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Method for production of durene by pseudocumene alkylation and reactor thereof

A technology of reactors and distributors, applied in the field of reactors, can solve the problems of unsatisfactory market demand, high cost of coal chemical industry, and low output, and achieve the goal of being suitable for large-scale industrial production, high production safety, and low consumption of raw and auxiliary materials Effect

Inactive Publication Date: 2019-07-05
JIANGSU ZHENGDAN CHEM IND CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

According to the existing relevant literature, patents and public information, the crystallization separation method of C10 heavy aromatics has been industrialized, but the output is too low to meet the market demand
The coal-to-gasoline coal tar separation method has also achieved industrial production, but due to the high cost of coal chemical industry at this stage, most of them are in a state of suspension

Method used

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  • Method for production of durene by pseudocumene alkylation and reactor thereof
  • Method for production of durene by pseudocumene alkylation and reactor thereof
  • Method for production of durene by pseudocumene alkylation and reactor thereof

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Effect test

Embodiment 1

[0060] figure 2 The part on the left side shows the technical process of raw material gasification: the first heat exchanger 11 under the radial fixed bed reactor 10 passes through the first heat exchanger 11 below the radial fixed bed reactor 10, and absorbs the reaction product in the radial fixed bed reactor 10. The heat is then sent to the second heat exchanger 12, and the steam from the heating furnace 13 is sent to the second heat exchanger 12 at the same time, so that the trimethylbenzene and the alkylating agent are heat-exchanged with the steam to obtain the gasified Trimethylbenzene and alkylating agent.

[0061] Such as figure 2 As shown, the raw material trimethylene (volume space velocity is 0.1h -1 ) and methanol are gasified by heat exchange with steam, and the gasified raw materials are sent into the radial fixed bed reactor through the inlet pipe at the top of the radial fixed bed reactor. 1.0m 3 ZSM-5 molecular sieve catalyst, alkylation reaction at 0.1...

Embodiment 2

[0064] The raw material trimethylene (volume space velocity is 0.1h -1 ) and methanol are gasified by heat exchange with steam, and the gasified raw materials are sent into the radial fixed bed reactor through the inlet pipe at the top of the radial fixed bed reactor. 1.85m 3 ZSM-5 molecular sieve catalyst, alkylation reaction at 0.5MPa, 350°C. The alkylation liquid obtained by the alkylation reaction is discharged from the outlet pipe at the bottom of the radial fixed bed reactor, and is sent to the rectification tower T1 after being heat-exchanged in the first heat exchanger (the operating pressure at the top of the tower is 110KPa, the operating temperature at the top of the tower is 90°C, and the operating temperature at the bottom of the tower is 110°C), the material produced at the top of the rectifying tower T1 is sent to the cooler; The uncondensed gas (hydrogen, methane, methyl ether, etc.) obtained after that is extracted and sent back to the radial fixed-bed react...

Embodiment 3

[0067] The raw material trimethylene (volume space velocity is 1.5h -1 ) and methanol are gasified by heat exchange with steam, and the gasified raw materials are sent into the radial fixed bed reactor through the inlet pipe at the top of the radial fixed bed reactor. 1.15m 3 HZSM-5 molecular sieve catalyst, carry out alkylation reaction at 0.9MPa, 380°C. The alkylation liquid obtained by the alkylation reaction is discharged from the outlet pipe at the bottom of the radial fixed bed reactor, and is sent to the rectification tower T1 after being heat-exchanged in the first heat exchanger (the operating pressure at the top of the tower is 115KPa, the operating temperature at the top of the tower is 95°C, and the operating temperature at the bottom of the tower is 115°C), the material produced at the top of the rectifying tower T1 is sent to the cooler; The uncondensed gas (hydrogen, methane, methyl ether, etc.) obtained after that is extracted and sent back to the radial fixe...

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Abstract

The invention discloses a method for production of durene by pseudocumene alkylation. The method includes: raw material gasification mixing, alkylation reaction, gas-oil-water separation, refining, freezing crystallization filtration and squeezing, wherein a radial fixed bed reactor is employed for alkylation reaction of pseudocumene. The invention also provides the radial fixed bed reactor used by the above method. The method for production of durene by pseudocumene alkylation has the advantages of: high catalyst activity and long service life, high product selectivity, high production safety, few alkylation by-product, stable finished product quality, low consumption of raw and auxiliary materials, long equipment service life, and is suitable for large-scale industrial production.

Description

technical field [0001] This application relates to but not limited to durene production technology, in particular to but not limited to a method for producing durene by alkylation of trimethylene and the reactor used. Background technique [0002] Durene is an important fine chemical raw material, mainly used to produce pyromellitic dianhydride, and then to produce new materials such as polyimide resin or film, which has a very wide range of uses. At present, the synthesis methods of durene are: crystallization separation method of C10 heavy aromatics, coal tar separation method of coal-made gasoline, isomerization method of C10 aromatics, alkylation of methyl chloride, isomerization disproportionation method of mesitylene, partial Trimethylbenzenemethanol alkylation method and so on. According to the existing relevant literature, patents and public information, the crystallization separation method of C10-heavy aromatics has been industrialized, but the output is too low t...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): B01J8/02C07C2/86C07C15/02
CPCB01J8/02B01J8/0221B01J8/0257B01J8/0278B01J2208/00911C07C2/864C07C2/865C07C2529/40C07C15/02
Inventor 曹正国荆晓平李江华王福张小平
Owner JIANGSU ZHENGDAN CHEM IND CO LTD
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