and 90° C. or lower, even more preferably 70° C. or higher and 85° C. or lower, and still more preferably 80° C. or higher and 85° C. or lower. <36> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <35>, wherein the pH of the system solution in the mixing step (a2) is preferably 9.3 or higher, more preferably 9.5, even more preferably 9.8 or higher, still more preferably 10.0 or higher, still more preferably 10.2 or higher, still more preferably 10.4 or higher, and preferably 11.4 or lower, more preferably 11.3 or lower, still more preferably 11.0 or lower, still more preferably 10.8 or lower, and still more preferably 10.5 or lower. <37> The method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <36>, wherein the mixing step (a2) is preferably carried out in a batchwise, semi-batchwise, or continuous manner, more preferably in a continuous manner. <38> The method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <37>, wherein the mixing step (a2) is carried out in a continuous manner, wherein the internal olefin sulfonate composition before the decolorization treatment and the bleaching agent (an aqueous solution of the bleaching agent) are added while circulating the mixed liquid using a loop reactor, and simultaneously the decolorized mixed liquid is withdrawn.<39> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <38>, wherein the mixing step (a2) is carried out using a reaction vessel having an impeller or an impeller-type mixer, and the peripheral speed of the impeller is 0.01 m / s or more and 50 m / s or less. <40> The method for producing a bleached internal olefin sulfonate composition according to <39>, wherein in the mixing step (a2), the peripheral speed of the impeller is preferably 0.01 m / s or more, more preferably 0.05 m / s or more, even more preferably 0.1 m / s or more, still more preferably 0.3 m / s or more, still more preferably 0.9 m / s or more, still more preferably 4.7 m / s or more, still more preferably 7.0 m / s or more, still more preferably 9.0 m / s or more, and preferably 50 m / s or less, more preferably 40 m / s, even more preferably 26 m / s or less, and still more preferably 15 m / s or less. <41> The method for producing a bleached internal olefin sulfonate composition according to <39>, wherein the mixing step (a2) is carried out continuously, and the peripheral speed of the stirring blade is preferably 0.3 m / s or more, more preferably 0.9 m / s or more, even more preferably 4.7 m / s or more, still more preferably 7.0 m / s or more, still more preferably 9.0 m / s or more, and is preferably 50 m / s or less, more preferably 40 m / s, even more preferably 26 m / s or less, and still more preferably 15 m / s or less. <42> The method for producing a decolorized internal olefin sulfonate composition according to <39>, wherein the mixing step (a2) is carried out in a semi-batch manner, and the peripheral speed of the stirring blade is preferably 0.01 m / s or more, more preferably 0.1 m / s or more, even more preferably 0.3 m / s or more, still more preferably 0.9 m / s or more, and is preferably 50 m / s or less, more preferably 40 m / s, even more preferably 26 m / s or less, still more preferably 15 m / s or less, and still more preferably 10 m / s or less.<43> The method for producing a bleached internal olefin sulfonate composition according to <39>, wherein the mixing step (a2) is carried out batchwise, and the peripheral speed of the stirring blade is preferably 0.01 m / s or more, more preferably 0.1 m / s or more, even more preferably 0.3 m / s or more, still more preferably 0.9 m / s or more, still more preferably 1.5 m / s or more, and preferably 50 m / s or less, more preferably 40 m / s, even more preferably 26 m / s or less, still more preferably 15 m / s or less, still more preferably 10 m / s or less, still more preferably 5 m / s or less, still more preferably 3 m / s or less. <44> The method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <43>, wherein the mixing step (a2) is carried out using a reaction vessel having an impeller or an impeller-type mixer, and the ratio of the impeller diameter d to the vessel diameter D (d / D) is preferably 0.01 or more, more preferably 0.05 or more, even more preferably 0.1 or more, still more preferably 0.3 or more, still more preferably 0.4 or more, still more preferably 0.5 or more, still more preferably 0.55 or more, and is preferably less than 1, more preferably 0.9 or less, even more preferably 0.8 or less, and still more preferably 0.7 or less, and from the viewpoint of improving mixability, is preferably 0.7 or more, more preferably 0.8 or more, even more preferably 0.9 or more, and is preferably less than 1. <45> The method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <44>, wherein the mixing step (a2) is carried out using a reaction vessel having an impeller or an impeller-type mixer, and the ratio of the impeller height h to the vessel height H (h / H) is preferably 0.01 or more, more preferably 0.05 or more, even more preferably 0.1 or more, still more preferably 0.3 or more, still more preferably 0.4 or more, still more preferably 0.5 or more, still more preferably 0.55 or more, and is preferably less than 1, more preferably 0.9 or less, even more preferably 0.8 or less, and still more preferably 0.7 or less, and from the viewpoint of improving mixability, is preferably 0.7 or more, more preferably 0.8 or more, even more preferably 0.9 or more, and is preferably less than 1.<46> The method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <45>, wherein the mixing step (a2) is carried out using a reaction vessel having a stirring blade or a stirring blade-type mixer, and the number of stirring blades is preferably 1 or more, more preferably 2 or more, even more preferably 3 or more, and is preferably 10 or less, more preferably 9 or less, even more preferably 8 or less. <47> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <46>, wherein the shear rate in the mixing step (a2) is preferably 5 / s or more, more preferably 10 / s or more, even more preferably 100 / s or more, still more preferably 500 / s or more, still more preferably 1000 / s or more, still more preferably 1500 / s or more, and is preferably 100,000 / s or less, more preferably 80,000 / s or less, even more preferably 70,000 / s or less, still more preferably 50,000 / s or less, still more preferably 40,000 / s or less, still more preferably 30,000 / s or less, and still more preferably 20,000 / s or less. <48> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <46>, wherein the mixing step (a2) is carried out continuously, and the shear rate in the mixing step (a2) is preferably 100 / s or more, more preferably 500 / s or more, even more preferably 1000 / s or more, still more preferably 1500 / s or more, and is preferably 100,000 / s or less, more preferably 80,000 / s or less, even more preferably 70,000 / s or less, still more preferably 50,000 / s or less, still more preferably 40,000 / s or less, still more preferably 30,000 / s or less, and still more preferably 20,000 / s or less.<49> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <46>, wherein the mixing step (a2) is carried out in a semi-batch manner, and the shear rate in the mixing step (a2) is preferably 10 / s or more, more preferably 100 / s or more, even more preferably 500 / s or more, still more preferably 1000 / s or more, still more preferably 1500 / s or more, and is preferably 100,000 / s or less, more preferably 80,000 / s or less, even more preferably 70,000 / s or less, still more preferably 50,000 / s or less, still more preferably 40,000 / s or less, still more preferably 30,000 / s or less, and still more preferably 20,000 / s or less. <50> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <46>, wherein the mixing step (a2) is carried out batchwise, and the shear rate in the mixing step (a2) is preferably 5 / s or more, more preferably 8 / s or more, even more preferably 10 / s or more, still more preferably 12 / s or more, and preferably 5000 / s or less, more preferably 1000 / s or less, even more preferably 500 / s or less, still more preferably 100 / s or less, and still more preferably 30 / s or less. <51> The stirring power (Pv) per unit liquid volume of the mixer used in the mixing step (a2) is preferably 0.1 kW / m. ３ More preferably, 0.2 kW / m ３ More preferably, 0.3 kW / m ３ or more, preferably 100 kW / m ３ Less than 50 kW / m, more preferably ３ More preferably, 30 kW / m or less ３ More preferably, 10 kW / m or less ３ More preferably, 5 kW / m or less ３ More preferably, 1 kW / m or less ３<52> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <51>, wherein the system pressure in the mixing step (a2) is preferably 0 MPaG or more, more preferably 0.01 MPaG or more, more preferably 0.05 MPaG or more, even more preferably 0.1 MPaG or more, even more preferably 0.2 MPaG or more, and is preferably 10 MPaG or less, more preferably 5 MPaG or less, even more preferably 1 MPaG or less, and even more preferably 0.5 MPaG or less. <53> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <52>, wherein the adjusting step (a1) is carried out after the mixing step (a2) or when the adjusting step (a1) is carried out simultaneously with the mixing step (a2), the system pressure in the adjusting step is preferably 0 MPaG or more, more preferably 0.01 MPaG or more, even more preferably 0.05 MPaG or more, still more preferably 0.1 MPaG or more, still more preferably 0.2 MPaG or more, and is preferably 10 MPaG or less, more preferably 5 MPaG or less, even more preferably 1 MPaG or less, and still more preferably 0.5 MPaG or less. <54> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <53>, further comprising an aging step (b) after the mixing step (a2). <55> The method for producing a decolorized internal olefin sulfonate composition according to <54>, wherein the temperature range of the aging step (b) is preferably 40° C. or higher, more preferably 50° C. or higher, even more preferably 60° C. or higher, and preferably 120° C. or lower, more preferably 110° C. or lower, even more preferably 100° C. or lower. <56> The aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １) is preferably 0.1 or more, more preferably 1 or more, even more preferably 1.5 or more, and is preferably 300 or less, more preferably 200 or less, even more preferably 100 or less, still more preferably 50 or less, still more preferably 30 or less, still more preferably 10 or less, and still more preferably 5 or less. <57> The method for producing a bleached internal olefin sulfonate composition according to any of <54> to <56>, wherein the residence time in the aging step (b) is preferably 10 minutes or more, more preferably 20 minutes or more, even more preferably 30 minutes or more, still more preferably 45 minutes or more, still more preferably 60 minutes or more, and is preferably 500 minutes or less, more preferably 400 minutes or less, even more preferably 300 minutes or less, and still more preferably 200 minutes or less. <58> The method for producing a bleached internal olefin sulfonate composition according to any one of <54> to <57>, wherein the pressure in the aging step (b) is preferably 0 MPaG or more, more preferably 0.01 MPaG or more, more preferably 0.05 MPaG or more, even more preferably 0.1 MPaG or more, still more preferably 0.2 MPaG or more, and is preferably 10 MPaG or less, more preferably 5 MPaG or less, even more preferably 1 MPaG or less, and still more preferably 0.5 MPaG or less. <59> The method for producing a bleached internal olefin sulfonate composition according to any one of <54> to <58>, wherein the aging step (b) is preferably carried out continuously, semi-batchwise, or batchwise, and more preferably carried out batchwise or semi-batchwise. <60> The aging step (b) is carried out continuously,The method for producing a bleached internal olefin sulfonate composition according to any one of <54> to <59>, wherein the linear speed of the internal olefin sulfonate composition is preferably 0.001 mm / s or more, more preferably 0.005 mm / s or more, even more preferably 0.01 mm / s or more, still more preferably 0.1 mm / s or more, and is preferably 1,000 mm / s or less, more preferably 800 mm / s or less, even more preferably 500 mm / s or less, still more preferably 300 mm / s or less, still more preferably 100 mm / s or less, still more preferably 50 mm / s or less, still more preferably 10 mm / s or less, still more preferably 5 mm / s or less, and still more preferably 1 mm / s or less. <61> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <60>, wherein the bleached internal olefin sulfonate composition obtained in the bleaching step (A) has a fading rate of preferably 50% or more, more preferably 60% or more, even more preferably 63% or more, and still more preferably 65% ​​or more relative to the internal olefin sulfonate composition before bleaching. <62> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <61>, wherein the bleached internal olefin sulfonate composition obtained in the bleaching step (A) has a peroxide value of preferably 37.0 meq or less, more preferably 30.0 meq or less, even more preferably 20.0 meq or less, still more preferably 10 meq or less, still more preferably 7 meq or less, and still more preferably 5 meq or less, relative to 1 kg of internal olefin sulfonate in the internal olefin sulfonate composition. <63> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <62>, further comprising a pH adjustment step. <64> The method for producing a bleached internal olefin sulfonate composition according to <63>, wherein the pH of the internal olefin sulfonate composition after the pH adjustment is preferably 8.5 or more, more preferably 9.0 or more, and preferably 11.0 or less, more preferably 10.5 or less. <65> The method for producing a bleached internal olefin sulfonate composition according to <63> or <64>, wherein the acid used for the pH adjustment is preferably one or more selected from the group consisting of citric acid and phosphoric acid, more preferably citric acid. <66>The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <65>, wherein the internal olefin sulfonate composition is obtained by a method for producing an internal olefin sulfonate comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the number of carbon atoms in the internal olefin is preferably 10 or more, more preferably 12 or more, even more preferably 14 or more, and preferably 22 or less, more preferably 18 or less. <67> The method for producing a bleached internal olefin sulfonate composition according to <66>, wherein the internal olefin is preferably at least one selected from the group consisting of an internal olefin having 16 carbon atoms and an internal olefin having 18 carbon atoms. <68> The method for producing a bleached internal olefin sulfonate composition according to <66> or <67>, wherein the treatment temperature in the sulfonation step is preferably 0°C or more and preferably 50°C or less. <69> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <68>, wherein the concentration of sulfur trioxide gas in the sulfonation step is preferably 0.5% by volume or more, more preferably 1.0% by volume or more, and preferably 10% by volume or less, more preferably 6.0% by volume or less. <70> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <69>, wherein the amount of sulfur trioxide gas used in the sulfonation treatment is preferably 0.8 mol or more, more preferably 0.9 mol or more, even more preferably 0.95 mol or more, and preferably 1.2 mol or less, more preferably 1.10 mol or less, even more preferably 1.05 mol or less, per 1 mol of internal olefin. <71> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <70>, wherein the sulfonation reactor used in the sulfonation step is preferably a reactor equipped with an external jacket, and more preferably a falling film sulfonation reactor in which internal olefin is allowed to flow downward in the form of a thin film to react with sulfur trioxide gas. <72> The method for producing a decolorized internal olefin sulfonate composition according to <71>, wherein the sulfonation reactor is provided with an external jacket and cooled by passing cooling water through it. <73><72> The method for producing a bleached internal olefin sulfonate composition according to <72>, wherein the temperature of the cooling water passed through the outer jacket of the sulfonation reactor is preferably 0°C or higher, preferably 30°C or lower, and more preferably 20°C or lower. <74> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <73>, wherein the reaction rate of the internal olefin in the sulfonation reaction is preferably 95% or higher, more preferably 96% or higher, even more preferably 97% or higher, and preferably 99.8% or lower. <75> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <74>, wherein the alkali compound used for the neutralization is preferably an inorganic alkali compound, more preferably an alkali metal hydroxide, and even more preferably at least one selected from sodium hydroxide and potassium hydroxide. <76> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <75>, wherein the alkaline compound used in the neutralization is an alkaline aqueous solution, and the concentration of the alkaline aqueous solution, or the concentration of the mixed solution when the alkaline aqueous solution is mixed with water, is preferably 1% by mass or more, more preferably 4.5% by mass or more, even more preferably 7% by mass or more, still more preferably 10% by mass or more, still more preferably 12% by mass or more, and is preferably 50% by mass or less, more preferably 32% by mass or less, even more preferably 23% by mass or less, still more preferably 20% by mass or less, and still more preferably 18% by mass or less. <77> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <76>, wherein the concentration of the alkaline compound in the internal olefin sulfonate composition after the hydrolysis step is controlled by adjusting the amount of the alkaline compound used in the neutralization step and / or the hydrolysis step. <78>The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <77>, wherein the amount of the alkali compound used for the neutralization is preferably 1 mole or more, more preferably 1.02 mole or more, even more preferably 1.03 mole or more, still more preferably 1.034 mole or more, still more preferably 1.035 mole or more, still more preferably 1.040 mole or more, and is preferably 1.13 mole or less, more preferably 1.12 mole or less, even more preferably 1.110 mole or less, still more preferably 1.105 mole or less, still more preferably 1.10 mole or less, still more preferably 1.09 mole or less, still more preferably 1.08 mole or less, still more preferably 1.07 mole or less, and still more preferably 1.06 mole or less, relative to the amount of the sulfonic acid groups. <79> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <78>, wherein in the neutralization step, the temperature when mixing the sulfonated product with the aqueous alkaline solution and the temperature during the neutralization reaction are preferably 40° C. or lower, more preferably 35° C. or lower, even more preferably 30° C. or lower, still more preferably 25° C. or lower, and preferably 0° C. or higher, more preferably 10° C. or higher, even more preferably 15° C. or higher, and still more preferably 20° C. or higher. <80> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <79>, wherein the mixer used in the neutralization step is a stirring blade type mixer. <81> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <80>, wherein the stirring speed of the impeller mixer is preferably 5 m / s or more, more preferably 10 m / s or more, even more preferably 20 m / s or more, and is preferably 50 m / s or less, preferably 30 m / s, more preferably 27.5 m / s or less, even more preferably 25 m / s or less. <82> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <81>, wherein the neutralization step is carried out continuously by adding the sulfonated product and an aqueous alkali solution while circulating the reaction solution using a loop reactor, and simultaneously withdrawing the reaction solution. <83><84> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <83>, wherein the mixing time for mixing the sulfonated product with the aqueous alkaline solution in the neutralization step is preferably 10 minutes or more, more preferably 20 minutes or more, even more preferably 30 minutes or more, and preferably 120 minutes or less, more preferably 90 minutes or less, even more preferably 60 minutes or less, and still more preferably 50 minutes or less. <85> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <84>, wherein the concentration of the internal olefin sulfonate in the neutralization product is preferably 40% by mass or more, more preferably 45% by mass or more, even more preferably 48% by mass or more, and preferably 65% ​​by mass or less, more preferably 60% by mass or less. <85> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <84>, wherein the temperature during hydrolysis in the hydrolysis step is preferably 120°C or higher, more preferably 140°C or higher, even more preferably 160°C or higher, and preferably 220°C or lower, more preferably 200°C or lower. <86> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <85>, wherein the treatment time for the hydrolysis step is preferably 30 minutes or longer, more preferably 45 minutes or longer, more preferably 1 hour or longer, and preferably 4 hours or shorter, more preferably 3 hours or shorter. <87> The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <86>, wherein the average number of double bonds in the raw material olefins of the internal olefin sulfonic acid is preferably 3 or higher, more preferably 3.5 or higher, even more preferably 3.8 or higher, and preferably 5 or lower, more preferably 4.5 or lower, even more preferably 4.4 or lower, and still more preferably 4.3 or lower. <88> The method for producing a bleaching internal olefin sulfonate composition according to any one of <1> to <87>, wherein the internal olefin sulfonate preferably contains at least one internal olefin sulfonate selected from the group consisting of internal olefin sulfonates having 16 carbon atoms and internal olefin sulfonates having 18 carbon atoms. <89>The method for producing a bleached internal olefin sulfonate composition according to any one of <66> to <88>, wherein the concentration of the alkali compound in the internal olefin sulfonate composition obtained in the hydrolysis step and / or before carrying out the bleaching step (A) is preferably 0.010 mmol or more, more preferably 0.015 mmol or more, even more preferably 0.020 mmol or more, still more preferably 0.025 mmol or more, still more preferably 0.029 mmol or more, and preferably 0.27 mmol or less, more preferably 0.240 mmol or less, even more preferably 0.210 mmol or less, and also preferably 0.27 mmol or less, more preferably 0.240 mmol or less, even more preferably 0.220 mmol or less, still more preferably 0.210 mmol or less, still more preferably 0.20 mmol or less, still more preferably 0.18 mmol or less, still more preferably 0.16 mmol or less, still more preferably 0.10 mmol or less, and more preferably 0.08 mmol or less, relative to 1 g of internal olefin sulfonate in the internal olefin sulfonate composition. <90> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, carrying out an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the internal olefin sulfonate after the hydrolysis step comprises at least one or more selected from the group consisting of an internal olefin sulfonate having 16 carbon atoms and an internal olefin sulfonate having 18 carbon atoms, and the average double bond positions of the raw material olefins in the internal olefin sulfonate are 3.8 to 4.4,the alkali compound used in the neutralization is at least one selected from sodium hydroxide and potassium hydroxide, the agitation speed of the agitator blade type mixer in the neutralization step is 20 m / s or more and 200 m / s or less, the concentration of the internal olefin sulfonate in the neutralization product is 45 mass% or more and 65 mass% or less, the temperature during the neutralization reaction is 0°C or more and 35°C or less, and neutralization is performed for a residence time in the neutralization device of 30 minutes or more and 120 minutes or less, and the concentration of the alkali compound in the internal olefin sulfonate composition is adjusted by adjusting the amount of the alkali compound used in the neutralization step; the internal olefin sulfonate composition is a method for controlling the concentration of the alkali compound in the internal olefin sulfonate composition after the hydrolysis step by a method of adjusting the amount of the alkali compound used in the neutralization step, the temperature during hydrolysis in the hydrolysis step is 160°C or more and 220°C or less, and the treatment time of the hydrolysis step is 1 hour or more and 4 hours or less, the adjusting step (a1) is continuous, the circulation ratio is more than 0 and not more than 20, a reaction vessel having an agitator blade or an agitator-type mixer is used in the adjusting step (a1), d / D is 0.01 or more and less than 1, and h / H is 0.01 or more and less than 1, the concentration of the alkali compound in the system is adjusted in the adjusting step (a1) to be 0.005 mmol or more and 0.26 mmol or less per g of the internal olefin sulfonate after the mixing step (a2), the mixing step (a2) is continuous, the pH of the liquid in the system in the mixing step (a2) is 9.3 or more and 11.4, the mixing step (a2) is continuous, a reaction vessel having an agitator blade or an agitator-type mixer is used in the mixing step (a2), d / D is 0.01 or more and less than 1, h / H is 0.01 or more and less than 1, the peripheral speed of the agitator blade is 0.01 m / s or more and 50 m / s or less, and the pressure in the system is 0 MPaG or more and 10 MPaG or less, The aging step (b) is a continuous process, the temperature range is 40°C or more and 100°C or less, and the residence time is 10 minutes or more and 500 minutes or less. The aging step (b) is carried out using a vertical cylindrical reactor, and H １ / D １is 0.1 or more and 300 or less, the linear velocity of the internal olefin sulfonate composition is 0.01 mm / s or more and 1000 mm / s or less, and the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less. <91> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the internal olefin sulfonate after the hydrolysis step comprises at least one or more selected from the group consisting of an internal olefin sulfonate having 16 carbon atoms and an internal olefin sulfonate having 18 carbon atoms, and the average double bond positions of the raw material olefins in the internal olefin sulfonate are 3.8 to 4.4, the alkali compound used in the neutralization is at least one selected from sodium hydroxide and potassium hydroxide, the agitation speed of the agitator blade type mixer in the neutralization step is 20 m / s or more and 200 m / s or less, the concentration of the internal olefin sulfonate in the neutralization product is 45 mass% or more and 65 mass% or less, the temperature during the neutralization reaction is 0°C or more and 35°C or less, and neutralization is performed for a residence time in the neutralization device of 30 minutes or more and 120 minutes or less, and the concentration of the alkali compound in the internal olefin sulfonate composition is adjusted by adjusting the amount of the alkali compound used in the neutralization step; the internal olefin sulfonate composition is a method for controlling the concentration of the alkali compound in the internal olefin sulfonate composition after the hydrolysis step by a method of adjusting the amount of the alkali compound used in the neutralization step, the temperature during hydrolysis in the hydrolysis step is 160°C or more and 220°C or less, and the treatment time of the hydrolysis step is 1 hour or more and 4 hours or less,the adjusting step (a1) is continuous, the circulation ratio is more than 0 and not more than 20, a reaction vessel having an agitator blade or an agitator-type mixer is used in the adjusting step (a1), d / D is 0.01 or more and less than 1, and h / H is 0.01 or more and less than 1, the concentration of the alkali compound in the system is adjusted in the adjusting step (a1) to be 0.005 mmol or more and 0.26 mmol or less per g of the internal olefin sulfonate after the mixing step (a2), the mixing step (a2) is continuous, the pH of the liquid in the system in the mixing step (a2) is 9.3 or more and 11.4, the mixing step (a2) is continuous, the reaction vessel having an agitator blade or an agitator-type mixer is used in the mixing step (a2), d / D is 0.01 or more and less than 1, h / H is 0.01 or more and less than 1, the shear rate is 5 / s or more and 100,000 / s or less, and the pressure in the system is 0 MPaG or more and 10 MPaG or less, The aging step (b) is a continuous process, the temperature range is 40°C or more and 100°C or less, and the residence time is 10 minutes or more and 500 minutes or less. The aging step (b) is carried out using a vertical cylindrical reactor, and H １ / D １is 0.1 or more and 300 or less, the linear velocity of the internal olefin sulfonate composition is 0.01 mm / s or more and 1000 mm / s or less, and the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less. <92> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the internal olefin sulfonate after the hydrolysis step comprises at least one selected from the group consisting of an internal olefin sulfonate having 16 carbon atoms and an internal olefin sulfonate having 18 carbon atoms, and the average double bond positions of the raw material olefins in the internal olefin sulfonate are 3.8 to 4.4, the alkali compound used in the neutralization is at least one selected from sodium hydroxide and potassium hydroxide, the agitation speed of the agitator blade type mixer in the neutralization step is 20 m / s or more and 200 m / s or less, the concentration of the internal olefin sulfonate in the neutralization product is 45 mass% or more and 65 mass% or less, the temperature during the neutralization reaction is 0°C or more and 35°C or less, and neutralization is performed for a residence time in the neutralization device of 30 minutes or more and 120 minutes or less, and the concentration of the alkali compound in the internal olefin sulfonate composition is adjusted by adjusting the amount of the alkali compound used in the neutralization step; the internal olefin sulfonate composition is a method for controlling the concentration of the alkali compound in the internal olefin sulfonate composition after the hydrolysis step by a method of adjusting the amount of the alkali compound used in the neutralization step, the temperature during hydrolysis in the hydrolysis step is 160°C or more and 220°C or less, and the treatment time of the hydrolysis step is 1 hour or more and 4 hours or less,the adjusting step (a1) is continuous, the circulation ratio is more than 0 and not more than 20, a reaction vessel having an agitating blade or an agitating blade type mixer is used in the adjusting step (a1), d / D is 0.01 or more and less than 1, and h / H is 0.01 or more and less than 1, the concentration of the alkali compound in the system in the adjusting step (a1) is adjusted to 0.005 mmol or more and 0.26 mmol or less per g of the internal olefin sulfonate after the mixing step (a2), the mixing step (a2) is continuous, the pH of the liquid in the system in the mixing step (a2) is 9.3 or more and 11.4, the mixing step (a2) is continuous, the reaction vessel having an agitating blade or an agitating blade type mixer is used in the mixing step (a2), d / D is 0.01 or more and less than 1, and h / H is 0.01 or more and less than 1, and the required stirring power (Pv) is 0.1 kW / m ３ More than 100kW / m ３ the system pressure is 0 MPaG or more and 10 MPaG or less, the aging step (b) is a continuous type, the temperature range is 40°C or more and 100°C or less, the residence time is 10 minutes or more and 500 minutes or less, the aging step (b) is carried out using a vertical cylindrical reactor, and H １ / D １is 0.1 or more and 300 or less, the linear velocity of the internal olefin sulfonate composition is 0.01 mm / s or more and 1000 mm / s or less, and the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less. <93> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a bleaching step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), a method for controlling the concentration of an alkali compound in an internal olefin sulfonate composition after a hydrolysis step by a method selected from a method for adjusting the amount of an alkali compound used in a neutralization step and a method for adjusting the amount of an alkali compound in a hydrolysis step, wherein the number of carbon atoms in the internal olefin sulfonate after a hydrolysis step is 10 to 22, the average number of double bond positions in the internal olefin sulfonate is 3 to 5, the alkali compound used in the neutralization is an inorganic alkali compound, the stirring speed of the stirring blade type mixer in the neutralization step is 5 to 200 m / s, the concentration of the internal olefin sulfonate in the neutralization product is 40 to 65 mass%, the temperature during the neutralization reaction is 0 to 40°C, and the internal olefin sulfonate is neutralized for a residence time in a neutralization device of 10 to 120 minutes, and the concentration of the alkali compound in the internal olefin sulfonate composition after a hydrolysis step is controlled by a method for adjusting the amount of an alkali compound used in a neutralization step and a method for adjusting the amount of an alkali compound in a hydrolysis step,the adjusting step (a1) is carried out in a batchwise, semi-batchwise, or continuous manner, the circulation ratio is more than 0 and not more than 20, a reaction vessel having an agitator blade or an agitator-type mixer is used in the adjusting step (a1), d / D is 0.01 or more and less than 1, and h / H is 0.01 or more and less than 1, and the concentration of the alkali compound in the system in the adjusting step (a1) is adjusted to 0.005 mmol or more and 0.26 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), The mixing step (a2) is continuous, the pH of the liquid in the system in the mixing step (a2) is 9.3 to 11.4, a reaction vessel having an agitator blade or an agitator-type mixer is used in the mixing step (a2), d / D is 0.01 to less than 1, h / H is 0.01 to less than 1, the peripheral speed of the agitator blade is 0.01 to 50 m / s, and the system pressure is 0 MPaG to 10 MPaG, the aging step (b) is continuous, the temperature range is 40°C to 120°C, and the residence time is 10 to 500 minutes, and the aging step (b) is performed using a vertical cylindrical reactor, and H １ / D １is 0.1 or more and 300 or less, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less. <94> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), a method for controlling the concentration of an alkali compound in an internal olefin sulfonate composition after a hydrolysis step by a method selected from a method for adjusting the amount of an alkali compound used in a neutralization step and a method for adjusting the amount of an alkali compound in a hydrolysis step, wherein the number of carbon atoms in the internal olefin sulfonate after a hydrolysis step is 10 to 22, the average number of double bond positions in the internal olefin sulfonate is 3 to 5, the alkali compound used in the neutralization is an inorganic alkali compound, the stirring speed of the stirring blade type mixer in the neutralization step is 5 to 200 m / s, the concentration of the internal olefin sulfonate in the neutralization product is 40 to 65 mass%, the temperature during the neutralization reaction is 0 to 40°C, and the internal olefin sulfonate is neutralized for a residence time in a neutralization device of 10 to 120 minutes, and the concentration of the alkali compound in the internal olefin sulfonate composition after a hydrolysis step is controlled by a method for adjusting the amount of an alkali compound used in a neutralization step and a method for adjusting the amount of an alkali compound in a hydrolysis step,the adjusting step (a1) is carried out in a batchwise, semi-batchwise, or continuous manner, the circulation ratio is more than 0 and not more than 20, a reaction vessel having an agitator blade or an agitator-type mixer is used in the adjusting step (a1), d / D is 0.01 or more and less than 1, and h / H is 0.01 or more and less than 1, the concentration of the alkali compound in the system is adjusted in the adjusting step (a1) to be 0.005 mmol or more and 0.26 mmol or less per g of the internal olefin sulfonate after the mixing step (a2), the mixing step (a2) is continuous, the pH of the liquid in the system in the mixing step (a2) is 9.3 or more and 11.4, the mixing step (a2) is carried out in a reaction vessel having an agitator blade or an agitator-type mixer is used, d / D is 0.01 or more and less than 1, and h / H is 0.01 or more and less than 1, the shear rate is 5 / s or more and 100,000 / s or less, and the pressure in the system is 0 MPaG or more and 10 MPaG or less, The aging step (b) is a continuous process, the temperature range is 40°C or more and 120°C or less, and the residence time is 10 minutes or more and 500 minutes or less. The aging step (b) is carried out using a vertical cylindrical reactor, and H １ / D １is 0.1 or more and 300 or less, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less. <95> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a bleaching step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), a method for controlling the concentration of an alkali compound in an internal olefin sulfonate composition after a hydrolysis step by a method selected from a method for adjusting the amount of an alkali compound used in a neutralization step and a method for adjusting the amount of an alkali compound in a hydrolysis step, wherein the number of carbon atoms in the internal olefin sulfonate after a hydrolysis step is 10 to 22, the average number of double bond positions in the internal olefin sulfonate is 3 to 5, the alkali compound used in the neutralization is an inorganic alkali compound, the stirring speed of the stirring blade type mixer in the neutralization step is 5 to 200 m / s, the concentration of the internal olefin sulfonate in the neutralization product is 40 to 65 mass%, the temperature during the neutralization reaction is 0 to 40°C, and the internal olefin sulfonate is neutralized for a residence time in a neutralization device of 10 to 120 minutes, and the concentration of the alkali compound in the internal olefin sulfonate composition after a hydrolysis step is controlled by a method for adjusting the amount of an alkali compound used in a neutralization step and a method for adjusting the amount of an alkali compound in a hydrolysis step,the adjusting step (a1) is carried out in a batch, semi-batch or continuous manner, the circulation ratio is more than 0 and not more than 20, a reaction vessel having an agitator blade or an agitator-type mixer is used in the adjusting step (a1), d / D is 0.01 or more and less than 1, and h / H is 0.01 or more and less than 1, the concentration of the alkali compound in the system in the adjusting step (a1) is adjusted to 0.005 mmol or more and 0.26 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), the mixing step (a2) is continuous, the pH of the liquid in the system in the mixing step (a2) is 9.3 or more and 11.4, the mixing step (a2) is carried out in a reaction vessel having an agitator blade or an agitator-type mixer is used, d / D is 0.01 or more and less than 1, and h / H is 0.01 or more and less than 1, and the required stirring power (Pv) is 0.1 kW / m ３ More than 100kW / m ３ The aging step (b) is a continuous process, the temperature range is 40°C or higher and 120°C or lower, and the residence time is 10 minutes or higher and 500 minutes or lower, and the aging step (b) is carried out using a vertical cylindrical reactor, and H １ / D １ is 0.1 or more and 300 or less, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less. <96> A method for producing a bleached internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, the method comprising: a bleaching step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present; and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, the method further comprising: an aging step (b) after the mixing step (a2), wherein the required stirring power (Pv) in the mixing step (a2) is 0.1 kW / m ３ More than 100kW / m３ <97> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, which is as follows: <97> A method for producing a bleached internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a bleaching step (A) in which, after the hydrolysis step, a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present is subjected to an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the required stirring power (Pv) in the mixing step (a2) is 0.3 kW / m ３ More than 30kW / m ３ <98> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, which is as follows: <98> A method for producing a bleached internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a bleaching step (A) in which, after the hydrolysis step, a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present is subjected to an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the required stirring power (Pv) in the mixing step (a2) is 0.2 kW / m ３ More than 50kW / m ３<99> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, which is as follows: <99> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, carrying out, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the shear rate in the mixing step (a2) is 5 / s or more and 100,000 / s or less. <100> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising, after the mixing step (a2), an aging step (b), wherein the shear rate in the mixing step (a2) is 1500 / s or more and 20000 / s or less.<101> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising, after the mixing step (a2), an aging step (b), wherein the shear rate in the mixing step (a2) is 500 / s or more and 50,000 / s or less. <102> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less.<103> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 9.0 m / s or more and 15 m / s or less. <104> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.9 m / s or more and 26 m / s or less.<105> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2). <106> A method for producing a decolorized internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the concentration of the alkali compound in the adjusting step (a1) is 0.030 mmol or more and 0.06 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2).<107> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the concentration of the alkali compound in the adjusting step (a1) is 0.020 mmol or more and 0.20 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2). <108> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an agitating blade or an agitating blade-type mixer, the peripheral speed of the agitating blade is 0.01 m / s or more and 50 m / s or less, and the pH of the liquid in the system in the mixing step (a2) is 9.3 or more and 11.4 or less. The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>.<109> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an impeller or an impeller-type mixer, the peripheral speed of the impeller is 0.01 m / s or more and 50 m / s or less, and the pH of the liquid in the system in the mixing step (a2) is 10.0 or more and 10.5 or less. The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>. <110> A method for producing a bleached internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an impeller or an impeller-type mixer, the peripheral speed of the impeller is 0.01 m / s or more and 50 m / s or less, and the pH of the liquid in the system in the mixing step (a2) is 9.8 or more and 11.0 or less.<111> A method for producing a decolorized internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present; and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), and the adjusting step (a1) is carried out batchwise. <112> A method for producing a decolorized internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), and the adjusting step (a1) is carried out in a semi-batch manner.<113> A method for producing a decolorized internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present; and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), and the adjusting step (a1) is carried out continuously.<114> A method for producing a bleached internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, an adjusting step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprises an aging step (b) after the mixing step (a2), wherein: when the mixing step (a2) uses the reaction vessel having an impeller or an impeller-type mixer, the peripheral speed of the impeller is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out batchwise; and the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), <89> The method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, wherein the adjusting step (a1) is carried out in a batchwise, semi-batchwise, or continuous manner.<115> A method for producing a decolorized internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an impeller or an impeller-type mixer, the peripheral speed of the impeller is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is performed in a semi-batch manner, <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), and the adjusting step (a1) is carried out in a batchwise, semi-batchwise, or continuous manner.<116> A method for producing a decolorized internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an agitating blade or an agitating blade-type mixer, the peripheral speed of the agitating blade is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out continuously, <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), and the adjusting step (a1) is carried out in a batchwise, semi-batchwise, or continuous manner.<117> A method for producing a decolorized internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an impeller or an impeller-type mixer, the peripheral speed of the impeller is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), and the adjusting step (a1) is carried out continuously, with a circulation ratio of more than 0 times and 20 times or less.<118> A method for producing a decolorized internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an impeller or an impeller-type mixer, the peripheral speed of the impeller is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), and the adjusting step (a1) is carried out continuously at a circulation rate of 4 times or more and 8 times or less.<119> A method for producing a decolorized internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an impeller or an impeller-type mixer, the peripheral speed of the impeller is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), and the adjusting step (a1) is carried out continuously at a circulation rate of 2 times or more and 10 times or less.<120> A method for producing a bleached internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, an adjusting step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprises an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an agitating blade or an agitating blade-type mixer, the peripheral speed of the agitating blade is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, and wherein the concentration of the alkali compound in the adjusting step (a1) is 0.01 m / s or more per 1 g of internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out continuously at a circulation rate of more than 0 times and not more than 20 times; and the aging step (b) is carried out continuously at a linear velocity of the internal olefin sulfonate composition of 0.001 mm / s or more and 1000 mm / s or less.<121> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an agitating blade or an agitating blade-type mixer, the peripheral speed of the agitating blade is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is performed in a batchwise, semi-batchwise, or continuous manner, <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out continuously at a circulation rate of more than 0 times and 20 times or less, and the aging step (b) is carried out continuously at a linear velocity of the internal olefin sulfonate composition of 0.1 mm / s or more and 1 mm / s or less.<122> A method for producing a decolorized internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an impeller or an impeller-type mixer, the peripheral speed of the impeller is 0.01 m / s or more and 100 m / s or less, and the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and 20 times or less, and the aging step (b) is carried out continuously and the linear speed of the internal olefin sulfonate composition is 0.005 mm / s or more and 800 mm / s or less.<123> A method for producing a decolorized internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an impeller or an impeller-type mixer, the peripheral speed of the impeller is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the internal olefin sulfonate; the adjusting step (a1) is carried out continuously at a circulation rate of more than 0 times and 20 times or less; the aging step (b) is carried out continuously at a linear velocity of the internal olefin sulfonate composition of 0.001 mm / s or more and 1000 mm / s or less; the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<124> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the ρ is 0.1 or more and 300 or less. <124> A method for producing a bleached internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a bleaching step (A) in which, after the hydrolysis step, a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present is subjected to an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an agitating blade or an agitating blade-type mixer, the peripheral speed of the agitating blade is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and 20 times or less, the aging step (b) is carried out continuously and the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<125> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the saturation ratio ... <126> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a bleaching step (A) in which, after the hydrolysis step, a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present is subjected to an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses the reaction vessel having an agitating blade or an agitating blade-type mixer, the peripheral speed of the agitating blade is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and 20 times or less, the aging step (b) is carried out continuously and the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １) is 1 or more and 50 or less. <126> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a bleaching step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having an impeller or the impeller-type mixer, the peripheral speed of the impeller is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per g of the internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out in a continuous manner and the circulation ratio is more than 0 times and 20 times or less, the aging step (b) is carried out in a continuous manner and the linear speed of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, The aging step (b) is carried out using the vertical cylindrical reactor, and the height H １ and reactor inner diameter D １ The ratio (H １ / D １<89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the β-amino group is 0.1 or more and 300 or less. <127> A method for producing a bleached internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein, when the mixing step (a2) uses a reaction vessel having an agitating blade or an agitating blade-type mixer, the peripheral speed of the agitating blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, and the bleaching agent is hydrogen peroxide, the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and 20 times or less, the aging step (b) is carried out continuously and the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<128> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the saturation ratio (s) of a raw material olefin sulfonate composition is 0.1 or more and 300 or less. <128> A method for producing a bleached internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and further comprising a bleaching step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out in a continuous manner, and the circulation ratio is more than 0 times and 20 times or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<129> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less. <129> A method for producing a bleached internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and further comprising a bleaching step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out in a continuous manner, and the circulation ratio is more than 0 times and 20 times or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<130> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pressure in the aging step (b) is 0.2 MPaG or more and 0.5 MPaG or less. <131> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, carrying out, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising, after the mixing step (a2), an aging step (b), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out in a continuous manner, and the circulation ratio is more than 0 times and 20 times or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<131> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pressure in the aging step (b) is 0.05 MPaG or more and 1 MPaG or less. <132> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising, after the mixing step (a2), an aging step (b), When the mixing step (a2) uses the reaction vessel having an impeller or the impeller-type mixer, the peripheral speed of the impeller is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per g of the internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out in a continuous manner and the circulation ratio is more than 0 times and 20 times or less, the aging step (b) is carried out in a continuous manner, and the linear speed of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, The aging step (b) is carried out using the vertical cylindrical reactor, and the height H １ and reactor inner diameter D １ The ratio (H １ / D １<132> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, wherein the saturation ratio (Sr) of a raw material olefin is 0.1 or more and 300 or less, and the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less. <132> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out in a continuous manner, and the circulation ratio is more than 0 times and 20 times or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<133> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pressure in the aging step (b) is from 0 to 10 MPaG, and the residence time in the aging step (b) is from 60 to 200 minutes. <133> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out in a continuous manner, and the circulation ratio is more than 0 times and 20 times or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<134> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pressure in the aging step (b) is from 0 MPaG to 10 MPaG, and the residence time in the aging step (b) is from 30 minutes to 400 minutes. <134> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out in a continuous manner, and the circulation ratio is more than 0 times and 20 times or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<135> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40° C. or more and 120° C. or less. <135> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and further comprising a decolorization step (A) in which, after the hydrolysis step, a system containing an internal olefin sulfonate composition is present, the system is subjected to an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out in a continuous manner, and the circulation ratio is more than 0 times and 20 times or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<136> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 60° C. or more and 100° C. or less. <136> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and further comprising a decolorization step (A) in which, after the hydrolysis step, a system containing an internal olefin sulfonate composition is present, the system is subjected to an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out in a continuous manner, and the circulation ratio is more than 0 times and 20 times or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 50° C. or more and 110° C. or less. <137> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein, after the hydrolysis step, the method comprises a decolorization step (A) of performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out in a continuous manner, the circulation ratio is more than 0 times and 20 times or less, and the system pressure in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<138> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40° C. or more and 120° C. or less. <138> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and further comprising a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out in a continuous manner, the circulation ratio is more than 0 times and 20 times or less, and the system pressure in the adjusting step (a1) is 0.2 MPaG or more and 0.5 MPaG or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40° C. or more and 120° C. or less. <139> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein, after the hydrolysis step, the method comprises a decolorization step (A) of performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out in a continuous manner, the circulation ratio is more than 0 times and 20 times or less, and the system pressure in the adjusting step (a1) is 0.05 MPaG or more and 1 MPaG or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<140> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40° C. or more and 120° C. or less. <141> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and further comprising a decolorization step (A) in which, after the hydrolysis step, a system containing an internal olefin sulfonate composition is present, the system is subjected to an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the system pressure in the mixing step (a2) is 0 MPaG or more and 10 MPaG or less, the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out in a continuous manner, the circulation ratio is more than 0 times and 20 times or less, and the system pressure in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<141> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40° C. or more and 120° C. or less. <141> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and further comprising a decolorization step (A) in which, after the hydrolysis step, a system containing an internal olefin sulfonate composition is present, the system is subjected to an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the system pressure in the mixing step (a2) is 0.2 MPaG or more and 0.5 MPaG or less, the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out in a continuous manner, the circulation ratio is more than 0 times and 20 times or less, and the system pressure in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<142> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40° C. or more and 120° C. or less. <142> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and further comprising a decolorization step (A) in which, after the hydrolysis step, a system containing an internal olefin sulfonate composition is present, the system is subjected to an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the system pressure in the mixing step (a2) is 0.05 MPaG or more and 5 MPaG or less, the concentration of the alkali compound in the adjusting step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate after the mixing step (a2), the adjusting step (a1) is carried out in a continuous manner, the circulation ratio is more than 0 times and 20 times or less, and the system pressure in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40°C or more and 120°C or less.<143> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method further comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprises an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the system pressure in the mixing step (a2) is 0 MPaG or more and 10 MPaG or less, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and 20 times or less, the pressure inside the system in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less, when the reaction vessel having an agitator or an agitator-type mixer is used in the adjusting step (a1), the peripheral speed of the agitator is 0.01 m / s or more and 50 m / s or less, the ratio of the agitator diameter d to the vessel diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the agitator height h to the vessel height H (h / H) is 0.01 or more and less than 1, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor. １ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40°C or more and 120°C or less.<144> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and further comprising a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses a reaction vessel having an impeller or an impeller-type mixer, the peripheral speed of the impeller is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the system pressure in the mixing step (a2) is 0 MPaG or more and 10 MPaG or less, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and not more than 20 times, the pressure inside the system in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less, when the reaction vessel having an agitator or an agitator-type mixer is used in the adjusting step (a1), the peripheral speed of the agitator is 9.0 m / s or more and 15 m / s or less, the ratio of the agitator diameter d to the vessel diameter D (d / D) is 0.55 or more and less than 1, and the ratio of the agitator height h to the vessel height H (h / H) is 0.50 or more and less than 1, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor. １ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40°C or more and 120°C or less.<145> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and further comprising a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the system pressure in the mixing step (a2) is 0 MPaG or more and 10 MPaG or less, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and 20 times or less, the pressure inside the system in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less, when the reaction vessel having an agitator or an agitator-type mixer is used in the adjusting step (a1), the peripheral speed of the agitator is 0.3 m / s or more and 26 m / s or less, the ratio of the agitator diameter d to the vessel diameter D (d / D) is 0.1 or more and less than 1, and the ratio of the agitator height h to the vessel height H (h / H) is 0.1 or more and less than 1, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor. １ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40°C or more and 120°C or less.<146> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and further comprising a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the system pressure in the mixing step (a2) is 0 MPaG or more and 10 MPaG or less, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the internal olefin sulfonate; the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and not more than 20 times; the system pressure in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less; when the reaction vessel having an agitator or an agitator-type mixer is used in the adjusting step (a1), the peripheral speed of the agitator is 0.01 m / s or more and 50 m / s or less, and the ratio (d / D) of the agitator diameter d to the vessel diameter D is 0.5 or more and less than 1; the aging step (b) is carried out continuously and the linear speed of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less; １ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40°C or more and 120°C or less.<147> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method further comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprises an aging step (b) after the mixing step (a2), When the mixing step (a2) uses the reaction vessel having the stirring blade or the stirring blade-type mixer, the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batchwise, semi-batchwise, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the system pressure in the mixing step (a2) is 0 MPaG or more and 10 MPaG or less, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the internal olefin sulfonate; the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and not more than 20 times; the system pressure in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less; when the reaction vessel having an agitator or an agitator-type mixer is used in the adjusting step (a1), the peripheral speed of the agitator is 0.01 m / s or more and 50 m / s or less, and the ratio (h / H) of the agitator height h to the vessel height H is 0.3 or more and less than 1; the aging step (b) is carried out continuously and the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less; １ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40°C or more and 120°C or less.<148> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and further comprising a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the system pressure in the mixing step (a2) is 0 MPaG or more and 10 MPaG or less, when the reaction vessel having the stirring blade or the stirring blade type mixer is used in the mixing step (a2), the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, the ratio of the stirring blade diameter d to the vessel diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the stirring blade height h to the vessel height H (h / H) is 0.01 or more and less than 1, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and 20 times or less, the pressure inside the system in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less, when the reaction vessel having an agitator or an agitator-type mixer is used in the adjusting step (a1), the peripheral speed of the agitator is 0.01 m / s or more and 50 m / s or less, the ratio of the agitator diameter d to the vessel diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the agitator height h to the vessel height H (h / H) is 0.01 or more and less than 1, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor.１ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40°C or more and 120°C or less.<149> A method for producing a decolorized internal olefin sulfonate composition, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and further comprising a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the system pressure in the mixing step (a2) is 0 MPaG or more and 10 MPaG or less, when the reaction vessel having an agitator blade or an agitator blade-type mixer is used in the mixing step (a2), the peripheral speed of the agitator blade is 9.0 m / s or more and 15 m / s or less, the ratio of the agitator blade diameter d to the vessel diameter D (d / D) is 0.55 or more and less than 1, and the ratio of the agitator blade height h to the vessel height H (h / H) is 0.55 or more and less than 1, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and 20 times or less, the pressure inside the system in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less, when the reaction vessel having an agitator or an agitator-type mixer is used in the adjusting step (a1), the peripheral speed of the agitator is 0.01 m / s or more and 50 m / s or less, the ratio of the agitator diameter d to the vessel diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the agitator height h to the vessel height H (h / H) is 0.01 or more and less than 1, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor.１ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40°C or more and 120°C or less.<150> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method further comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprises an aging step (b) after the mixing step (a2), the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the system pressure in the mixing step (a2) is 0 MPaG or more and 10 MPaG or less, when the reaction vessel having an agitator or an agitator-type mixer is used in the mixing step (a2), the peripheral speed of the agitator is 0.05 m / s or more and 40 m / s or less, the ratio of the agitator diameter d to the vessel diameter D (d / D) is 0.3 or more and less than 1, and the ratio of the agitator height h to the vessel height H (h / H) is 0.3 or more and less than 1, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and 20 times or less, the pressure inside the system in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less, when the reaction vessel having an agitator or an agitator-type mixer is used in the adjusting step (a1), the peripheral speed of the agitator is 0.01 m / s or more and 50 m / s or less, the ratio of the agitator diameter d to the vessel diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the agitator height h to the vessel height H (h / H) is 0.01 or more and less than 1, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor.１ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40°C or more and 120°C or less.<151> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method further comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present; and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the system pressure in the mixing step (a2) is 0 MPaG or more and 10 MPaG or less, when the reaction vessel having the stirring blade or the stirring blade type mixer is used in the mixing step (a2), the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, and the ratio (d / D) of the stirring blade diameter d to the vessel diameter D is 0.5 or more and less than 1, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and 20 times or less, the pressure inside the system in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less, when the reaction vessel having an agitator or an agitator-type mixer is used in the adjusting step (a1), the peripheral speed of the agitator is 0.01 m / s or more and 50 m / s or less, the ratio of the agitator diameter d to the vessel diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the agitator height h to the vessel height H (h / H) is 0.01 or more and less than 1, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor. １ and reactor inner diameter D １ The ratio (H１ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40°C or more and 120°C or less.<152> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method further comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprises an aging step (b) after the mixing step (a2), the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner, the decolorizing agent is at least one selected from the group consisting of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, the system pressure in the mixing step (a2) is 0 MPaG or more and 10 MPaG or less, when the reaction vessel having the stirring blade or the stirring blade type mixer is used in the mixing step (a2), the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less, and the ratio (h / H) of the stirring blade height h to the vessel height H is 0.3 or more and less than 1, the concentration of the alkali compound in the adjusting step (a1) after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the internal olefin sulfonate, the adjusting step (a1) is carried out continuously and the circulation ratio is more than 0 times and 20 times or less, the pressure inside the system in the adjusting step (a1) is 0 MPaG or more and 10 MPaG or less, when the reaction vessel having an agitator or an agitator-type mixer is used in the adjusting step (a1), the peripheral speed of the agitator is 0.01 m / s or more and 50 m / s or less, the ratio of the agitator diameter d to the vessel diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the agitator height h to the vessel height H (h / H) is 0.01 or more and less than 1, The aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor. １ and reactor inner diameter D １ The ratio (H１ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40°C or more and 120°C or less. <153> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising, after the mixing step (a2), an aging step (b), wherein the aging step (b) is performed continuously, and the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less. <154> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is performed continuously, and the linear velocity of the internal olefin sulfonate composition is 0.1 mm / s or more and 1 mm / s or less.<155> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising, after the mixing step (a2), an aging step (b), wherein the aging step (b) is performed continuously, and the linear velocity of the internal olefin sulfonate composition is 0.005 mm / s or more and 100 mm / s or less. <156> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the method comprises a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is performed using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is set to 100. １ and reactor inner diameter D １ The ratio (H １ / D １<157> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, wherein the saturation ratio (Sr) of a raw material olefin sulfonate composition is 0.1 or more and 300 or less. <157> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a decolorization step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is 1000 or less. １ and reactor inner diameter D １ The ratio (H １ / D １ <158> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, wherein the saturation ratio (Sr) of a raw material olefin sulfonate composition is 1.5 or more and 5 or less. <159> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the decolorization step (A) comprises, after the hydrolysis step, performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is 1.5 or more and 5 or less. １ and reactor inner diameter D １ The ratio (H １ / D １<159> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the ρ is 1 or more and ρ is 1 or less and 50 or less. <159> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less. <160> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, carrying out, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising, after the mixing step (a2), an aging step (b), wherein the pressure in the aging step (b) is 0.2 MPaG or more and 0.5 MPaG or less.<161> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, carrying out, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the pressure in the aging step (b) is 0.05 MPaG or more and 1 MPaG or less. <162> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, carrying out, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less.<163> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising, after the mixing step (a2), an aging step (b), wherein the residence time in the aging step (b) is 30 minutes or more and 200 minutes or less. <164> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, carrying out, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising, after the mixing step (a2), an aging step (b), wherein the residence time in the aging step (b) is 20 minutes or more and 400 minutes or less.<165> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, carrying out, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the temperature range of the aging step (b) is 40°C or higher and 120°C or lower. <166> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising, after the mixing step (a2), an aging step (b), wherein the temperature range of the aging step (b) is 60°C or higher and 100°C or lower.<167> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, carrying out, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the temperature range of the aging step (b) is 50°C or higher and 110°C or lower. <168> A method for producing a bleached internal olefin sulfonate composition, the method comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is performed continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the aging step (b) is performed using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<169> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the saturation coefficient (σ) of the internal olefin sulfonate composition is 0.1 or more and 300 or less. <169> A method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a bleaching step (A) of performing, after the hydrolysis step, an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is performed continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the aging step (b) is performed using a vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １ <170> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, wherein the saturation ratio (Sr) of the internal olefin sulfonate composition is 1.5 or more and 5 or less. <171> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the decolorization step (A) comprises, after the hydrolysis step, performing, for a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D１ ) is 1 or more and 50 or less. <171> A method for producing a decolorized internal olefin sulfonate composition according to any one of <1> to <89>, comprising a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product, and comprising a decolorization step (A) in which, after the hydrolysis step, a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present is subjected to an adjustment step (a1) of adjusting the concentration of an alkali compound in the system, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is carried out continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the aging step (b) is carried out using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １ <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pH is 0.1 or more and 300 or less, and the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less. <172> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the decolorization step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is performed continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the aging step (b) is performed using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １and reactor inner diameter D １ The ratio (H １ / D １ <89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pH is 0.1 or more and 300 or less, and the pressure in the aging step (b) is 0.2 MPaG or more and 0.5 MPaG or less. <173> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the decolorization step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is performed continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the aging step (b) is performed using a vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １<89> The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the pH is 0.1 or more and 300 or less, and the pressure in the aging step (b) is 0.05 MPaG or more and 1 MPaG or less. <174> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the decolorization step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is performed continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the aging step (b) is performed using a vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, and the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less. <175> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the decolorization step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is performed continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the aging step (b) is performed using a vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, and the residence time in the aging step (b) is 60 minutes or more and 200 minutes or less. <176> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the decolorization step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is performed continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the aging step (b) is performed using a vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, and the residence time in the aging step (b) is 20 minutes or more and 400 minutes or less. <177> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the decolorization step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is performed continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the aging step (b) is performed using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 40°C or more and 120°C or less. <178> A method for producing a bleached internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the bleaching step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a bleaching agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is performed continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the aging step (b) is performed using the vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １) is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 60°C or more and 100°C or less. <179> A method for producing a decolorized internal olefin sulfonate composition, comprising: a sulfonation step of sulfonating a raw material olefin; a neutralization step of neutralizing the obtained sulfonated product; and a hydrolysis step of hydrolyzing the obtained neutralized product, wherein the decolorization step (A) comprises, after the hydrolysis step, performing an adjustment step (a1) of adjusting the concentration of an alkali compound in a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, and further comprising an aging step (b) after the mixing step (a2), wherein the aging step (b) is performed continuously, the linear velocity of the internal olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, and the aging step (b) is performed using a vertical cylindrical reactor, and the height H of the vertical cylindrical reactor is １ and reactor inner diameter D １ The ratio (H １ / D １ The method for producing a bleached internal olefin sulfonate composition according to any one of <1> to <89>, wherein the viscosity index (SSI) of the bleached internal olefin sulfonate composition is 0.1 or more and 300 or less, the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the aging step (b) is 10 minutes or more and 500 minutes or less, and the temperature range in the aging step (b) is 50° C. or more and 110° C. or less. <180> Use of the bleached internal olefin sulfonate composition obtained by the production method according to any one of <1> to <179> in at least one selected from the group consisting of body cleansers, shampoos, laundry detergents, and dishwashing detergents.

[0110] The present invention will be described in detail below based on examples. Unless otherwise specified in the tables, the concentration of each component is expressed in mass %. Various measurement and evaluation methods are as follows.

[0111] <Method for measuring double bond distribution of internal olefins> The double bond positions of internal olefins were measured by gas chromatography (hereinafter abbreviated as GC). Specifically, internal olefins were reacted with dimethyl disulfide to form dithiolated derivatives, and then each component was separated by GC. The double bond positions of the internal olefins were determined from the respective peak areas, and the average double bond position was calculated using the following formula. The apparatus and measurement conditions used for the measurement are as follows. [Apparatus and Measurement Conditions] GC apparatus: HP6890 (manufactured by Hewlett-Packard) Column: Ultra-Alloy-1HT capillary column, 30 m x 250 μm x 0.15 μm (manufactured by Frontier Labs, Inc.) Detector: Hydrogen flame ionization detector (FID) Injection temperature: 300°C Detector temperature: 350°C He flow rate: 4.6 mL / min [Calculation formula for average double bond position] (In the formula, n represents the number of carbon atoms in the olefin, m represents the position of the double bond in the olefin, and Y represents the percentage of m-olefins in the olefins having n carbon atoms.)

[0112] <Method for Producing Internal Olefins> Production Example A (Synthesis of Internal Olefins Having 16 Carbon Atoms) 7,000 g (28.9 mol) of 1-hexadecanol "Kalcol 6098" (Kao Corporation) and 700 g (10% by mass based on the raw material alcohol) of γ-alumina (STREM Chemicals, Inc.) as a solid acid catalyst were charged into a flask equipped with a stirrer, and the reaction was carried out for 3 hours or more at 280°C while flowing nitrogen (7,000 mL / min) through the system under stirring. To obtain internal olefins with the desired average double bond positions, periodic sampling was performed to analyze the average double bond positions, and cooling was initiated at appropriate times. The average double bond positions after completion of the reaction were 4.2 for the internal olefins used in Examples 1 to 14, 17, 20, 23, and 25 to 31, 4.3 for the internal olefin used in Example 15, 4.1 for the internal olefin used in Example 21, and 3.8 for Example 24.

[0113] Production Example B (Synthesis of Internal Olefin Having 18 Carbon Atoms) 7,000 g (25.9 mol) of 1-octadecanol "Kalcol 8098" (Kao Corporation) and 1,050 g (10% by mass based on the raw material alcohol) of γ-alumina (STREM Chemicals, Inc.) as a solid acid catalyst were charged into a flask equipped with a stirrer, and the reaction was carried out for 10 hours or more at 280°C while flowing nitrogen (7,000 mL / min) through the system under stirring. In order to obtain an internal olefin having the desired average double bond position, sampling was performed periodically to analyze the average double bond position, and cooling was initiated at an appropriate time. The average double bond position after completion of the reaction was 4.2 for the internal olefin used in Example 16, 3.6 for the internal olefin used in Example 18, 4.4 for the internal olefin used in Example 22, 4.0 for the internal olefin used in Example 32, and 3.8 for Example 24.

[0114] <Method for producing a decolorized internal olefin sulfonate composition> Example 1 A thin-film sulfonation reactor having an external jacket was used. Cooling water at 10°C was passed through the external jacket, and the internal olefin having 16 carbon atoms obtained in Production Example A was allowed to flow down along the inner wall of the reactor in the form of a thin film. SO 4 diluted with dehumidified air was also added. ３ Gas (SO ３ Concentration: 1.1% by volume, SO ３A sulfonation reaction was carried out under the conditions of a molar ratio of olefin to sulfonate of 1.01 to obtain a sulfonated product. A continuous loop neutralization reactor equipped with a Milder MDN303V mixer (manufactured by Pacific Machinery Co., Ltd.) and an external jacket was used. After filling the reactor with ion-exchanged water, the resulting sulfonated product and an aqueous potassium hydroxide solution (concentration: 17% by mass) were supplied to initiate the neutralization reaction, under conditions such that the temperature of the neutralized product at the reactor outlet was 25°C. The mixer was operated at a peripheral speed of 24 m / s. Once the neutralization reactor reached a steady state, the neutralized product was confirmed to flow out of the reactor outlet, yielding a neutralized product. The concentration of internal olefin sulfonate in the neutralized product was 55% by mass. The amount of alkali compound used in the neutralization was 1.04 molar times the sulfonic acid groups. After neutralization, the neutralized product was heated in an autoclave at 160°C for 1 hour and hydrolyzed to obtain an internal olefin sulfonate composition before decolorization treatment. The average double bond position of the raw olefins of the internal olefin sulfonate was 4.2. The potassium hydroxide concentration of the internal olefin sulfonate composition obtained by the hydrolysis treatment was 0.029 mmol per 1 g of the internal olefin sulfonate. A 48% aqueous potassium hydroxide solution was added to the internal olefin sulfonate composition to adjust the potassium hydroxide concentration to 0.246 mmol per 1 g of the internal olefin sulfonate (adjustment step). In the decolorization step, a continuous loop decolorization reactor equipped with a Milder MDN303V (manufactured by Pacific Machinery Works, Ltd.) was used as a mixer. The Milder MDN303V was equipped with G rotors and stators, and the reaction was carried out in one stage. After the internal olefin sulfonate composition was heated to 80°C, the internal olefin sulfonate composition and an aqueous hydrogen peroxide solution (concentration: 45%) were supplied into the reactor (mixing step), and the decolorization treatment was initiated. The peripheral speed of the mixer in the mixing step was 4.7 m / s, and the shear rate was 9,400 / s. The amount of hydrogen peroxide mixed was 10 mg per 1 g of the internal olefin sulfonate in the internal olefin sulfonate composition. The pressure inside the reactor was adjusted to 0.3 MPaG by adjusting the opening of the valve provided at the outlet of the reactor. The residence time inside the reactor was 6 minutes.After the steady state was reached, immediately after the mixing step, the pH meter installed in the decolorization reaction apparatus indicated 11.4. The potassium hydroxide concentration in the internal olefin sulfonate composition at this time was 0.233 mmol per 1 g of internal olefin sulfonate. The internal olefin sulfonate composition after the 6-minute residence time was extracted and held for 1 hour in a thermostatic bath at the same temperature as during the decolorization treatment (aging step), thereby obtaining an internal olefin sulfonate composition after the decolorization treatment. The internal olefin sulfonate composition after the decolorization treatment was subjected to measurement of hue, evaluation of the color fading rate, evaluation of odor, evaluation of storage stability, and measurement of the peroxide value.

[0115] Examples 2 to 14, 20, Comparative Examples 1 and 2 Bleached internal olefin sulfonate compositions were produced in the same manner as in Example 1, except that the production conditions shown in Tables 1 and 2 were adopted. The potassium hydroxide concentration was adjusted by adding a 48% aqueous potassium hydroxide solution or a 98% aqueous sulfuric acid solution to the internal olefin sulfonate composition before the bleaching treatment. In addition, the hue measurement, fading rate evaluation, odor evaluation, storage stability evaluation, and peroxide value measurement were performed in the same manner as in Example 1. The concentrations in the adjustment step in Table 1 indicate the concentrations of the alkali compounds immediately after the mixing step.

[0116] Example 15 An internal olefin sulfonate composition was obtained in the same manner as in Example 13, except that an internal olefin having 16 carbon atoms and an average number of double bond positions of 4.3 was used among the internal olefins having 16 carbon atoms obtained in Production Example A. A bleached internal olefin sulfonate composition was produced in the same manner as in Example 13, except that the obtained internal olefin sulfonate composition before bleaching treatment was used. In addition, measurement of hue, evaluation of fading rate, evaluation of odor, evaluation of storage stability, and measurement of peroxide value were performed in the same manner as in Example 13.

[0117] Example 16 An internal olefin sulfonate composition was obtained in the same manner as in Example 13, except that the internal olefin having 18 carbon atoms and an average number of double bonds of 4.2, obtained in Production Example B, was used instead of the internal olefin having 16 carbon atoms obtained in Production Example A. A bleached internal olefin sulfonate composition was produced in the same manner as in Example 13, except that the obtained internal olefin sulfonate composition before bleaching treatment was used. In addition, measurement of hue, evaluation of fading rate, evaluation of odor and storage stability, and measurement of peroxide value were performed in the same manner as in Example 13.

[0118] Example 17 An internal olefin sulfonate composition before bleaching treatment was produced in the same manner as in Example 13, except that a sodium hydroxide aqueous solution (concentration: 12.5 mass%) was used as the alkaline agent instead of a potassium hydroxide aqueous solution. The concentration of the internal olefin sulfonate in the neutralization product was 53 mass%. To the obtained internal olefin sulfonate composition before bleaching treatment, a 48% sodium hydroxide aqueous solution or a 98% sulfuric acid aqueous solution was added to adjust the alkali concentration. The prepared internal olefin sulfonate composition before bleaching treatment was subjected to a bleaching treatment in the same manner as in Example 13, except for the production conditions shown in Table 2. Thereafter, the hue measurement, the fading rate evaluation, the odor evaluation, the storage stability evaluation, and the peroxide value measurement were performed in the same manner as in Example 13.

[0119] Example 18 An internal olefin sulfonate composition before bleaching treatment was obtained in the same manner as in Example 17, except that the internal olefin having 18 carbon atoms and an average number of double bond positions of 3.6 obtained in Production Example B was used instead of the internal olefin having 16 carbon atoms obtained in Production Example A. The concentration of the internal olefin sulfonate in the neutralization product was 53 mass%. A bleached internal olefin sulfonate composition was produced in the same manner as in Example 17, except for the production conditions shown in Table 2. In addition, hue measurement, fading rate evaluation, odor evaluation, storage stability evaluation, and peroxide value measurement were also performed in the same manner as in Example 17.

[0120] Example 19 The storage stability of the decolorized internal olefin sulfonate composition obtained in Example 13 was evaluated in the same manner as in Example 13, except that the pH was adjusted using an aqueous phosphoric acid solution (concentration: 75% by mass). As a result, the storage stability was evaluated as A, as in Example 13.

[0121] Example 21 An internal olefin sulfonate composition was obtained in the same manner as in Example 13, except that an internal olefin having 16 carbon atoms and an average number of double bond positions of 4.1 was used among the internal olefins having 16 carbon atoms obtained in Production Example A. A bleached internal olefin sulfonate composition was produced in the same manner as in Example 13, except that the obtained internal olefin sulfonate composition before bleaching treatment was used. In addition, measurement of hue, evaluation of fading rate, evaluation of odor, evaluation of storage stability, and measurement of peroxide value were performed in the same manner as in Example 13.

[0122] Example 22 An internal olefin sulfonate composition was obtained in the same manner as in Example 16, except that the internal olefin having 18 carbon atoms and an average number of double bonds of 4.4, obtained in Production Example B, was used instead of the internal olefin having 16 carbon atoms obtained in Production Example A. A bleached internal olefin sulfonate composition was produced in the same manner as in Example 16, except that the obtained internal olefin sulfonate composition before bleaching treatment was used. In addition, hue measurement, fading rate evaluation, odor evaluation, storage stability evaluation, and peroxide value measurement were performed in the same manner as in Example 16.

[0123] Example 23 An internal olefin sulfonate composition was prepared by the method of Example 1 using the internal olefin having 16 carbon atoms obtained in Production Example A. 98% sulfuric acid was added to the obtained internal olefin sulfonate composition before bleaching treatment to adjust the potassium hydroxide concentration. The potassium hydroxide concentration was 0.054 mmol per 1 g of internal olefin sulfonate. A bleached internal olefin sulfonate composition was produced by the same method as in Example 13, except that the preparation step and the mixing step were performed in parallel on the prepared internal olefin sulfonate composition before bleaching treatment (recirculation ratio in the mixing step and the preparation step: 4 times). In the preparation step, a 48% aqueous potassium hydroxide solution was added. The potassium hydroxide concentration immediately after the mixing step was 0.059 mmol per 1 g of internal olefin sulfonate. Thereafter, the hue, fading rate, odor, storage stability, and peroxide value were measured by the same methods as in Example 13.

[0124] <Measurement and Evaluation Methods> (Measurement of Potassium Hydroxide (or Sodium Hydroxide) Concentration in Internal Olefin Sulfonate Composition) An appropriate amount of sample (approximately 5 g, accurate to three decimal places) was weighed out and diluted with ion-exchanged water. Approximately 0.05 g of a 1% phenolphthalein ethanol solution was added to the solution to cause it to turn red. The sample solution was titrated with 1 / 10 N hydrochloric acid, and the titration volume was read when the red color no longer appeared. The potassium hydroxide (or sodium hydroxide) concentration in the sample was calculated using the following formula. Potassium hydroxide (or sodium hydroxide) concentration (mmol / g of internal olefin sulfonate) = {(1 / 10 x f x d x M) / (c x 1000)} x 100, c: sample amount (g), d: amount of 1 / 10 N hydrochloric acid used (ml), f: factor of 1 / 10 N hydrochloric acid, M: molecular weight of potassium hydroxide (or sodium hydroxide). The range in which phenolphthalein does not color (less than pH 8.3) was determined using the following method. The potassium hydroxide (or sodium hydroxide) concentration in the sample was calculated from the measured pH value using the following equation, which was established by assuming an approximately linear relationship between the concentration of potassium hydroxide (or sodium hydroxide) in the sample on the horizontal axis and the pH on the vertical axis from pH 7 to 8.3. Potassium hydroxide (or sodium hydroxide) concentration (mmol / g of internal olefin sulfonate) = ((measured pH) - 7) / 1010.1

[0125] (Measurement of hue, evaluation of discoloration rate) A tristimulus value direct reading type petroleum product color tester "OME 2000" (manufactured by Nippon Denshoku Industries Co., Ltd.) was used. The Hazen color number (APHA) at 25°C of the internal olefin sulfonate composition before bleaching treatment and the bleached internal olefin sulfonate composition after bleaching treatment was measured. Note that the concentration of the internal olefin sulfonate in each composition was adjusted to 10 mass% before measurement. The discoloration rate (%) was calculated using the following formula, where the Hazen color number before bleaching treatment is A and the Hazen color number after bleaching treatment is B. A larger absolute value of the discoloration rate indicates a better bleaching effect, and the evaluation was based on the following criteria: Discoloration rate (%) = 100 × (A - B) / A [Evaluation criteria] A: Discoloration rate of 70% or more B: Discoloration rate of 65% or more but less than 70% C: Discoloration rate of 60% or more but less than 65% D: Discoloration rate of less than 60%

[0126] (Evaluation of odor) The odor levels of the internal olefin sulfonate compositions after bleaching treatment produced in Examples 1 to 23 and Comparative Example 2 were compared with a standard product (the internal olefin sulfonate composition after bleaching treatment produced in Comparative Example 1). Five odor evaluation experts evaluated each composition according to the following criteria, and then averaged the scores of the five experts to give an overall rating (A to C) as shown below. [Evaluation criteria] 3 points: odor level is very low compared to the standard product 2 points: odor level is slightly low compared to the standard product 1 point: odor level is the same as the standard product [Overall rating] A: average 2.5 points or more B: average 1.5 points or more, less than 2.5 points C: average less than 1.5 points

[0127] (Evaluation of storage stability) The prepared internal olefin sulfonate composition after the bleaching treatment was ２ SO ４ Add the monohydrate and ２ SO ４ The solution was added so that the concentration was 5 parts by mass relative to 100 parts by mass of the internal olefin sulfonate. Thereafter, a 50% aqueous citric acid solution (a 75% aqueous phosphoric acid solution was used in Example 19) was added to the internal olefin sulfonate composition, and the pH at 25°C was adjusted to 10 when the concentration of the internal olefin sulfonate in the internal olefin sulfonate composition after the bleaching treatment was adjusted to 10% by mass (pH adjustment step). Then, ion-exchanged water was added to the bleached internal olefin sulfonate composition prepared above, and the concentration of the internal olefin sulfonate in the internal olefin sulfonate composition was adjusted to 25%. After the adjustment, the composition was stored at 25°C for 24 hours. The storage stability was then evaluated. Evaluation was performed visually and based on the following criteria: A: No precipitates were formed. B: A small amount of precipitates were formed and dispersed. C: A large amount of precipitates were formed and accumulated.

[0128] (Peroxide Value Measurement) 10 g of the prepared bleached internal olefin sulfonate composition was placed in a stoppered Erlenmeyer flask, and 15 mL of chloroform and 20 mL of acetic acid were added. The flask was then stoppered and dissolved. Nitrogen gas was passed through the stoppered Erlenmeyer flask to displace the air. While passing nitrogen gas through the flask, 1 mL of saturated aqueous potassium iodide solution was added, the flask was stoppered, and the flask was shaken for 1 minute and then stored in a dark room at room temperature for 5 minutes. 75 mL of a methyl alcohol aqueous solution prepared by previously mixing methyl alcohol and water in a 1:1 ratio was then added, the stopper was reattached, and the flask was mixed. The stopper was then washed with approximately 50 mL of methyl alcohol aqueous solution, and immediately titrated with a 0.01 mol / L aqueous sodium thiosulfate solution using a potentiometric titrator (AT-510, manufactured by Kyoto Electronics Manufacturing Co., Ltd.). A blank test (without the addition of the bleached internal olefin sulfonate composition) was also conducted in parallel. In the table, the peroxide value per 1 kg of internal olefin sulfonate in the internal olefin sulfonate composition is expressed, and the results evaluated according to the following evaluation criteria are also shown. Peroxide value (meq / kg) = (a - b) x f x 10 / sample amount (g) a: Amount (mL) of 0.01 mol / L sodium thiosulfate aqueous solution required to titrate the sample b: Amount (mL) of 0.01 mol / L sodium thiosulfate aqueous solution required to titrate the blank test f: Factor of 0.01 mol / L sodium thiosulfate aqueous solution [Evaluation criteria] A: 11.5 meq / kg or less B: More than 11.5 meq / kg and 27 meq / kg or less C: More than 27 meq / kg.

[0129] (Method for measuring pH when the concentration of internal olefin sulfonate is 10% by mass) Measurement was carried out using a pH meter (Horiba, Ltd., pH meter D-51) calibrated with a pH standard solution. The decolorized internal olefin sulfonate composition was diluted with ion-exchanged water so that the concentration of internal olefin sulfonate became 10% by mass, and the obtained diluted solution was adjusted to 25°C. Then, the pH glass electrode of the pH meter was immersed in the diluted solution, and the value when the display stabilized was read.

[0130]

[0131]

[0132] In Examples 1 to 23, the concentration of potassium hydroxide or sodium hydroxide in the internal olefin sulfonate composition at the start of the bleaching treatment was adjusted to 0.004 mmol or more and 0.26 mmol or less per 1 g of internal olefin sulfonate by the adjustment step of the bleaching process, and therefore bleached internal olefin sulfonate compositions with good color fading, low odor level, and good storage stability were obtained. On the other hand, in Comparative Examples 1 and 2, the odor of the internal olefin sulfonate composition after the bleaching treatment became strong or the storage stability was reduced.

[0133] Example 24 An internal olefin sulfonate composition before decolorization treatment was obtained in the same manner as in Example 1 using an internal olefin mixture (C16 / C18 mass ratio: 80 / 20) prepared by mixing the internal olefin having 16 carbon atoms and an average double bond position of 3.8 obtained in Production Example A with the internal olefin having 18 carbon atoms and an average double bond position of 3.8 obtained in Production Example B. The average double bond positions of the raw material olefins for the internal olefin sulfonate was 3.8. Sodium hydroxide was used as the alkaline agent for neutralization. The sodium hydroxide concentration of the internal olefin sulfonate composition obtained by the hydrolysis treatment was 0.08 mmol per 1 g of the internal olefin sulfonate, and the active ingredient concentration was 65 mass%. 180 kg of the obtained internal olefin sulfonate composition before decolorization treatment was charged into a reaction tank (volume: approximately 250 L). The reaction vessel was equipped with an MR205 (manufactured by Satake Multimix Co., Ltd.) impeller, with the impeller diameter d / reaction vessel inner diameter D being 0.59, and the impeller height h / reaction vessel height H being 0.61. A circulation line was provided outside the reaction vessel, and the circulation line was equipped with a Milder MDN303V (manufactured by Pacific Machinery Works Co., Ltd.) mixer. The Milder MDN303V was equipped with G as a rotor / stator, and the reaction was carried out in a single stage. After the internal olefin sulfonate composition was charged into the apparatus and heated to 80°C, the internal olefin sulfonate composition in the reaction vessel was supplied to the Milder section, and then a 48% aqueous sodium hydroxide solution and an aqueous hydrogen peroxide solution (concentration: 35%) were simultaneously supplied to initiate the decolorization treatment. The aqueous hydrogen peroxide solution was added dropwise in 20 portions over a period of 2 hours, and the decolorization treatment was initiated (semi-batch method) (mixing step and adjustment step). The amount of hydrogen peroxide mixed was 10 mg per gram of internal olefin sulfonate in the internal olefin sulfonate composition. The peripheral speed in the mixer in the mixing step and the adjusting step was 0.9 m / s, and the shear rate was 1800 / s. The pressure in the reaction tank was normal pressure (0 MPaG). During the mixing step, the pH meter installed in the decolorization reaction apparatus indicated 11.0±0.2. The concentration of sodium hydroxide in the internal olefin sulfonate composition immediately after the mixing step was 0.08 mmol per gram of internal olefin sulfonate.Thereafter, the internal olefin sulfonate composition after the decolorization treatment in the reactor was aged at 80°C under normal pressure (0 MPaG) for a residence time of 60 minutes (aging step). The internal olefin sulfonate composition after the 60-minute residence time was extracted to obtain an internal olefin sulfonate composition after the decolorization treatment. The internal olefin sulfonate composition after the decolorization treatment was subjected to measurement of hue, evaluation of the fading rate, evaluation of odor, evaluation of storage stability, and measurement of the peroxide value.

[0134] Example 25 180 kg of the internal olefin sulfonate composition before decolorization treatment obtained in Example 1 was charged into a reaction vessel (volume: approximately 250 L) equipped with an agitator blade. The reaction vessel was equipped with an MR205 agitator blade (manufactured by Satake Multimix Co., Ltd.), with the agitator blade diameter d / reaction vessel inner diameter D being 0.59 and the agitator blade height h / reaction vessel height H being 0.61. After charging the internal olefin sulfonate composition into the reaction vessel (batch type), the temperature was raised to 80°C, and then a 48% aqueous potassium hydroxide solution was added dropwise to adjust the alkali concentration to 0.041 mmol. Thereafter, an aqueous hydrogen peroxide solution (concentration: 35%) was added dropwise into the reaction vessel over 2 hours in five portions, and a 48% aqueous sodium hydroxide solution was simultaneously supplied (mixing step and adjustment step), to initiate the decolorization treatment. The peripheral speed of the reaction blade in the mixing step and the adjusting step was 1.74 m / s, the shear rate was 13.4 l / s, and the stirring power required per unit liquid volume (Pv) was 0.453 kW / m ３The pressure in the reaction tank was atmospheric pressure (0 MPaG). The amount of hydrogen peroxide mixed was 20 mg relative to 1 g of the internal olefin sulfonate in the internal olefin sulfonate composition. During the mixing step, the pH meter installed in the decolorization reaction tank indicated 9.6±0.3. The potassium hydroxide concentration in the internal olefin sulfonate composition immediately after the mixing step was 0.041 mmol relative to 1 g of the internal olefin sulfonate. Thereafter, the internal olefin sulfonate composition after the decolorization treatment in the reaction tank was aged at 80°C, atmospheric pressure (0 MPaG), and a residence time of 30 minutes (aging step). The internal olefin sulfonate composition after the 30-minute residence time was extracted to obtain an internal olefin sulfonate composition after the decolorization treatment. The internal olefin sulfonate composition after the decolorization treatment was subjected to measurement of hue, evaluation of the discoloration rate, evaluation of the odor, evaluation of storage stability, and measurement of the peroxide value.

[0135] Example 26 A decolorized internal olefin sulfonate composition was produced in the same manner as in Example 25, except that the production conditions shown in Table 3 were used. Furthermore, the hue measurement, fading rate evaluation, odor evaluation, storage stability evaluation, and peroxide value measurement were also carried out in the same manner as in Example 1. The concentration in the preparation step in Table 3 indicates the concentration of the alkali compound immediately after the mixing step. The concentration of the alkali compound in the internal olefin sulfonate composition before the mixing step was 0.06 mmol. Furthermore, during the mixing step, the pH value measured by the pH meter installed in the decolorization reaction tank was 10.4±0.2.

[0136]

[0137] In Example 24, the bleaching step was carried out in a semi-batch system, and a bleached internal olefin sulfonate composition was obtained that exhibited good color removal, a low odor level, and good storage stability. In Examples 25 and 26, the bleaching step was carried out in a batch system, and a bleached internal olefin sulfonate composition was obtained that exhibited low odor level and good storage stability.

[0138] Example 27 An internal olefin sulfonate composition before decolorization treatment was obtained in the same manner as in Example 1. The average double bond position of the raw material olefins in the internal olefin sulfonate was 4.2. The potassium hydroxide concentration of the internal olefin sulfonate composition obtained by the hydrolysis treatment was 0.029 mmol per 1 g of internal olefin sulfonate. A 48% aqueous potassium hydroxide solution was added to the internal olefin sulfonate composition to adjust the potassium hydroxide concentration to 0.030 mmol per 1 g of internal olefin sulfonate immediately after the mixing step (adjustment step). The potassium hydroxide concentration after the adjustment was 0.043 mmol per 1 g of internal olefin sulfonate. In the decolorization step, a continuous loop decolorization reactor equipped with a Milder MDN303V (manufactured by Pacific Machinery Works, Ltd.) was used as a mixer. The Milder MDN303V was equipped with G rotors and stators, and the decolorization was carried out in a single stage. After the temperature of the internal olefin sulfonate composition was raised to 80°C, the internal olefin sulfonate composition and an aqueous hydrogen peroxide solution (concentration: 45%) were supplied into a reactor, and the pressure inside the reactor was adjusted to 0.3 MPaG by adjusting the aperture of a valve provided at the outlet of the reactor, thereby starting a decolorization treatment (mixing step). The peripheral speed of the mixer in the mixing step was 4.7 m / s, and the shear rate was 9,400 / s. The amount of hydrogen peroxide mixed was 10 mg per gram of internal olefin sulfonate in the internal olefin sulfonate composition. After the s...

Claims

1. For a system containing an internal olefin sulfonate composition, an adjustment step (a1) is performed to adjust the concentration of the alkali compound in the system, and A method for producing a decolorized internal olefin sulfonate composition, comprising a decolorization step (A) in which a mixing step (a2) is performed in which a decolorizing agent is mixed with an internal olefin sulfonate composition present in the system, A method for producing a decolorized internal olefin sulfonate composition, wherein the adjustment step (a1) is a step of adjusting the concentration of the alkali compound so that the concentration of the alkali compound after mixing the decolorizing agent with the internal olefin sulfonate composition present in the system in the decolorization step (A) is 0.004 mmol or more and 0.26 mmol or less per 1 g of internal olefin sulfonate.

2. A method for producing a decolorized internal olefin sulfonate composition according to claim 1, wherein the adjustment step (a1) is performed after the mixing step (a2).

3. A method for producing a decolorized internal olefin sulfonate composition according to claim 1, wherein the mixing step (a2) is performed after the adjustment step (a1).

4. A method for producing a decolorized internal olefin sulfonate composition according to claim 1, wherein the adjustment step (a1) and the mixing step (a2) are carried out in parallel.

5. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 4, wherein in the mixing step (a2), the mixing is carried out under shear conditions where the shear rate is 5 / s or more and 100,000 / s or less.

6. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 5, wherein the adjustment step (a1) is performed under shear conditions in which the shear rate is 5 / s or more and 100,000 / s or less.

7. The stirring power (Pv) per unit volume of liquid in the mixer of the mixing step (a2) is 0.1 kW / m ３ More than 100kW / m ３ A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 6, as follows:

8. The required stirring power (Pv) per unit volume of liquid in the mixer of the adjustment step (a1) is 0.1 kW / m³ or more, and 100 kW / m³. ３ A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 7, as follows:

9. The mixing step (a2) is carried out using a reaction vessel having a stirring blade or a stirring blade type mixer. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 8, wherein the ratio of the diameter of the stirring blade d to the diameter D of the reaction vessel (d / D) is 0.01 or more and less than 1.

10. The mixing step (a2) is carried out using a reaction vessel having a stirring blade or a stirring blade type mixer. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 9, wherein the ratio of the height h of the stirring blade to the height H of the reaction vessel (h / H) is 0.01 or more and less than 1.

11. The adjustment step (a1) is carried out using a reaction vessel having a stirring blade or a stirring blade type mixer. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 10, wherein the ratio of the diameter of the stirring blade d to the diameter D of the reaction vessel (d / D) is 0.01 or more and less than 1.

12. The adjustment step (a1) is carried out using a reaction vessel having a stirring blade or a stirring blade type mixer. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 11, wherein the ratio of the height h of the stirring blade to the height H of the reaction vessel (h / H) is 0.01 or more and less than 1.

13. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 12, wherein the pressure in the adjustment step (a1) is 0 MPaG or more and 10 MPaG or less.

14. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 13, wherein the pressure in the mixing step (a2) is 0 MPaG or more and 10 MPaG or less.

15. The mixing step (a2) is carried out using a reaction vessel having a stirring blade or a stirring blade type mixer. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 14, wherein the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less.

16. The adjustment step (a1) is carried out using a reaction vessel having a stirring blade or a stirring blade type mixer. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 15, wherein the peripheral speed of the stirring blade is 0.01 m / s or more and 50 m / s or less.

17. The method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 16, wherein the mixing step (a2) is performed at a temperature of 40°C or higher and 100°C or lower.

18. The method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 17, wherein the amount of the decolorizing agent mixed is 1 mg or more and 300 mg or less per 1 g of internal olefin sulfonate in the internal olefin sulfonate composition.

19. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 18, wherein the decolorizing agent is an oxidizing agent.

20. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 19, wherein the decolorizing agent is hydrogen peroxide.

21. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 20, wherein after the mixing step (a2), a maturation step (b) is performed.

22. A method for producing a decolorized internal olefin sulfonate composition according to claim 21, wherein the temperature of the maturation step (b) is 40°C or higher and 120°C or lower.

23. A method for producing a decolorized internal olefin sulfonate composition according to claim 21 or 22, wherein the residence time of the maturation step (b) is 10 minutes or more and 500 minutes or less.

24. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 21 to 23, wherein the pressure in the aging step (b) is 0 MPaG or more and 10 MPaG or less.

25. Height H of the apparatus for performing the aging step (b) １ and device diameter D １ The ratio (H １ / D １ A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 21 to 24, wherein the ratio is 0.1 or more and 300 or less.

26. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 21 to 25, wherein the linear velocity of the internal olefin sulfonate composition in the maturation step (b) is 0.001 mm / s or more and 1000 mm / s or less.

27. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 26, wherein the alkali compound comprises at least one alkali metal hydroxide selected from the group consisting of sodium hydroxide and potassium hydroxide.

28. The method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 27, wherein the internal olefin sulfonate comprises at least one selected from the group consisting of internal olefin sulfonates having 16 carbon atoms and internal olefin sulfonates having 18 carbon atoms.

29. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 28, wherein the average number of double bond positions of the raw material olefin of the internal olefin sulfonate is 3 or more and 5 or less.

30. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 29, wherein the concentration of the alkali compound in the internal olefin sulfonate composition before performing the decolorization step (A) is 0.010 mmol or more and 0.27 mmol or less per 1 g of internal olefin sulfonate in the internal olefin sulfonate composition.

31. The internal olefin sulfonate composition is obtained by a method for producing an internal olefin sulfonate, which includes a sulfonation step of sulfonating a raw material olefin, a neutralization step of neutralizing the obtained sulfonated product, and a hydrolysis step of hydrolyzing the obtained neutralized product. A method for producing a decolorized internal olefin sulfonate composition according to claim 30, wherein the concentration of the alkali compound in the internal olefin sulfonate composition after the hydrolysis step is controlled by an adjustment method selected from a method for adjusting the amount of alkali compound used in the neutralization step and a method for adjusting the amount of alkali compound in the hydrolysis step.

32. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 21 to 26, wherein the maturation step (b) is carried out in a semi-batch manner.

33. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 21 to 26, wherein the maturation step (b) is carried out in a continuous manner.

34. A method for producing a decolorized internal olefin sulfonate composition according to any one of claims 1 to 33, wherein the adjustment step (a1) is carried out in a continuous manner having a circulation system, and the circulation ratio of the internal olefin sulfonate composition is greater than 0.

35. A method for producing a decolorized internal olefin sulfonate composition, comprising a decolorization step (A) of performing an adjustment step (a1) to adjust the concentration of an alkaline compound in a system containing an internal olefin sulfonate composition, and a mixing step (a2) of mixing a decolorizing agent with the internal olefin sulfonate composition present in the system, wherein the pH of the liquid in the system in the mixing step (a2) is 9.3 or more and 11.4 or less.