Method for automatically regulating and controlling acidity and alkalinity in process of preparing durene through alkylation

Abstract

The method comprises the following steps: cooling a reaction product in a high-temperature state, generating a part of by-product steam through a steam generator, effectively utilizing waste heat, separating and cooling through a gas-liquid separator, and separating and cooling through a gas-liquid separator; after being cooled by the air cooler, the gas enters a three-phase separator for gas-water-oil separation, a gas phase enters a thermal oxidation furnace for incineration, a water phase is sent to a methanol recovery section for methanol recovery and water treatment, an oil phase firstly enters an alkaline tower for organic acid neutralization reaction, and a treated oil phase product is sent to a rectification section for next-step rectification separation; and the alkaline washing tower and the water washing tower exchange alkali and replace alkali regularly according to the operation condition. According to the method for automatically regulating and controlling the acidity and alkalinity in the process of preparing durene through alkylation, corrosion of an acidic working solution to equipment pipelines of a reaction system is slowed down, meanwhile, waste heat of a reaction product can be utilized to byproduct part of steam, the pH value of wastewater can be regulated in advance, and the wastewater can directly enter a water treatment biochemical pool to be treated.

Description

Technical Field

[0001] The invention relates to the technical field of duren preparation, in particular to an automatic acidity and alkalinity control method in a duren preparation process by alkylation. Background Art

[0002] Durene, also known as 1,2,4,5-tetramethylbenzene, is a white crystal. Its main use is in the production of pyromellitic anhydride, which can be used to produce polyimide. As the market usage of polyimide continues to expand, the demand for durene is also increasing day by day. However, the current domestic production of durene is limited and the product quality is poor. Reducing production costs and improving product quality have become the current goals of the industry.

[0003] At present, the industry mainly adopts two major methods: C10 separation method and synthesis method. At present, the method of preparing durenyl through alkylation and isomerization of xylene and trimethylbenzene is highly corrosive due to the side reaction during the reaction. Organic acids such as formic acid will be generated at high temperature, which are highly corrosive. In order to improve the service life of the reaction device, the overall material of the reaction device needs to be improved, but it will lead to a significant increase in construction costs. This method is aimed at the alkylation technology of durenyl using methanol as raw material. Because the reaction is a violent exothermic reaction, methanol generates some organic acids such as formic acid at high temperature. Formic acid is an organic acid and the strongest acid among organic weak acids. Since formic acid is the simplest organic acid, it has a relatively small binding force on ionizable hydrogen, so the degree of ionization of formic acid is relatively large. Therefore, the acidity of formic acid is greater than that of other organic acids, which will cause serious corrosion to production pipelines and equipment facilities, resulting in a short production life of the device, and it is very easy to leak and cause safety accidents such as fire and explosion, so this problem needs to be solved urgently. Summary of the invention

[0004] The purpose of the present invention is to provide an automatic control method for the acidity and alkalinity of an alkylation process for producing durenyl, so as to improve the overall pH value of the alkylation process for producing durenyl, slow down the corrosion of the acidic working fluid on the equipment pipelines of the reaction system, and simultaneously utilize the waste heat of the reaction product to produce part of the steam as a by-product, so as to adjust the pH value of the wastewater in advance so that the wastewater can directly enter the water treatment biochemical pool for treatment, thereby extending the service life of the production device.

[0005] To achieve the above object, the present invention provides a method for automatically controlling the acidity and alkalinity of a durene production process by alkylation, comprising the following steps:

[0006] The high-temperature reaction products produced in the alkylation process to produce durene need to be cooled down. Part of the steam is produced as a by-product of the steam generator to effectively utilize the waste heat, and then separated and cooled down by a gas-liquid separator. After cooling down in an air cooler, they enter a three-phase separator for gas, water and oil separation. The gas phase is de-heated and incinerated in an oxidation furnace. The water phase is sent to the methanol recovery section to recover methanol and water treatment. The oil phase first enters the alkali washing tower for organic acid neutralization reaction, and then passes through the water washing tower to extract and dissolve the reaction salt product and a small amount of unreacted organic acid. The treated oil phase product is sent to the distillation section for the next step of distillation separation. The alkali washing tower and the water washing tower are regularly replaced and replaced according to the operating conditions.

[0007] Preferably, the specific operation of cooling the reaction product in a high temperature state is as follows: the temperature of the reaction product is 420°C, and after heat exchange between the reaction inlet and outlet materials, it still reaches 220°C, and the steam generator is increased to produce 0.5Mpa steam as a by-product, and the temperature is reduced to 180-195°C at the same time. The by-product steam can be used for heating the alkali washing tower and the water washing tower, and the surplus low-pressure steam is sent to the by-product low-pressure steam pipeline network.

[0008] Preferably, the specific operation of separation and cooling in the gas-liquid separator is: the reaction product after cooling enters the gas-liquid separator for gas-liquid separation, the non-condensable gas after the by-product steam is further cooled and condensed by circulating water cooling, and the liquid phase is cooled by an air cooler.

[0009] Preferably, the specific operation of the organic acid neutralization reaction is: the reaction product after gas-liquid separation continues to be separated into three phases, the main product oil phase is passed through an alkali washing tower to neutralize the organic acid, the water washing tower washes and extracts impurities, the pH value of the product is adjusted to neutral, and 32% NaOH alkali solution is sent to the alkali washing tower, and desalted water is added for dilution. After dilution, the concentration of the alkali solution in the tower is not higher than 0.01%, and the pH value is less than 11.4.

[0010] Preferably, the three-phase separator, alkali washing tower and water washing tower are equipped with pH online analyzers. The working status of the alkali washing tower and the water washing tower are monitored by online instruments, and timely replacement is carried out to ensure the smooth operation and controllability of the neutralization system. Automatic adjustment is achieved by cooperating with a self-adjusting valve group to reduce the influence of human factors.

[0011] The advantages and positive effects of the automatic acidity and alkalinity control method for the alkylation process of durene according to the present invention are:

[0012] 1. The technology of the present invention can recover the heat of the reaction products to the maximum extent, and the by-product steam saves the use of circulating water and electricity. It can also ensure the properties of the reaction products to prevent corrosion of equipment pipelines due to excessive acidity, ensure the safety of the production equipment, and at the same time obtain good benefits and economic benefits. The technology is safe, reliable and easy to implement.

[0013] 2. The present invention can modify the properties of the reaction products and adjust them to be neutral or weakly alkaline, thereby ensuring the safety of equipment pipelines, reducing the construction investment of equipment pipelines, solving the problem of serious equipment corrosion under existing processes, utilizing the waste heat of the products to produce steam as a by-product, eliminating the circulating water required for cooling, and ensuring that the heat used in the newly added alkali solution system further realizes thermal coupling.

[0014] 3. The present invention can pre-treat the reaction wastewater in the product in advance, eliminating the acid-base adjustment link before the acidic wastewater enters the water treatment, and can be directly sent to the water treatment biochemical system for treatment, which can be said to kill two birds with one stone. Various control methods are used to achieve automatic control, which can greatly reduce human errors and improve control stability.

[0015] The technical solution of the present invention is further described in detail below through the accompanying drawings and embodiments. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Figure 1 This is a schematic flow chart of a method for automatically controlling the acidity and alkalinity of a process for preparing durene by alkylation according to the present invention;

[0017] Figure 2 The present invention is a schematic diagram of an automatic control scheme in a method for automatically regulating the acidity and alkalinity of a process for producing durene by alkylation.

[0018] Reference numerals

[0019] 1. Reaction product steam generator; 2. Gas-liquid separator; 3. Gas phase cooler; 4. Liquid phase air cooler; 5. Three-phase separator; 6. Alkali washing tower; 7. Water washing tower; 8. Alkali buffer tank; 9. Alkali online flowmeter; 10. Alkali adding self-adjusting valve group; 11. Water phase buffer tank; 12. Water phase delivery pump; 13. Online water phase pH detector; 14. Desalted water self-adjusting valve; 15. Oil phase online pH detector; 16. Alkali adding self-adjusting valve in water phase buffer tank; 17. Online pH detector; 18. Alkali washing tower discharge valve; 19. Water washing tower discharge valve; 20. Water washing tower water adding valve; 21. Online interface meter; 22. Online liquid level meter; 23. Oil phase discharge valve; 24. Water phase discharge valve; 25. System pressure regulating valve; 26. Steam regulating valve; 27. Online thermometer; 28. Gas-liquid separation discharge valve; 29. ​​Alkali washing tower desalted water self-adjusting valve. DETAILED DESCRIPTION

[0020] The technical solution of the present invention is further described below through the accompanying drawings and embodiments.

[0021] Unless otherwise defined, the technical terms or scientific terms used in the present invention should be understood by people with ordinary skills in the field to which the present invention belongs. The words "first", "second" and similar words used in the present invention do not indicate any order, quantity or importance, but are only used to distinguish different components. "Include" or "comprise" and similar words mean that the elements or objects appearing before the word include the elements or objects listed after the word and their equivalents, without excluding other elements or objects. "Connect" or "connected" and similar words are not limited to physical or mechanical connections, but may include electrical connections, whether direct or indirect. "Up", "down", "left", "right" and the like are only used to indicate relative positional relationships. When the absolute position of the described object changes, the relative positional relationship may also change accordingly.

[0022] Example

[0023] A method for automatically controlling the acidity and alkalinity of a durene production process by alkylation, comprising the following steps:

[0024] The reaction products in the high temperature state generated in the process of alkylation to produce durene need to be cooled down. The by-product steam is produced by the steam generator 1 to effectively utilize the waste heat, and then separated and cooled by the gas-liquid separator 2. After cooling by the air cooler, the products enter the three-phase separator 5 for gas, water and oil separation. The gas phase is de-heated and incinerated in the oxidation furnace. The water phase is sent to the methanol recovery section to recover methanol and water treatment. The oil phase first enters the alkali washing tower 6 for organic acid neutralization reaction, and then passes through the water washing tower 7 to extract and dissolve the reaction salt product and a small amount of unreacted organic acid. The treated oil phase product is sent to the distillation section for the next step of distillation separation. The alkali washing tower 6 and the water washing tower 7 are regularly replaced and replaced according to the operating conditions.

[0025] like Figure 1 As shown, a device for realizing an automatic control method of acidity and alkalinity in an alkylation process of preparing durene comprises a reaction product steam generator 1, a gas-liquid separator 2, a gas phase cooler 3, a liquid phase air cooler 4, a three-phase separator 5, an alkali washing tower 6, a water washing tower 7, an alkali solution buffer tank 8, an alkali solution online flow meter 9, an alkali addition self-regulating valve group 10, an aqueous phase buffer tank 11, an aqueous phase delivery pump 12, an online aqueous phase pH detector 13, a desalted water self-regulating valve 14, an oil phase online pH detector 15, an alkali addition self-regulating valve 16 for the aqueous phase buffer tank, an online pH detector 17, an alkali washing tower discharge valve 18, a water washing tower discharge valve 19, a water washing tower water addition valve 20, an online interface meter 21, an online liquid level meter 22, an oil phase discharge valve 23, an aqueous phase discharge valve 24, a system pressure regulating valve 25, a steam regulating valve 26, an online thermometer 27, a gas-liquid separation discharge valve 28, and an alkali washing tower desalted water self-regulating valve 29.

[0026] After the reaction product comes out of the reactor, it enters the reaction product steam generator 1 (to recover part of the waste heat and by-product steam), and then is separated in the liquid side inlet tank of the gas-liquid separator 2. The gas phase enters the gas phase cooler 3 from the liquid top outlet of the gas-liquid separator 2 for cooling and then enters the three-phase separator 5. The liquid phase enters the three-phase separator 5 after being cooled by the air cooler 4 from the bottom outlet of the gas-liquid separator 2. After separation by the three-phase separator 5, the gas phase non-condensable gas is sent to the tail gas treatment system by the system pressure regulating valve 25, the oil phase product is sent to the subsequent section after being alkali washed, purified and adjusted for pH by the alkali washing tower 6 and the water washing tower 7, and the water phase enters the water phase buffer tank 11. The alkali liquid buffer tank 8 replenishes the alkali liquid into the alkali washing tower 6 and the water phase buffer tank 11 in time, and the wastewater in the water phase buffer tank 11 is sent to the post-treatment section by the water phase delivery pump 12.

[0027] The reaction products come from the upstream process, which is:

[0028] After dehydration pretreatment, the raw material trimethylol is mixed with the excess trimethylol recovered from the distillation section and enters the raw material buffer tank. After being pressurized by the feed pump, it is sent to the electric heater to heat the reaction product to heat the trimethylol to 350°C; after being pressurized by the methanol feed pump, methanol is sent to the methanol feed heater to be heated to 150-160°C and sent to each catalytic bed of the alkylation reactor to control the reaction temperature of the catalyst bed; in order to ensure the control of reaction heat, the trimethylol in the alkylation reactor material adopts an excessive circulation process; an inlet and outlet heat exchanger is added at the reactor outlet to heat the trimethylol feed and recover part of the heat, which is sent to the steam generator 1 after the heat exchange is completed.

[0029] The reaction product of the reaction section is sent to the reaction product steam generator 1 for by-product steam, and the pressure of the by-product steam is controlled by the steam regulating valve 26. After gas-liquid separation, the gas phase enters the cooler for further cooling, and the liquid phase enters the air cooler for cooling. The cooled products enter the three-phase separator 5 for three-phase separation. The gas-liquid separation discharge valve 28 controls the liquid level of the gas-liquid separator 2 to prevent cross-pressure. The non-condensable gas is sent to the tail gas treatment system through the system pressure regulating valve 25. The three-phase separator 5 monitors the liquid level and interface of the water phase and the oil phase through the online interface meter 21 and the online liquid level meter 22 to prevent the water phase from entering the subsequent distillation section. The product oil phase is sent to the alkali washing tower 6 through the oil phase discharge valve 23, and the water phase is sent to the water phase buffer tank 11 through the water phase discharge valve 24.

[0030] The oil phase enters the bottom of the alkali washing tower 6 and is interlocked with the alkali adding self-adjusting valve group 10, the online pH detector 17, the alkali washing tower discharge valve 18, and the alkali washing tower desalted water self-adjusting valve 29 to complete the alkali washing tower 6 alkali addition, replacement, neutralization and other operations. The product is then sent to the water washing tower 7 for purification and pH fine-tuning. The normal operation of the water washing tower 7 is completed through the oil phase online pH detector 17, the water washing tower discharge valve 19, and the water washing tower water adding valve 20, and the qualified product is sent to the subsequent distillation section.

[0031] The wastewater in the water phase buffer tank 11 is put into daily operation through the water phase delivery pump 12, the online water phase pH detector 13, the desalted water self-regulating valve 14, and the water phase buffer tank alkali adding self-regulating valve 16, and finally the qualified wastewater is sent to the sewage treatment section.

[0032] The specific operation process of an automatic control method for acidity and alkalinity in the process of preparing durene by alkylation is as follows:

[0033] a. The specific operation of cooling the reaction product under high temperature state is as follows: the temperature of the reaction product can reach 420℃, and after heat exchange between the reaction inlet and outlet materials, it is still 220℃. Increase the by-product steam of the steam generator by 0.5Mpa, and at the same time reduce the temperature to 180-195℃. The by-product steam can be used for heating the alkali washing tower 6 and the water washing tower 7, and the surplus low-pressure steam is sent to the by-product low-pressure steam pipeline network.

[0034] b. The specific operation of separation and cooling in gas-liquid separator 2 is as follows: the reaction product after cooling enters gas-liquid separator 2 for gas-liquid separation, the non-condensable gas after by-product steam is further cooled and condensed by circulating water cooling, and the liquid phase is cooled by air cooler. Since durene has a melting point of 72°C and a low crystallization point, the lower the temperature, the easier it is to crystallize. The air cooler can control the temperature at 60-70°C to prevent the large cooling range of water cooling from causing crystallization to block the pipeline equipment.

[0035] c. The specific operation of the organic acid neutralization reaction is as follows: the reaction product after gas-liquid separation is further subjected to three-phase separation, the main product oil phase is passed through the alkali washing tower 6 for organic acid neutralization, the water washing tower 7 is used to wash and extract organic salts and other impurities, the pH value of the product is adjusted to neutral, and 32% NaOH alkali solution is sent to the alkali washing tower 6, and desalted water is added for dilution. After dilution, the concentration of the alkali solution in the tower is not higher than 0.01%, and the pH value is less than 11.4.

[0036] d. The three-phase separator 5, alkali washing tower 6 and water washing tower 7 are all equipped with pH online analyzers. The working status of the alkali washing tower 6 and water washing tower 7 are monitored through online instruments, and timely replacement is carried out to ensure the smooth operation and controllability of the neutralization system. Automatic adjustment is achieved with the self-adjusting valve group to reduce the influence of human factors.

[0037] In the method of the present invention, online instruments and self-adjusting valves are fully adopted to realize automatic control, including the automatic adjustment and control of liquid level, pressure and temperature at various locations, and alkali solution and pH adjustment from the discharge of materials from the gas-liquid separator 2 to the entry of products into the downstream process.

[0038] In steps a, b, c and d, the heat from the top of the trimethylol tower is continuously recovered through the durene tower reboiler and the steam generator, and the trimethylol liquid temperature after condensation by the steam generator is between 160° C. and 175° C., and can be used as circulating trimethylol as a raw material and returned to the buffer tank, raising the trimethylol feed of the reaction system to 100° C., saving the load of the electric heater, and being reused.

[0039] The automatic control in the method of the present invention involves:

[0040] ① The steam generator by-product steam control mainly includes a steam regulating valve 26 to control the steam generator pressure and the by-product steam volume.

[0041] ② The outlet discharge valve of the gas-liquid separator 2 is interlocked with the online liquid level meter 22 to automatically control the liquid level.

[0042] ③ The load adjustment of the air cooler is adjusted in real time by the feedback of the online thermometer 27 at the outlet of the air cooler, which can avoid the high load operation of the air cooler due to improper adjustment.

[0043] ④ The three-phase separator 5 can regulate the entire system, including the pre-reaction section, through the gas phase outlet system pressure regulating valve 25. The oil phase and water phase interface are controlled by the online interface meter 21 and the liquid level oil phase discharge valve 23, and the liquid level is controlled by the online liquid level meter 22 and the water phase discharge valve 24 to achieve cascade automatic control.

[0044] ⑤ The oil phase of the final product enters the alkali washing tower 6 for organic acid neutralization, and is washed by the water washing tower 7. After adjusting to pH 6.5-7.5, it is sent to the subsequent distillation section. For the alkali washing tower 6 sewage discharge and replacement, when the value measured by the online pH detector 17 is lower than 7.5, the alkali adding self-regulating valve group 10, the alkali washing tower 6 water adding valve and the alkali washing tower 6 discharge valve are opened to replace the alkali solution in the tower. After the alkali solution online flow meter 9 adds 60L cumulatively, the interlocking alkali adding self-regulating valve group 10 is closed, and the alkali washing tower 6 desalted water self-regulating valve 14 uses the 0.8MPa pressure of the desalted water network to add 3.5m of desalted water. 3 , control the sodium hydroxide concentration in the alkali washing tower 6 to be no higher than 0.01% and the pH to be no higher than 11.

[0045] ⑥ The alkali solution buffer tank 8 is placed at a high point and alkali solution is added by gravity flow without setting up a power system.

[0046] ⑦ The frequency and amount of water replacement in water washing tower 7 are interlocked and adjusted through the oil phase online pH detector 15 and the water adding valve and discharge valve of water washing tower 7. When the reading range of the oil phase online pH detector 15 exceeds 6.5-7.5, the water adding valve and discharge valve of water washing tower 7 are interlocked and adjusted and opened at the same time to replace water washing tower 7; at the same time, the water adding, drainage and liquid level are designed to operate in cascade to prevent the liquid level from being too low or too high.

[0047] ⑧Alkali washing tower 6 and water washing tower 7 are both equipped with low-pressure steam heating devices, which are controlled by steam self-regulating valves to ensure that the temperature in the tower is between 60-80°C. The low-pressure steam comes from the by-product steam of the reaction product steam generator.

[0048] ⑨ The pH of the wastewater in the water phase buffer tank 11 is adjusted through the online water phase pH detector 13, the desalted water self-adjusting valve 14, and the alkali adding self-adjusting valve of the water phase buffer tank 11. When the displayed value is lower than 7.5, the alkali adding self-adjusting valve of the water phase buffer tank 11 is opened to add an appropriate amount of alkali solution for adjustment. When the pH value is greater than 7.5, the desalted water self-adjusting valve 14 is opened to add pure water to dilute and reduce the alkalinity of the wastewater.

[0049] ⑩ The above control process adopts a predictive control scheme that is different from PID control. It has four basic characteristics: prediction model, feedback correction, rolling optimization, and reference trajectory. Because the pH value of the system changes differently, predictive control is adopted as the optimal control strategy.

[0050] like Figure 2 As shown, the set value is between the pH set value of 6.5-7.5. In the predictive control, the reference trajectory takes into account the dynamic nature of the process. In order to avoid a sharp change in input and output during the process, resulting in excessive pH and liquid level in the alkali washing tower 6 and the water washing tower 7, it is necessary to reach the set value along a gentle curve; the optimization calculation is performed online, and through a specific sampling time, dynamic optimization is continuously performed for each adjacent sampling time, which belongs to a local optimization index; the online correction compares the output measurement value y(k) and the valve opening with the model's estimated value ym(k), and makes corrections; the prediction model is mainly an algorithm using a pulse response model, which is obtained by calculating various related parameters. The above control method can realize the addition and discharge of materials in the alkali washing tower 6 and the water washing tower 7, thereby realizing automatic adjustment control.

[0051] Therefore, the present invention adopts the above-mentioned method for automatically controlling the acidity and alkalinity of the alkylation process for producing durenyl, improves the overall pH value of the alkylation process for producing durenyl, slows down the corrosion of the acidic working fluid on the pipelines of the reaction system equipment, and can also utilize the waste heat of the reaction product to produce part of the steam by-product, so as to adjust the pH value of the wastewater in advance and allow it to directly enter the water treatment biochemical pool for treatment, thereby extending the service life of the production device.

[0052] Finally, it should be noted that the above embodiments are only used to illustrate the technical solution of the present invention rather than to limit it. Although the present invention has been described in detail with reference to the preferred embodiments, those skilled in the art should understand that they can still modify or replace the technical solution of the present invention with equivalents, and these modifications or equivalent replacements cannot cause the modified technical solution to deviate from the spirit and scope of the technical solution of the present invention.

Claims

1. A method for automatically controlling the acidity and alkalinity of durene in an alkylation process, characterized in that: The steps include: The high-temperature reaction products generated during the alkylation process to produce durene are cooled, and part of the steam produced as a by-product of the steam generator is used to effectively utilize the waste heat, and then separated and cooled by a gas-liquid separator. After cooling by an air cooler, they enter a three-phase separator for gas, water and oil separation. The gas phase is de-heated and incinerated in an oxidation furnace, and the water phase is sent to the methanol recovery section to recover methanol and water treatment. The oil phase first enters the alkali washing tower for organic acid neutralization reaction, and then passes through the water washing tower to extract and dissolve the reaction salt product and a small amount of unreacted organic acid. The treated oil phase product is sent to the distillation section for the next step of distillation separation. The alkali washing tower and the water washing tower are regularly replaced and replaced according to the operating conditions.

2. The method for automatically controlling the acidity and alkalinity of durene production by alkylation according to claim 1, characterized in that: The specific operation of cooling the reaction product under high temperature state is as follows: the temperature of the reaction product is 420℃, and after heat exchange between the reaction inlet and outlet materials, it still reaches 220℃, and the by-product steam of the steam generator is increased to 0.5Mpa, and the temperature is reduced to 180-195℃ at the same time. The by-product steam can be used for heating the alkali washing tower and the water washing tower, and the surplus low-pressure steam is sent to the by-product low-pressure steam pipeline network.

3. The method for automatically controlling the acidity and alkalinity of durene production by alkylation according to claim 1, characterized in that: The specific operation of separation and cooling in the gas-liquid separator is as follows: the reaction product after cooling enters the gas-liquid separator for gas-liquid separation, the non-condensable gas after the by-product steam is further cooled and condensed by circulating water cooling, and the liquid phase is cooled by an air cooler.

4. The method for automatically controlling the acidity and alkalinity of durene production by alkylation according to claim 1, characterized in that: The specific operation of the organic acid neutralization reaction is as follows: the reaction product after gas-liquid separation continues to be separated into three phases, the main product oil phase is passed through the alkali washing tower for organic acid neutralization, the water washing tower washes and extracts impurities, the product pH is adjusted to neutral, and 32% NaOH alkali solution is sent to the alkali washing tower, and desalted water is added for dilution. After dilution, the alkali solution concentration in the tower is not higher than 0.01%, and the pH value is less than 11.

4.

5. The method for automatically controlling the acidity and alkalinity of durene in the alkylation process according to claim 1, characterized in that: The three-phase separator, alkali washing tower and water washing tower are all equipped with pH online analyzers. The working status of the alkali washing tower and water washing tower are monitored through online instruments, and timely replacement is carried out to ensure the smooth operation and controllability of the neutralization system. Automatic adjustment is achieved with the self-adjusting valve group to reduce the impact of human factors.

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