Continuous deodorization, decoloration and desulfurization system and method for coal gasification naphtha

Abstract

The invention discloses a continuous deodorization, decoloration and desulfurization system and method for coal gasification naphtha, and relates to the technical field of naphtha production. An alkali washing unit; an oxidation deodorization unit; a washing unit; a coalescence dehydration unit; and a rectification unit. According to the continuous deodorization, decoloration and desulfurization system and method for the coal gasification naphtha, disclosed by the invention, the steps of acid washing, alkali washing, oxidation deodorization and water washing are sequentially carried out, so that the naphtha can be deodorized, decolorized, denitrified and desulfurized, and is turned into light yellow to colorless transparent liquid which is odorless, extremely low in nitride content and sulfide content and free of colloid; the research octane number (RON) can reach more than 90, the motor octane number (MON) can reach more than 80, and the product can be directly used as a naphtha blending component or a gasoline blending component and a reforming raw material so as to be used.

Description

Technical Field

[0001] The present invention relates to the technical field, and more particularly to a continuous deodorization, decolorization and desulfurization system and method for coal gasification naphtha. Background Art

[0002] Naphtha is a general term for a part of the light fraction of petroleum. Naphtha, also known as crude gasoline, is a light oil product with various distillation ranges depending on its use. my country stipulates that the distillation range is from the initial distillation point to about 220°C. It is mainly used as a reforming and chemical raw material. With the development of coal-to-gas technology, the aromatic solvent from coal tar in the gasification process is also called heavy naphtha or solvent naphtha. Since the market price of naphtha is much lower than that of unleaded gasoline for vehicles, the use of naphtha and petrochemical additives to prepare unleaded gasoline for vehicles has become an important way for private petrochemical companies to increase the profits of refined oil products.

[0003] Compared with naphtha produced from crude oil, naphtha produced by coal gasification has the characteristics of high sulfur, high nitrogen, bad odor, deep chroma, etc. At the same time, it has high aromatics, high olefin content, and high octane number. Due to the high odor and colloid content, it cannot be directly used as a naphtha blending component or as a gasoline blending component and reforming raw material. It must be refined and deodorized, decolorized, denitrogenated, and desulfurized before it can be transported and further processed. When processing naphtha, a desulfurization process will be used. For example, Chinese patent application number 200510004256.0 discloses a method for hydrodesulfurization of naphtha, in which full boiling range naphtha is simultaneously separated into light, heavy naphtha and thioetherified light naphtha in a catalytic distillation tower reactor. Only heavy naphtha is processed to remove organic ammonia catalyst poisons, and then hydrodesulfurized. Light hydrocarbons and light naphtha streams can be subjected to the final hydrodesulfurization treatment in the refining reactor. Although the method of naphtha hydrodesulfurization has a desulfurization effect on naphtha, since the naphtha produced by coal gasification has the characteristics of high sulfur, high nitrogen, bad odor, deep color, etc., this method cannot control it well to achieve the desulfurization and deodorization effects. At the same time, the hydrogen consumption and catalyst regeneration in the desulfurization process will bring additional energy consumption and emission problems.

[0004] Therefore, it is necessary to propose a continuous deodorization, decolorization and desulfurization system and method for gasified naphtha to solve the above problems. Summary of the invention

[0005] In view of the above situation, in order to overcome the defects of the prior art, the present invention provides a continuous deodorization, decolorization and desulfurization system and method for gasified naphtha to solve the problems raised in the above background technology.

[0006] The technical solution is as follows: the present invention comprises:

[0007] A pickling unit, the pickling unit comprising an acid liquid storage tank and a sulfuric acid settling tank, the water outlet end of the acid liquid storage tank is connected to the water inlet end of the sulfuric acid settling tank through a mixer, and the other water inlet end of the mixer is connected to the naphtha supply end;

[0008] An alkali washing unit, the alkali washing unit comprising an alkali liquid storage tank and an alkali liquid settling tank, the water outlet end of the sulfuric acid settling tank is connected to the water inlet end of the alkali liquid settling tank through a mixer, and the water outlet end of the alkali liquid storage tank is connected to the other water inlet end of the mixer;

[0009] An oxidative deodorization unit, the oxidative deodorization unit comprising an oxidant storage tank and an oxidation tank, the water outlet end of the alkali solution settling tank is connected to the water inlet end of the oxidation tank through a mixer, and the oxidant storage tank is connected to the other water inlet end of the mixer;

[0010] A water washing unit, wherein the water washing unit comprises a water washing tank, the water outlet of the oxidation tank is connected to the water inlet of the water washing tank through a mixer, and the other water inlet of the mixer is connected to an external water supply end;

[0011] A coalescence and dehydration unit, wherein the coalescence and dehydration unit comprises a coalescence separator, and the water outlet of the water washing tank is connected to the water inlet of the coalescence separator;

[0012] A distillation unit is connected to the coalescence and dehydration unit, and an output end of the distillation unit is connected to a finished product storage tank.

[0013] Furthermore, the acid liquid storage tank stores acid liquid, the acid liquid is sulfuric acid with a concentration of 70-98% or hydrochloric acid with a concentration of 20-25%, and the amount of the acid liquid added is 1-5% of the amount of naphtha processed.

[0014] Furthermore, the alkali solution storage tank stores alkali solution, which is 10-20% sodium hydroxide, to which 0.05% of the mass of the alkali solution is added sulfonated cobalt phthalocyanine HZ-3 or polyphthalocyanine cobalt catalyst, and the amount of alkali solution added is 10-20% of the naphtha processing amount.

[0015] Furthermore, the oxidant storage tank stores hydrogen peroxide with a concentration of 20-30%, and the added amount of the hydrogen peroxide is 1-4% of the naphtha processing amount.

[0016] Furthermore, the distillation unit includes a distillation tower and a condenser, the top gas outlet of the distillation tower is connected to the gas inlet of the condenser, the bottom water outlet of the condenser is connected to the finished product storage tank, and cooling water circulates inside the condenser;

[0017] The bottom of the distillation tower is circulatedly connected with a reboiler, a heat transfer coil is arranged in the reboiler, and high-temperature heat transfer oil circulates in the heat transfer coil.

[0018] Furthermore, the water outlet end of the coalescing separator is connected to the water inlet end of a distillation tower, and the distillation tower performs fraction cutting at 60°C-°C.

[0019] Furthermore, the bottoms of the sulfuric acid sedimentation tank, oxidation tank, water washing tank and agglomeration separator are connected to a wastewater discharge pipe, the bottom of the alkali solution sedimentation tank is connected to a circulation pipe and a wastewater discharge pipe, and the other end of the circulation pipe extends into the alkali solution storage tank.

[0020] Furthermore, a steam heating pipeline is connected to the bottom of the alkali solution storage tank, and the temperature inside the alkali solution storage tank is 20-30°C.

[0021] The continuous deodorization, decolorization and desulfurization method of gasified naphtha comprises the following steps:

[0022] S1, pickling: the naphtha raw material is mixed with the acid in the acid storage tank through a mixer and then transported to the sulfuric acid settling tank, and the sulfide in the naphtha is removed after pickling in the sulfuric acid settling tank;

[0023] S2, alkali washing: the naphtha after acid washing is mixed with the alkali in the alkali storage tank through a mixer, and then transported to the alkali settling tank for alkali washing to remove the residual acidic substances and the acidic substances in the naphtha at the same time:

[0024] S3, oxidative deodorization: the alkali-washed naphtha is mixed with hydrogen peroxide in the oxidant storage tank through a mixer, and then transported to an oxidation tank for oxidative deodorization to further remove sulfides and other volatile organic compounds in the naphtha, while improving the antioxidant capacity of the naphtha;

[0025] S4, water washing: the oxidatively deodorized naphtha is mixed with water through a mixer, and then enters a water washing tank for water washing, where the unreacted impurities in the naphtha are removed by sedimentation to separate the naphtha;

[0026] S5, coalescence dehydration: The washed naphtha is transported to the coalescence separator to remove free water in the naphtha and improve the efficiency of subsequent distillation;

[0027] S6, distillation: The dehydrated naphtha is passed through the distillation tower and condenser in sequence to remove sediment and impurities, and finally stored in the finished product storage tank.

[0028] Compared with the existing known technologies, the technical solution provided by the present invention has the following significant effects:

[0029] 1. Through the effect of alkali washing first and then oxidation deodorization, the naphtha can be pre-alkaline washed to remove a small amount of hydrogen sulfide and some mercaptans and thiophenols in the naphtha, avoiding the copper sheet corrosion and oxidation of the oil product caused by hydrogen sulfide. At the same time, the remaining mercaptans can react with the oxidant in the subsequent steps to produce oxygen and transform into disulfides. The generated disulfides remain in the oil, which improves the stability and antioxidant capacity of the oil product and can also deodorize the naphtha.

[0030] 2. By adding sulfonated cobalt phthalocyanine HZ-3 or polyphthalocyanine cobalt catalyst to the alkali solution, the washing effect of the alkali solution on naphtha can be improved, and hydrogen sulfide, mercaptan and thiophenol in naphtha can be removed. At the same time, the dilute alkali solution can be regenerated and recycled, which also increases the economy and environmental friendliness of the whole process.

[0031] 3. Through the steps of acid washing, alkali washing, oxidation deodorization and water washing in sequence, the naphtha can be deodorized, decolorized, denitrogenated and desulfurized, and turned into a light yellow to colorless transparent liquid with no odor, extremely low nitrogen compounds and sulfides, and no colloid. The research octane number (RON) can reach above 90, and the motor octane number (MON) can reach above 80, which is suitable for direct use as a naphtha blending component or as a gasoline blending component and reforming raw material. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] Figure 1 It is a schematic diagram of the structure of the present invention;

[0033] Figure 2 It is a schematic diagram of the process of the present invention.

[0034] Reference numerals:

[0035] 100. Mixer; 101. Acid storage tank; 102. Sulfuric acid settling tank; 103. Alkali storage tank; 104. Alkali settling tank; 105. Oxidant storage tank; 106. Oxidation tank; 107. Washing tank; 108. Coagulation separator; 109. Finished product storage tank; 110. Distillation tower; 111. Condenser; 112. Reboiler; 113. Heat transfer coil; 114. Circulation pipeline; 115. Steam heating pipeline. DETAILED DESCRIPTION

[0036] In order to make the purpose, technical scheme and advantages of the present invention more clearly understood, the present invention is further described in detail below in conjunction with the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not used to limit the present invention, that is, the embodiments described are only part of the embodiments of the present invention, rather than all of the embodiments. The components of the embodiments of the present invention described and shown in the drawings herein can be arranged and designed in various different configurations.

[0037] Depend on Figure 1 to Figure 2 Given, including:

[0038] The following provides a structure capable of desulfurizing naphtha: a pickling unit, the pickling unit includes an acid liquid storage tank 101 and a sulfuric acid settling tank 102, the water outlet end of the acid liquid storage tank 101 is connected to the water inlet end of the sulfuric acid settling tank 102 through a mixer 100, and the naphtha and the acid liquid are mixed and enter the sulfuric acid settling tank 102, and the desulfurization effect is achieved through the sedimentation effect in the sulfuric acid settling tank 102, and the other water inlet end of the mixer 100 is connected to the naphtha supply end, and the mixer 100 is preferably a Venturi pipeline mixer 100;

[0039] The following provides a structure capable of removing acidic substances in naphtha: an alkali washing unit, the alkali washing unit includes an alkali liquid storage tank 103 and an alkali liquid settling tank 104, the water outlet end of the sulfuric acid settling tank 102 is connected to the water inlet end of the alkali liquid settling tank 104 through a mixer 100, the naphtha and the alkali liquid are mixed and enter the alkali liquid settling tank 104, and the effect of removing acidic substances is achieved in the alkali liquid settling tank 104, the water outlet end of the alkali liquid storage tank 103 is connected to the other water inlet end of the mixer 100, preferably, the concentration of the alkali liquid in the alkali liquid settling tank 104 is always maintained at 15%, when the concentration is reduced, the alkali liquid storage tank 103 supplies alkali liquid to it, and at the same time, the circulation pipeline 114 at the bottom is connected to transport the reacted alkali liquid in the alkali liquid settling tank 104 back to the alkali liquid storage tank 103, when too much alkali liquid is produced after the reaction, the wastewater pipeline is started to discharge the excess;

[0040] Since gasified naphtha is different from naphtha in crude oil, it has a higher sulfide content. One-time desulfurization can only remove most of the sulfides, but a small amount of sulfides will remain. The following provides a structure for desulfurizing naphtha again: an oxidation deodorization unit, the oxidation deodorization unit includes an oxidant storage tank 105 and an oxidation tank 106, the water outlet end of the alkali solution settling tank 104 is connected to the water inlet end of the oxidation tank 106 through a mixer 100, and the naphtha and the oxidant are mixed and then enter the oxidation tank 106 for sedimentation. Under the action of the oxidant, mercaptans react with oxygen to convert into disulfides, and the generated disulfides remain in the oil, which improves the stability of the oil. The oxidant storage tank 105 is connected to the other water inlet end of the mixer 100. The main purpose of alkali washing is to remove the residual hydrogen sulfide, mercaptan and thiophenol in the naphtha. Hydrogen sulfide will not only cause the copper sheet corrosion of the oil product to be unqualified, but also have an oxidizing effect on the oil product, causing the oil product to become darker in color and reduce its antioxidant capacity. Gasified naphtha contains a high content of mercaptan, which produces a bad smell and is corrosive. Moreover, mercaptan is an oxidation initiator, which can promote the oxidation condensation of unstable components in naphtha into a colloid, causing the storage stability of naphtha to deteriorate. Therefore, it is necessary to remove the hydrogen sulfide and a part of mercaptan and thiophenol in the naphtha.

[0041] The following provides a structure for removing unreacted impurities in naphtha: a water washing unit, the water washing unit includes a water washing tank 107, the water outlet end of the oxidation tank 106 is connected to the water inlet end of the water washing tank 107 through a mixer 100, and the unreacted impurities in the naphtha are removed by water washing, and the other water inlet end of the mixer 100 is connected to the external water supply end;

[0042] There is free water in the naphtha after water washing. The following provides a structure capable of removing free water in the naphtha: a coalescing and dehydrating unit, the coalescing and dehydrating unit comprises a coalescing and dehydrating device 108, through which free water and impurities in the naphtha can be removed to improve the quality and yield of the final product, and the water outlet end of the water washing tank 107 is connected to the water inlet end of the coalescing and dehydrating device 108;

[0043] The following provides a structure capable of distilling and storing naphtha: a distillation unit, the distillation unit is connected to a coalescence and dehydration unit, to remove the precipitates and impurities in the naphtha after the reaction, and to improve the quality of the oil product at the factory. The output end of the distillation unit is connected to a finished product storage tank 109. The naphtha after distillation is a light yellow to colorless transparent liquid, odorless, and contains very low nitrogen compounds and sulfides, and does not contain colloid. The research octane number RON can reach more than 90, and the motor octane number MON can reach more than 80.

[0044] Specifically, acid liquid is stored in the acid liquid storage tank 101, and the acid liquid is sulfuric acid with a concentration of 70-98% or hydrochloric acid with a concentration of 20-25%. The acid liquid and naphtha are continuously supplied. The pickling efficiency of naphtha is improved by the continuous supply of acid liquid. The amount of acid liquid added is 1-5% of the naphtha processing amount. During the operation, the waste acid liquid needs to be continuously discharged, and the liquid content in each sedimentation tank is two-thirds of the total capacity of the tank.

[0045] Specifically, alkali solution is stored in the alkali solution storage tank 103, and the alkali solution is sodium hydroxide with a concentration of 10-20%. The circulation amount of alkali solution supply and discharge is 10-20%. Sulfonated cobalt phthalocyanine HZ-3 or cobalt polyphthalocyanine catalyst is added to the alkali solution at a mass percentage of 0.05%. Sulfonated cobalt phthalocyanine HZ-3 or cobalt polyphthalocyanine catalyst has good catalytic performance, especially for the oxidation removal of mercaptans. It is very effective. By adding sulfonated cobalt phthalocyanine HZ-3 or cobalt polyphthalocyanine catalyst to the alkali solution, the oxidation of mercaptans can be effectively catalyzed, and mercaptans in refined naphtha can be removed, thereby purifying the product. At the same time, the dilute alkali solution can be regenerated and recycled, which also increases the economy and environmental friendliness of the whole process. The amount of alkali solution added is 10-20% of the naphtha processing amount, and the alkali solution is continuously supplied.

[0046] Specifically, the oxidant storage tank 105 stores hydrogen peroxide with a concentration of 20-30%. The amount of hydrogen peroxide added is 1-4% of the naphtha processing amount. Under the action of the oxidant, mercaptans react with oxygen to be converted into disulfides. The generated disulfides remain in the oil, which improves the stability of the oil and enhances the antioxidant capacity of the oil. The naphtha is deoxygenated and deodorized by hydrogen peroxide.

[0047] Specifically, the distillation unit includes a distillation tower 110 and a condenser 111. The top gas outlet of the distillation tower 110 is connected to the gas inlet of the condenser 111 to remove the sediment and impurities after the reaction in the naphtha and improve the quality of the oil product. The bottom water outlet of the condenser 111 is connected to the finished product storage tank 109. Cooling water circulates inside the condenser 111.

[0048] The bottom of the distillation tower 110 is circulatedly connected to a reboiler 112 , in which a heat transfer coil 113 is provided. The reboiler 112 is heated by high-temperature heat transfer oil in the heat transfer coil 113 , and high-temperature heat transfer oil circulates in the heat transfer coil 113 .

[0049] Specifically, the water outlet of the coalescing separator 108 is connected to the water inlet of the distillation tower 110, and the distillation tower 110 performs fraction cutting at 60°C-180°C.

[0050] Specifically, the bottoms of the sulfuric acid sedimentation tank 102, the oxidation tank 106, the water washing tank 107 and the agglomeration separator 108 are connected with wastewater discharge pipes, and the waste solution is continuously discharged from the bottom while the solution is continuously input to maintain the concentration of the solution in the tank. The bottom of the alkali solution sedimentation tank 104 is connected with a circulation pipe 114 and a wastewater discharge pipe, and the other end of the circulation pipe 114 extends into the alkali solution storage tank 103. The circulation pipe 114 is used for recycling waste alkali solution. When the alkali solution is excessive after the reaction, part of the waste alkali solution will be discharged through the wastewater discharge pipe.

[0051] Specifically, a steam heating pipe 115 is connected to the bottom of the alkali liquid storage tank 103 to increase the temperature in the alkali liquid storage tank 103 to prevent crystallization. The temperature in the alkali liquid storage tank 103 is 20-30°C.

[0052] refer to Figure 2 The continuous deodorization, decolorization and desulfurization method of gasified naphtha comprises the following steps:

[0053] S1, pickling: the naphtha raw material is mixed with the acid in the acid storage tank 101 through the mixer 100 and then transported to the sulfuric acid settling tank 102. The sulfide in the naphtha is removed after pickling in the sulfuric acid settling tank 102. This is the first desulfurization;

[0054] S2, alkali washing: the acid-washed naphtha is mixed with the alkali solution in the alkali solution storage tank 103 through the mixer 100. The mixer 100 is a venturi pipeline mixer 100, which is used to improve the mixing effect. After mixing, it is transported to the alkali solution settling tank 104 for alkali washing to remove the residual acidic substances and the acidic substances in the naphtha at the same time. This is the second desulfurization. In order to completely remove hydrogen sulfide, mercaptan and thiophenol in the naphtha, sulfonated cobalt phthalocyanine HZ-3 or polyphthalocyanine cobalt catalyst is added to the alkali solution:

[0055] S3, oxidative deodorization: the naphtha after alkali washing is mixed with hydrogen peroxide in the oxidant storage tank 105 through the mixer 100, and then transported to the oxidation tank 106 for oxidative deodorization. Under the action of the oxidant, the remaining mercaptan reacts with oxygen to be converted into disulfide, and the generated disulfide remains in the oil, which improves the stability of the oil product and enhances the antioxidant capacity of the oil product, further removes sulfides and other volatile organic compounds in the naphtha, and at the same time improves the antioxidant capacity of the naphtha;

[0056] S4, water washing: the oxidatively deodorized naphtha is mixed with water through a mixer 100, and then enters a water washing tank 107 for water washing, where the unreacted impurities in the naphtha are removed by separation through sedimentation;

[0057] S5, coalescence dehydration: The washed naphtha is transported to the coalescence separator 108 to remove free water in the naphtha. During the water washing, waste water is discharged from the bottom, and the efficiency of subsequent distillation is improved;

[0058] S6, distillation: the naphtha after coalescence and dehydration is sequentially passed through the distillation tower 110 and the condenser 111 to remove the sediment and impurities, and the fractions are cut at 60° C.-180° C., and finally stored in the finished product storage tank 109.

[0059] The above-mentioned embodiments are only preferred embodiments of the present invention and cannot be used to limit the scope of protection of the present invention. Any non-substantial changes and substitutions made by technicians in this field on the basis of the present invention shall fall within the scope of protection required by the present invention.

Claims

1. A continuous deodorization, decolorization and desulfurization system for gasified naphtha, characterized in that: include: A pickling unit, the pickling unit comprising an acid liquid storage tank (101) and a sulfuric acid sedimentation tank (102), the water outlet end of the acid liquid storage tank (101) being connected to the water inlet end of the sulfuric acid sedimentation tank (102) via a mixer (100), and the other water inlet end of the mixer (100) being connected to a naphtha supply end; An alkali washing unit, the alkali washing unit comprising an alkali liquid storage tank (103) and an alkali liquid settling tank (104), the water outlet of the sulfuric acid settling tank (102) being connected to the water inlet of the alkali liquid settling tank (104) via a mixer (100), and the water outlet of the alkali liquid storage tank (103) being connected to the other water inlet of the mixer (100); An oxidative deodorization unit, the oxidative deodorization unit comprising an oxidant storage tank (105) and an oxidation tank (106), the water outlet of the alkali solution settling tank (104) being connected to the water inlet of the oxidation tank (106) via a mixer (100), and the oxidant storage tank (105) being connected to the other water inlet of the mixer (100); A water washing unit, the water washing unit comprising a water washing tank (107), the water outlet end of the oxidation tank (106) is connected to the water inlet end of the water washing tank (107) through a mixer (100), and the other water inlet end of the mixer (100) is connected to an external water supply end; A coalescence and dehydration unit, wherein the coalescence and dehydration unit comprises a coalescence separator (108), and the water outlet end of the water washing tank (107) is connected to the water inlet end of the coalescence separator (108); A distillation unit is connected to the coalescence and dehydration unit, and an output end of the distillation unit is connected to a finished product storage tank (109).

2. The continuous deodorization, decolorization and desulfurization system of gasified naphtha according to claim 1, characterized in that: The acid liquid storage tank (101) stores acid liquid, which is sulfuric acid with a concentration of 70-98% or hydrochloric acid with a concentration of 20-25%. The amount of acid liquid added is 1-5% of the amount of naphtha processed.

3. The continuous deodorization, decolorization and desulfurization system of gasified naphtha according to claim 1, characterized in that: The alkali solution storage tank (103) stores alkali solution, which is sodium hydroxide with a concentration of 10-20%. The alkali solution is added with 0.05% of the mass of the alkali solution sulfonated cobalt phthalocyanine HZ-3 or polyphthalocyanine cobalt catalyst, and the amount of the alkali solution added is 10-20% of the naphtha processing amount.

4. The continuous deodorization, decolorization and desulfurization system of gasified naphtha according to claim 1, characterized in that: The oxidant storage tank (105) stores hydrogen peroxide with a concentration of 20-30%, and the amount of hydrogen peroxide added is 1-4% of the amount of naphtha processed.

5. The continuous deodorization, decolorization and desulfurization system of gasified naphtha according to claim 1, characterized in that: The distillation unit comprises a distillation tower (110) and a condenser (111), wherein the top gas outlet of the distillation tower (110) is connected to the gas inlet of the condenser (111), the bottom water outlet of the condenser (111) is connected to the finished product storage tank (109), and cooling water circulates inside the condenser (111); The bottom of the distillation tower (110) is circulatedly connected to a reboiler (112), a heat transfer coil (113) is arranged in the reboiler (112), and high-temperature heat transfer oil circulates in the heat transfer coil (113).

6. The continuous deodorization, decolorization and desulfurization system of gasified naphtha according to claim 5, characterized in that: The water outlet of the coalescing separator (108) is connected to the water inlet of the distillation tower (110), and the distillation tower (110) performs fraction cutting at 60°C-180°C.

7. The continuous deodorization, decolorization and desulfurization system for gasified naphtha according to claim 6, characterized in that: The bottoms of the sulfuric acid sedimentation tank (102), the oxidation tank (106), the washing tank (107) and the coalescing separator (108) are connected to a wastewater discharge pipe, and the bottom of the alkali solution sedimentation tank (104) is connected to a circulation pipe (114) and a wastewater discharge pipe, and the other end of the circulation pipe (114) extends into the alkali solution storage tank (103).

8. The continuous deodorization, decolorization and desulfurization system of gasified naphtha according to claim 3, characterized in that: The bottom of the alkali solution storage tank (103) is connected to a steam heating pipeline (115), and the temperature inside the alkali solution storage tank (103) is 20-30°C.

9. A method for continuous deodorization, decolorization and desulfurization of gasified naphtha, using the continuous deodorization, decolorization and desulfurization system of gasified naphtha according to claim 8, characterized in that: The following steps are involved: S1, pickling: mixing the naphtha raw material with the acid solution in the acid solution storage tank (101) through a mixer (100) and then transporting the mixture to a sulfuric acid settling tank (102), and removing sulfides in the naphtha through pickling in the sulfuric acid settling tank (102); S2, alkali washing: the acid-washed naphtha is mixed with the alkali solution in the alkali solution storage tank (103) through the mixer (100), and then transported to the alkali solution settling tank (104) for alkali washing to remove the residual acidic substances and the acidic substances in the naphtha at the same time: S3, oxidative deodorization: the alkali-washed naphtha is mixed with hydrogen peroxide in the oxidant storage tank (105) through a mixer (100), and then transported to an oxidation tank (106) for oxidative deodorization to further remove sulfides and other volatile organic compounds in the naphtha, while improving the antioxidant capacity of the naphtha; S4, water washing: the oxidatively deodorized naphtha is mixed with water through a mixer (100), and then enters a water washing tank (107) for water washing, where the naphtha is separated by sedimentation to remove unreacted impurities in the naphtha; S5, coalescence dehydration: The washed naphtha is transported to a coalescence separator (108) to remove free water from the naphtha and improve the efficiency of subsequent distillation; S6, distillation: The naphtha after coalescence and dehydration passes through a distillation tower (110) and a condenser (111) in sequence to remove sediments and impurities, and is finally stored in a finished product storage tank (109).

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