Hydrocarbonylation reaction optimization method for isopropylbenzene process preparation
By accurately controlling the parameters of hydrocarbonization reaction in the isopropyl benzene process and optimizing the preparation of isopropyl benzene process, the problems of high purity and energy consumption of isopropyl benzene products are solved, and efficient production and market competitiveness are achieved.
Patent Information
- Application Number
- CN202411255524.5
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2024-09-09
- Publication Date
- 2024-12-13
AI Technical Summary
In the preparation of existing isopropyl benzene processes, it is difficult for the purity of isopropyl benzene products to meet the high-quality product indicators, which affects market competitiveness, has high energy consumption and high production costs.
By accurately controlling the mass ratio of benzene to propylene in the hydrocarbonization reaction system, the feed temperature of the catalyst bed, the circulation amount of the hydrocarbonization liquid in the hydrocarbonization reactor and the feed amount of the catalyst bed, the hydrocarbonization reaction conditions are optimized. Reduce the generation of by-products, reduce the difficulty of refining and purification, and improve product purity and production efficiency.
The purity of the isopropyl benzene products has been achieved to meet the excellent product index, reduce high-pressure steam consumption and circulating pump current, avoid excessive or low temperature rise of the catalyst bed, and improve market competitiveness and production efficiency.
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Abstract
Description
Technical Field
[0001] The invention relates to an alkylation reaction optimization method for preparing cumene by process, and belongs to the technical field of chemical industry. Background Art
[0002] Cumene is produced using benzene and propylene as the main raw materials using the American Mobil / Badger cumene technology.
[0003] The preparation process of cumene mainly consists of four parts: the first part is the raw material processing system, which is to subject benzene and propylene to secondary pretreatment to graded removal of basic nitrogen compounds and non-alkaline nitrogen compounds in benzene, as well as sulfides, arsenic, phosphorus, water and total nitrogen in propylene, which are impurities that are toxic to the catalyst; the second part is the hydrocarbonization reaction system, which synthesizes cumene from benzene and propylene, and a small part of the cumene is further hydrocarbonized to form polyisopropylbenzenes. The hydrocarbonization reaction is an exothermic reaction, and the reaction temperature of the hydrocarbonization reactor is controlled by an external circulation cooling system; the third part is the dehydrogenation reaction system, which reacts polyisopropylbenzenes with benzene to form cumene. The dehydrogenation reaction is a constant temperature reaction, and the dehydrogenation reactor is a single-bed reactor; the fourth part is the distillation system, which recovers unreacted benzene through a benzene tower and returns it to the reactor, outputs cumene as a product, and recovers polyisopropylbenzenes for dehydrogenation.
[0004] Cumene is the main product of cumene plant, which is divided into quality grades. Superior cumene can bring better economic benefits. As a superior cumene, the main indicators are purity ≥ 99.92%, other benzene ≤ 10ppm, butylbenzene ≤ 200ppm, diisopropylbenzene ≤ 20ppm, ethylbenzene ≤ 100ppm, and n-propylbenzene ≤ 300ppm.
[0005] In the existing technology, when preparing isopropylbenzene products, the purity of the isopropylbenzene products cannot reach that of high-quality products, and the reaction degree of the hydrocarbonization reactor is the main factor affecting the isopropylbenzene products. Therefore, the present invention provides an optimization method for the hydrocarbonization reaction of isopropylbenzene process preparation by studying the operating parameters of the hydrocarbonization reactor. Under the premise of ensuring that the product is of high quality, the production cost of the product is reduced and the market competitiveness of the product is improved. Summary of the invention
[0006] In order to solve at least one problem existing in the above-mentioned prior art, the present invention provides a method for optimizing the hydrocarbonization reaction of isopropylbenzene process preparation, which can make the purity of the isopropylbenzene product reach the high-quality product index, improve production efficiency, reduce energy consumption and enhance market competitiveness.
[0007] In order to achieve the above-mentioned object, the present invention adopts the following technical scheme: a method for optimizing the alkylation reaction of isopropylbenzene process preparation, the alkylation reaction system of isopropylbenzene process preparation comprises four parts: a raw material processing system, an alkylation reaction system, a reverse alkylation reaction system and a finished product refining system, the alkylation reaction system: the high-purity and dry fresh benzene and fresh propylene subjected to secondary pretreatment are introduced into the top of the alkylation reactor, the mass flow rate of the benzene feed and the mass flow rate of the total propylene feed are measured, and then the benzene and propylene are reacted through the catalyst beds of each stage: the first stage propylene is mixed with benzene and the alkylation liquid circulating outside the alkylation reactor and then enters the first stage catalyst bed for reaction, and the second, third and fourth stage propylene is mixed with the alkylation liquid circulating outside the alkylation reactor and then enters the catalyst beds of each stage for reaction;
[0008] The mass ratio of benzene to propylene is controlled to be 3.6:1 to 3.7:1;
[0009] Control the circulation rate of hydrocarbonation liquid outside the hydrocarbonation reactor to 290-310 t / h;
[0010] Control the feed amount (load) of each catalyst bed layer to 80% load to 100% load;
[0011] The feed temperature of each catalyst bed was controlled at 127-129°C.
[0012] Preferably, the mass ratio of benzene to propylene is 3.6:1 to 3.65:1.
[0013] Preferably, the mass ratio of benzene to propylene is 3.65:1.
[0014] Preferably, the circulation rate of the hydrocarbonation liquid circulating outside the hydrocarbonation reactor is 290-305 t / h.
[0015] Preferably, the circulation rate of the hydrocarbonation liquid circulating outside the hydrocarbonation reactor is 290 t / h.
[0016] Preferably, the feed amount (load) of each catalyst bed layer is 80% load to 95% load.
[0017] Preferably, the feed amount (load) of each catalyst bed layer is 90% load.
[0018] Preferably, the feed temperature of each catalyst bed is 127-129°C.
[0019] Preferably, the feed temperature of each catalyst bed is 128°C.
[0020] Beneficial effects of the present invention: The hydrocarbonization reaction optimization method for preparing cumene by the process of the present invention can accurately control the mass ratio of benzene to propylene, the feed temperature of the catalyst bed, the circulation amount of hydrocarbonation liquid circulating outside the hydrocarbonation reactor and the feed amount (load) of the catalyst bed in the hydrocarbonation reaction system. At this time, the by-products generated by the hydrocarbonation reaction will be greatly reduced, thereby reducing the difficulty of refining and purifying the final cumene product, so that the purity of the cumene product reaches the first-class product index, and the market competitiveness is improved; the hydrocarbonization reaction optimization method for preparing cumene by the process of the present invention not only ensures that the cumene product reaches the first-class product index, but also reduces the consumption of high-pressure steam by accurately controlling the mass ratio of benzene to propylene; the present invention can also reduce the phenomenon that impurities in the raw material are prone to propylene polymerization by accurately controlling the feed temperature of the catalyst bed; the present invention can also reduce the current of the circulation pump by accurately controlling the circulation amount of hydrocarbonation liquid circulating outside the hydrocarbonation reactor; the present invention can avoid excessive or excessive low temperature rise of the catalyst bed by accurately controlling the feed amount (load) of the catalyst bed, thereby improving production efficiency. DETAILED DESCRIPTION
[0021] The following is a clear and complete description of the technical solutions in the implementation of the present invention. The described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in the field without making creative work are within the scope of protection of the present invention. If the specific conditions are not specified in the embodiments, they are carried out according to the normal conditions or the conditions recommended by the manufacturer. If the manufacturer is not specified for the reagents, instruments, and components used, they are all conventional products that can be purchased commercially.
[0022] The cumene preparation process of the present invention comprises four parts: a raw material processing system, an alkylation reaction system, a reverse alkylation reaction system, and a finished product refining system;
[0023] (1) Raw material processing system: fresh benzene and propylene are respectively subjected to secondary pretreatment by passing through an upstream device equipped with an adsorbent treatment bed and a distillation tower to grade and remove basic nitrogen compounds and non-basic nitrogen compounds in benzene, as well as sulfides, arsenic, phosphorus, water and total nitrogen in propylene, which are impurities that are poisonous to the catalyst, and control the moisture content in the reactor feed to ≤20 mg / kg, the sulfur compound content in the benzene feed to ≤3 ppm, the nitrogen compound content in the benzene feed to ≤1 ppm; the sulfur content in the propylene feed to ≤3 ppm; and the arsenic + phosphorus content in the propylene to ≤0.03 ppm;
[0024] (2) Hydrocarbonation reaction system: high-purity and dry fresh benzene (benzene content is 95%) and fresh propylene after secondary pretreatment are introduced into the top of the hydrocarbonation reactor, and the mass flow rate of the benzene feed and the mass flow rate of the total propylene feed are measured. Then, the benzene and propylene are reacted in the catalyst beds of each stage: the first stage propylene is mixed with benzene and the hydrocarbonation liquid circulating outside the hydrocarbonation reactor and then enters the first stage catalyst bed for reaction; the second, third and fourth stages propylene are mixed with the hydrocarbonation liquid circulating outside the hydrocarbonation reactor and then enter the catalyst beds of each stage for reaction; the mass ratio of benzene to propylene, the feed temperature of each catalyst bed, the feed amount (load) of each catalyst bed, and the circulation amount of the hydrocarbonation liquid circulating outside the hydrocarbonation reactor are controlled;
[0025] Main reaction equation: C6H6(benzene)+CH3CH=CH2(propylene)→C6H5CH(CH3)2(isopropylbenzene);
[0026] (3) Dehydrogenation reaction system: diisopropylbenzene and triisopropylbenzene generated in the dehydrogenation reactor will undergo dehydrogenation reaction with benzene in the dehydrogenation reactor to generate isopropylbenzene. The mass flow rate of benzene entering the dehydrogenation reactor and the mass flow rate of circulating polyisopropylbenzene are measured, and the feed ratio of benzene to polyisopropylbenzene in the dehydrogenation reactor is controlled to be 1:1 and the temperature of the dehydrogenation reactor is adjusted to 180°C.
[0027] (4) Finished product refining system:
[0028] a. Benzene tower: The unreacted benzene in the hydrocarbonation liquid and the unreacted benzene in the dehydrocarbonation liquid are introduced into the benzene tower and heated by steam in the reboiler of the benzene tower kettle; the vapor of the top material is condensed in the condenser at the top of the benzene tower, and the recovered benzene product is used as the side-line fraction, and enters the dry benzene tank from the side-line discharge plate for drying, and then is sent to the benzene secondary pretreatment device by the dry benzene circulation pump for further pretreatment, and then enters the hydrocarbonation reactor and the dehydrocarbonation reactor; the isopropylbenzene, polyisopropylbenzene and other heavy components at the bottom of the benzene tower are transported to the isopropylbenzene tower by the bottom pump; the discharge flow rate of the benzene tower bottom is regulated by the bottom liquid level; the dry benzene reflux liquid is sent back to the lower part of the tower (below the side-line discharge plate) by the dry benzene circulation pump; the fresh benzene is sent to the benzene primary pretreatment device by the benzene delivery pump of the benzene feed buffer tank for pretreatment and then enters the benzene tower for dehydration, and the replenishment amount of fresh benzene is determined according to the liquid level of the dry benzene tank, and then enters from the top of the benzene tower.
[0029] b Isopropylbenzene tower: The cumene, polyisopropylbenzenes and other heavy components at the bottom of the benzene tower are transported to the cumene tower by the bottom pump and enter the cumene tower kettle reboiler. The material vapor at the top of the cumene tower is condensed in the top condenser. The cumene product is first cooled in the (cumene product / circulating benzene) heat exchanger and then cooled in the cumene finished product cooler. The cumene product is recovered in the reflux tank of the cumene tower and then transported from the tower side to the outside through the cumene tower product pump. Diisopropylbenzene and heavy components are recovered at the bottom of the cumene tower.
[0030] c. Polyisopropylbenzene tower: The polyisopropylbenzene collected from the side of the polyisopropylbenzene tower enters the dealkylation reactor for dealkylation reaction and is converted into isopropylbenzene; the material vapor entering the top of the tower is condensed in the air cooler at the top of the tower, flows into the reflux tank of the polyisopropylbenzene tower for collection, and the light components in the collected liquid are separated, and then the light components are sent to the heavy aromatics tank after being cooled by the polyisopropylbenzene tower reflux pump through the residual liquid and aromatics cooler; the residual liquid at the bottom of the polyisopropylbenzene tower is pumped out by the polyisopropylbenzene tower kettle pump under direct flow regulation, and sent to the heavy aromatics tank after being cooled by the residual liquid and aromatics cooler.
[0031] 1. The influence of the mass ratio of benzene to propylene on the production of cumene
[0032] A method for optimizing the alkylation reaction of cumene process preparation:
[0033] Hydrocarbonization reaction system: high-purity and dry fresh benzene (benzene content is 95%) and fresh propylene after secondary pretreatment are introduced into the top of the hydrocarbonization reactor, the mass flow rate of the benzene feed and the mass flow rate of the total propylene feed are measured, and the mass ratio of benzene to propylene is controlled, as shown in Table 1, and then benzene and propylene are reacted through catalyst beds of various levels: the first stage propylene is mixed with benzene and hydrocarbonated liquid circulating outside the hydrocarbonization reactor and then enters the first stage catalyst bed for reaction, the second, third and fourth stages propylene is mixed with hydrocarbonated liquid circulating outside the hydrocarbonization reactor and then enters each stage catalyst bed for reaction, the circulation amount of hydrocarbonated liquid circulating outside the hydrocarbonization reactor is controlled to be 290 t / h, the feed amount (load) of each stage catalyst bed is controlled to be 80% load, and the feed temperature of each stage catalyst bed is controlled to be 128° C.;
[0034] The remaining three parts are prepared according to the above-mentioned existing cumene process; finally, the content and impurities of the collected cumene product are measured, and the results are shown in Table 1.
[0035] Table 1 Effect of the mass ratio of benzene to propylene on cumene production
[0036]
[0037]
[0038] It can be seen from Table 1 above that in the alkylation reaction, the mass ratio of benzene to propylene has a great influence on the cumene product: if the mass ratio of benzene to propylene is too low, the content of diisopropylbenzene, ethylbenzene and n-propylbenzene in the cumene product is high, resulting in the cumene product not meeting the premium product index; if the mass ratio of benzene to propylene is too high, although the impurity content in the cumene product does not change much, the excessive benzene requires more high-pressure steam in the subsequent distillation tower benzene tower to balance it; therefore, the mass ratio of benzene to propylene is within the range of 3.6:1 to 3.7:1, which can not only meet the premium product of the cumene product, but also reduce the high-pressure steam consumption; more preferably, the mass ratio of benzene to propylene is within the range of 3.6:1 to 3.65:1, and the high-pressure steam consumption can be reduced to 11 t / h, which greatly reduces the consumption of high-pressure steam; optimally, the mass ratio of benzene to propylene is 3.6:1, which ensures that the benzene product is a premium product while ensuring the lowest high-pressure steam consumption.
[0039] 2. Effect of the circulation rate of hydrocarbonation liquid outside the hydrocarbonation reactor on the production of cumene
[0040] A method for optimizing the alkylation reaction of cumene process preparation:
[0041] Hydrocarbonization reaction system: high-purity and dry fresh benzene (benzene content is 95%) and fresh propylene after secondary pretreatment are introduced into the top of the hydrocarbonization reactor, and the mass flow rate of the benzene feed and the mass flow rate of the total propylene feed are measured to control the mass ratio of benzene to propylene to be 3.6:1, the mass flow rate of the benzene feed to be 49.3 t / h and the mass flow rate of the total propylene feed to be 13 t / h. Then benzene and propylene are reacted through catalyst beds of various levels: the first stage propylene is mixed with benzene and the hydrocarbonation liquid circulating outside the hydrocarbonization reactor and then enters the first stage catalyst bed for reaction; the second, third and fourth stages propylene are mixed with the hydrocarbonation liquid circulating outside the hydrocarbonization reactor and then enter each stage catalyst bed for reaction; the circulation amount of the hydrocarbonation liquid circulating outside the hydrocarbonization reactor is controlled as shown in Table 2, the feed amount (load) of each stage catalyst bed is controlled to be 80% load, and the feed temperature of each stage catalyst bed is controlled to be 128° C.;
[0042] The remaining three parts are prepared according to the above-mentioned existing isopropylbenzene process; finally, the content and impurities of the collected isopropylbenzene product are measured, and the results are shown in Table 2.
[0043] Table 2 Effect of the circulation rate of hydrocarbonation liquid outside the hydrocarbonation reactor on the production of cumene
[0044]
[0045] It can be seen from Table 2 that in the hydrocarbonation reaction, the circulation rate of hydrocarbonation liquid outside the hydrocarbonation reactor also has a great influence on the cumene product: as the circulation rate of hydrocarbonation liquid outside the hydrocarbonation reactor increases, the temperature rise of each catalyst bed layer will decrease. However, too low a circulation rate of hydrocarbonation liquid outside the hydrocarbonation reactor will result in the cumene product not meeting the premium quality index, and the content of n-propylbenzene is too high. If the circulation rate of hydrocarbonation liquid outside the hydrocarbonation reactor is too high, the impurity content in the cumene product will not change much, which will inevitably increase the load of the pump. Therefore, the circulation rate of hydrocarbonation liquid outside the hydrocarbonation reactor is controlled at 290-310 t / h, which can increase the temperature rise of each catalyst bed layer. The temperature rise is controlled at 9-12°C, which is an ideal state. It can not only meet the requirement that the isopropylbenzene product is of high quality, but also ensure that there is enough hydrocarbonation liquid circulation outside the hydrocarbonation reactor to remove heat, and the circulating pump current of the circulation amount is less than 260A; more preferably, the hydrocarbonation liquid circulation volume outside the hydrocarbonation reactor is controlled at 290-305t / h, while ensuring that the benzene product is of high quality and the temperature rise is relatively low, the circulating pump current of the circulation volume is less than 250A; optimally, the hydrocarbonation liquid circulation volume outside the hydrocarbonation reactor is controlled at 290t / h, while ensuring that the benzene product is of high quality and the temperature rise is relatively low, the circulating pump current is minimized.
[0046] 3. Effect of catalyst bed feed rate (load) on cumene production
[0047] A method for optimizing the alkylation reaction of cumene process preparation:
[0048] Hydrocarbonization reaction system: high-purity and dry fresh benzene (benzene content is 95%) and fresh propylene after secondary pretreatment are introduced into the top of the hydrocarbonization reactor, and the mass flow rate of the benzene feed and the mass flow rate of the total propylene feed are measured to control the mass ratio of benzene to propylene to be 3.6:1, the mass flow rate of the benzene feed to be 49.3 t / h and the mass flow rate of the total propylene feed to be 13 t / h. Then benzene and propylene are reacted through catalyst beds of various levels: the first stage propylene is mixed with benzene and hydrocarbonation liquid circulating outside the hydrocarbonization reactor and then enters the first stage catalyst bed for reaction; the second, third and fourth stages propylene are mixed with hydrocarbonation liquid circulating outside the hydrocarbonization reactor and then enter each stage catalyst bed for reaction; the circulation amount of hydrocarbonation liquid circulating outside the hydrocarbonization reactor is controlled to be 290 H / T, the feed amount (load) of each stage catalyst bed is controlled as shown in Table 3, and the feed temperature of each stage catalyst bed is controlled to be 128° C.
[0049] The remaining three parts are prepared according to the above-mentioned existing isopropylbenzene process; finally, the content and impurities of the collected isopropylbenzene product are measured, and the results are shown in Table 3.
[0050] Table 3 Effect of catalyst bed feed rate (load) on cumene production
[0051]
[0052] It can be seen from Table 3 that in the hydrocarbonation reaction, the feed amount (load) of the catalyst bed also has a great influence on the cumene product: different loads correspond to different feed amounts. The higher the load, that is, the higher the feed amount, the more intense the hydrocarbonation reaction is and the higher the temperature rise of the catalyst bed is. If the load is too low, although the purity of the cumene product meets the index of high-quality products, the feed amount is too low, the production time will be extended, and the production efficiency will be reduced. If the load is too high, the reaction will be more intense, resulting in the cumene product not meeting the index of high-quality products and the catalyst bed temperature rise is too high. Therefore, the feed amount (load) of the catalyst bed is 80% load to 100% load, and the catalyst bed temperature rise reaches the ideal state, 9 to 12° C., while ensuring that the cumene product meets the high-quality products. More preferably, the feed amount (load) of the catalyst bed is 80% load to 95% load, which can not only make it easier to control the temperature rise of the catalyst bed, but also ensure that the cumene product meets the high-quality products and improve production efficiency.
[0053] 4. Effect of catalyst bed feed temperature on cumene production
[0054] A method for optimizing the alkylation reaction of cumene process preparation:
[0055] Hydrocarbonization reaction system: high-purity and dry fresh benzene (benzene content is 95%) and fresh propylene after secondary pretreatment are introduced into the top of the hydrocarbonization reactor, and the mass flow rate of the benzene feed and the mass flow rate of the total propylene feed are measured to control the mass ratio of benzene to propylene to be 3.6:1, the mass flow rate of the benzene feed to be 49.3 t / h and the mass flow rate of the propylene feed to be 13 t / h. Then, benzene and propylene react through catalyst beds of various levels: the first stage propylene is mixed with benzene and the hydrocarbonation liquid circulating outside the hydrocarbonization reactor and then enters the first stage catalyst bed for reaction; the second, third and fourth stages propylene are mixed with the hydrocarbonation liquid circulating outside the hydrocarbonization reactor and then enter each stage catalyst bed for reaction; the circulation amount of the hydrocarbonation liquid circulating outside the hydrocarbonization reactor is controlled to be 290 H / T, the feed amount (load) of each stage catalyst bed is controlled to be 90% load, and the feed temperature of each stage catalyst bed is controlled as shown in Table 4;
[0056] The remaining three parts are prepared according to the above-mentioned existing isopropylbenzene process; finally, the content and impurities of the collected isopropylbenzene product are measured, and the results are shown in Table 4.
[0057] Table 4 Effect of catalyst bed feed temperature on cumene production
[0058]
[0059] It can be seen from Table 4 that in the hydrocarbonation reaction, the feed temperature of the catalyst bed also has a great influence on the cumene product: when the feed temperature of the catalyst bed is high, cumene isomerizes to normal propylbenzene, the normal propylbenzene in the hydrocarbonation liquid increases, the normal propylbenzene content in the cumene product increases, and the contents of other impurities in the cumene product, such as butylbenzene and diisopropylbenzene, also exceed the standard, resulting in the cumene product not meeting the high-quality index; when the feed temperature of the catalyst bed is too low, although the cumene product reaches the high-quality index, the impurities in the raw material are prone to propylene polymerization, which increases the non-aromatic content of the system and reduces the conversion rate of propylene; therefore, the feed temperature of the catalyst bed is 127-129° C. Since the temperature rise in each catalyst bed is quite small, the average bed temperature in the reactor is actually controlled by the feed temperature of each bed. On the premise of ensuring the high-quality of the cumene product, the non-aromatic content of the system is less than 26%, and the service life of the catalyst can be extended; more preferably, the feed temperature of the catalyst bed is 128° C.
[0060] It will be apparent to those skilled in the art that the present invention is not limited to the details of the exemplary embodiments described above, and that the present invention can be implemented in other specific forms without departing from the spirit and essential features of the present invention. Therefore, the embodiments should be considered exemplary and non-restrictive in all respects, and the scope of the present invention is defined by the appended claims rather than the above description, and it is intended that all changes falling within the meaning and scope of the equivalent elements of the claims be included in the present invention.
[0061] In addition, it should be understood that although the present specification is described according to implementation modes, not every implementation mode contains only one independent technical solution. This description of the specification is only for the sake of clarity. Those skilled in the art should regard the specification as a whole. The technical solutions in each embodiment may also be appropriately combined to form other implementation modes that can be understood by those skilled in the art.
Claims
1. A method for optimizing the alkylation reaction of cumene process preparation, the cumene process preparation comprises four parts: a raw material processing system, an alkylation reaction system, a reverse alkylation reaction system, and a finished product refining system, characterized in that: The alkylation reaction system comprises: introducing high-purity and dry fresh benzene and fresh propylene subjected to secondary pretreatment into the top of the alkylation reactor, measuring the mass flow rate of the benzene feed and the mass flow rate of the total propylene feed, and then reacting the benzene and propylene through the catalyst beds of various stages: the first-stage propylene is mixed with benzene and the alkylation liquid circulating outside the alkylation reactor and then enters the first-stage catalyst bed for reaction; the second, third and fourth-stage propylene is mixed with the alkylation liquid circulating outside the alkylation reactor and then enters the catalyst beds of various stages for reaction; The mass ratio of benzene to propylene is controlled to be 3.6:1 to 3.7:1; Control the circulation rate of hydrocarbonation liquid outside the hydrocarbonation reactor to 290-310 t / h; Control the feed amount of each catalyst bed layer to 80% load ~ 100% load; The feed temperature of each catalyst bed was controlled at 127-129°C.
2. The method for optimizing the alkylation reaction of cumene according to claim 1, characterized in that: The mass ratio of benzene to propylene is 3.6:1 to 3.65:
1.
3. The method for optimizing the alkylation reaction of cumene according to claim 1 or 2, characterized in that: The mass ratio of benzene to propylene is 3.65:
1.
4. The method for optimizing the alkylation reaction of cumene according to claim 1, characterized in that: The circulation rate of the hydrocarbonation liquid circulating outside the hydrocarbonation reactor is 290-305 t / h.
5. The method for optimizing the alkylation reaction of cumene preparation according to claim 1 or 4, characterized in that: The circulation rate of the hydrocarbonation liquid circulating outside the hydrocarbonation reactor is 290 t / h.
6. The method for optimizing the alkylation reaction of cumene production according to claim 1, characterized in that: The feed amount of each catalyst bed layer is 80% load to 95% load.
7. The method for optimizing the alkylation reaction of cumene production according to claim 1 or 6, characterized in that: The feed amount of each catalyst bed layer is 90% load.
8. The method for optimizing the alkylation reaction of cumene production according to claim 1, characterized in that: The feed temperature of each catalyst bed layer is 128°C.