Method for producing decolorized internal olefin sulfonate composition

Abstract

Provided is a method for producing a decolorized internal olefin sulfonate composition which has a light odor and good storage stability. This method for producing a decolored internal olefin sulfonate composition comprises a decoloring step (A) in which a system in which an internal olefin sulfonate composition containing an internal olefin sulfonate is present is subjected to: an adjustment step (a1) in which the concentration of a basic compound in the system is adjusted; and a mixing step (a2) in which a decolorizing agent is mixed with the internal olefin sulfonate composition present in the system, and a step for adjusting the concentration of the basic compound such that the concentration of the basic compound obtained by mixing the decolorizing agent with the internal olefin sulfonate composition present in the system in the decolorizing step (A) is 0.004-0.26 mmol inclusive with respect to 1 g of the internal olefin sulfonate.

Description

Technical Field

[0001] This invention relates to a method for manufacturing a decolorized olefin sulfonate composition. Background Technology

[0002] To date, anionic surfactants, especially alkyl sulfates and polyoxyalkylene alkyl ether sulfates, are widely used as cleaning agents in both household and industrial applications due to their excellent cleaning and foaming properties. Additionally, as anionic surfactants, olefin sulfonates have been reported, particularly those obtained from internal olefins (whose double bonds are located internally rather than at the end of the olefin).

[0003] The aforementioned alkylene sulfonates can generally be obtained by reacting the alkylene with sulfur trioxide to sulfonate it, neutralizing the obtained sulfonate, and then further hydrolyzing it.

[0004] The aforementioned olefin sulfonates are typically obtained in the form of an aqueous solution containing olefin sulfonates (olefin sulfonate composition), which can cause discoloration, which is unsuitable when used as a cleaning agent.

[0005] Regarding the decolorization of olefin sulfonate compositions, for example, Patent Document 1 discloses a technique for decolorizing olefin sulfonate compositions using hydrogen peroxide.

[0006] Existing technical documents

[0007] Patent documents

[0008] Patent Document 1: Japanese Patent Application Publication No. 2015-178467 Summary of the Invention

[0009] [The technical problem that the invention aims to solve]

[0010] However, it was found that the sulfonate compositions of olefins decolorized using hydrogen peroxide exhibited increased odor or reduced storage stability.

[0011] Regarding the technical issues (odor or storage stability) of such decolorized olefin sulfonate compositions decolorized using decolorizing agents such as hydrogen peroxide, the prior art has not conducted sufficient research. The present invention provides a method for manufacturing a decolorized olefin sulfonate composition with a light odor and good storage stability.

[0012] [Technical means to solve technical problems]

[0013] This invention relates to a method for manufacturing a decolorized olefin sulfonate composition, comprising a decolorization step (A).

[0014] The decolorization process (A) involves the following steps for a system containing an internal olefin sulfonate composition:

[0015] Adjustment step (a1), adjusting the concentration of the basic compound in the above system: and

[0016] In the mixing step (a2), the decolorizing agent is mixed with the olefin sulfonate composition present in the system.

[0017] The above-mentioned adjustment step (a1) is a step of adjusting the concentration of the alkaline compound so that the concentration of the alkaline compound after mixing the decolorizing agent with the olefin sulfonate composition present in the system in the above-mentioned decolorization step (A) is 0.004 mmol or more and 0.26 mmol or less relative to 1 g of olefin sulfonate.

[0018] [Invention Effects]

[0019] According to the manufacturing method of the invention, when the decolorizing agent is mixed with the olefin sulfonate composition, the concentration of the alkaline compound in the system is adjusted to a specific range, thereby obtaining a decolorized olefin sulfonate composition that has good fading properties, a light odor, and good storage stability. Detailed Implementation

[0020] The present invention will now be described in detail.

[0021] The method for manufacturing the decolorized olefin sulfonate composition of the present invention includes a decolorization step (A).

[0022] The decolorization process (A) involves the following steps for a system containing an internal olefin sulfonate composition:

[0023] Adjustment step (a1), adjusting the concentration of the basic compound in the above system: and

[0024] In the mixing step (a2), the decolorizing agent is mixed with the olefin sulfonate composition present in the system.

[0025] The above-mentioned adjustment step (a1) is a step of adjusting the concentration of the alkaline compound so that the concentration of the alkaline compound after mixing the decolorizing agent with the olefin sulfonate composition present in the system in the above-mentioned decolorization process (A) is 0.004 mmol or more and 0.26 mmol or less relative to 1 g of olefin sulfonate.

[0026] In this invention, the sulfonate is obtained by sulfonation, neutralization, and hydrolysis of the olefin. Specifically, sulfonation of the olefin yields β-sulactone, γ-sulactone, and olefin sulfonic acid. Further, these are converted to hydroxysulfonates and olefin sulfonates in the neutralization and hydrolysis processes. The resulting products are primarily mixtures of these. In this invention, these products and mixtures thereof are collectively referred to as olefin sulfonates.

[0027] The olefin sulfonate composition is an aqueous solution containing the above-mentioned olefin sulfonate, obtained by the following sulfonation process, neutralization process and any hydrolysis process.

[0028] <Sulfonation Process>

[0029] The sulfonation process is a process in which an internal olefin reacts with sulfur trioxide gas to obtain a sulfonated product.

[0030] Internal alkenes are alkenes that have double bonds at positions other than the ends of the olefin chain, that is, alkenes with double bonds at positions 2 or higher on the carbon chain. Internal alkenes may also contain trace amounts of so-called α-alkenes, where the double bond is located at position 1 on the carbon chain.

[0031] From the viewpoint of cleaning performance when using olefin sulfonates in detergents, the number of carbon atoms in the olefin is preferably 10 or more, more preferably 12 or more, even more preferably 14 or more, even more preferably 16 or more, and preferably 22 or less, even more preferably 18 or less.

[0032] The internal olefin can be used alone or in combination of two or more. From the viewpoint of cleaning performance when internal olefin sulfonates are used in detergents, the internal olefin is at least one selected from internal olefins with 16 carbon atoms and internal olefins with 18 carbon atoms. When two or more internal olefins are used in combination, from the viewpoint of cleaning performance when internal olefin sulfonates are used in detergents, it is preferable to use a combination of internal olefins with 16 carbon atoms and internal olefins with 18 carbon atoms.

[0033] Internal olefins can be manufactured by known methods, such as those described in International Publication No. 2011 / 052732.

[0034] There are no particular restrictions on the sulfur trioxide gas, but sulfur trioxide gas diluted with inert gases such as air and nitrogen is preferred. Regarding the concentration of sulfur trioxide gas, from the viewpoint of reducing the reactor volume by efficiently reacting the internal olefins with sulfur trioxide gas, thereby improving economy, it is preferably 0.5% by volume or more, more preferably 1.0% by volume or more. From the viewpoint of obtaining a sulfonate with good color by appropriately controlling the reaction rate, it is preferably 10% by volume or less, more preferably 6.0% by volume or less.

[0035] From the viewpoint of increasing the yield of sulfonates, the amount of sulfur trioxide gas used relative to 1 mole of olefin is preferably 0.8 moles or more, more preferably 0.9 moles or more, and even more preferably 0.95 moles or more. From the viewpoint of improving economy and suppressing the coloring of sulfonates, it is preferably 1.2 moles or less, more preferably 1.10 moles or less, and even more preferably 1.05 moles or less.

[0036] There are no particular limitations on the sulfonation reactor used in the sulfonation process. From the viewpoint of controlling the reaction temperature to obtain high-quality sulfonates, an external casing is preferred. Furthermore, from the viewpoint of efficiently reacting the liquid olefin with the gaseous sulfur trioxide gas, a falling film sulfonation reactor is preferred, in which the olefin flows down in a thin film and reacts with the sulfur trioxide gas. Examples of such sulfonation reactors include various reactors described in Japanese Patent Application Publication No. 11-315061, Japanese Patent Application Publication No. 49-48409, IT1248079A, and US3257175A.

[0037] From the viewpoint of preventing the solidification of sulfur trioxide and sulfonates, the processing temperature of the sulfonation process is preferably above 0°C. In addition, from the viewpoint of suppressing the coloring of sulfonates, it is preferably below 50°C.

[0038] Since sulfonation is an exothermic reaction, it is preferable to install an external sleeve on the sulfonation reactor and to circulate cooling water through the external sleeve for cooling. From the viewpoint of increasing the reaction rate, the temperature of the cooling water circulated into the external sleeve of the sulfonation reactor is preferably 0°C or higher. Furthermore, from the viewpoint of suppressing side reactions and reducing impurities such as internal olefins and inorganic salts in the final obtained internal olefin sulfonate, it is preferably 30°C or lower, and more preferably 20°C or lower.

[0039] Furthermore, in order to control the reaction rate and suppress the deterioration of the quality of the sulfonate, an inert gas can be introduced between the internal olefin and the sulfur trioxide gas. Examples of such reactors include those described in Japanese Patent Application Publication No. 11-315061 and Japanese Patent Application Publication No. 49-48409.

[0040] From the viewpoint of increasing the yield of sulfonates, the reaction rate of the inner olefin in the sulfonation reaction is preferably 95% or more, more preferably 96% or more, and even more preferably 97% or more. In addition, from the viewpoint of suppressing the coloring of sulfonates caused by excess sulfur trioxide, it is preferably 99.8% or less.

[0041] <Neutralization Process>

[0042] The neutralization process is a process of neutralizing the sulfonated product obtained in the sulfonation process to obtain a neutralized product.

[0043] The basic compound used for neutralization can be an inorganic basic compound or an organic basic compound. Examples of inorganic basic 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 basic compounds include amine compounds such as ammonia and 2-aminoethanol, which have 1 or more but fewer than 6 carbon atoms.

[0044] From the viewpoint of ease of acquisition and improved economy, the alkaline compound used for neutralization is preferably an inorganic alkaline compound, more preferably an alkali metal hydroxide, and even more preferably at least one selected from sodium hydroxide and potassium hydroxide.

[0045] From the viewpoint of ease of use, the alkaline compound used for neutralization is preferably used in the form of an alkaline aqueous solution. Furthermore, during neutralization, the aforementioned sulfonate can be mixed with the alkaline aqueous solution, or the aforementioned sulfonate, alkaline aqueous solution, and water can be mixed. When the aforementioned sulfonate, alkaline aqueous solution, and water are mixed, a high concentration of alkaline aqueous solution can be used. From the viewpoint of improving economy and suppressing the formation of impurities such as internal olefins and inorganic salts, the concentration of the alkaline aqueous solution, or the concentration of the mixture when the alkaline aqueous solution and water are mixed, is preferably 1% by mass or more, more preferably 4.5% by mass or more, further preferably 7% by mass or more, further more preferably 10% by mass or more, and even more preferably 12% by mass or more. Furthermore, from the viewpoint of improving productivity in the hydrolysis process, it is preferably 50% by mass or less, more preferably 32% by mass or less, further preferably 23% by mass or less, further more preferably 20% by mass or less, and even more preferably 18% by mass or less.

[0046] In this invention, it is preferable to control the concentration of the alkaline compound in the olefin sulfonate composition after the hydrolysis process by adjusting the amount of alkaline compound used in the neutralization process. From the viewpoint of suppressing the formation of impurities such as internal olefins and inorganic salts, and from the viewpoint of improving reactivity, the amount of alkaline compound used in the neutralization process is preferably 1 molar ratio or more, more preferably 1.02 molar ratio or more, and even more preferably 1.030 molar ratio or more, relative to the sulfonic acid group. From the viewpoint of suppressing the deterioration of odor after decolorization, it is more preferably 1.034 molar ratio or more, even more preferably 1.035 molar ratio or more, and even more preferably 1.04 molar ratio or more. In addition, from the viewpoint of improving economy and improving storage stability, it is preferably 1.13 molar ratio or less, more preferably 1.12 molar ratio or less, even more preferably 1.110 molar ratio or less, even more preferably 1.105 molar ratio or less, even more preferably 1.10 molar ratio or less, even more preferably 1.09 molar ratio or less, even more preferably 1.08 molar ratio or less, even more preferably 1.07 molar ratio or less, and even more preferably 1.06 molar ratio or less.

[0047] From the viewpoint of suppressing impurities such as internal olefins and inorganic salts generated due to side reactions, the temperature at which the sulfonate is mixed with the alkaline aqueous solution in the neutralization process, and the temperature at which the neutralization reaction is carried out, are preferably 40°C or lower, more preferably 35°C or lower, even more preferably 30°C or lower, and even more preferably 25°C or lower. In addition, from the viewpoint of improving reactivity, the temperature is preferably 0°C or higher, more preferably 10°C or higher, even more preferably 15°C or higher, and even more preferably 20°C or higher.

[0048] In the neutralization process, any type of mixer can be used as long as it can efficiently mix the sulfonate and the alkaline aqueous solution and apply shear force to the oily substance. Examples of such mixers include: static mixers, impact mixers, impeller mixers, and vibratory mixers. Examples of static mixers include the static mixer manufactured by Noritake. Examples of impact mixers include the high-pressure emulsifier manufactured by Nanozizer. Examples of impeller mixers include the Milder manufactured by Pacific Machine Co., Ltd., and the HOMO MIXER manufactured by Primix. From the viewpoint of equipment cost, impeller mixers are preferred.

[0049] When using a blade-type mixer, from the viewpoint of suppressing the formation of impurities such as internal olefins and inorganic salts, the mixing speed of the mixer is preferably 5 m / s or more, more preferably 10 m / s or more, and even more preferably 20 m / s or more. Furthermore, from the viewpoint of suppressing exothermic reactions, it is preferably 200 m / s or less, more preferably 100 m / s or less, even more preferably 50 m / s or less, even more preferably 30 m / s or less, even more preferably 27.5 m / s or less, and even more preferably 25 m / s or less. Here, the mixing speed refers to the speed of the tip of the mixing blade, expressed as 2 × (pi) × (radius of the mixing blade) × (rotational speed per unit time).

[0050] Regarding the neutralization process, examples include continuous and batch processes. From the viewpoint of suppressing byproduct formation and improving productivity, a continuous process is preferred, where the reaction liquid is circulated using a ring reactor while sulfonate and alkaline aqueous solution are added, and the reaction liquid is simultaneously withdrawn. Here, "batch process" refers to a process where the reaction is started and carried out after the raw materials are added to the reactor, and the product is recovered afterward; "continuous process" refers to a process where both raw material input and product recovery are carried out simultaneously during the reaction. Furthermore, the "semi-batch process" described below refers to a process where either raw material input or product recovery is carried out simultaneously during the reaction.

[0051] From the viewpoint of reducing impurities, the mixing time when mixing the sulfonate with the alkaline aqueous solution in the neutralization process is preferably 10 minutes or more, more preferably 20 minutes or more, and even more preferably 30 minutes or more. From the viewpoint of improving economy, it is preferably 120 minutes or less, more preferably 90 minutes or less, even more preferably 60 minutes or less, and even more preferably 50 minutes or less.

[0052] From the viewpoint of obtaining a high concentration of olefin sulfonate composition, the concentration of 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. Furthermore, from the viewpoint of suppressing the increase in viscosity of the neutralization product, it is preferably 65% ​​by mass or less, more preferably 60% by mass or less. The concentration of olefin sulfonate in the neutralization product is calculated as: olefin sulfonate concentration + γ-sulfonyl lactone concentration × (molecular weight of 3-hydroxysulfonate / molecular weight of γ-sulfonyl lactone).

[0053] <Hydrolysis Process>

[0054] The hydrolysis process is a process of obtaining hydrolysate by heating the neutralized product obtained in the neutralization process.

[0055] In the hydrolysis process, from the viewpoint of improving reactivity, the hydrolysis temperature is preferably 120°C or higher, more preferably 140°C or higher, and even more preferably 160°C or higher. In addition, from the viewpoint of suppressing product decomposition, the temperature is preferably 220°C or lower, and more preferably 200°C or lower.

[0056] The hydrolysis reaction can be carried out in a batch reactor or a continuous reactor. When using a batch reactor, mixing is preferably performed using a mixer or similar device.

[0057] From the viewpoint of ending the reaction, the processing time of the hydrolysis process is preferably 30 minutes or more, more preferably 45 minutes or more, and even more preferably 1 hour or more. In addition, from the viewpoint of improving productivity, it is preferably 4 hours or less, and more preferably 3 hours or less.

[0058] From the viewpoint of the color of the sulfonate composition obtained by the reaction and the color of the sulfonate composition obtained after decolorization, the average double bond position of the raw olefin of the above-mentioned inner olefin sulfonate is preferably 3 or more, more preferably 3.5 or more, and even more preferably 3.8 or more. In addition, from the viewpoint of suppressing the mixing of by-products and reducing the peroxide value of the sulfonate composition obtained after decolorization, it 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.

[0059] From the viewpoint of cleaning performance when the decolorized internal olefin sulfonate composition (decolorized internal olefin sulfonate composition) obtained by the decolorization process (A) described below is used in a detergent, the internal olefin sulfonate is preferably one or more internal olefin sulfonates selected from internal olefin sulfonates having 16 carbon atoms and internal olefin sulfonates having 18 carbon atoms. Here, the number of carbon atoms in the internal olefin sulfonate is derived from the carbon chain of the internal olefin.

[0060] Regarding the concentration of alkaline compounds in the olefin sulfonate composition obtained in the hydrolysis process, from the viewpoint of suppressing the deterioration of the odor of the olefin sulfonate composition after the decolorization process (A) and reducing the peroxide value of the olefin sulfonate composition after the decolorization process (A), it is preferably 0.010 mmol or more, more preferably 0.015 mmol, even more preferably 0.020 mmol or more, even more preferably 0.025 mmol or more, and even more preferably 0.029 mmol or more. Furthermore, from the viewpoint of suppressing the decrease in preservation stability, it is preferable to be 0.27 mmol or less, more preferably 0.240 mmol or less, and even more preferably 0.210 mmol or less. In addition, from the viewpoint of improving the fading rate, it is preferable to be 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.

[0061] The hydrolysis process is not limited to the steps described above to obtain hydrolysates. The concentration of alkaline compounds in the olefin sulfonate composition can also be controlled by adjusting the amount of alkaline compounds.

[0062] From the viewpoint of reducing impurities in the olefin sulfonate composition, the olefin sulfonate composition is preferably manufactured by a method in which the concentration of the alkaline compound in the olefin sulfonate composition after the hydrolysis step is controlled within the aforementioned suitable range by an adjustment method selected from adjusting the amount of alkaline compound used in the neutralization step and adjusting the amount of alkaline compound in the hydrolysis step. Furthermore, from the same viewpoint, the olefin sulfonate composition is more preferably manufactured by a method in which the concentration of the alkaline compound in the olefin sulfonate composition after the hydrolysis step is controlled within the aforementioned suitable range by adjusting the amount of alkaline compound used in the neutralization step. The suitable range for the amount of alkaline compound used in the neutralization step is as described above.

[0063] <Decolorization Process (A)>

[0064] The decolorization process (A) is a process in which the following steps are performed on a system containing an internal olefin sulfonate composition:

[0065] Adjustment step (a1), adjusting the concentration of the basic compound in the above system: and

[0066] In the mixing step (a2), the decolorizing agent is mixed with the olefin sulfonate composition present in the system.

[0067] The above-mentioned adjustment step (a1) is a step of adjusting the concentration of the alkaline compound so that the concentration of the alkaline compound after mixing the decolorizing agent with the olefin sulfonate composition present in the system in the above-mentioned decolorization step (A) is 0.004 mmol or more and 0.26 mmol or less relative to 1 g of olefin sulfonate.

[0068] In this invention, "reactor" refers to the reaction vessel itself used in a batch or semi-batch manner, and "reaction apparatus" refers to the entire unit that participates in the reaction, including the reaction vessel, piping, etc. A continuous reaction apparatus sometimes does not include a reaction vessel.

[0069] The system containing the above-mentioned olefin sulfonate composition can also be a liquid (liquid composition) containing the olefin sulfonate composition.

[0070] There is no particular limitation on the order in which the adjustment step (a1) and the mixing step (a2) are performed. The adjustment step (a1) can be performed after the mixing step (a2), or the mixing step (a2) can be performed after the adjustment step (a1). Alternatively, the mixing step (a2) and the adjustment step (a1) can be performed simultaneously. Since the decolorization treatment (decolorization reaction) is initiated by mixing (contacting) the decolorizing agent with the olefin sulfonate composition, when the adjustment step (a1) is performed after the mixing step (a2), from the viewpoint of suppressing odor deterioration, it is preferable to perform the adjustment step (a1) immediately after the mixing step (a2). In this invention, from the viewpoint of suppressing odor deterioration and improving economy, it is preferable to perform the mixing step (a2) and the adjustment step (a1) simultaneously.

[0071] The above-mentioned decolorization treatment (decolorization reaction) refers to the state in which the decolorizing agent and the internal olefin sulfonate composition coexist, and the decolorization treatment includes the above-mentioned mixing step (a2) and the following aging step (b). Here, the aging step (b) refers to the process of maintaining the state in which the decolorizing agent and the internal olefin sulfonate composition coexist after mixing the decolorizing agent.

[0072] The decolorization step (A) described above can be carried out at any stage after the formation of the olefin sulfonate composition in the manufacturing process of the olefin sulfonate composition described above, preferably after the neutralization step described above or after the hydrolysis step described above, and from the viewpoint of suppressing the generation of by-products, it is even more preferably carried out after the hydrolysis step.

[0073] The suitable form of the concentration of basic compounds in the olefin sulfonate composition before the above-mentioned decolorization step (A) is the same as the suitable form of the concentration of basic compounds in the olefin sulfonate composition obtained in the above-mentioned hydrolysis step.

[0074] The aforementioned system containing an internal olefin sulfonate composition includes an internal olefin sulfonate composition before decolorization treatment. Specifically, examples include a system containing an internal olefin sulfonate composition after the above-mentioned neutralization step, or a system containing an internal olefin sulfonate composition after the above-mentioned hydrolysis step. The steps are described below.

[0075] [Adjustment Step (a1)]

[0076] The adjustment step (a1) is a step of adjusting the concentration of the alkaline compound so that the concentration of the alkaline compound after mixing the decolorizing agent with the olefin sulfonate composition present in the system in the decolorization step (A) is 0.004 mmol or more and 0.26 mmol or less relative to 1 g of the olefin sulfonate. By mixing the decolorizing agent with the olefin sulfonate composition to carry out the decolorization reaction, the concentration of the alkaline compound in the reaction system is reduced. Therefore, the concentration of the alkaline compound in the system is controlled (adjusted) in the adjustment step (a1). In this invention, it is preferable to adjust the concentration of the alkaline compound in the system immediately after the mixing step (a2) so that it is within the above-mentioned range.

[0077] In adjustment step (a1), the concentration of the alkaline compound in the system is adjusted to be 0.004 mmol or more and 0.26 mmol or less relative to 1 g of the olefin sulfonate after mixing step (a2). By achieving this concentration of the alkaline compound, a decolorized olefin sulfonate composition with good fading properties, mild odor, and good storage stability can be obtained. From the viewpoint of suppressing odor deterioration and reducing peroxide value, the concentration of the alkaline compound is preferably 0.005 mmol or more, more preferably 0.010 mmol or more, further preferably 0.015 mmol or more, even more preferably 0.020 mmol or more, and even more preferably 0.030 mmol or more. Furthermore, from the viewpoint of suppressing the decrease in the storage stability of the decolorized olefin sulfonate composition, the concentration of the alkaline compound is preferably 0.23 mmol or less, more preferably 0.215 mmol or less, and even more preferably 0.20 mmol or less. Additionally, from the viewpoint of improving the fading rate, it 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. Since the concentration of the alkaline compound decreases during the decolorization process, it is preferable to adjust the concentration of the alkaline compound immediately after the decolorization process (i.e., after the mixing step (a2)). Furthermore, the adjustment step (a1) is a step for adjusting the concentration of the alkaline compound. If the concentration of the alkaline compound is already within a suitable range, it is not necessary to change the concentration of the alkaline compound. Such cases where the concentration of the alkaline compound does not need to be adjusted are also included in the "adjustment step (a1)" of the present invention.

[0078] When the adjustment step (a1) is performed after the mixing step (a2), the concentration of the alkaline compound can be adjusted to the aforementioned concentration in the adjustment step (a1). On the other hand, when the adjustment step (a1) is performed before the mixing step (a2), it is preferable to adjust the concentration of the alkaline compound by increasing the concentration of the alkaline compound that has decreased due to the decolorization treatment. Specifically, from the viewpoints of suppressing odor deterioration and reducing peroxide value, the concentration of the alkaline compound in the adjustment step (a1) relative to 1g of the inner olefin sulfonate is preferably 0.010 mmol or more, more preferably 0.015 mmol, even more preferably 0.020 mmol or more, even more preferably 0.025 mmol or more, even more preferably 0.030 mmol or more, and even more preferably 0.035 mmol or more. Furthermore, from the viewpoint of suppressing the decrease in storage stability, it is preferable to be 0.270 mmol or less, more preferably 0.240 mmol or less, and even more preferably 0.210 mmol or less. In addition, from the viewpoint of improving the fading rate, it is even more preferable to be 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.

[0079] There are no particular restrictions on the adjustment method, which can be carried out as follows: Extract the liquid from the system and rapidly analyze the concentration of the basic compound in the extracted liquid at room temperature. If the result of this analysis is below the aforementioned suitable concentration range (e.g., the concentration of the basic compound after the mixing step is less than 0.004 mmol per 1g of the olefin sulfonate), then the basic compound can be added back into the system to adjust the concentration of the basic compound after the mixing step to the aforementioned suitable concentration.

[0080] The aforementioned basic compounds can be either inorganic or organic. Examples of inorganic basic 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 basic compounds include amine compounds such as ammonia and 2-aminoethanol, which have 1 to 6 carbon atoms.

[0081] From the viewpoint of ease of acquisition and improved economy, the above-mentioned alkaline compound is preferably an inorganic alkaline compound, more preferably an alkali metal hydroxide, and even more preferably at least one selected from sodium hydroxide and potassium hydroxide.

[0082] From the viewpoint of ease of use, the above-mentioned alkaline compound is preferably used in the form of an alkaline aqueous solution.

[0083] The above adjustment steps (a1) can be carried out in batches, semi-batches, or continuously, but from the point of view of improving productivity, continuous operation is preferred.

[0084] Regarding the above adjustment step (a1), for example, when using the above-described ring-shaped reaction apparatus, the liquid in the system can be extracted, and the concentration of the alkaline compound in the extracted mixture can be quickly analyzed at room temperature, so this is preferred.

[0085] In the adjustment step (a1), from the viewpoint of reducing odor, it is preferable to perform the process continuously with a circulation system. For example, it is preferable to continuously adjust the process while circulating the internal olefin sulfonate composition using the aforementioned cyclic reaction apparatus or the like. From the viewpoint of reducing odor, the circulation ratio is preferably greater than 0 times, more preferably 1 times or more, further preferably 2 times or more, more preferably 3 times or more, and even more preferably 4 times or more. In addition, from the viewpoint of improving economy, it is preferably 20 times or less, more preferably 10 times or less, and even more preferably 8 times or less. Here, the circulation ratio refers to the ratio of the flow rate circulating in the reaction apparatus to the flow rate input into the reaction apparatus, and is expressed as ((flow rate in the reaction apparatus) / (flow rate input into the reaction apparatus)) - 1. Furthermore, here, the flow rate in the reaction apparatus refers to the flow rate immediately after merging with the fluid input into the reaction apparatus.

[0086] In adjustment step (a1), any type of mixer can be used, as long as it can efficiently mix the internal olefin sulfonate composition with the decolorizing agent (an aqueous solution of the decolorizing agent). Examples of such mixers include: stirring blades, static mixers, impact mixers, stirring blade mixers, and vibrating mixers. Stirring blades include small blades and large blades; examples of small blades include flat paddle stirring blades, inclined paddle stirring blades, and propeller blades. Examples of large blades include: anchor blades, ribbon blades, screw blades, MAXBLEND, high-speed mixing blades (MR205 (product name, manufactured by SATAKE MultiMix Co., Ltd.) etc.), and FULLZONE, etc. Examples of static mixers include static mixers manufactured by Noritake Co., Ltd. Examples of impact mixers include high-pressure emulsifiers manufactured by Nanozer Co., Ltd. Examples of impeller-type mixers include Milder manufactured by Pacific Machinery Co., Ltd., Cavitron manufactured by Pacific Machinery Co., Ltd., and the PIPELINE-HOMO MIXER manufactured by Primix. Among these, from the viewpoint of improving colorfastness, impeller-type mixers are preferred, large-blade impeller-type mixers are more preferred, and impeller-type mixers are even more preferred.

[0087] When using the reaction tank with stirring blades or the stirring blade type mixer described above in adjustment step (a1), from the viewpoint of decolorization effect (fading rate) and improved mixing, the circumferential speed of the stirring blades 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, even more preferably 0.3 m / s or more, even more preferably 0.9 m / s or more, even more preferably 4.7 m / s or more, even more preferably 7.0 m / s or more, even more preferably 9.0 m / s or more. In addition, from the viewpoint of improving economy, it is preferably 50 m / s or less, more preferably 40 m / s or less, even more preferably 26 m / s or less, and even more preferably 15 m / s or less. When the adjustment step (a1) is carried out continuously, from the viewpoint of improving the fading rate, the circumferential 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, even more preferably 7.0 m / s or more, and even more preferably 9.0 m / s or more. In addition, from the viewpoint of reducing odor deterioration and improving economy, it is preferably 50 m / s or less, more preferably 40 m / s or less, even more preferably 26 m / s or less, and even more preferably 15 m / s or less. When the adjustment step (a1) is performed in a semi-batch manner, from the viewpoint of improving the fading rate, the circumferential 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. In addition, from the viewpoint of reducing odor deterioration and improving economy, it 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. When adjusting in batches (a1), from the viewpoint of improving the fading rate, the circumferential 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, even more preferably 1.0 m / s or more, and even more preferably 1.5 m / s or more. In addition, from the viewpoint of reducing odor deterioration and improving economy, it 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, even more preferably 5 m / s or less, and even more preferably 3 m / s or less.

[0088] When using a reaction tank with stirring blades or a stirring blade type mixer in adjustment step (a1), from the viewpoint of improving production capacity, mixing quality, or fading rate, the ratio of the stirring blade diameter d to the tank diameter D (d / D) is preferably 0.01 or more, more preferably 0.05 or more, further preferably 0.1 or more, further more preferably 0.3 or more, further more preferably 0.4 or more, further more preferably 0.5 or more, and further more preferably 0.55 or more. Furthermore, from the viewpoint of improving economy, it is preferably less than 1, more preferably 0.9 or less, further preferably 0.8 or less, and further more preferably 0.7 or less. Additionally, from the viewpoint of improving mixing quality, it is preferably 0.7 or more, more preferably 0.8 or more, further preferably 0.9 or more, and preferably less than 1.

[0089] When using a reaction tank with stirring blades or a stirring blade type mixer in adjustment step (a1), from the viewpoint of improving mixing and fading rate, the ratio of the stirring blade height h to the tank height H (h / H) is preferably 0.01 or more, more preferably 0.05 or more, further preferably 0.1 or more, further more preferably 0.3 or more, and even more preferably 0.4 or more. Furthermore, from the viewpoint of suppressing foaming, it is preferably less than 1, more preferably 0.9 or less, further preferably 0.8 or less, and even more preferably 0.7 or less. Additionally, from the viewpoint of improving mixing, it is preferably 0.7 or more, more preferably 0.8 or more, further preferably 0.9 or more, and preferably less than 1.

[0090] When a reaction tank with stirring blades or a stirring blade type mixer is used in adjustment step (a1), from the viewpoint of improving mixing, the number of blades of the stirring blade is preferably 1 or more, more preferably 2 or more, and even more preferably 3 or more. In addition, from the viewpoint of improving economy, it is preferably 10 or less, more preferably 9 or less, and even more preferably 8 or less.

[0091] When a reaction tank with stirring blades is used in the above adjustment step (a1) and the adjustment is carried out in batches, the above d / D, h / H, and the number of stirring blades are preferably within the above suitable range.

[0092] The above-mentioned adjustment step (a1) is preferably performed under shear conditions. From the viewpoint of improving mixing, the shear rate is preferably 5 / s or more, more preferably 10 / s or more, even more preferably 100 / s or more, even more preferably 500 / s or more, even more preferably 1000 / s or more, even more preferably 1500 / s or more. In addition, from the viewpoint of reducing odor deterioration and improving economy, it is preferably 100000 / s or less, more preferably 50000 / s or less, even more preferably 30000 / s or less, and even more preferably 20000 / s or less. When the adjustment step (a1) is performed continuously, from the viewpoint of improving the fading rate, the shearing speed 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. In addition, from the viewpoint of reducing odor deterioration and improving economy, it is preferably 100000 / s or less, more preferably 50000 / s or less, even more preferably 30000 / s or less, and even more preferably 20000 / s or less. When adjusting the process in a semi-batch manner (a1), from the viewpoint of improving the fading rate, the shearing speed is preferably 10 / s or more, more preferably 100 / s or more, even more preferably 500 / s or more, even more preferably 1000 / s or more, and even more preferably 1500 / s or more. In addition, from the viewpoint of reducing odor deterioration and improving economy, it is preferably 100000 / s or less, more preferably 50000 / s or less, even more preferably 40000 / s or less, even more preferably 30000 / s or less, even more preferably 20000 / s or less, even more preferably 10000 / s or less, and even more preferably 8000 / s or less. When adjusting in batches (a1), from the viewpoint of improving the fading rate, 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. Furthermore, from the viewpoint of reducing odor deterioration and improving economy, 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) = rotational speed of the stirring blade (rpm) × pi × stirring blade diameter (m) / (30 × (inner diameter of the reaction tank (m) - stirring blade diameter (m))).

[0093] From the viewpoint of improving mixing, the power (Pv) required for stirring per unit volume of liquid in the mixer used in the above adjustment step (a1) is preferably 0.1 kW / m. 3 The above is preferred, with 0.2kW / m 3 The above is further preferred to be 0.3kW / m 3In addition, from the viewpoint of improving economic efficiency, 100 kW / m is preferred. 3 The following is more preferably 50 kW / m 3 The following is further preferred: 30 kW / m 3 Hereinafter, a further preferred value is 10 kW / m 3 The following is a further preferred option: 5 kW / m 3 The following is a further preferred value: 1 kW / m 3 Below. Additionally, the power required for stirring per unit volume of liquid (Pv) (kW / m²) is as follows. 3 = Power required for stirring P (kW) / Liquid volume (m³) 3 Here, the power P required for stirring is represented by subtracting the idling power from the power in the actual liquid.

[0094] From the viewpoints of pH control, improved mixing, and suppression of foaming, the system pressure in the above-mentioned adjustment step (a1) is preferably 0 MPaG or more, more preferably 0.01 MPaG or more, even more preferably 0.05 MPaG or more, even more preferably 0.1 MPaG or more, and even more preferably 0.2 MPaG or more. Furthermore, from the viewpoint of improving economy, 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 represents gauge pressure.

[0095] [Mixing Step (a2)]

[0096] There are no particular limitations on the decolorizing agent used, but an oxidizing agent is preferred. Examples of oxidizing agents include hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate. One of these can be used alone, or two or more can be used in combination. Among these, hydrogen peroxide is preferred from the viewpoint of suppressing the introduction of impurities.

[0097] From the viewpoint of improving the decolorization effect (fading rate), the mixing amount of the above-mentioned decolorizing agent relative to 1g of the olefin sulfonate in the olefin sulfonate composition is preferably 1 mg or more, more preferably 5 mg or more, further preferably 10 mg or more, further more preferably 15 mg or more, and even more preferably 20 mg or more. In addition, from the viewpoint of improving economy and inhibiting peroxide value, the mixing amount of the above-mentioned decolorizing agent relative to 1g of the olefin sulfonate in the olefin sulfonate composition is preferably 300 mg or less, more preferably 100 mg or less, further preferably 40 mg or less, and even more preferably 30 mg or less.

[0098] In the mixing step (a2), the decolorizing agent can be mixed all at once or in multiple batches; there is no limit to the number of batches.

[0099] From the viewpoint of ease of use, the decolorizing agent is preferably used in the form of an aqueous solution. There is no particular limitation on the concentration of the decolorizing agent in the aqueous solution. From the viewpoint of reducing the storage tank of the decolorizing agent and improving economy, it is preferably 5% or more, more preferably 10% or more, and even more preferably 30% or more. From the viewpoint of ease of use, it is preferably 70% or less, more preferably 60% or less, and even more preferably 50% or less.

[0100] From the viewpoints of improving the decolorization effect (fading rate) and reducing the peroxide value, 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, even more preferably 80°C or higher, and from an economic point of view, preferably 100°C or lower, more preferably 90°C or lower, even more preferably 85°C or lower. As described above, the decolorization reaction is initiated by mixing the internal olefin sulfonate composition with the decolorizing agent; therefore, the temperature in the mixing step (a2) indicates the temperature at which the decolorization reaction occurs.

[0101] From the viewpoints of suppressing odor deterioration and reducing peroxide value, the pH value of the liquid in the system during mixing step (a2) is preferably 9.3 or higher, more preferably 9.5, and further preferably 9.8 or higher, more preferably 10.0 or higher, from the viewpoint of reducing peroxide value. Furthermore, from the viewpoint of suppressing a decrease in storage stability, it is preferably 11.4 or lower, more preferably 11.3 or lower, and further preferably 11.0 or lower, more preferably 10.8 or lower, and even more preferably 10.5 or lower. The pH value described above can be a value measured using a pH meter installed in the ring reaction apparatus. Additionally, it is preferable to set the pH value within an appropriate range corresponding to the characteristics of the type of alkaline compound.

[0102] The mixing step (a2) described above can be carried out in a batch, semi-batch, or continuous manner. From the viewpoint of improving productivity, it is preferable to carry it out in a so-called continuous manner, that is, while circulating the mixture using a cyclic reactor, the untreated olefin sulfonate composition and the decolorizing agent (an aqueous solution of the decolorizing agent) are added, and the decolorized mixture is simultaneously extracted. In the decolorization step (A), the concentration of the alkaline compound is reduced by the reaction between the olefin sulfonate composition and the decolorizing agent. Therefore, the concentration of the alkaline compound is controlled in the adjustment step (a1) described above.

[0103] In the mixing step (a2), any type of mixer can be used, as long as it can efficiently mix the internal olefin sulfonate composition with the decolorizing agent (an aqueous solution of the decolorizing agent). Examples of such mixers include: impeller mixers, static mixers, impact mixers, impeller mixers, and vibrating mixers. Impellers can be small or large; examples of small impellers include flat paddle impellers, inclined paddle impellers, and propeller impellers. Examples of large impellers include: anchor impellers, ribbon impellers, screw impellers, MAXBLEND, high-speed mixing impellers (MR205 (product name, manufactured by SATAKE MultiMix Co., Ltd.) etc.), and FULLZONE. Examples of static mixers include static mixers manufactured by Noritake. Examples of impact mixers include high-pressure emulsifiers manufactured by Nanozer. Examples of impeller mixers include Milder (manufactured by Pacific Machinery Co., Ltd.), Cavitron (manufactured by Pacific Machinery Co., Ltd.), and HOMO MIXER (manufactured by Primix). Among these, impeller mixers or impeller-type mixers are preferred from the viewpoint of mixing efficiency and improving the fading rate, larger impeller mixers or impeller-type mixers are more preferred, and impeller-type mixers are even more preferred.

[0104] When using the reaction tank with stirring blades or the stirring blade type mixer described above in the mixing step (a2), from the viewpoint of improving the decolorization effect (fading rate), the circumferential speed of the stirring blades 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, even more preferably 0.3 m / s or more, even more preferably 0.9 m / s or more, even more preferably 4.7 m / s or more, even more preferably 7.0 m / s or more, even more preferably 9.0 m / s or more. In addition, from the viewpoint of reducing odor deterioration and improving economy, it 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. When the mixing step (a2) is carried out continuously, from the viewpoint of improving the fading rate, the circumferential 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, even more preferably 7.0 m / s or more, and even more preferably 9.0 m / s or more. In addition, from the viewpoint of reducing odor deterioration and improving economy, it 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. When the mixing step (a2) is carried out in a semi-batch manner, from the viewpoint of improving the fading rate, the circumferential 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. In addition, from the viewpoint of reducing odor deterioration and improving economy, it 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. When the mixing step (a2) is carried out in batches, from the viewpoint of improving the fading rate, the circumferential 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, even more preferably 0.9 m / s or more, and even more preferably 1.5 m / s or more. In addition, from the viewpoint of reducing odor deterioration and improving economy, it 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, even more preferably 10 m / s or less, even more preferably 5 m / s or less, and even more preferably 3 m / s or less.

[0105] When a reaction vessel with stirring blades or a stirring blade type mixer is used in the mixing step (a2), from the viewpoint of improving mixing performance, the ratio of the stirring 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. Furthermore, 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. Additionally, from the viewpoint of improving mixing performance, it is preferably 0.7 or more, more preferably 0.8 or more, even more preferably 0.9 or more, and preferably less than 1.

[0106] When a reaction vessel with stirring blades or a stirring blade type mixer is used in the mixing step (a2), from the viewpoint of improving mixing performance, the ratio of the stirring 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, 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. Furthermore, from the viewpoint of suppressing foaming, it is preferably less than 1, more preferably less than 0.9, even more preferably less than 0.8, and even more preferably less than 0.7. Additionally, from the viewpoint of improving mixing performance, it is preferably 0.7 or more, more preferably 0.8 or more, even more preferably 0.9 or more, and preferably less than 1.

[0107] When a reaction tank with stirring blades or a stirring blade type mixer is used in the mixing step (a2), from the viewpoint of improving mixing, the number of blades of the stirring blades is preferably 1 or more, more preferably 2 or more, and even more preferably 3 or more. Furthermore, from the viewpoint of improving economy, it is preferably 10 or less, more preferably 9 or less, and even more preferably 8 or less.

[0108] When a reaction tank with stirring blades is used in the above mixing step (a2) and adjustments are made in batches, the above d / D, h / H, and the number of stirring blades are preferably within the above suitable ranges.

[0109] From the viewpoint of improving the fading rate, 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, even more preferably 500 / s or more, even more preferably 1000 / s or more, even more preferably 1500 / s or more. In addition, from the viewpoint of reducing odor deterioration and improving economy, it is preferably 100000 / s or less, more preferably 80000 / s or less, even more preferably 70000 / s or less, even more preferably 50000 / s or less, even more preferably 40000 / s or less, even more preferably 30000 / s or less, even more preferably 20000 / s or less. When the mixing step (a2) is carried out continuously, from the viewpoint of improving the fading rate, 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. In addition, from the viewpoint of reducing odor deterioration and improving economy, it is preferably 100000 / s or less, more preferably 80000 / s or less, even more preferably 70000 / s or less, even more preferably 50000 / s or less, even more preferably 40000 / s or less, even more preferably 30000 / s or less, and even more preferably 20000 / s or less. When the mixing step (a2) is carried out in a semi-batch manner, from the viewpoint of improving the fading rate, the shear rate is preferably 10 / s or more, more preferably 100 / s or more, even more preferably 500 / s or more, even more preferably 1000 / s or more, and even more preferably 1500 / s or more. In addition, from the viewpoint of reducing odor deterioration and improving economy, it is preferably 100000 / s or less, more preferably 80000 / s or less, even more preferably 70000 / s or less, even more preferably 50000 / s or less, even more preferably 40000 / s or less, even more preferably 30000 / s or less, and even more preferably 20000 / s or less. When the mixing step (a2) is carried out in batches, from the viewpoint of improving the fading rate, the shearing speed 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. In addition, from the viewpoint of reducing odor deterioration and improving economy, 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 30 / s or less.

[0110] From the viewpoint of improving the fading rate, the power (Pv) required for stirring per unit volume of liquid in the mixer used in the above mixing step (a2) is preferably 0.1 kW / m. 3 The above is preferred, with 0.2kW / m 3The above is further preferred to be 0.3kW / m 3 Furthermore, from the viewpoint of reducing odor deterioration and improving economic efficiency, 100 kW / m² is preferred. 3 The following is more preferably 50kW / m 3 The following is further preferred: 30 kW / m 3 Hereinafter, a further preferred value is 10 kW / m 3 The following is a further preferred option: 5kW / m 3 The following is a further preferred value: 1 kW / m 3 the following.

[0111] From the viewpoint of reducing device volume and peroxide value, the system pressure in the above-mentioned mixing step (a2) is preferably 0 MPaG or more, more preferably 0.01 MPaG or more, even more preferably 0.05 MPaG or more, even more preferably 0.1 MPaG or more, and even more preferably 0.2 MPaG or more. Furthermore, from the viewpoint of improving economy, 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 represents gauge pressure.

[0112] Regarding the system pressure during the adjustment step (a1) performed after the mixing step (a2) or during the adjustment step (a1) performed simultaneously, from the viewpoint of easily controlling the concentration of the basic compound, it is preferably 0 MPaG or more, more preferably 0.01 MPaG or more, even more preferably 0.05 MPaG or more, even more preferably 0.1 MPaG or more, and even more preferably 0.2 MPaG or more. Furthermore, from the viewpoint of improving economy, 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.

[0113] The decolorization process (A) includes the mixing step (a2) and adjustment step (a1) described above, and may also include other steps, for example, preferably a aging step (b).

[0114] [Cooking Step (b)]

[0115] The aging step (b) is a process in which, after the mixing step (a2) described above, no new decolorizing agent is added, but the decolorizing agent and the internal olefin sulfonate composition coexist, and mixing is not required by a mixer or the like. In this invention, from the viewpoint of reducing peroxide value, the aging step (b) is preferred.

[0116] From an economic point of view, the suitable temperature range for the curing step (b) can be the same as the suitable temperature range for the mixing step (a2). On the other hand, for example, from the viewpoint of economy and reducing peroxide value, it is preferably 40°C or higher, more preferably 50°C or higher, and even more preferably 60°C or higher. In addition, from the viewpoint of improving economy, it is preferably 120°C or lower, more preferably 110°C or lower, and even more preferably 100°C or lower.

[0117] There are no particular limitations on the reaction apparatus for the ripening step (b). In a batch reactor, a constant temperature bath or a trough reactor can be used. Additionally, in a semi-batch or continuous reactor, a trough reactor can be used. The shape of the trough reactor can be cylindrical, rectangular, or spherical; from an economic point of view, a cylindrical reactor is preferred. Furthermore, trough reactors with cylindrical troughs can be horizontally or vertically oriented; from an efficiency point of view, a vertically oriented cylindrical reactor is preferred. Additionally, to improve reaction efficiency, a dispersion component such as a perforated plate or dispersion plate can be provided within the reactor as needed.

[0118] When using the above-described vertical cylindrical reactor for the curing step (b), from the viewpoint of improving reaction efficiency, the ratio (H1 / D1) of the height H1 of the vertical cylindrical reactor to the reactor inner diameter D1 is preferably 0.1 or more, more preferably 1 or more, and even more preferably 1.5 or more. In addition, from the viewpoint of suppressing pressure loss and improving economy, it is preferably 300 or less, more preferably 200 or less, even more preferably 100 or less, even more preferably 50 or less, even more preferably 30 or less, even more preferably 10 or less, and even more preferably 5 or less.

[0119] Regarding the residence time in the curing step (b), from the viewpoint of reducing peroxide value, it is preferably 10 minutes or more, more preferably 20 minutes or more, further preferably 30 minutes or more, further more preferably 45 minutes or more, and even more preferably 60 minutes or more. In addition, from the viewpoint of improving economy, it is preferably 500 minutes or less, more preferably 400 minutes or less, further preferably 300 minutes or less, and even more preferably 200 minutes or less.

[0120] Regarding the pressure in the curing step (b), from the viewpoint of reducing the device volume and reducing the peroxide value, it is preferably 0 MPaG or more, more preferably 0.01 MPaG or more, even more preferably 0.05 MPaG or more, even more preferably 0.1 MPaG or more, and even more preferably 0.2 MPaG or more. In addition, from the viewpoint of improving economy, 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.

[0121] The above-mentioned maturation step (b) can be continuous, semi-batch or batch. From the viewpoint of reaction efficiency, batch or semi-batch is preferred, and from the viewpoint of improving productivity, continuous is preferred.

[0122] When the curing step (b) is carried out continuously, from the viewpoint of maintaining the uniformity of the composition of the internal olefin sulfonate composition, the linear velocity 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 even more preferably 0.1 or more. From the viewpoint of reducing the peroxide value, it is preferably 1000 mm / s or less, more preferably 800 mm / s or less, even more preferably 500 mm / s or less, even more preferably 300 mm / s or less, even more preferably 100 mm / s or less, even more preferably 50 mm / s or less, even more preferably 10 mm / s or less, even more preferably 5 mm / s or less, and even more preferably 1 mm / s or less.

[0123] The decolorized olefin sulfonate composition obtained by the above-described decolorization process (A) preferably has a fading rate of 50% or more, more preferably 60% or more, even more preferably 63% or more, and even more preferably 65% ​​or more. Here, the fading rate can be determined by the method described in the examples.

[0124] Regarding the peroxide value of the decolorized internal olefin sulfonate composition obtained through the above-described decolorization process (A), from the viewpoint of the stability of the decolorized internal olefin sulfonate composition, it is preferably 37.0 meq or less, more preferably 30.0 meq or less, even more preferably 20.0 meq or less, even more preferably 10 meq or less, even more preferably 7 meq or less, and even more preferably 5 meq or less, relative to 1 kg of internal olefin sulfonate in the internal olefin sulfonate composition. Furthermore, the above concentration can also be achieved by reducing and decomposing any remaining oxidizing agents or other decolorizing agents. Here, the peroxide value can be measured using the method described in the examples.

[0125] The decolorized olefin sulfonate composition obtained by the manufacturing method of the present invention can be used directly for various applications, or it can be further refined by defoaming or pH adjustment processes, or by desalination. Furthermore, the concentration of the active ingredient can be adjusted by adding water or by concentration, or it can be used after mixing with other surfactants or solvents.

[0126] The defoaming process can also be combined in the above-mentioned processes (adjustment step, mixing step, maturation step).

[0127] <pH Adjustment Procedure>

[0128] A pH adjustment step can also be performed after the above-mentioned decolorization step (A) to adjust the pH value of the decolorized olefin sulfonate composition.

[0129] When performing a pH adjustment step, from the viewpoint of suppressing the increase of impurities in the decolorized olefin sulfonate composition, the pH value of the olefin sulfonate composition after pH adjustment is preferably 8.5 or higher, more preferably 9.0 or higher, and from the viewpoint of ease of use, preferably 12.0 or lower, more preferably 11.4 or lower, further preferably 11.0 or lower, and even more preferably 10.5 or lower. Here, the above-mentioned pH value is the pH value measured at 25°C after adjusting the concentration of olefin sulfonate in the decolorized olefin sulfonate composition to 10% by mass.

[0130] There are no particular restrictions on the acids used to adjust the pH value. Examples 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 can be used alone or in combination with two or more. Preferably, one or more of citric acid and phosphoric acid are selected, more preferably citric acid. Furthermore, to improve pH controllability, one or more pH buffers can be used or used in combination. There are no particular restrictions on the pH buffers; examples include acetic acid, citric acid, phosphoric acid, EDTA, and sodium carbonate.

[0131] From the viewpoint of ease of use, the acid is preferably used in the form of an aqueous solution.

[0132] The decolorized olefin sulfonate composition obtained by the manufacturing method of the present invention has good fading properties, a mild odor, and good storage stability. Therefore, it can be suitable for various applications such as body wash, shampoo, laundry detergent, and dishwashing detergent.

[0133] In addition to the foregoing description, the present invention and its preferred embodiments are illustrated below.

[0134] <1> A method for manufacturing a decolorized internal olefin sulfonate composition, comprising a decolorization step (A) in which the system containing the internal olefin sulfonate composition is subjected to the following steps:

[0135] Adjustment step (a1): Adjust the concentration of the basic compound in the above system; and

[0136] In the mixing step (a2), the decolorizing agent is mixed with the olefin sulfonate composition present in the system.

[0137] The above-mentioned adjustment step (a1) is a step of adjusting the concentration of the alkaline compound so that the concentration of the alkaline compound after mixing the decolorizing agent with the olefin sulfonate composition present in the system in the above-mentioned decolorization step (A) is 0.004 mmol or more and 0.26 mmol or less relative to 1 g of olefin sulfonate.

[0138] <2> The method for manufacturing the decolorized olefin sulfonate composition according to <1>, wherein the above-mentioned adjustment step (a1) is performed after the above-mentioned mixing step (a2).

[0139] <3> The method for manufacturing the decolorized olefin sulfonate composition according to <1>, wherein the above-mentioned mixing step (a2) is performed after the above-mentioned adjustment step (a1).

[0140] <4> The method for manufacturing the decolorized olefin sulfonate composition according to <1>, wherein the above-mentioned adjustment step (a1) and the above-mentioned mixing step (a2) are performed simultaneously.

[0141] <5> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <4>, wherein the decolorization step (A) is performed after the neutralization step or after the hydrolysis step, preferably after the hydrolysis step.

[0142] <6> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <1> to <5>, wherein, after adjusting the concentration of the alkaline compound in the adjustment step (a1), the concentration of the alkaline compound in the liquid relative to 1g of the olefin sulfonate is preferably 0.005 mmol or more, more preferably 0.010 mmol or more, even more preferably 0.015 mmol or more, even more preferably 0.020 mmol or more, even more preferably 0.030 mmol or more, 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, even more preferably 0.06 mmol or less.

[0143] <7> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <1> to <5>, wherein, after adjusting the concentration of the alkaline compound in the adjustment step (a1), the concentration of the alkaline compound in the liquid relative to 1 g of the olefin sulfonate is preferably 0.010 mmol or more, more preferably 0.015 mmol, even more preferably 0.020 mmol or more, even more preferably 0.025 mmol or more, even more preferably 0.030 mmol or more, even more preferably 0.035 mmol or more, preferably 0.270 mmol or less, even more preferably 0.240 mmol or less, even more preferably 0.210 mmol or less, 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, even more preferably 0.08 mmol or less.

[0144] <8> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <7>, wherein the above-mentioned adjustment method is performed by extracting liquid from the system and rapidly analyzing the concentration of the alkaline compound in the extracted liquid at room temperature.

[0145] <9> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <8>, wherein the alkaline compound is preferably an inorganic alkaline compound, more preferably an alkali metal hydroxide, and even more preferably at least one selected from sodium hydroxide and potassium hydroxide.

[0146] <10> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <9>, wherein the above-mentioned adjustment step (a1) is preferably carried out in a batch, semi-batch or continuous manner, more preferably in a continuous manner.

[0147] <11> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <10>, wherein the above-mentioned adjustment step (a1) is carried out using a cyclic reaction apparatus.

[0148] <12> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <11>, wherein the above-mentioned adjustment step (a1) is carried out continuously with a circulating system.

[0149] <13> The method for manufacturing the decolorized olefin sulfonate composition according to <12>, wherein the cycle ratio of the above-mentioned cycle system is preferably greater than 0 times, more preferably more than 1 times, more preferably more than 2 times, even more preferably more than 3 times, even more preferably more than 4 times, preferably less than 20 times, more preferably less than 10 times, and even more preferably less than 8 times.

[0150] <14> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <13>, wherein,

[0151] The above adjustment step (a1) is performed using a reaction vessel with stirring blades or a stirring blade type mixer.

[0152] The circumferential speed of the aforementioned stirring blades is between 0.01 m / s and 50 m / s.

[0153] <15> In the method for manufacturing the decolorized olefin sulfonate composition according to <14>, the circumferential speed of the stirring blade in 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, even more preferably 0.3 m / s or more, even more preferably 0.9 m / s or more, even more preferably 4.7 m / s or more, even more preferably 7.0 m / s or more, even more preferably 9.0 m / s or more, preferably 50 m / s or less, even more preferably 40 m / s or less, even more preferably 26 m / s or less, even more preferably 15 m / s or less.

[0154] <16> The method for manufacturing the decolorized olefin sulfonate composition according to <14>, wherein,

[0155] The above adjustment steps (a1) are performed sequentially.

[0156] The circumferential 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, even more preferably 7.0 m / s or more, even more preferably 9.0 m / s or more, preferably 50 m / s or less, even more preferably 40 m / s or less, even more preferably 26 m / s or less, and even more preferably 15 m / s or less.

[0157] <17> The method for manufacturing the decolorized olefin sulfonate composition according to <14>, wherein,

[0158] The above adjustment steps (a1) are carried out in a semi-batch manner.

[0159] The circumferential 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, even more preferably 0.7 m / s or more, 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, even more preferably 8 m / s or less.

[0160] <18> The method for manufacturing the decolorized olefin sulfonate composition according to <14>, wherein,

[0161] The above adjustment steps (a1) are carried out in batches.

[0162] The circumferential 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, even more preferably 1.0 m / s or more, even more preferably 1.5 m / s or more, preferably 50 m / s or less, even 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, even more preferably 5 m / s or less, even more preferably 3 m / s or less.

[0163] <19> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <18>, wherein,

[0164] The above adjustment step (a1) is performed using a reaction vessel with stirring blades or a stirring blade type mixer.

[0165] The ratio (d / D) of the stirring blade diameter d to the groove diameter 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, preferably less than 1, more preferably less than 0.9, even more preferably less than 0.8, even more preferably less than 0.7. From the viewpoint of improving mixing, it is preferably 0.7 or more, more preferably 0.8 or more, even more preferably 0.9 or more, and preferably less than 1.

[0166] <20> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <19>, wherein,

[0167] The above adjustment step (a1) is performed using a reaction vessel with stirring blades or a stirring blade type mixer.

[0168] The ratio (h / H) of the stirring blade height h to the tank height H 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, preferably less than 1, more preferably less than 0.9, even more preferably less than 0.8, even more preferably less than 0.7. From the viewpoint of improving mixing, it is preferably 0.7 or more, more preferably 0.8 or more, even more preferably 0.9 or more, and preferably less than 1.

[0169] <21> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <20>, wherein,

[0170] The above adjustment step (a1) is performed using a reaction vessel with stirring blades or a stirring blade type mixer.

[0171] The number of blades of the stirring blade is preferably 1 or more, more preferably 2 or more, even more preferably 3 or more, preferably 10 or less, more preferably 9 or less, and even more preferably 8 or less.

[0172] <22> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <21>, wherein the above-mentioned adjustment step (a1) is carried out under shear conditions.

[0173] <23> In the method for manufacturing the decolorized olefin sulfonate composition according to <22>, the shear rate is preferably 5 / s or more, more preferably 10 / s or more, even more preferably 100 / s or more, even more preferably 500 / s or more, even more preferably 1000 / s or more, even more preferably 1500 / s or more, preferably 100000 / s or less, even more preferably 50000 / s or less, even more preferably 30000 / s or less, even more preferably 20000 / s or less.

[0174] <24> The method for manufacturing the decolorized olefin sulfonate composition according to <22>, wherein,

[0175] The above adjustment steps (a1) are performed sequentially.

[0176] The aforementioned shearing rate is preferably 100 / s or more, more preferably 500 / s or more, even more preferably 1000 / s or more, even more preferably 1500 / s or more, preferably 100000 / s or less, even more preferably 50000 / s or less, even more preferably 10000 / s or less, even more preferably 8000 / s or less.

[0177] <25> The method for manufacturing the decolorized olefin sulfonate composition according to <22>, wherein,

[0178] The above adjustment steps (a1) are carried out in a semi-batch manner.

[0179] The aforementioned shearing rate is preferably 10 / s or more, more preferably 100 / s or more, even more preferably 500 / s or more, even more preferably 1000 / s or more, even more preferably 1500 / s or more, preferably 100000 / s or less, even more preferably 50000 / s or less, even more preferably 40000 / s or less, even more preferably 30000 / s or less, even more preferably 20000 / s or less, even more preferably 10000 / s or less, even more preferably 8000 / s or less.

[0180] <26> The method for manufacturing the decolorized olefin sulfonate composition according to <22>, wherein,

[0181] The above adjustment steps (a1) are carried out in batches.

[0182] The aforementioned shearing rate is preferably 5 / s or more, more preferably 8 / s or more, even more preferably 10 / s or more, even more preferably 12 / s or more, 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, even more preferably 50 / s or less.

[0183] <27> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <1> to <26>, wherein the stirring power (Pv) required per unit volume of liquid in the mixer used in the above-mentioned adjustment step (a1) is preferably 0.1 kW / m. 3 The above is preferred, with 0.2kW / m 3 The above is further preferred to be 0.3kW / m 3 The above is preferably 100kW / m 3 The following is more preferably 50kW / m 3 The following is a further preferred value: 30kW / m 3 Hereinafter, a further preferred value is 10kW / m 3 The following is a further preferred setting: 5kW / m 3 Hereinafter, a further preferred value is 1kW / m 3 the following.

[0184] <28> The method for manufacturing the decolorized olefinic acid salt composition according to any one of <1> to <27>, wherein the system pressure in the above-mentioned adjustment 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, 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.

[0185] <29> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <28>, wherein the decolorizing agent is an oxidizing agent.

[0186] <30> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <29>, wherein the decolorizing agent is preferably selected from at least one of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate and persulfate, more preferably hydrogen peroxide.

[0187] <31> The method for manufacturing the decolorizing internal olefin sulfonate composition according to any one of <1> to <30>, wherein, relative to 1g of internal olefin sulfonate in the above-mentioned internal olefin sulfonate composition, the mixing amount of the decolorizing agent is preferably 1mg or more, more preferably 5mg or more, further preferably 10mg or more, further more preferably 15mg or more, further more preferably 20mg or more, preferably 300mg or less, more preferably 100mg or less, further preferably 40mg or less, and further more preferably 30mg or less.

[0188] <32> A method for manufacturing a decolorizing internal olefin sulfonate composition according to any one of <1> to <31>, wherein, relative to 1g of internal olefin sulfonate in the above-mentioned internal olefin sulfonate composition, the mixing amount of the decolorizing agent is preferably 1mg or more and 300mg or less, more preferably 5mg or more and 100mg or less, even more preferably 10mg or more and 40mg or less, even more preferably 15mg or more and 30mg or less, and even more preferably 20mg or more and 30mg or less.

[0189] <33> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <32>, wherein the decolorizing agent is an aqueous solution of the decolorizing agent, and the concentration of the decolorizing agent in the aqueous solution is preferably 5% or more, more preferably 10% or more, further preferably 30% or more, preferably 70% or less, more preferably 60% or less, and further preferably 50% or less.

[0190] <34> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <1> to <33>, wherein 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, even more preferably 80°C or higher, preferably 100°C or lower, even more preferably 90°C or lower, and even more preferably 85°C or lower.

[0191] <35> The method for manufacturing the decolorized 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 even more preferably 80°C or higher and 85°C or lower.

[0192] <36> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <1> to <35>, wherein the pH value of the liquid in the system in the mixing step (a2) is preferably 9.3 or more, more preferably 9.5, even more preferably 9.8 or more, even more preferably 10.0 or more, even more preferably 10.2 or more, even more preferably 10.4 or more, preferably 11.4 or less, even more preferably 11.3 or less, even more preferably 11.0 or less, even more preferably 10.8 or less, even more preferably 10.5 or less.

[0193] <37> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <36>, wherein the mixing step (a2) is preferably carried out in a batch, semi-batch or continuous manner, more preferably in a continuous manner.

[0194] <38> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <37>, wherein the above-mentioned mixing step (a2) is carried out continuously, wherein the mixture is circulated using a cyclic reaction apparatus while the undecolorized olefin sulfonate composition and the decolorizing agent (an aqueous solution of the decolorizing agent) are added, and the decolorized mixture is extracted at the same time.

[0195] <39> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <38>, wherein,

[0196] The mixing step (a2) described above is performed using a reaction vessel with stirring blades or a stirring blade type mixer.

[0197] The circumferential speed of the aforementioned stirring blade is above 0.01 m / s and below 50 m / s.

[0198] <40> The method for manufacturing the decolorized olefin sulfonate composition according to <39>, wherein, in the mixing step (a2), the circumferential speed of the stirring blade 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, even more preferably 0.3 m / s or more, even more preferably 0.9 m / s or more, even more preferably 4.7 m / s or more, even more preferably 7.0 m / s or more, even more preferably 9.0 m / s or more, preferably 50 m / s or less, even more preferably 40 m / s, even more preferably 26 m / s or less, even more preferably 15 m / s or less.

[0199] <41> The method for manufacturing the decolorized olefin sulfonate composition according to <39>, wherein,

[0200] The above mixing step (a2) is performed continuously.

[0201] The circumferential 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, even more preferably 7.0 m / s or more, even more preferably 9.0 m / s or more, 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.

[0202] <42> The method for manufacturing the decolorized olefin sulfonate composition according to <39>, wherein,

[0203] The above mixing step (a2) is performed in a semi-batch manner.

[0204] The circumferential 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, even more preferably 0.9 m / s or more, 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, even more preferably 10 m / s or less.

[0205] <43> The method for manufacturing the decolorized olefin sulfonate composition according to <39>, wherein,

[0206] The above mixing step (a2) is performed in batches.

[0207] The circumferential 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, even more preferably 0.9 m / s or more, even more preferably 1.5 m / s or more, 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, even more preferably 10 m / s or less, even more preferably 5 m / s or less, even more preferably 3 m / s or less.

[0208] <44> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <43>, wherein,

[0209] The mixing step (a2) described above is performed using a reaction vessel with stirring blades or a stirring blade type mixer.

[0210] The ratio (d / D) of the stirring blade diameter d to the groove diameter 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, preferably less than 1, more preferably less than 0.9, even more preferably less than 0.8, even more preferably less than 0.7. From the viewpoint of improving mixing, it is preferably 0.7 or more, more preferably 0.8 or more, even more preferably 0.9 or more, and preferably less than 1.

[0211] <45> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <44>, wherein,

[0212] The mixing step (a2) described above is performed using a reaction vessel with stirring blades or a stirring blade type mixer.

[0213] The ratio (h / H) of the stirring blade height h to the tank height H 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, preferably less than 1, more preferably less than 0.9, even more preferably less than 0.8, even more preferably less than 0.7. From the viewpoint of improving mixing, it is preferably 0.7 or more, more preferably 0.8 or more, even more preferably 0.9 or more, and preferably less than 1.

[0214] <46> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <45>, wherein,

[0215] The mixing step (a2) described above is performed using a reaction vessel with stirring blades or a stirring blade type mixer.

[0216] The number of blades of the stirring blade is preferably 1 or more, more preferably 2 or more, even more preferably 3 or more, preferably 10 or less, more preferably 9 or less, and even more preferably 8 or less.

[0217] <47> The method for manufacturing the decolorized 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, even more preferably 500 / s or more, even more preferably 1000 / s or more, even more preferably 1500 / s or more, preferably 100000 / s or less, even more preferably 80000 / s or less, even more preferably 70000 / s or less, even more preferably 50000 / s or less, even more preferably 40000 / s or less, even more preferably 30000 / s or less, even more preferably 20000 / s or less.

[0218] <48> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <46>, wherein,

[0219] The above mixing step (a2) is performed continuously.

[0220] The shear rate in the above mixing step (a2) is preferably 100 / s or more, more preferably 500 / s or more, even more preferably 1000 / s or more, even more preferably 1500 / s or more, preferably 100000 / s or less, even more preferably 80000 / s or less, even more preferably 70000 / s or less, even more preferably 50000 / s or less, even more preferably 40000 / s or less, even more preferably 30000 / s or less, even more preferably 20000 / s or less.

[0221] <49> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <46>, wherein,

[0222] The above mixing step (a2) is performed in a semi-batch manner.

[0223] The shear rate in the above mixing step (a2) is preferably 10 / s or more, more preferably 100 / s or more, even more preferably 500 / s or more, even more preferably 1000 / s or more, even more preferably 1500 / s or more, preferably 100000 / s or less, even more preferably 80000 / s or less, even more preferably 70000 / s or less, even more preferably 50000 / s or less, even more preferably 40000 / s or less, even more preferably 30000 / s or less, even more preferably 20000 / s or less.

[0224] <50> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <46>, wherein,

[0225] The above mixing step (a2) is performed in batches.

[0226] The shear rate in the above mixing step (a2) is preferably 5 / s or more, more preferably 8 / s or more, even more preferably 10 / s or more, even more preferably 12 / s or more, 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, even more preferably 30 / s or less.

[0227] <51> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <1> to <50>, wherein the stirring power (Pv) required per unit volume of liquid in the mixer used in the mixing step (a2) is preferably 0.1 kW / m. 3 The above is preferred, with 0.2kW / m 3 The above is further preferred to be 0.3kW / m 3 The above is preferably 100kW / m 3 The following is more preferably 50kW / m 3 The following is a further preferred value: 30kW / m 3 Hereinafter, a further preferred value is 10kW / m 3 The following is a further preferred setting: 5kW / m 3 Hereinafter, a further preferred value is 1kW / m 3 the following.

[0228] <52> The method for manufacturing the decolorized 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, 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.

[0229] <53> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <1> to <52>, wherein the system pressure during the adjustment step (a1) performed after the mixing step (a2) or during the adjustment step performed simultaneously with the mixing step (a2) is preferably 0 MPaG or more, more preferably 0.01 MPaG or more, even more preferably 0.05 MPaG or more, even more preferably 0.1 MPaG or more, even more preferably 0.2 MPaG or more, preferably 10 MPaG or less, even more preferably 5 MPaG or less, even more preferably 1 MPaG or less, even more preferably 0.5 MPaG or less.

[0230] <54> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <53>, wherein a curing step (b) is further included after the above-mentioned mixing step (a2).

[0231] <55> In the method for manufacturing the decolorized olefin sulfonate composition according to <54>, the temperature range of the above-mentioned curing step (b) is preferably 40°C or higher, more preferably 50°C or higher, even more preferably 60°C or higher, preferably 120°C or lower, more preferably 110°C or lower, and even more preferably 100°C or lower.

[0232] <56> The method for manufacturing the decolorized olefin sulfonate composition according to <54> or <55>, wherein,

[0233] The above-described ripening step (b) is carried out using the above-described vertical cylindrical reactor.

[0234] The ratio (H1 / D1) of the height H1 of the above-mentioned vertical cylindrical reactor to the reactor inner diameter D1 is preferably 0.1 or more, more preferably 1 or more, even more preferably 1.5 or more, preferably 300 or less, more preferably 200 or less, even more preferably 100 or less, even more preferably 50 or less, even more preferably 30 or less, even more preferably 10 or less, even more preferably 5 or less.

[0235] <57> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <54> to <56>, wherein the residence time in the above-mentioned curing step (b) is preferably 10 minutes or more, more preferably 20 minutes or more, even more preferably 30 minutes or more, even more preferably 45 minutes or more, even more preferably 60 minutes or more, preferably 500 minutes or less, even more preferably 400 minutes or less, even more preferably 300 minutes or less, even more preferably 200 minutes or less.

[0236] <58> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <54> to <57>, wherein the pressure in the above-mentioned curing 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, even more preferably 0.2 MPaG or more, preferably 10 MPaG or less, more preferably 5 MPaG or less, even more preferably 1 MPaG or less, even more preferably 0.5 MPaG or less.

[0237] <59> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <54> to <58>, wherein the above-mentioned curing step (b) is preferably carried out continuously, semi-batch or batch, more preferably in batch or semi-batch manner.

[0238] <60> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <54> to <59>, wherein,

[0239] The above-mentioned ripening step (b) is carried out continuously.

[0240] The linear velocity 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, even more preferably 0.1 mm / s or more, preferably 1000 mm / s or less, even more preferably 800 mm / s or less, even more preferably 500 mm / s or less, even more preferably 300 mm / s or less, even more preferably 100 mm / s or less, even more preferably 50 mm / s or less, even more preferably 10 mm / s or less, even more preferably 5 mm / s or less, even more preferably 1 mm / s or less.

[0241] <61> A method for manufacturing a decolorized inner olefin sulfonate composition according to any one of <1> to <60>, wherein the decolorization rate of the decolorized inner olefin sulfonate composition obtained by the above-described decolorization step (A) relative to the inner olefin sulfonate composition before decolorization is preferably 50% or more, more preferably 60% or more, even more preferably 63% or more, and even more preferably 65% ​​or more.

[0242] <62> The method for manufacturing a decolorized internal olefin sulfonate composition according to any one of <1> to <61>, wherein the peroxide value of the decolorized internal olefin sulfonate composition obtained by the above-described decolorization step (A) is preferably 37.0 meq or less, more preferably 30.0 meq or less, even more preferably 20.0 meq or less, even more preferably 10 meq or less, even more preferably 7 meq or less, and even more preferably 5 meq or less.

[0243] <63> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <62>, wherein the method further includes a pH adjustment step.

[0244] <64> The method for manufacturing the decolorized olefin sulfonate composition according to <63>, wherein the pH value of the pH-adjusted olefin sulfonate composition is preferably 8.5 or higher, more preferably 9.0 or higher, more preferably 11.0 or lower, and more preferably 10.5 or lower.

[0245] <65> The method for manufacturing the decolorized olefin sulfonate composition according to <63> or <64>, wherein the acid used to adjust the pH value is preferably selected from one or more of citric acid and phosphoric acid, more preferably citric acid.

[0246] <66> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <65>, wherein,

[0247] The above-mentioned internal olefin sulfonate composition is obtained by a method for manufacturing internal olefin sulfonates, 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.

[0248] The number of carbon atoms in the inner olefin is preferably 10 or more, more preferably 12 or more, even more preferably 14 or more, preferably 22 or less, and more preferably 18 or less.

[0249] <67> The method for manufacturing the decolorized internal olefin sulfonate composition according to <66>, wherein the internal olefin is preferably selected from at least one of internal olefins having 16 carbon atoms and internal olefins having 18 carbon atoms.

[0250] <68> The method for manufacturing the decolorized olefin sulfonate composition according to <66> or <67>, wherein the processing temperature of the above-mentioned sulfonation process is preferably 0°C or higher, and preferably 50°C or lower.

[0251] <69> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <66> to <68>, wherein the concentration of sulfur trioxide gas in the above-mentioned sulfonation process is preferably 0.5% by volume or more, more preferably 1.0% by volume or more, preferably 10% by volume or less, and more preferably 6.0% by volume or less.

[0252] <70> The method for manufacturing the decolorized inner olefin sulfonate composition according to any one of <66> to <69>, wherein the amount of sulfur trioxide gas used in the above-mentioned sulfonation treatment is preferably 0.8 moles or more, more preferably 0.9 moles or more, even more preferably 0.95 moles or more, preferably 1.2 moles or less, more preferably 1.10 moles or less, and even more preferably 1.05 moles or less.

[0253] <71> A method for manufacturing a decolorized inner olefin sulfonate composition according to any one of <66> to <70>, wherein the sulfonation reactor used in the above-mentioned sulfonation process is preferably a reactor equipped with an external sleeve, and more preferably a falling film sulfonation reactor in which the inner olefin flows down in a thin film and reacts with sulfur trioxide gas.

[0254] <72> The method for manufacturing the decolorized olefin sulfonate composition according to <71>, wherein an external sleeve is provided on the sulfonation reactor and cooling water is introduced into the external sleeve for cooling.

[0255] <73> In the method for manufacturing the decolorized olefin sulfonate composition according to <72>, the temperature of the cooling water introduced into the outer sleeve of the sulfonation reactor is preferably 0°C or higher, preferably 30°C or lower, and more preferably 20°C or lower.

[0256] <74> The method for manufacturing the decolorized inner olefin sulfonate composition according to any one of <66> to <73>, wherein the reaction rate of the inner olefin in the sulfonation reaction is preferably 95% or more, more preferably 96% or more, even more preferably 97% or more, and preferably 99.8% or less.

[0257] <75> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <66> to <74>, wherein the alkaline compound used in the above-mentioned neutralization is preferably an inorganic alkaline compound, more preferably an alkali metal hydroxide, and even more preferably at least one selected from sodium hydroxide and potassium hydroxide.

[0258] <76> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <66> to <75>, wherein the alkaline compound used in the above-mentioned neutralization is an alkaline aqueous solution, and the concentration of the alkaline aqueous solution, or the concentration of the mixture when the alkaline aqueous solution and water are mixed, is preferably 1% by mass or more, more preferably 4.5% by mass or more, further preferably 7% by mass or more, further more preferably 10% by mass or more, further more preferably 12% by mass or more, preferably 50% by mass or less, more preferably 32% by mass or less, further preferably 23% by mass or less, further more preferably 20% by mass or less, and further more preferably 18% by mass or less.

[0259] <77> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <66> to <76>, wherein the concentration of the alkaline compound in the olefin sulfonate composition after the hydrolysis step is controlled by adjusting the amount of alkaline compound used in the neutralization step and / or hydrolysis step.

[0260] <78> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <66> to <77>, wherein the amount of the basic compound used in the above-mentioned neutralization is preferably 1 molar multiple or more, more preferably 1.02 molar multiple or more, even more preferably 1.03 molar multiple or more, even more preferably 1.034 molar multiple or more, even more preferably 1.035 molar multiple or more, even more preferably 1.040 molar multiple or more, preferably 1.13 molar multiple or less, even more preferably 1.12 molar multiple or less, even more preferably 1.110 molar multiple or less, even more preferably 1.105 molar multiple or less, even more preferably 1.10 molar multiple or less, even more preferably 1.09 molar multiple or less, even more preferably 1.08 molar multiple or less, even more preferably 1.07 molar multiple or less, even more preferably 1.06 molar multiple or less.

[0261] <79> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <66> to <78>, wherein, in the above-mentioned neutralization step, the temperature at which the sulfonate and the alkaline aqueous solution are mixed, and the temperature at which the neutralization reaction is carried out, are preferably 40°C or lower, more preferably 35°C or lower, even more preferably 30°C or lower, even more preferably 25°C or lower, preferably 0°C or higher, more preferably 10°C or higher, even more preferably 15°C or higher, even more preferably 20°C or higher.

[0262] <80> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <66> to <79>, wherein the mixer used in the neutralization step is a stirring blade mixer.

[0263] <81> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <66> to <80>, wherein the stirring speed of the above-mentioned stirring blade type mixer is preferably 5 m / s or more, more preferably 10 m / s or more, even more preferably 20 m / s or more, preferably 50 m / s or less, preferably 30 m / s, more preferably 27.5 m / s or less, and even more preferably 25 m / s or less.

[0264] <82> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <66> to <81>, wherein the above-mentioned neutralization step is carried out continuously, wherein the reaction liquid is circulated using a ring-type reaction apparatus while the sulfonate and the alkaline aqueous solution are added, and the reaction liquid is simultaneously withdrawn.

[0265] <83> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <66> to <82>, wherein, in the neutralization step, the mixing time when mixing the sulfonate and the alkaline aqueous solution is preferably 10 minutes or more, more preferably 20 minutes or more, further preferably 30 minutes or more, preferably 120 minutes or less, more preferably 90 minutes or less, further preferably 60 minutes or less, and even more preferably 50 minutes or less.

[0266] <84> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <66> to <83>, wherein the concentration of the olefin sulfonate in the neutralized product is preferably 40% by mass or more, more preferably 45% by mass or more, further preferably 48% by mass or more, preferably 65% ​​by mass or less, and more preferably 60% by mass or less.

[0267] <85> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <66> to <84>, wherein the temperature during hydrolysis in the above-mentioned hydrolysis step is preferably 120°C or higher, more preferably 140°C or higher, even more preferably 160°C or higher, preferably 220°C or lower, and more preferably 200°C or lower.

[0268] <86> The method for manufacturing the decolorized olefin sulfonate composition according to any one of <66> to <85>, wherein the processing time of the above-mentioned hydrolysis step is preferably 30 minutes or more, more preferably 45 minutes or more, more preferably 1 hour or more, preferably 4 hours or less, and more preferably 3 hours or less.

[0269] <87> The method for manufacturing a decolorized inner olefin sulfonate composition according to any one of <66> to <86>, wherein the average double bond position of the olefin raw material of the inner olefin sulfonate is preferably 3 or more, more preferably 3.5 or more, even more preferably 3.8 or more, 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.

[0270] <88> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <87>, wherein the olefin sulfonate preferably comprises at least one olefin sulfonate selected from olefin sulfonates having 16 carbon atoms and olefin sulfonates having 18 carbon atoms.

[0271] <89> The method for manufacturing a decolorized olefin sulfonate composition according to any one of <66> to <88>, wherein the concentration of the alkaline compound in the olefin sulfonate composition obtained in the hydrolysis step and / or before the above-mentioned decolorization step (A) is preferably 0.010 mmol or more, more preferably 0.015 mmol or more, even more preferably 0.020 mmol or more, even more preferably 0.025 mmol or more, even more preferably 0.029 mmol or more, preferably 0.27 mmol or less, even more preferably 0.240 mmol or less, even more preferably 0.210 mmol or less, and preferably 0.27 mmol or less, 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, even more preferably 0.08 mmol or less, relative to 1 g of olefin sulfonate in the olefin sulfonate composition.

[0272] <90> A method for manufacturing a decolorized olefin sulfonate composition, wherein,

[0273] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0274] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0275] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0276] The olefin sulfonate following the hydrolysis process comprises at least one selected from olefin sulfonates with 16 carbon atoms and olefin sulfonates with 18 carbon atoms, wherein the average double bond position of the olefin in the raw material for the olefin sulfonate is 3.8 or higher and 4.4 or lower.

[0277] The alkaline compound used in the above-mentioned neutralization is at least one selected from sodium hydroxide and potassium hydroxide. The stirring speed of the impeller mixer in the above-mentioned neutralization process is 20 m / s or more and 200 m / s or less. The concentration of the olefin sulfonate in the neutralization product is 45% by mass or more and 65% by mass or less. The temperature during the neutralization reaction is 0°C or more and 35°C or less. The residence time in the neutralization device during the neutralization process is 30 minutes or more and 120 minutes or less. The concentration of the alkaline compound in the olefin sulfonate composition is controlled by adjusting the amount of alkaline compound used in the neutralization process.

[0278] For olefin sulfonate compositions, the concentration of the alkaline compound in the olefin sulfonate composition after the hydrolysis step is controlled by adjusting the amount of alkaline compound used in the neutralization process.

[0279] The hydrolysis temperature in the above-mentioned hydrolysis process is above 160℃ and below 220℃, and the processing time of the hydrolysis process is above 1 hour and below 4 hours.

[0280] The above adjustment step (a1) is carried out continuously, with a cycle ratio greater than 0 and less than 20. In adjustment step (a1), a reaction vessel with stirring blades or a stirring blade type mixer is used, with d / D greater than or equal to 0.01 and less than 1, and h / H greater than or equal to 0.01 and less than 1. In adjustment step (a1), the concentration of the basic compound in the system is adjusted so that it is greater than or equal to 0.005 mmol and less than 0.26 mmol relative to 1 g of the internal olefin sulfonate after mixing step (a2).

[0281] The above mixing step (a2) is continuous. In mixing step (a2), the pH of the liquid in the system is 9.3 or higher and 11.4. A reaction vessel with stirring blades or a stirring blade type mixer is used in mixing step (a2). The d / D ratio is 0.01 or higher and less than 1, the h / H ratio is 0.01 or higher and less than 1, the circumferential speed of the stirring blades is 0.01 m / s or higher and less than 50 m / s, and the pressure in the system is 0 MPaG or higher and less than 10 MPaG.

[0282] The above-mentioned curing step (b) is continuous, with a temperature range of 40°C or higher and 100°C or lower, a residence time of 10 minutes or higher and 500 minutes or lower, a vertical cylindrical reactor used for curing step (b), an H1 / D1 ratio of 0.1 or higher and 300 or lower, a linear velocity of 0.01 mm / s or higher and 1000 mm / s or lower for the internal olefin sulfonate composition, and a pressure of 0 MPaG or higher and 10 MPaG or lower for curing step (b).

[0283] <91> A method for manufacturing a decolorized olefin sulfonate composition, wherein,

[0284] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0285] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0286] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0287] The olefin sulfonate following the hydrolysis process comprises at least one selected from olefin sulfonates with 16 carbon atoms and olefin sulfonates with 18 carbon atoms, wherein the average double bond position of the olefin in the raw material for the olefin sulfonate is 3.8 or higher and 4.4 or lower.

[0288] The alkaline compound used in the above-mentioned neutralization is at least one selected from sodium hydroxide and potassium hydroxide. The stirring speed of the impeller mixer in the above-mentioned neutralization process is 20 m / s or more and 200 m / s or less. The concentration of the olefin sulfonate in the neutralization product is 45% by mass or more and 65% by mass or less. The temperature during the neutralization reaction is 0°C or more and 35°C or less. The residence time in the neutralization device during the neutralization process is 30 minutes or more and 120 minutes or less. The concentration of the alkaline compound in the olefin sulfonate composition is controlled by adjusting the amount of alkaline compound used in the neutralization process.

[0289] For olefin sulfonate compositions, the concentration of the alkaline compound in the olefin sulfonate composition after the hydrolysis step is controlled by adjusting the amount of alkaline compound used in the neutralization process.

[0290] The hydrolysis temperature in the above-mentioned hydrolysis process is above 160℃ and below 220℃, and the processing time of the hydrolysis process is above 1 hour and below 4 hours.

[0291] The above adjustment step (a1) is continuous, with a circulation ratio greater than 0 and less than 20. In adjustment step (a1), a reaction vessel with stirring blades or a stirring blade type mixer is used, with d / D greater than or less than 1 and h / H greater than or less than 1. In adjustment step (a1), the concentration of the basic compound in the system is adjusted so that it is greater than or less than 0.005 mmol and less than 0.26 mmol relative to 1 g of the internal olefin sulfonate after mixing step (a2).

[0292] The above mixing step (a2) is continuous. In mixing step (a2), the pH of the liquid in the system is 9.3 or higher and 11.4. A reaction vessel with stirring blades or a stirring blade type mixer is used in mixing step (a2). The d / D ratio is 0.01 or higher and less than 1, the h / H ratio is 0.01 or higher and less than 1, the shear rate is 5 / s or higher and less than 100,000 / s, and the system pressure is 0 MPaG or higher and less than 10 MPaG.

[0293] The above-mentioned curing step (b) is continuous, with a temperature range of 40°C or higher and 100°C or lower, a residence time of 10 minutes or higher and 500 minutes or lower, a vertical cylindrical reactor used for curing step (b), an H1 / D1 ratio of 0.1 or higher and 300 or lower, a linear velocity of 0.01 mm / s or higher and 1000 mm / s or lower for the internal olefin sulfonate composition, and a pressure of 0 MPaG or higher and 10 MPaG or lower for curing step (b).

[0294] <92> A method for manufacturing a decolorized olefin sulfonate composition, wherein,

[0295] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0296] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0297] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0298] The olefin sulfonate following the hydrolysis process comprises at least one selected from olefin sulfonates with 16 carbon atoms and olefin sulfonates with 18 carbon atoms, wherein the average double bond position of the olefin in the raw material for the olefin sulfonate is 3.8 or higher and 4.4 or lower.

[0299] The alkaline compound used in the above-mentioned neutralization is at least one selected from sodium hydroxide and potassium hydroxide. The stirring speed of the impeller mixer in the above-mentioned neutralization process is 20 m / s or more and 200 m / s or less. The concentration of the olefin sulfonate in the neutralization product is 45% by mass or more and 65% by mass or less. The temperature during the neutralization reaction is 0°C or more and 35°C or less. The residence time in the neutralization device during the neutralization process is 30 minutes or more and 120 minutes or less. The concentration of the alkaline compound in the olefin sulfonate composition is controlled by adjusting the amount of alkaline compound used in the neutralization process.

[0300] For olefin sulfonate compositions, the concentration of the alkaline compound in the olefin sulfonate composition after the hydrolysis step is controlled by adjusting the amount of alkaline compound used in the neutralization process.

[0301] The hydrolysis temperature in the above-mentioned hydrolysis process is above 160℃ and below 220℃, and the processing time of the hydrolysis process is above 1 hour and below 4 hours.

[0302] The above adjustment step (a1) is continuous, with a circulation ratio greater than 0 and less than 20. In adjustment step (a1), a reaction vessel with stirring blades or a stirring blade type mixer is used, with d / D greater than or less than 1 and h / H greater than or less than 1. In adjustment step (a1), the concentration of the basic compound in the system is adjusted so that it is greater than or less than 0.005 mmol and less than 0.26 mmol relative to 1 g of the internal olefin sulfonate after mixing step (a2).

[0303] The above mixing step (a2) is continuous. The pH value of the solution in the system in mixing step (a2) is 9.3 or higher and 11.4. A reaction tank with stirring blades or a stirring blade type mixer is used in mixing step (a2). The d / D ratio is 0.01 or higher and less than 1, the h / H ratio is 0.01 or higher and less than 1, and the stirring power (Pv) required is 0.1 kW / m. 3 Above and 100kW / m 3 Below, the system pressure is above 0 MPaG and below 10 MPaG.

[0304] The above-mentioned curing step (b) is continuous, with a temperature range of 40°C or higher and 100°C or lower, a residence time of 10 minutes or higher and 500 minutes or lower, a vertical cylindrical reactor used for curing step (b), an H1 / D1 ratio of 0.1 or higher and 300 or lower, a linear velocity of 0.01 mm / s or higher and 1000 mm / s or lower for the internal olefin sulfonate composition, and a pressure of 0 MPaG or higher and 10 MPaG or lower for curing step (b).

[0305] <93> A method for manufacturing a decolorized olefin sulfonate composition, wherein,

[0306] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0307] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0308] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0309] The alkylene sulfonate after hydrolysis has 10 to 22 carbon atoms, and the average number of double bonds is 3 to 5. The alkaline compound used in the neutralization process is an inorganic alkaline compound. The stirring speed of the impeller mixer in the neutralization process is 5 m / s to 200 m / s. The concentration of the alkylene sulfonate in the neutralization product is 40% to 65% by mass. The temperature during the neutralization reaction is 0°C to 40°C. The residence time in the neutralization apparatus is 10 minutes to 120 minutes.

[0310] For the olefin sulfonate composition, the concentration of the alkaline compound in the olefin sulfonate composition after the hydrolysis step is controlled by an adjustment method selected from methods for adjusting the amount of alkaline compound used in the neutralization step and methods for adjusting the amount of alkaline compound in the hydrolysis step.

[0311] The hydrolysis temperature in the above-mentioned hydrolysis process is above 120℃ and below 220℃, and the processing time of the hydrolysis process is above 30 minutes and below 4 hours.

[0312] The above adjustment step (a1) is carried out in a batch, semi-batch, or continuous manner, with a cycle ratio greater than 0 and less than 20. In adjustment step (a1), a reaction vessel with stirring blades or a stirring blade type mixer is used, with a d / D ratio greater than or equal to 0.01 and less than 1, and an h / H ratio greater than or equal to 0.01 and less than 1. In adjustment step (a1), the concentration of the basic compound in the system is adjusted so that it is greater than or equal to 0.005 mmol and less than 0.26 mmol relative to 1 g of the internal olefin sulfonate after mixing step (a2).

[0313] The above mixing step (a2) is continuous. In mixing step (a2), the pH of the solution in the system is 9.3 or higher and 11.4. A reaction vessel with stirring blades or a stirring blade type mixer is used in mixing step (a2). The d / D ratio is 0.01 or higher and less than 1, the h / H ratio is 0.01 or higher and less than 1, the circumferential speed of the stirring blades is 0.01 m / s or higher and less than 50 m / s, and the pressure in the system is 0 MPaG or higher and less than 10 MPaG.

[0314] The above-mentioned curing step (b) is continuous, with a temperature range of 40°C or higher and 120°C or lower, a residence time of 10 minutes or higher and 500 minutes or lower, a vertical cylindrical reactor used for curing step (b), an H1 / D1 ratio of 0.1 or higher and 300 or lower, a linear velocity of 0.001 mm / s or higher and 1000 mm / s or lower for the internal olefin sulfonate composition, and a pressure of 0 MPaG or higher and 10 MPaG or lower for curing step (b).

[0315] <94> A method for manufacturing a decolorized olefin sulfonate composition, wherein,

[0316] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0317] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0318] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0319] The alkylene sulfonate after hydrolysis has 10 to 22 carbon atoms, and the average number of double bonds is 3 to 5. The alkaline compound used in the neutralization process is an inorganic alkaline compound. The stirring speed of the impeller mixer in the neutralization process is 5 m / s to 200 m / s. The concentration of the alkylene sulfonate in the neutralization product is 40% to 65% by mass. The temperature during the neutralization reaction is 0°C to 40°C. The residence time in the neutralization apparatus is 10 minutes to 120 minutes.

[0320] For the olefin sulfonate composition, the concentration of the alkaline compound in the olefin sulfonate composition after the hydrolysis step is controlled by an adjustment method selected from methods for adjusting the amount of alkaline compound used in the neutralization step and methods for adjusting the amount of alkaline compound in the hydrolysis step.

[0321] The hydrolysis temperature in the above-mentioned hydrolysis process is above 120℃ and below 220℃, and the processing time of the hydrolysis process is above 30 minutes and below 4 hours.

[0322] The above adjustment step (a1) is carried out in a batch, semi-batch, or continuous manner, with a cycle ratio greater than 0 and less than 20. In adjustment step (a1), a reaction vessel with stirring blades or a stirring blade type mixer is used, with a d / D ratio greater than or equal to 0.01 and less than 1, and an h / H ratio greater than or equal to 0.01 and less than 1. In adjustment step (a1), the concentration of the basic compound in the system is adjusted so that it is greater than or equal to 0.005 mmol and less than 0.26 mmol relative to 1 g of the internal olefin sulfonate after mixing step (a2).

[0323] The above mixing step (a2) is continuous. In mixing step (a2), the pH of the solution in the system is 9.3 or higher and 11.4. A reaction vessel with stirring blades or a stirring blade type mixer is used in mixing step (a2). The d / D ratio is 0.01 or higher and less than 1, the h / H ratio is 0.01 or higher and less than 1, the shear rate is 5 / s or higher and less than 100,000 / s, and the system pressure is 0 MPaG or higher and less than 10 MPaG.

[0324] The above-mentioned curing step (b) is continuous, with a temperature range of 40°C or higher and 120°C or lower, a residence time of 10 minutes or higher and 500 minutes or lower, a vertical cylindrical reactor used for curing step (b), an H1 / D1 ratio of 0.1 or higher and 300 or lower, a linear velocity of 0.001 mm / s or higher and 1000 mm / s or lower for the internal olefin sulfonate composition, and a pressure of 0 MPaG or higher and 10 MPaG or lower for curing step (b).

[0325] <95> A method for manufacturing a decolorized olefin sulfonate composition, wherein,

[0326] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0327] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0328] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0329] The number of carbon atoms in the alkylene sulfonate after the hydrolysis process is 10 or more and 22 or less; the average number of double bonds in the alkylene sulfonate is 3 or more and 5 or less; the alkaline compound used in the neutralization process is an inorganic alkaline compound; the stirring speed of the impeller mixer in the neutralization process is 5 m / s or more and 200 m / s or less; the concentration of the alkylene sulfonate in the neutralization product is 40% by mass or more and 65% by mass or less; the temperature during the neutralization reaction is 0°C or more and 40°C or less; and the residence time in the neutralization device during neutralization is 10 minutes or more and 120 minutes or less.

[0330] For olefin sulfonate compositions, a method is used to control the concentration of the alkaline compound in the olefin sulfonate composition after the hydrolysis step by adjusting the amount of alkaline compound used in the neutralization step and adjusting the amount of alkaline compound in the hydrolysis step.

[0331] The hydrolysis temperature in the above-mentioned hydrolysis process is above 120℃ and below 220℃, and the processing time of the hydrolysis process is above 30 minutes and below 4 hours.

[0332] The above adjustment step (a1) is carried out in a batch, semi-batch, or continuous manner, with a cycle ratio greater than 0 and less than 20. In adjustment step (a1), a reaction vessel with stirring blades or a stirring blade type mixer is used, with a d / D ratio greater than or equal to 0.01 and less than 1, and an h / H ratio greater than or equal to 0.01 and less than 1. In adjustment step (a1), the concentration of the basic compound in the system is adjusted so that it is greater than or equal to 0.005 mmol and less than 0.26 mmol relative to 1 g of the internal olefin sulfonate after mixing step (a2).

[0333] The above mixing step (a2) is continuous. The pH value of the liquid in the system in mixing step (a2) is 9.3 or higher and 11.4. A reaction tank with stirring blades or a stirring blade type mixer is used in mixing step (a2). The d / D ratio is 0.01 or higher and less than 1, the h / H ratio is 0.01 or higher and less than 1, and the stirring power (Pv) required is 0.1 kW / m. 3 Above and 100kW / m 3 Below, the system pressure is above 0 MPaG and below 10 MPaG.

[0334] The above-mentioned curing step (b) is continuous, with a temperature range of 40°C or higher and 120°C or lower, a residence time of 10 minutes or higher and 500 minutes or lower, a vertical cylindrical reactor used for curing step (b), an H1 / D1 ratio of 0.1 or higher and 300 or lower, a linear velocity of 0.001 mm / s or higher and 1000 mm / s or lower for the internal olefin sulfonate composition, and a pressure of 0 MPaG or higher and 10 MPaG or lower for curing step (b).

[0335] <96> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0336] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0337] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0338] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0339] The stirring power (Pv) required in the mixing step (a2) above is 0.1 kW / m. 3Above and 100kW / m 3 the following.

[0340] <97> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0341] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0342] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0343] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0344] The stirring power (Pv) required in the mixing step (a2) above is 0.3 kW / m. 3 Above and 30kW / m 3 the following.

[0345] <98> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0346] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0347] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0348] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0349] The stirring power (Pv) required in the mixing step (a2) above is 0.2 kW / m. 3 Above and 50kW / m 3 the following.

[0350] <99> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0351] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0352] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0353] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0354] The shear rate in the above mixing step (a2) is 5 / s or more and 100,000 / s or less.

[0355] <100> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0356] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0357] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0358] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0359] The shear rate in the above mixing step (a2) is above 1500 / s and below 20000 / s.

[0360] <101> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0361] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0362] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0363] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0364] The shear rate in the above mixing step (a2) is above 500 / s and below 50000 / s.

[0365] <102> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0366] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0367] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0368] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0369] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the above mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less.

[0370] <103> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0371] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0372] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0373] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0374] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the above mixing step (a2), the circumferential speed of the stirring blades is 9.0 m / s or more and 15 m / s or less.

[0375] <104> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0376] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0377] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0378] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0379] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the above mixing step (a2), the circumferential speed of the stirring blades is 0.9 m / s or more and 26 m / s or less.

[0380] <105> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0381] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0382] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0383] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0384] When the above-described reaction tank with stirring blades or a stirring blade type mixer is used in the mixing step (a2) above, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less.

[0385] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2).

[0386] <106> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0387] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0388] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0389] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0390] When the above-described reaction tank with stirring blades or a stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less.

[0391] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.030 mmol or more and 0.06 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2).

[0392] <107> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0393] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0394] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0395] The mixing step (a2) described above is followed by a ripening step (b).

[0396] When the above-described reaction tank with stirring blades or a stirring blade type mixer is used in the mixing step (a2) above, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less.

[0397] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.020 mmol or more and 0.20 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2).

[0398] <108> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0399] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0400] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0401] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0402] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the above mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the pH value of the liquid in the system in the mixing step (a2) is 9.3 or more and 11.4 or less.

[0403] <109> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0404] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0405] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0406] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0407] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the above mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the pH value of the liquid in the system in the mixing step (a2) is 10.0 or more and 10.5 or less.

[0408] <110> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0409] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0410] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0411] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0412] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the above mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the pH value of the liquid in the system in the mixing step (a2) is 9.8 or more and 11.0 or less.

[0413] <111> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0414] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0415] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0416] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0417] When the above-described reaction tank with stirring blades or a stirring blade type mixer is used in the mixing step (a2) above, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less.

[0418] The concentration of the alkaline compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2), and the adjustment step (a1) is performed in batches.

[0419] <112> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0420] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0421] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0422] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0423] When the above-described reaction tank with stirring blades or a stirring blade type mixer is used in the mixing step (a2) above, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less.

[0424] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2), and the adjustment step (a1) is performed in a semi-batch manner.

[0425] <113> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0426] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0427] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0428] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0429] When the above-described reaction tank with stirring blades or a stirring blade type mixer is used in the mixing step (a2) above, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less.

[0430] The concentration of the alkaline compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2), and the adjustment step (a1) is carried out continuously.

[0431] <114> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0432] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0433] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0434] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0435] When the above-described mixing step (a2) uses a reaction tank with stirring blades or a stirring blade type mixer, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is performed in batches.

[0436] The concentration of the basic compound in step (a1) is adjusted to be ≥0.005 mmol and ≤0.23 mmol per 1 g of the olefin sulfonate after mixing step (a2).

[0437] The above adjustment steps (a1) can be carried out in batches, semi-batches, or continuously.

[0438] <115> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0439] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0440] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0441] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0442] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a semi-batch manner.

[0443] The concentration of the alkaline compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2), and the adjustment step (a1) is carried out in a batch, semi-batch or continuous manner.

[0444] <116> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0445] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0446] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0447] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0448] When the above-described mixing step (a2) uses a reaction tank with stirring blades or a stirring blade type mixer, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out continuously.

[0449] The concentration of the alkaline compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2), and the adjustment step (a1) is carried out in a batch, semi-batch or continuous manner.

[0450] <117> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0451] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0452] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0453] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0454] When the above-described mixing step (a2) uses a reaction tank with stirring blades or a stirring blade type mixer, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner.

[0455] The concentration of the alkaline compound in the above adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0456] <118> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0457] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0458] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0459] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0460] When the above-described mixing step (a2) uses a reaction tank with stirring blades or a stirring blade type mixer, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner.

[0461] The concentration of the alkaline compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio of 4 times or more and 8 times or less.

[0462] <119> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0463] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0464] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0465] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0466] When the above-described mixing step (a2) uses a reaction tank with stirring blades or a stirring blade type mixer, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner.

[0467] The concentration of the alkaline compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio of 2 times or more and 10 times or less.

[0468] <120> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0469] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0470] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0471] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0472] When the above-described mixing step (a2) uses a reaction tank with stirring blades or a stirring blade type mixer, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner.

[0473] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0474] The above-mentioned curing step (b) is carried out continuously, and the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less.

[0475] <121> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0476] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0477] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0478] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0479] When the above-described mixing step (a2) uses a reaction tank with stirring blades or a stirring blade type mixer, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner.

[0480] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0481] The above-mentioned ripening step (b) is carried out continuously, and the linear velocity of the internal olefin sulfonate composition is 0.1 mm / s or more and 1 mm / s or less.

[0482] <122> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0483] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0484] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0485] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0486] When the above-described mixing step (a2) uses a reaction tank with stirring blades or a stirring blade type mixer, the circumferential speed of the stirring blades is 0.01 m / s or more and 100 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner.

[0487] The concentration of the basic compound in adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the olefin sulfonate after mixing step (a2). Adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0488] The above-mentioned curing step (b) is carried out continuously, and the linear velocity of the inner olefin sulfonate composition is 0.005 mm / s or more and 800 mm / s or less.

[0489] <123> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0490] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0491] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0492] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0493] When the above-described mixing step (a2) uses a reaction tank with stirring blades or a stirring blade type mixer, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner.

[0494] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0495] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, and the ratio (H1 / D1) of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor is 0.1 or more and 300 or less.

[0496] <124> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0497] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0498] The process includes a decolorization step (A) following the hydrolysis step described above. This decolorization step (A) involves the following steps on the system containing the olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to subsequently mix the decolorizing agent with the olefin sulfonate composition present in the system.

[0499] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0500] When the above-described mixing step (a2) uses a reaction tank with stirring blades or a stirring blade type mixer, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner.

[0501] The concentration of the alkaline compound in adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the olefin sulfonate after mixing step (a2). Adjustment step (a1) is carried out continuously with a cycle rate greater than 0 times and less than 20 times. The above-mentioned ripening step (b) is carried out continuously with a linear velocity of 0.001 mm / s or more and less than 1000 mm / s.

[0502] The above-mentioned maturation step (b) is carried out using the above-mentioned vertical cylindrical reactor, wherein the ratio (H1 / D1) of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor is 1.5 or more and 5 or less.

[0503] <125> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0504] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0505] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0506] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0507] When the above-described mixing step (a2) uses a reaction tank with stirring blades or a stirring blade type mixer, the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner.

[0508] The concentration of the alkaline compound in adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the olefin sulfonate after mixing step (a2). Adjustment step (a1) is carried out continuously with a cycle rate greater than 0 times and less than 20 times. The above-mentioned ripening step (b) is carried out continuously with a linear velocity of 0.001 mm / s or more and less than 1000 mm / s.

[0509] The above-mentioned maturation step (b) is carried out using the above-mentioned vertical cylindrical reactor, wherein the ratio (H1 / D1) of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor is more than 1 and less than 50.

[0510] <126> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0511] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0512] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0513] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0514] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate.

[0515] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0516] The above-described curing step (b) is carried out continuously, with the linear velocity of the internal olefin sulfonate composition being 0.001 mm / s or more and 1000 mm / s or less.

[0517] The above-mentioned maturation step (b) is carried out using the above-mentioned vertical cylindrical reactor, wherein the ratio (H1 / D1) of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor is 0.1 or more and 300 or less.

[0518] <127> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0519] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0520] The process includes a decolorization step (A) following the hydrolysis step described above. This decolorization step (A) involves the following steps on the system containing the olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the olefin sulfonate composition present in the system.

[0521] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0522] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the above-mentioned mixing step (a2), the circumferential speed of the stirring blades is more than 0.01 m / s and less than 50 m / s, the mixing step (a2) is carried out in a batch, semi-batch or continuous manner, and the above-mentioned decolorizing agent is hydrogen peroxide.

[0523] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0524] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, and the ratio (H1 / D1) of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor is 0.1 or more and 300 or less.

[0525] <128> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0526] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0527] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0528] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0529] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate.

[0530] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0531] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, and the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less.

[0532] <129> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0533] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0534] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0535] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0536] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate.

[0537] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0538] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, and the pressure in the curing step (b) is 0.2 MPaG or more and 0.5 MPaG or less.

[0539] <130> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0540] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0541] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0542] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0543] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate.

[0544] The concentration of the basic compound in adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the olefin sulfonate after mixing step (a2). Adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0545] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, and the pressure in the curing step (b) is 0.05 MPaG or more and 1 MPaG or less.

[0546] <131> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0547] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0548] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0549] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0550] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate.

[0551] The concentration of the alkaline compound in adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less per 1 g of the olefin sulfonate after mixing step (a2). Adjustment step (a1) is carried out continuously with a cycle rate greater than 0 times and less than 20 times. The above-mentioned ripening step (b) is carried out continuously with a linear velocity of 0.001 mm / s or more and less than 1000 mm / s.

[0552] The above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, wherein the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, and the residence time in curing step (b) is 10 minutes or more and 500 minutes or less.

[0553] <132> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0554] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0555] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0556] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0557] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate.

[0558] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0559] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, and the residence time in the curing step (b) is 60 minutes or more and 200 minutes or less.

[0560] <133> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0561] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0562] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0563] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0564] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate.

[0565] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0566] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the reactor inner diameter D1 (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, and the residence time in the curing step (b) is 30 minutes or more and 400 minutes or less.

[0567] <134> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0568] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0569] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0570] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0571] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate.

[0572] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0573] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0574] <135> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0575] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0576] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0577] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0578] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate.

[0579] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0580] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 60°C or more and 100°C or less.

[0581] <136> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0582] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0583] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0584] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0585] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate.

[0586] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20.

[0587] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 50°C or more and 110°C or less.

[0588] <137> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0589] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0590] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0591] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0592] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate.

[0593] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG.

[0594] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0595] <138> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0596] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0597] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0598] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0599] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate.

[0600] The concentration of the basic compound in the adjustment step (a1) above is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20. The system pressure in the adjustment step (a1) is 0.2 MPaG or more and less than 0.5 MPaG.

[0601] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0602] <139> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0603] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0604] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0605] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0606] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate.

[0607] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less per g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20. The system pressure in the adjustment step (a1) is 0.05 MPaG or more and less than 1 MPaG.

[0608] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0609] <140> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0610] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0611] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0612] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0613] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner, the above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the pressure in the system during the mixing step (a2) is 0 MPaG or more and 10 MPaG or less.

[0614] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG.

[0615] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0616] <141> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0617] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0618] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0619] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0620] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner, the above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the pressure in the system in the mixing step (a2) is 0.2 MPaG or more and 0.5 MPaG or less.

[0621] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG.

[0622] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0623] <142> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0624] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0625] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0626] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0627] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner, the above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the pressure in the system in the mixing step (a2) is 0.05 MPaG or more and 5 MPaG or less.

[0628] The concentration of the basic compound in the above-mentioned adjustment step (a1) is 0.005 mmol or more and 0.23 mmol or less relative to 1 g of the inner olefin sulfonate after the mixing step (a2). The adjustment step (a1) is carried out continuously with a cycle ratio greater than 0 and less than 20. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG.

[0629] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0630] <143> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0631] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0632] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0633] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0634] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner, the above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the pressure in the system during the mixing step (a2) is 0 MPaG or more and 10 MPaG or less.

[0635] In the above-mentioned adjustment step (a1), the concentration of the basic compound relative to 1 g of the internal olefin sulfonate after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less. The adjustment step (a1) is carried out continuously with a circulation ratio greater than 0 times and less than 20 times. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG. When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the adjustment step (a1), the circumferential speed of the stirring blades is 0.01 m / s or more and less than 50 m / s, the ratio of the stirring blade diameter d to the tank diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the stirring blade height h to the tank height H (h / H) is 0.01 or more and less than 1.

[0636] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0637] <144> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0638] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0639] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0640] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0641] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner, the above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the pressure in the system in the mixing step (a2) is 0 MPaG or more and 10 MPaG or less.

[0642] In the above-mentioned adjustment step (a1), the concentration of the basic compound relative to 1 g of the internal olefin sulfonate after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less. The adjustment step (a1) is carried out continuously with a circulation ratio greater than 0 and less than 20. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG. When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the adjustment step (a1), the circumferential speed of the stirring blades is 9.0 m / s or more and less than 15 m / s, the ratio of the stirring blade diameter d to the tank diameter D (d / D) is 0.55 or more and less than 1, and the ratio of the stirring blade height h to the tank height H (h / H) is 0.5 or more and less than 1.

[0643] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0644] <145> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0645] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0646] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0647] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0648] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner, the above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the pressure in the system during the mixing step (a2) is 0 MPaG or more and 10 MPaG or less.

[0649] In the above-mentioned adjustment step (a1), the concentration of the basic compound relative to 1 g of the internal olefin sulfonate after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less. The adjustment step (a1) is carried out continuously with a circulation ratio greater than 0 times and less than 20 times. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG. When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the adjustment step (a1), the circumferential speed of the stirring blades is 0.3 m / s or more and less than 26 m / s, the ratio of the stirring blade diameter d to the tank diameter D (d / D) is 0.1 or more and less than 1, and the ratio of the stirring blade height h to the tank height H (h / H) is 0.1 or more and less than 1.

[0650] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0651] <146> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0652] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0653] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0654] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0655] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner, the above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the pressure in the system during the mixing step (a2) is 0 MPaG or more and 10 MPaG or less.

[0656] In the above-mentioned adjustment step (a1), the concentration of the basic compound relative to 1 g of the inner olefin sulfonate after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less. The adjustment step (a1) is carried out continuously with a circulation ratio greater than 0 and less than 20. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG. When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the adjustment step (a1), the circumferential speed of the stirring blades is 0.01 m / s or more and less than 50 m / s, and the ratio of the stirring blade diameter d to the tank diameter D (d / D) is 0.5 or more and less than 1.

[0657] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0658] <147> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0659] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0660] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0661] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0662] When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, the mixing step (a2) is carried out in a batch, semi-batch, or continuous manner, the above-mentioned decolorizing agent is at least one selected from hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate, and the pressure in the system during the mixing step (a2) is 0 MPaG or more and 10 MPaG or less.

[0663] In the above-mentioned adjustment step (a1), the concentration of the basic compound relative to 1 g of the inner olefin sulfonate after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less. The adjustment step (a1) is carried out continuously with a circulation ratio greater than 0 and less than 20. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG. When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the adjustment step (a1), the circumferential speed of the stirring blades is 0.01 m / s or more and less than 50 m / s, and the ratio of the stirring blade height h to the tank height H (h / H) is 0.3 or more and less than 1.

[0664] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0665] <148> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0666] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0667] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0668] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0669] The mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The decolorizing agent is selected from at least one of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate. The pressure in the system during the mixing step (a2) is 0 MPaG or more and 10 MPaG or less. When the reaction tank with stirring blades or a stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, the ratio of the stirring blade diameter d to the tank diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the stirring blade height h to the tank height H (h / H) is 0.01 or more and less than 1.

[0670] In the above-mentioned adjustment step (a1), the concentration of the basic compound relative to 1 g of the internal olefin sulfonate after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less. The adjustment step (a1) is carried out continuously with a circulation ratio greater than 0 times and less than 20 times. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG. When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the adjustment step (a1), the circumferential speed of the stirring blades is 0.01 m / s or more and less than 50 m / s, the ratio of the stirring blade diameter d to the tank diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the stirring blade height h to the tank height H (h / H) is 0.01 or more and less than 1.

[0671] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0672] <149> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0673] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0674] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0675] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0676] The mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The decolorizing agent is selected from at least one of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate. The pressure in the system during the mixing step (a2) is 0 MPaG or more and 10 MPaG or less. When the reaction tank with stirring blades or a stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 9.0 m / s or more and 15 m / s or less, the ratio of the stirring blade diameter d to the tank diameter D (d / D) is 0.55 or more and less than 1, and the ratio of the stirring blade height h to the tank height H (h / H) is 0.55 or more and less than 1.

[0677] In the above-mentioned adjustment step (a1), the concentration of the basic compound relative to 1 g of the internal olefin sulfonate after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less. The adjustment step (a1) is carried out continuously with a circulation ratio greater than 0 times and less than 20 times. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG. When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the adjustment step (a1), the circumferential speed of the stirring blades is 0.01 m / s or more and less than 50 m / s, the ratio of the stirring blade diameter d to the tank diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the stirring blade height h to the tank height H (h / H) is 0.01 or more and less than 1.

[0678] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0679] <150> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0680] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0681] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0682] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0683] The mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The decolorizing agent is selected from at least one of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate. The pressure in the system during the mixing step (a2) is 0 MPaG or more and 10 MPaG or less. When the reaction tank with stirring blades or a stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.05 m / s or more and 40 m / s or less, the ratio of the stirring blade diameter d to the tank diameter D (d / D) is 0.3 or more and less than 1, and the ratio of the stirring blade height h to the tank height H (h / H) is 0.3 or more and less than 1.

[0684] In the above-mentioned adjustment step (a1), the concentration of the basic compound relative to 1 g of the internal olefin sulfonate after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less. The adjustment step (a1) is carried out continuously with a circulation ratio greater than 0 times and less than 20 times. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG. When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the adjustment step (a1), the circumferential speed of the stirring blades is 0.01 m / s or more and less than 50 m / s, the ratio of the stirring blade diameter d to the tank diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the stirring blade height h to the tank height H (h / H) is 0.01 or more and less than 1.

[0685] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0686] <151> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0687] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0688] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0689] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0690] The mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The decolorizing agent is selected from at least one of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate. The pressure in the system during the mixing step (a2) is 0 MPaG or more and 10 MPaG or less. When the reaction tank with stirring blades or a stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the ratio of the stirring blade diameter d to the tank diameter D (d / D) is 0.5 or more and less than 1.

[0691] In the above-mentioned adjustment step (a1), the concentration of the basic compound relative to 1 g of the internal olefin sulfonate after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less. The adjustment step (a1) is carried out continuously with a circulation ratio greater than 0 times and less than 20 times. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG. When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the adjustment step (a1), the circumferential speed of the stirring blades is 0.01 m / s or more and less than 50 m / s, the ratio of the stirring blade diameter d to the tank diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the stirring blade height h to the tank height H (h / H) is 0.01 or more and less than 1.

[0692] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0693] <152> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0694] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0695] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0696] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0697] The mixing step (a2) is carried out in a batch, semi-batch, or continuous manner. The decolorizing agent is selected from at least one of hydrogen peroxide, hypochlorous acid, nitric acid, potassium nitrate, permanganate, peroxide, chlorite, chlorate, perchlorate, and persulfate. The pressure in the system during the mixing step (a2) is 0 MPaG or more and 10 MPaG or less. When the reaction tank with stirring blades or a stirring blade type mixer is used in the mixing step (a2), the circumferential speed of the stirring blades is 0.01 m / s or more and 50 m / s or less, and the ratio of the stirring blade height h to the tank height H (h / H) is 0.3 or more and less than 1.

[0698] In the above-mentioned adjustment step (a1), the concentration of the basic compound relative to 1 g of the internal olefin sulfonate after the mixing step (a2) is 0.005 mmol or more and 0.23 mmol or less. The adjustment step (a1) is carried out continuously with a circulation ratio greater than 0 times and less than 20 times. The system pressure in the adjustment step (a1) is 0 MPaG or more and less than 10 MPaG. When the above-mentioned reaction tank with stirring blades or stirring blade type mixer is used in the adjustment step (a1), the circumferential speed of the stirring blades is 0.01 m / s or more and less than 50 m / s, the ratio of the stirring blade diameter d to the tank diameter D (d / D) is 0.01 or more and less than 1, and the ratio of the stirring blade height h to the tank height H (h / H) is 0.01 or more and less than 1.

[0699] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0700] <153> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0701] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0702] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0703] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0704] The above-mentioned curing step (b) is carried out continuously, and the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less.

[0705] <154> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0706] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0707] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0708] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0709] The above-mentioned ripening step (b) is carried out continuously, and the linear velocity of the internal olefin sulfonate composition is 0.1 mm / s or more and 1 mm / s or less.

[0710] <155> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0711] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0712] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0713] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0714] The above-mentioned curing step (b) is carried out continuously, and the linear velocity of the inner olefin sulfonate composition is 0.005 mm / s or more and 100 mm / s or less.

[0715] <156> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0716] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0717] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0718] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0719] The above-mentioned maturation step (b) is carried out using the above-mentioned vertical cylindrical reactor, wherein the ratio (H1 / D1) of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor is 0.1 or more and 300 or less.

[0720] <157> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0721] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0722] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0723] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0724] The above-mentioned maturation step (b) is carried out using the above-mentioned vertical cylindrical reactor, wherein the ratio (H1 / D1) of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor is 1.5 or more and 5 or less.

[0725] <158> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0726] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0727] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0728] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0729] The above-mentioned maturation step (b) is carried out using the above-mentioned vertical cylindrical reactor, wherein the ratio (H1 / D1) of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor is more than 1 and less than 50.

[0730] <159> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0731] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0732] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0733] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0734] The pressure in the curing step (b) is above 0 MPaG and below 10 MPaG.

[0735] <160> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0736] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0737] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0738] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0739] The pressure in the curing step (b) is above 0.2 MPaG and below 0.5 MPaG.

[0740] <161> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0741] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0742] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0743] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0744] The pressure in the curing step (b) is above 0.05 MPaG and below 1 MPaG.

[0745] <162> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0746] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0747] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0748] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0749] The residence time in maturation step (b) is more than 10 minutes and less than 500 minutes.

[0750] <163> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0751] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0752] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0753] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0754] The residence time in maturation step (b) is more than 30 minutes and less than 200 minutes.

[0755] <164> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0756] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0757] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0758] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0759] The residence time in maturation step (b) is more than 20 minutes and less than 400 minutes.

[0760] <165> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0761] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0762] The process includes a decolorization step (A) following the hydrolysis step described above. This decolorization step (A) involves the following steps on the system containing the olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the olefin sulfonate composition present in the system.

[0763] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0764] The temperature range for maturation step (b) is above 40°C and below 120°C.

[0765] <166> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0766] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0767] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0768] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0769] The temperature range for the maturation step (b) is above 60°C and below 100°C.

[0770] <167> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0771] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0772] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0773] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0774] The temperature range for the maturation step (b) is above 50°C and below 110°C.

[0775] <168> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0776] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0777] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0778] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0779] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, and the ratio (H1 / D1) of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor is 0.1 or more and 300 or less.

[0780] <169> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0781] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0782] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0783] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0784] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, and the ratio (H1 / D1) of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor is 1.5 or more and 5 or less.

[0785] <170> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0786] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0787] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0788] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0789] The above-mentioned maturation step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned maturation step (b) is carried out using the above-mentioned vertical cylindrical reactor, and the ratio (H1 / D1) of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor is 1 or more and 50 or less.

[0790] <171> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0791] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0792] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0793] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0794] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, and the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less.

[0795] <172> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0796] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0797] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0798] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0799] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, and the pressure in the curing step (b) is 0.2 MPaG or more and 0.5 MPaG or less.

[0800] <173> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0801] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0802] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0803] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0804] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, and the pressure in the curing step (b) is 0.05 MPaG or more and 1 MPaG or less.

[0805] <174> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0806] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0807] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on a system containing an olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the olefin sulfonate composition containing the decolorizing agent in the system.

[0808] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0809] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, and the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less.

[0810] <175> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0811] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0812] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0813] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0814] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, and the residence time in the curing step (b) is 60 minutes or more and 200 minutes or less.

[0815] <176> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0816] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0817] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0818] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0819] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, and the residence time in the curing step (b) is 20 minutes or more and 400 minutes or less.

[0820] <177> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0821] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0822] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0823] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0824] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 40°C or more and 120°C or less.

[0825] <178> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0826] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0827] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0828] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0829] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 60°C or more and 100°C or less.

[0830] <179> A method for manufacturing a decolorized olefin sulfonate composition according to any one of <1> to <89>, wherein,

[0831] The method for manufacturing the decolorized olefin sulfonate composition includes: a sulfonation step of sulfonating the raw material olefin, a neutralization step of neutralizing the obtained sulfonate, and a hydrolysis step of hydrolyzing the obtained neutralized product.

[0832] The above-mentioned hydrolysis process is followed by a decolorization process (A), which involves the following steps on the system containing an internal olefin sulfonate composition: an adjustment step (a1) to adjust the concentration of the alkaline compound in the system; and a mixing step (a2) to mix the decolorizing agent with the internal olefin sulfonate composition present in the system.

[0833] Following the mixing step (a2) described above, a ripening step (b) is also included.

[0834] The above-mentioned curing step (b) is carried out continuously, the linear velocity of the inner olefin sulfonate composition is 0.001 mm / s or more and 1000 mm / s or less, the above-mentioned curing step (b) is carried out using the above-mentioned vertical cylindrical reactor, the ratio of the height H1 of the vertical cylindrical reactor to the inner diameter D1 of the reactor (H1 / D1) is 0.1 or more and 300 or less, the pressure in the curing step (b) is 0 MPaG or more and 10 MPaG or less, the residence time in the curing step (b) is 10 minutes or more and 500 minutes or less, and the temperature range of the curing step (b) is 50°C or more and 110°C or less.

[0835] <180> Use of the decolorized olefin sulfonate composition obtained by any one of <1> to <179> in at least one of body cleansers, shampoos, laundry detergents and dishwashing detergents.

[0836] [Example]

[0837] The present invention will now be specifically described based on embodiments. Unless otherwise specified in the table, the concentration of each component is expressed as "mass %". Various determination and evaluation methods are shown below.

[0838] <Methods for determining the double bond distribution of internal alkenes>

[0839] The double bond positions of the inner olefin were determined by gas chromatography (hereinafter referred to as GC). Specifically, after preparing a disulfide derivative by reacting dimethyl disulfide with the inner olefin, the components were separated by GC. The double bond positions of the inner olefin were determined based on the peak areas of each component, and the average double bond position was calculated using the following formula. The apparatus and measurement conditions used are shown below.

[0840] [Apparatus and Measurement Conditions]

[0841] GC Unit: HP6890 (manufactured by Hewlett Packard)

[0842] Column: Ultra-Alloy-1HT capillary column, 30m × 250μm × 0.15μm (manufactured by Frontier Laboratories Co., Ltd.)

[0843] Detector: Flame Ionization Detector (FID)

[0844] Injection temperature: 300℃

[0845] Detector temperature: 350℃

[0846] He flow rate: 4.6 mL / min

[0847] [Formula for calculating the average double bond position]

[0848]

[0849] (In the formula, n represents the number of carbon atoms in the alkene, m represents the position of the double bond in the alkene, and Y represents the percentage of meta-alkenes in alkenes with n carbon atoms.)

[0850] <Methods for Manufacturing Internal Olefins>

[0851] Example A (Synthesis of an inner olefin with 16 carbon atoms)

[0852] 7000 g (28.9 mol) of 1-hexadecyl alcohol "KALCOL 6098" (manufactured by Kao Corporation) and 700 g (10% by mass relative to the starting alcohol) of solid acid catalyst γ-alumina (STREM Chemicals, Inc.) were added to a flask equipped with a stirrer. The reaction was carried out for at least 3 hours under stirring, with nitrogen gas introduced into the system at 280°C (7000 mL / min). To obtain the desired average double bond position of the inner olefin, samples were taken periodically for analysis of the average double bond position, and cooling was initiated at appropriate times. The average double bond positions after the reaction were as follows: 4.2 for the inner olefin used in Examples 1-14, 17 and 20, 23, 25-31; 4.3 for the inner olefin used in Example 15; 4.1 for the inner olefin used in Example 21; and 3.8 in Example 24.

[0853] Example B (Synthesis of an 18-carbon inner olefin)

[0854] 7000 g (25.9 mol) of 1-octadecyl alcohol "KALCOL 8098" (manufactured by Kao Corporation) and 1050 g (10% by mass relative to the starting alcohol) of solid acid catalyst γ-alumina (STREM Chemicals, Inc.) were added to a flask equipped with a stirrer. The reaction was carried out for at least 10 hours under stirring, with nitrogen gas introduced into the system at 280°C (7000 mL / min). To obtain the desired average double bond position of the inner olefin, samples were taken periodically for analysis of the average double bond position, and cooling was initiated at appropriate times. The average double bond positions after the reaction were as follows: 4.2 for the inner olefin used in Example 16; 3.6 for the inner olefin used in Example 18; 4.4 for the inner olefin used in Example 22; 4.0 for the inner olefin used in Example 32; and 3.8 in Example 24.

[0855] <Method for manufacturing decolorized olefin sulfonate compositions>

[0856] Example 1

[0857] A thin-film sulfonation reactor with an external sleeve was used. Cooling water at 10°C was flowed through the external sleeve, causing the 16-carbon olefin obtained in Manufacturing Example A to flow down the inner wall of the reactor in a thin film. Sulfonation was carried out using SO3 gas diluted with dehumidified air (SO3 concentration: 1.1 vol%), with a SO3 / olefin molar ratio of 1.01, thereby obtaining the sulfonate.

[0858] A continuous loop neutralization reaction apparatus equipped with a Milder MDN303V (manufactured by Pacific Machinery Co., Ltd.) as the mixer and an external casing was used. After injecting ion-exchanged water into the apparatus, the neutralization reaction was initiated by supplying the obtained sulfonate and an aqueous solution of potassium hydroxide (concentration: 17% by mass) at a temperature of 25°C at the apparatus outlet. The reaction was carried out at a circumferential speed of 24 m / s with the mixer. When the neutralization reaction reached a stable state within the apparatus, the neutralization product was confirmed to flow out of the apparatus outlet, thus obtaining the neutralized product. The concentration of the inner olefin sulfonate in the neutralized product was 55% by mass. The amount of the alkaline compound used for neutralization was set to 1.04 molar times relative to the sulfonic acid group.

[0859] After neutralization, the neutralization product was heated in an autoclave at 160°C for 1 hour to hydrolyze, obtaining the inner olefin sulfonate composition before decolorization. The average double bond position of the olefin in the inner olefin sulfonate was 4.2. The potassium hydroxide concentration of the inner olefin sulfonate composition obtained by hydrolysis was 0.029 mmol per 1g of inner olefin sulfonate.

[0860] Additionally, a 48% aqueous solution of potassium hydroxide was added to the olefin sulfonate composition to adjust the potassium hydroxide concentration to 0.246 mmol relative to 1 g of olefin sulfonate (adjustment step).

[0861] In the decolorization process, a continuous loop decolorization reactor equipped with a Milder MDN303V (manufactured by Pacific Machinery Co., Ltd.) as the mixer was used. The Milder MDN303V was equipped with a rotor and stator, and was implemented with a single blade. After heating the olefin sulfonate composition to 80°C, the olefin sulfonate composition and an aqueous hydrogen peroxide solution (concentration: 45%) were supplied to the reactor (mixing step) to begin the decolorization process. The circumferential speed of the mixer in the mixing step was 4.7 m / s, and the shear rate was 9400 / s. The amount of hydrogen peroxide after mixing was 10 mg relative to 1 g of olefin sulfonate in the olefin sulfonate composition. The pressure inside the reactor was adjusted to 0.3 MPaG by adjusting the opening of the valve at the outlet of the reactor. The residence time in the reactor was 6 minutes. After stabilization, immediately after the mixing step, the pH meter installed in the decolorization reactor showed 11.4. At this point, the potassium hydroxide concentration in the olefin sulfonate composition was 0.233 mmol per 1g of olefin sulfonate. The olefin sulfonate composition, after being held for 6 minutes, was extracted and kept in a constant temperature bath at the same temperature as during the decolorization treatment for 1 hour (aging step) to obtain the decolorized olefin sulfonate composition. The decolorized olefin sulfonate composition was then subjected to hue determination, fading rate evaluation, odor evaluation, storage stability evaluation, and peroxide value determination.

[0862] Examples 2-14, 20, and Comparative Examples 1 and 2

[0863] The decolorized olefin sulfonate composition was manufactured using the same manufacturing conditions as described in Tables 1 and 2, except that... In addition, the potassium hydroxide concentration was adjusted by adding a 48% aqueous potassium hydroxide solution or a 98% aqueous sulfuric acid solution to the olefin sulfonate composition before decolorization. Furthermore, the hue, fading rate, odor, storage stability, and peroxide value were measured using the same methods as in Example 1. The concentrations in the adjustment steps in Table 1 represent the concentrations of the alkaline compounds immediately after the mixing step.

[0864] Example 15

[0865] Using the 16-carbon inner olefin with an average double bond position of 4.3 obtained in Manufacturing Example A, an inner olefin sulfonate composition was obtained by the same method as in Example 13. Using the obtained inner olefin sulfonate composition before decolorization treatment, a decolorized inner olefin sulfonate composition was manufactured by the same method as in Example 13. Furthermore, hue determination, fading rate evaluation, odor evaluation, storage stability evaluation, and peroxide value determination were performed by the same method as in Example 13.

[0866] Example 16

[0867] The 18-carbon inner olefin with an average double bond position of 4.2 obtained in Manufacturing Example B was used instead of the 16-carbon inner olefin obtained in Manufacturing Example A. Otherwise, an inner olefin sulfonate composition was obtained by the same method as in Example 13. A decolorized inner olefin sulfonate composition was manufactured using the obtained inner olefin sulfonate composition before decolorization treatment, otherwise, by the same method as in Example 13. Furthermore, hue determination, fading rate evaluation, odor evaluation, storage stability evaluation, and peroxide value determination were performed by the same method as in Example 13.

[0868] Example 17

[0869] A sodium hydroxide aqueous solution (concentration: 12.5% ​​by mass) was used instead of a potassium hydroxide aqueous solution as the alkali, and the unbleached olefin sulfonate composition was prepared by the same method as in Example 13. The concentration of olefin sulfonate in the neutralized product was 53% by mass. The alkali concentration was adjusted by adding 48% sodium hydroxide aqueous solution or 98% sulfuric acid aqueous solution to the obtained unbleached olefin sulfonate composition. The adjusted unbleached olefin sulfonate composition was prepared under the manufacturing conditions described in Table 2, and the decolorization was performed by the same method as in Example 13. Subsequently, the hue, fading rate, odor, storage stability, and peroxide value were determined by the same method as in Example 13.

[0870] Example 18

[0871] The 18-carbon inner olefin with an average double bond position of 3.6 obtained in Manufacturing Example B was used instead of the 16-carbon inner olefin obtained in Manufacturing Example A. Otherwise, the inner olefin sulfonate composition before decolorization was obtained by the same method as in Example 17. The concentration of the inner olefin sulfonate in the neutralized product was 53% by mass. The decolorized inner olefin sulfonate composition was manufactured using the manufacturing conditions described in Table 2, except that it was produced by the same method as in Example 17. Furthermore, the hue, fading rate, odor, storage stability, and peroxide value were determined by the same method as in Example 17.

[0872] Example 19

[0873] The pH of the decolorized olefin sulfonate composition obtained in Example 13 was adjusted using an aqueous phosphoric acid solution (concentration: 75% by mass), and otherwise, its storage stability was evaluated using the same method as in Example 13. The results were the same as in Example 13, with a storage stability rating of A.

[0874] Example 21

[0875] Using the 16-carbon inner olefin with an average double bond position of 4.1 obtained in Manufacturing Example A, an inner olefin sulfonate composition was obtained by the same method as in Example 13. Using the obtained inner olefin sulfonate composition before decolorization treatment, a decolorized inner olefin sulfonate composition was manufactured by the same method as in Example 13. Furthermore, hue determination, fading rate evaluation, odor evaluation, storage stability evaluation, and peroxide value determination were performed by the same method as in Example 13.

[0876] Example 22

[0877] The 18-carbon inner olefin with an average double bond position of 4.4 obtained in Manufacturing Example B was used instead of the 16-carbon inner olefin obtained in Manufacturing Example A. Otherwise, an inner olefin sulfonate composition was obtained by the same method as in Example 16. A decolorized inner olefin sulfonate composition was manufactured using the obtained inner olefin sulfonate composition before decolorization treatment, otherwise, by the same method as in Example 16. Furthermore, hue determination, fading rate evaluation, odor evaluation, storage stability evaluation, and peroxide value determination were performed by the same method as in Example 16.

[0878] Example 23

[0879] Using the 16-carbon olefin obtained in Manufacturing Example A, an olefin sulfonate composition was obtained by the method of Example 1. 98% sulfuric acid was added to the obtained olefin sulfonate composition before decolorization to adjust the potassium hydroxide concentration. The potassium hydroxide concentration was 0.054 mmol per 1g of olefin sulfonate. For the adjusted olefin sulfonate composition before decolorization, the adjustment step and mixing step were performed simultaneously, except that a decolorized olefin sulfonate composition was prepared by the same method as in Example 13 (cycle ratio in the mixing and adjustment steps: 4 times). In the adjustment step, a 48% aqueous potassium hydroxide solution was added. The potassium hydroxide concentration immediately after the mixing step was 0.059 mmol per 1g of olefin sulfonate. Subsequently, the hue, fading rate, odor, storage stability, and peroxide value were determined by the same method as in Example 13.

[0880] <Measurement and Evaluation Methods>

[0881] (Determination of potassium hydroxide (or sodium hydroxide) concentration in the olefin sulfonate composition)

[0882] Take an appropriate amount of sample (approximately 5g with a precision of 3 decimal places), and add approximately 0.05g of 1% phenolphthalein ethanol solution to the solution diluted with deion-exchanged water until it turns red. Titrate the sample solution with 1 / 10N hydrochloric acid and read the titration amount when the red color disappears. The concentration of potassium hydroxide (or sodium hydroxide) in the sample is calculated using the following formula.

[0883] The concentration of potassium hydroxide (or sodium hydroxide) (mmol / g of olefin sulfonate) = {(1 / 10×f×d×M) / (c×1000)}×100

[0884] c: Sample size (g)

[0885] d: 1 / 10 of the volume of hydrochloric acid used (ml)

[0886] f: 1 / 10 N hydrochloric acid factor

[0887] M: Molecular weight of potassium hydroxide (or sodium hydroxide)

[0888] In addition, the region where phenolphthalein did not develop color (pH value less than 8.3) was determined using the following method. With the horizontal axis representing the concentration of potassium hydroxide (or sodium hydroxide) in the sample and the vertical axis representing the pH value, the following formula was established by approximating the relationship between them in the pH value range of 7 to 8.3 as a linear relationship. The concentration of potassium hydroxide (or sodium hydroxide) in the sample was then calculated based on the measured pH value.

[0889] The concentration of potassium hydroxide (or sodium hydroxide) (mmol / g of olefin sulfonate) = ((measured pH value) - 7) / 1010.1

[0890] (Measurement of hue and evaluation of fading rate)

[0891] The "OME 2000" petroleum product color tester (manufactured by Nippon Denshoku Kogyo Co., Ltd.), a tristimulus value direct-reading type, was used. The Hazen color value (APHA) of the olefin sulfonate composition before decolorization and the decolorized olefin sulfonate composition after decolorization was measur...

Claims

1. A method for manufacturing a decolorized olefin sulfonate composition, wherein, The process includes a decolorization step (A), which involves the following steps on a system containing an internal olefin sulfonate composition: Adjustment step (a1), adjusting the concentration of the alkaline compound in the system; and In the mixing step (a2), the decolorizing agent is mixed with the olefin sulfonate composition present in the system. The adjustment step (a1) is a step of adjusting the concentration of the alkaline compound so that the concentration of the alkaline compound after mixing the decolorizing agent with the olefin sulfonate composition present in the system in the decolorization process (A) is 0.004 mmol or more and 0.26 mmol or less relative to 1 g of olefin sulfonate.

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

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

4. The method for manufacturing the decolorized olefin sulfonate composition according to claim 1, wherein, The adjustment step (a1) and the mixing step (a2) are performed simultaneously.

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

6. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 5, wherein, In the adjustment step (a1), the adjustment is performed under shearing conditions where the shearing rate is 5 / s or more and 100,000 / s or less.

7. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 6, wherein, The mixing step (a2) requires 0.1 kW / m of power (Pv) per unit volume of liquid in the mixer. 3 Above and 100kW / m 3 the following.

8. A method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 7, wherein, The required power Pv for stirring per unit volume of liquid in the mixer during the adjustment step (a1) is 0.1 kW / m. 3 Above and 100kW / m 3 the following.

9. A method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 8, wherein, The mixing step (a2) is performed using a reaction vessel with stirring blades or a stirring blade type mixer. The ratio of the diameter d of the stirring blade to the diameter D of the reaction tank, d / D, is greater than 0.01 and less than 1.

10. A method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 9, wherein, The mixing step (a2) is performed using a reaction vessel with stirring blades or a stirring blade type mixer. The ratio of the stirring blade height h to the tank height H, h / H, is greater than 0.01 and less than 1.

11. A method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 10, wherein, The adjustment step (a1) is performed using a reaction vessel with stirring blades or a stirring blade type mixer. The ratio of the diameter d of the stirring blade to the diameter D of the reaction tank, d / D, is greater than 0.01 and less than 1.

12. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 11, wherein, The adjustment step (a1) is performed using a reaction vessel with stirring blades or a stirring blade type mixer. The ratio of the stirring blade height h to the tank height H, h / H, is greater than 0.01 and less than 1.

13. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 12, wherein, The pressure in the adjustment step (a1) is above 0 MPaG and below 10 MPaG.

14. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 13, wherein, The pressure of the mixing step (a2) is above 0 MPaG and below 10 MPaG.

15. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 14, wherein, The mixing step (a2) is performed using a reaction vessel with stirring blades or a stirring blade type mixer. The circumferential speed of the stirring blade is greater than 0.01 m / s and less than 50 m / s.

16. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 15, wherein, The adjustment step (a1) is performed using a reaction vessel with stirring blades or a stirring blade type mixer. The circumferential speed of the stirring blade is greater than 0.01 m / s and less than 50 m / s.

17. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 16, wherein, The mixing step (a2) is carried out at a temperature between 40°C and 100°C.

18. A method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 17, wherein, The amount of the decolorizing agent mixed is more than 1 mg and less than 300 mg relative to 1 g of the olefin sulfonate in the olefin sulfonate composition.

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

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

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

22. The method for manufacturing the decolorized olefin sulfonate composition according to claim 21, wherein, The temperature of the ripening step (b) is above 40°C and below 120°C.

23. The method for manufacturing the decolorized olefin sulfonate composition according to claim 21 or 22, wherein, The residence time in the ripening step (b) is more than 10 minutes and less than 500 minutes.

24. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 21 to 23, wherein, The pressure in the curing step (b) is above 0 MPaG and below 10 MPaG.

25. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 21 to 24, wherein, The ratio of the height H1 of the apparatus for performing the ripening step (b) to the diameter D1 of the apparatus, H1 / D1, is 0.1 or more and 300 or less.

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

27. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 26, wherein, The alkaline compound comprises at least one alkali metal hydroxide selected from sodium hydroxide and potassium hydroxide.

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

29. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 28, wherein, The average double bond position of the olefin in the inner olefin sulfonate is 3 or more and 5 or less.

30. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 29, wherein, The concentration of the basic compound in the olefin sulfonate composition prior to the decolorization step (A) is 0.010 mmol or more and 0.27 mmol or less relative to 1 g of olefin sulfonate in the olefin sulfonate composition.

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

32. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 21 to 26, wherein, The ripening step (b) is performed in a semi-batch manner.

33. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 21 to 26, wherein, The ripening step (b) is carried out continuously.

34. The method for manufacturing the decolorized olefin sulfonate composition according to any one of claims 1 to 33, wherein, The adjustment step (a1) is carried out continuously with a cyclic system, and the cyclic ratio of the internal olefin sulfonate composition exceeds 0.

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