CN115636714A - Method and system for producing pseudocumene and durene through alkylation - Google Patents
Method and system for producing pseudocumene and durene through alkylation Download PDFInfo
- Publication number
- CN115636714A CN115636714A CN202211336028.3A CN202211336028A CN115636714A CN 115636714 A CN115636714 A CN 115636714A CN 202211336028 A CN202211336028 A CN 202211336028A CN 115636714 A CN115636714 A CN 115636714A
- Authority
- CN
- China
- Prior art keywords
- methanol
- durene
- pseudocumene
- molecular sieve
- alkylation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to the technical field of aromatic hydrocarbon production, and relates to a method and a system for producing pseudocumene and durene through alkylation. Taking light aromatic hydrocarbon and methanol as raw materials, and carrying out alkylation reaction under the catalysis of a modified molecular sieve catalyst and at the temperature of 250-600 ℃; the material after the alkylation reaction continues to carry out alkylation reaction again under the catalysis of the modified molecular sieve catalyst and the condition of 250-600 ℃; the modified molecular sieve catalyst is composed of a molecular sieve and a metal oxide loaded in the molecular sieve, wherein the molecular sieve is one or more of HY, H beta, IM-5, NU87, EU-1 and mordenite, and the metal in the metal oxide is one or more of Mg, cu, la, zn and Mo. The invention solves the technical problems of low content of the components of the pseudocumene and the durene, difficult separation and the like in the industrial separation method by directly producing the pseudocumene and the durene.
Description
Technical Field
The invention belongs to the technical field of aromatic hydrocarbon production, and relates to a method and a system for producing pseudocumene and durene through alkylation.
Background
The information in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
According to the research of the inventor, the most common production method of the pseudocumene, the durene and the like in the industry at present is mainly a C9+ heavy aromatic hydrocarbon separation method, for example, a reforming byproduct is recycled, but the contents of components such as methyl ethyl benzene, the pseudocumene, the hemimellitene, the pseudodurene and the like in the reforming byproduct are more, and the boiling points of partial components are very close, so that the product purity is not high and the separation cost is extremely high when the separation method is used for separation; and then, for example, crude benzene and crude methanol are used as raw materials, and are subjected to acid washing, hydrogenation pretreatment, alkylation reaction, rectification, crystallization separation and isomerization reaction to produce p-xylene, o-xylene and unsym-trimethylbenzene, so that the production cost of the p-xylene, the o-xylene and the unsym-trimethylbenzene is reduced, the production of aromatic hydrocarbon products by a non-petroleum raw material route is realized, but the method mainly produces the xylene, has less unsym-trimethylbenzene amount and cannot produce high-end fine durene and other products.
Disclosure of Invention
In order to solve the technical problems of low content of components of pseudocumene and durene, difficult separation and the like existing in an industrial separation method, the invention aims to provide a method and a system for producing pseudocumene and durene through alkylation.
In order to achieve the purpose, the technical scheme of the invention is as follows:
on the one hand, the alkylation production method of pseudocumene and durene takes light aromatic hydrocarbon and methanol as raw materials, and the alkylation reaction is carried out under the catalytic action of a modified molecular sieve catalyst and the condition of 250-600 ℃; the material after the alkylation reaction continues to carry out alkylation reaction again under the catalysis of the modified molecular sieve catalyst and the condition of 250-600 ℃;
wherein the light aromatic hydrocarbon is one or more of benzene, toluene, o-xylene, m-xylene and p-xylene;
the modified molecular sieve catalyst is composed of a molecular sieve and a metal oxide loaded in the molecular sieve, wherein the molecular sieve is one or more of HY, H beta, IM-5, NU87, EU-1 and mordenite, and the metal in the metal oxide is one or more of Mg, cu, la, zn and Mo.
The method for directly obtaining the pseudocumene and the durene by chemical synthesis can avoid the difficulty of preparing the pseudocumene and the durene by an industrial separation method. In order to synthesize pseudocumene and durene, proper raw materials are adopted, and light aromatic hydrocarbon and methanol which are the most conventional chemical raw materials in industrial production are adopted in the invention. Secondly, a proper catalyst is adopted to catalyze light aromatic hydrocarbon and methanol to carry out alkylation reaction to generate pseudocumene and durene, and research shows that the modified molecular sieve catalyst provided by the invention can be used for directly alkylating the light aromatic hydrocarbon and the methanol to obtain the pseudocumene and the durene. Thirdly, in order to avoid the problem of low content of target products in the synthesis process, the alkylation reaction is carried out by adopting material circulation after the alkylation reaction, and researches show that the alkylation reaction is carried out by material circulation after the alkylation reaction and the increase of the time of the alkylation reaction are not equivalent, the increase of the yield of the pseudocumene and the yield of the durene are difficult to realize by only increasing the time of the alkylation reaction, and the increase of the yield of the pseudocumene and the yield of the durene can be realized by carrying out the alkylation reaction on the material circulation after the alkylation reaction. Through the technical scheme, the pseudocumene and the durene can be directly obtained through chemical reaction, so that the technical problems of low pseudocumene and durene component content, difficult separation and the like in an industrial separation method are solved.
In another aspect, a system for the alkylation production of pseudocumene and durene is used to implement the above process, comprising:
a light aromatic hydrocarbon source for delivering light aromatic hydrocarbons to the reactor;
a methanol source for delivering methanol to the reactor;
the reactor is used for carrying out alkylation reaction on light aromatic hydrocarbon and methanol to produce pseudocumene and durene;
a product material circulation pipeline for conveying the material discharged from the reactor after the alkylation reaction back to the reactor;
the online detection device is arranged on the product material circulating pipeline and is used for monitoring the pseudocumene and the durene in the product material circulating pipeline;
and the product side extraction pipeline is connected with the product material circulation pipeline and is used for extracting the pseudocumene and the durene which meet the standard according to the detection result of the online detection device.
The invention has the beneficial effects that:
1. the invention adopts a light aromatic alkylation method to realize the production of pseudocumene and durene products, can realize the high content control of target products and has few by-products.
2. The invention adopts the modified molecular sieve catalyst to catalyze the alkylation reaction of light aromatic hydrocarbon and methanol, and realizes the improvement of the selectivity and the yield of the pseudocumene and the durene through the shape-selective catalysis of the catalyst.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention and together with the description serve to explain the invention and not to limit the invention.
FIG. 1 is a schematic diagram of a system for producing pseudocumene and durene by alkylation in an embodiment of the present invention;
1. a light aromatic hydrocarbon feed tank; 2. a methanol tank; 3. a light aromatic hydrocarbon feed pump; 4. a methanol feed pump; 5. a mixer; 6. a preheater; 7. a fixed bed reactor; 8. a cooler; 9. a three-phase separator; 10. an oil phase reflux pump; 11. online chromatography; 51. a backflow stop valve; 52. a first methanol stop valve; 53. a second methanol stop valve; 71. a first methanol sectional feeding stop valve; 72. a second methanol sectional feed stop valve; 73. a third methanol sectional feeding stop valve; 74. a first methanol staged feed flowmeter; 75. a second methanol staged feed flow meter; 76. a third methanol staged feed flow meter; 111. an oil phase reflux valve; 112. an oil phase outlet valve;
FIG. 2 is an infrared spectrum of the La/HY catalyst prepared in the examples of the present invention.
Detailed Description
It is to be understood that the following detailed description is exemplary and is intended to provide further explanation of the invention as claimed. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the invention. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
The invention provides a method and a system for producing pseudocumene and durene by alkylation, aiming at solving the problems of low content of pseudocumene and durene, difficult separation and the like in the existing industrial separation method for producing pseudocumene and durene.
The invention provides a typical implementation mode of a method for producing pseudocumene and durene by alkylation, which takes light aromatic hydrocarbon and methanol as raw materials to carry out alkylation reaction under the catalysis of a modified molecular sieve catalyst and the condition of 250-600 ℃; the material after the alkylation reaction continues to carry out alkylation reaction again under the catalysis of the modified molecular sieve catalyst and the condition of 250-600 ℃;
wherein the light aromatic hydrocarbon is one or more of benzene, toluene, o-xylene, m-xylene and p-xylene;
the modified molecular sieve catalyst is composed of a molecular sieve and a metal oxide loaded in the molecular sieve, wherein the molecular sieve is one or more of HY, H beta, IM-5, NU87, EU-1 and mordenite, and the metal in the metal oxide is one or more of Mg, cu, la, zn and Mo.
In some embodiments, the modified molecular sieve catalyst is prepared by: and (2) saturating and impregnating the metal salt water solution into the molecular sieve by adopting a saturation impregnation method, and drying and roasting the saturated and impregnated molecular sieve to obtain the modified molecular sieve catalyst. More specifically, in the saturated impregnation method, the saturated water absorption of the molecular sieve is firstly known, then a metal salt aqueous solution with a specific concentration is prepared according to the saturated water absorption, and then the molecular sieve is saturated and adsorbs the metal salt aqueous solution, so that the modified molecular sieve catalyst with a specific metal loading can be obtained. The drying temperature is 100-200 ℃. The drying time is 3-5 h. The roasting temperature is 450-550 ℃. The roasting time is 2-6 h.
In some embodiments, the molecular sieve is HY, the metal in the metal oxide is La; or the molecular sieve is H beta, and the metal in the metal oxide is Zn. Research shows that the catalyst has higher raw material conversion rate and higher selectivity of pseudocumene and durene, wherein when the molecular sieve is HY and the metal in the metal oxide is La, the selectivity of the pseudocumene and the selectivity of the durene are the highest.
In some embodiments, the light aromatic hydrocarbon is one or more of toluene, ortho-xylene, meta-xylene, and para-xylene. Under the condition, the method is more favorable for producing pseudocumene and durene.
In some embodiments, the molar ratio of light aromatic hydrocarbons to methanol is 1:5 to 5:1.
In some embodiments, the pressure of the alkylation reaction is from 0.5 to 2MPa.
In some embodiments, the total space velocity of the mass of the raw material liquid is 0.5-5 h -1 。
In some embodiments, the oil phase material and the gas phase material after the alkylation reaction are subjected to the alkylation reaction again under the catalysis of the modified molecular sieve catalyst and the temperature of 250-600 ℃. Discharging the obtained water phase material.
In some embodiments, methanol is replenished during the alkylation reaction. The research shows that: methanol is easy to react under the action of a catalyst to generate alkanes such as dimethyl ether, propane, butane and the like, so when the mixed solution of light aromatic hydrocarbon and methanol is fed, the methanol is quickly reacted in a short time when entering a reactor, and the light aromatic hydrocarbon is not completely converted, so that the methanol needs to be supplemented in the reaction process.
In another embodiment of the present invention, there is provided a system for producing pseudocumene and durene by alkylation, which is used for implementing the above method, comprising:
a light aromatic hydrocarbon source for delivering light aromatic hydrocarbons to the reactor;
a methanol source for delivering methanol to the reactor;
the reactor is used for carrying out alkylation reaction on light aromatic hydrocarbon and methanol to produce pseudocumene and durene;
a product material circulation pipeline for conveying the material discharged from the reactor after the alkylation reaction back to the reactor;
the online detection device is arranged on the product material circulating pipeline and is used for monitoring the pseudocumene and the durene in the product material circulating pipeline;
and the product side extraction pipeline is connected with the product material circulation pipeline and is used for extracting the pseudocumene and the durene which meet the standard according to the detection result of the online detection device.
In some embodiments, the reactor is a fixed bed reactor.
In some embodiments, the reactor is provided with several methanol feed inlets. The plurality of methanol feed inlets are arranged for methanol multi-section side feeding, so that methanol can be supplemented, and the amount of methanol which is added into the reactor can be controlled, so that the self side reaction of the methanol is avoided, more methanol is reacted with light aromatic hydrocarbon, the product content is improved, and the content of byproducts is reduced.
In one or more embodiments, the device comprises a mixer, wherein an outlet of the light aromatic hydrocarbon source is connected with the mixer, an outlet of the methanol source is simultaneously connected with a plurality of methanol feeding holes, and an outlet of the mixer is connected with a mixture inlet of the reactor. The arrangement is beneficial to pre-mixing the light aromatic hydrocarbon and the methanol, and improves the contact between the light aromatic hydrocarbon and the methanol.
In one or more embodiments, a preheater is included, the preheater being disposed between the mixer outlet and the mix inlet of the reactor. This setting can preheat the miscellaneous material of light arene and methyl alcohol, in the serialization production, can avoid the influence of the direct addition of the miscellaneous material of light arene and methyl alcohol to the temperature in the reactor to improve continuous production's stability.
In some embodiments, the reactor comprises a cooler and a three-phase separator, the product material circulation line comprises a gas phase circulation line and an oil phase circulation line, the material outlet of the reactor is sequentially connected with the cooler and the three-phase separator, the gas phase outlet of the three-phase separator is connected with the gas phase circulation line, and the oil phase outlet of the three-phase separator is connected with the oil phase circulation line.
In order to make the technical solution of the present invention more clearly understood by those skilled in the art, the technical solution of the present invention will be described in detail below with reference to specific examples and comparative examples.
The preparation method of the modified molecular sieve catalyst in the following examples comprises the following steps:
(1) HY, H beta, IM-5, NU87, EU-1, mordenite were tested for saturated water absorption.
(2) Weighing 300g of molecular sieve (carrier), calculating the water absorption capacity, and dissolving one or more metal nitrates of Mg, cu, la, zn, mo and the like into water with corresponding water absorption capacity.
(3) And (3) dipping the prepared corresponding nitrate solution onto a corresponding molecular sieve by adopting a saturated dipping method, and standing for 2 hours at room temperature.
(4) And (4) drying the molecular sieve obtained in the step (3) at 150 ℃ for 4h, and roasting for 2h by programming the temperature to 550 ℃.
(5) Tabletting and sieving the roasted modified molecular sieve catalyst to prepare modified molecular sieve catalyst particles with 5-10 meshes.
The modified molecular sieve catalyst components obtained are shown in table 1.
Table 1 modified molecular sieve catalysts and loadings
The IR spectrum of the La/HY catalyst is shown in FIG. 2.
The system structure for synthesizing pseudocumene and durene through the alkylation reaction of toluene and methanol in the following embodiment is shown in fig. 1, and comprises a light aromatic hydrocarbon raw material tank 1, a methanol tank 2, a light aromatic hydrocarbon feed pump 3, a methanol feed pump 4, a mixer 5, a preheater 6, a fixed bed reactor 7, a cooler 8, a three-phase separator 9, an oil phase reflux pump 10 and an online chromatograph 11.
The fixed bed reactor 7 fixes the modified molecular sieve catalyst particles. The fixed bed reactor 7 is provided with three methanol side feed inlets.
The outlet of the light aromatic hydrocarbon raw material tank 1 is sequentially connected with a light aromatic hydrocarbon feed pump 3 and a mixer 5. The outlet of the methanol tank 2 is connected with a methanol feeding pump 4. The outlet of the methanol feeding pump 4 is simultaneously connected with the mixer 5 and three methanol side feeding ports of the fixed bed reactor 7. The outlet of the mixer 5 is connected with a preheater 6. The outlet of the preheater 6 is connected with the mixture inlet at the top of the fixed bed reactor 7. The outlet at the bottom of the fixed bed reactor 7 is connected with a cooler 8 and a three-phase separator 9 in sequence. The gas phase outlet of the three-phase separator 9 is connected to the preheater 6. An oil phase outlet of the three-phase separator 9 is sequentially connected with an oil phase reflux pump 10, an online chromatograph 11 and the mixer 5.
The first methanol stop valve 52 is installed in a pipeline connecting the outlet of the methanol feed pump 4 and the mixer 5. The pipeline between the outlet of the methanol feed pump 4 and the first methanol stop valve 52 is communicated with three methanol side line feed inlets of the fixed bed reactor 7 through methanol side compensation, the methanol side compensation pipeline comprises a methanol side compensation header pipe and three methanol side compensation branch pipes, the methanol side compensation header pipe is provided with a second methanol stop valve 53, and the three methanol side compensation branch pipes are provided with a first methanol sectional feed stop valve 71, a second methanol sectional feed stop valve 72, a third methanol sectional feed stop valve 73, a first methanol sectional feed flowmeter 74, a second methanol sectional feed flowmeter 75 and a third methanol sectional feed flowmeter 76.
An oil phase return valve 111 and a return shutoff valve 51 are installed in an oil phase circulation line between the line chromatograph 11 and the mixer 5. And an oil phase circulation pipeline between the oil phase reflux pump 10 and the on-line chromatograph 11 is provided with a product side extraction pipeline, and the product side extraction pipeline is provided with an oil phase outlet valve 112.
Example 1
The system is adopted to carry out the continuous reaction of the fixed bed to synthesize the pseudocumene and the durene.
The reaction conditions are as follows: the temperature is 400 ℃, the liquid mass space velocity is 1h -1 Toluene and methanol (molar ratio) = 1: 3, the reaction time is 4 hours, a methanol side-line feeding valve is closed, an oil phase reflux valve is closed, and all products are extracted. The results of the fixed catalyst reactions are shown in Table 2.
TABLE 2 results of different catalyst reactions
Table 2 shows that the modified molecular sieve catalyst can catalyze the alkylation reaction of toluene and methanol to obtain pseudocumene and durene. Wherein the catalytic effect of Zn/Hbeta and La/HY is better than that of other catalysts; compared with the catalytic effect of Zn/H beta and La/HY, the catalytic effect of La/HY is more remarkable.
Example 2
The system is adopted to carry out the continuous reaction of the fixed bed to synthesize the pseudocumene and the durene.
The catalyst is La/HY. The reaction conditions are as follows: the temperature is 400 ℃, the liquid mass space velocity is 1h -1 The mol ratio of p-xylene to methanol is not less than 1 to 2, the reaction time is 4 hours, the methanol side-line feeding valve is closed, the oil phase reflux valve is closed, and all products are extracted. The reaction results are shown in Table 3.
TABLE 3 results of the reaction
Comparison of table 3 with table 2 shows that both p-xylene and toluene are capable of producing pseudocumene and durene. When the raw material adopts p-xylene, the method is more favorable for producing pseudocumene and durene.
Example 3
The system is adopted to carry out the continuous reaction of the fixed bed to synthesize the pseudocumene and the durene.
The reaction conditions are as follows: the temperature is 350-450 ℃, the liquid mass space velocity is 0.5-1 h -1 Toluene and methanol (molar ratio) = 1: 3, the reaction time is 2 hours, a methanol side-line feeding valve is closed, an oil phase reflux valve is closed, and all products are extracted. The reaction results are shown in Table 4.
TABLE 4 reaction results at different reaction temperatures and mass space velocities
Table 4 shows that when the reaction temperature is 400 ℃ and the mass space velocity is 0.5h -1 Meanwhile, the method has better raw material conversion rate, selectivity of pseudocumene and selectivity of durene.
Example 4
The system is adopted to carry out the continuous reaction of the fixed bed to synthesize the pseudocumene and the durene.
The reaction conditions are as follows: the temperature is 400 ℃, and the liquid mass space velocities are 0.25 h and 0.5h respectively -1 And the mol ratio of the toluene to the methanol in the mixer is = 1: 2, a methanol side-stream feeding valve is opened, the mol ratio of the side-stream feeding methanol to the toluene is 1:1, the reaction time is 4 and 2 hours respectively, an oil phase reflux valve is closed, and all products are extracted. The reaction results are shown in Table 5.
TABLE 5 results of the reaction in the side-feed state
Table 5 shows that in the side feeding state, the mass space velocity is reduced, the reaction time is increased, the toluene conversion rate can be improved, the selectivity of the partial three and the partial four is reduced, mainly the contact time of the reaction raw materials and the catalyst is longer, and the side reaction is increased.
Example 5
The system is adopted to carry out the continuous reaction of the fixed bed to synthesize the pseudocumene and the durene.
The reaction conditions are as follows: the temperature is 400 ℃, the liquid mass space velocity is 0.5h -1 The molar ratio of toluene to methanol in the mixer is = 1: 2, the reaction time is 2 hours, a methanol side-stream feed valve is opened, the molar ratio of the side-stream feed methanol to the toluene is 1:1, an oil phase reflux valve is opened, and the product is circulated for one time without being extracted. The reaction results are shown in Table 6.
TABLE 6 reaction results of side feed and product recycle
As can be seen from the comparison of Table 5 and Table 6, at the same mass space velocity condition (0.5 h) -1 ) The specific analysis reason is that under the process condition, the reaction product and the catalyst have short single contact time, and the toluene conversion rate and the selectivity of the product of the pseudocumene and the durene are continuously improved by twice contact with the catalyst.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A method for producing pseudocumene and durene by alkylation is characterized in that light aromatic hydrocarbon and methanol are taken as raw materials, and alkylation reaction is carried out under the catalysis of a modified molecular sieve catalyst and the condition of 250-600 ℃; the material after the alkylation reaction continues to carry out alkylation reaction again under the catalytic action of the modified molecular sieve catalyst and the condition of 250-600 ℃;
wherein the light aromatic hydrocarbon is one or more of benzene, toluene, o-xylene, m-xylene and p-xylene;
the modified molecular sieve catalyst is composed of a molecular sieve and a metal oxide loaded in the molecular sieve, wherein the molecular sieve is one or more of HY, H beta, IM-5, NU87, EU-1 and mordenite, and the metal in the metal oxide is one or more of Mg, cu, la, zn and Mo.
2. The alkylation process of claim 1 to produce pseudocumene and durene, wherein the molecular sieve is HY and the metal of the metal oxide is La; or the molecular sieve is H beta, and the metal in the metal oxide is Zn.
3. The alkylation process of claim 1, wherein the light aromatic hydrocarbon is one or more of toluene, o-xylene, m-xylene, and p-xylene.
4. The alkylation process of claim 1 to produce pseudocumene and durene, wherein the molar ratio of light aromatic hydrocarbon to methanol is 1:5 to 5:1;
or, the total airspeed of the raw material liquid mass is 0.5-5 h -1 。
5. The method for producing pseudocumene and durene by alkylation according to claim 1, wherein the oil phase material and the gas phase material after the alkylation are subjected to the alkylation reaction again under the catalytic action of the modified molecular sieve catalyst and at a temperature of 250 to 600 ℃;
alternatively, methanol is replenished during the alkylation reaction.
6. A system for the alkylation production of pseudocumene and durene, characterized by the fact that it is used to implement the process according to claim 1, comprising:
a light aromatic hydrocarbon source for delivering light aromatic hydrocarbons to the reactor;
a methanol source for delivering methanol to the reactor;
the reactor is used for carrying out alkylation reaction on light aromatic hydrocarbon and methanol to produce pseudocumene and durene;
a product material circulation pipeline for conveying the material discharged from the reactor after the alkylation reaction back to the reactor;
the online detection device is arranged on the product material circulating pipeline and is used for monitoring the pseudocumene and the durene in the product material circulating pipeline;
and the product side extraction pipeline is connected with the product material circulation pipeline and is used for extracting the pseudocumene and the durene which meet the standard according to the detection result of the online detection device.
7. The alkylation system for producing pseudocumene and durene of claim 6, wherein the reactor is a fixed bed reactor.
8. The alkylation system of claim 6, wherein the reactor is provided with a plurality of methanol feed inlets.
9. The system for producing pseudocumene and durene by alkylation according to claim 6, comprising a mixer, wherein the outlet of the light aromatic hydrocarbon source is connected with the mixer, the outlet of the methanol source is simultaneously connected with a plurality of methanol feeding ports, and the outlet of the mixer is connected with the mixture inlet of the reactor;
preferably, a preheater is included, the preheater being disposed between the mixer outlet and the mix inlet of the reactor.
10. The system of claim 6, comprising a cooler and a three-phase separator, wherein the product material recycling line comprises a gas phase recycling line and an oil phase recycling line, the material outlet of the reactor is connected with the cooler and the three-phase separator in sequence, the gas phase outlet of the three-phase separator is connected with the gas phase recycling line, and the oil phase outlet of the three-phase separator is connected with the oil phase recycling line.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211336028.3A CN115636714A (en) | 2022-10-28 | 2022-10-28 | Method and system for producing pseudocumene and durene through alkylation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211336028.3A CN115636714A (en) | 2022-10-28 | 2022-10-28 | Method and system for producing pseudocumene and durene through alkylation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN115636714A true CN115636714A (en) | 2023-01-24 |
Family
ID=84946947
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211336028.3A Pending CN115636714A (en) | 2022-10-28 | 2022-10-28 | Method and system for producing pseudocumene and durene through alkylation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115636714A (en) |
-
2022
- 2022-10-28 CN CN202211336028.3A patent/CN115636714A/en active Pending
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7834227B2 (en) | Aromatics co-production in a methanol-to-propylene unit | |
| KR101138849B1 (en) | A process for producing lower carbon olefins from methanol or/and dimethyl ether | |
| EP2292573B1 (en) | Method for producing an alkylated aromatic compound and method for producing phenol | |
| CN102234212A (en) | Method for directly converting synthetic gas into low-carbon olefins | |
| US6500997B2 (en) | Catalysts and processes for the conversion of aromatic hydrocarbons and uses thereof in the production of aromatic hydrocarbons | |
| EP2834210A1 (en) | Process for the production of xylenes and light olefins from heavy aromatics | |
| CN102464559A (en) | Method for producing alkylated aromatic hydrocarbon | |
| US8653315B2 (en) | Multiple zeolite catalyst and method of using the same for toluene disproportionation | |
| RU2742576C1 (en) | Apparatus and method for synthesis of paraxylol and combined synthesis of light olefins from methanol and/or dimethyl ether and benzene | |
| WO2013151689A1 (en) | Multimetal zeolites based catalyst for transalkylation of heavy reformate to produce xylenes and petrochemical feedstocks | |
| RU2743135C1 (en) | Fluidised bed device and a method of producing para-xylene and co-producing lower olefins from methanol and/or dimethyl ether and benzene | |
| US20220144748A1 (en) | Method for producing methyl acetate by means of carbonylation of dimethyl ether | |
| CN104447176A (en) | Method for high-selectivity preparation of p-xylene | |
| CN102464540A (en) | Method for producing para-alkylated arene | |
| CN107266276B (en) | Method for producing o-xylene from coal-based raw material | |
| US4229320A (en) | Catalyst for making para-xylene | |
| CN115636714A (en) | Method and system for producing pseudocumene and durene through alkylation | |
| CN112299941B (en) | Preparation method of durene | |
| US4247726A (en) | Para-xylene process and catalyst | |
| CN106582791A (en) | Catalyst for producing ethylbenzene from benzene and ethane | |
| CN112028730B (en) | Xylene isomerization method | |
| US20110288358A1 (en) | Method for producing a product containing c3h6 and c2h4 | |
| CN115259984B (en) | Method for preparing alkylbenzene by alkylation of benzene and synthesis gas | |
| CN110372465B (en) | Method for preparing durene from xylene and methanol | |
| CN114456835B (en) | Treatment system and treatment method for gasoline component |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |