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Method for producing isopropylbenzene

A kind of technology of cumene and dicumene, applied in the field of producing cumene, can solve the problem of high n-propylbenzene content, achieve the effect of reducing content, good technical effect and improving product quality

Active Publication Date: 2012-05-23
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0005] The technical problem to be solved by the present invention is the problem that the prior art has a relatively high content of n-propylbenzene in the transalkylation product, and a new method for producing cumene is provided

Method used

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  • Method for producing isopropylbenzene
  • Method for producing isopropylbenzene
  • Method for producing isopropylbenzene

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0026] according to figure 1 The process flow, the first transalkylation reaction zone and the second transalkylation reaction zone are independent, two fixed-bed reactors connected in series. The first transalkylation reaction zone is loaded with 15 grams of shaped catalyst of Beta zeolite, and the second transalkylation reaction zone is loaded with 60 grams of shaped catalyst of SHY-1 zeolite. The reaction conditions in the first transalkylation reaction zone are: 150°C of reaction temperature, 110 g / hour of benzene flow (stream 6), 20 g / hour of multi-substituted cumene (stream 8), and diisopropyl benzene in stream 8 The benzene content is 99%. The reaction conditions of the second transalkylation reaction zone are as follows: reaction temperature 178° C., outlet pressure of the second reaction zone 1.5 MPa, stream 9 flow rate 90 g / hour, triisopropylbenzene content in stream 9 6%. Continuous reaction for 5 days.

[0027] The operating conditions of the multi-substituted c...

Embodiment 2

[0030] according to figure 1 The process flow, the first transalkylation reaction zone and the second transalkylation reaction zone are independent, two fixed-bed reactors connected in series. The first transalkylation reaction zone is loaded with 50 grams of Beta zeolite shaped catalyst, and the second transalkylation reaction zone is loaded with 30 grams of SHY-2 zeolite shaped catalyst. The reaction conditions in the first transalkylation reaction zone are: 148°C of reaction temperature, 100 g / hour of benzene flow (stream 6), 50 g / hour of multi-substituted cumene (stream 8), and diisopropyl benzene in stream 8 The benzene content is 99%. The reaction conditions in the second transalkylation reaction zone are: 185°C of reaction temperature, 1.5MPa of the second reaction zone outlet pressure, 25 grams / hour of multi-substituted cumene (streaming 9) flow rate, and 8% triisopropylbenzene content in the stream 9 . Continuous reaction for 5 days.

[0031] The operating conditi...

Embodiment 3

[0034] according to figure 1 The process flow, the first transalkylation reaction zone and the second transalkylation reaction zone are independent, two fixed-bed reactors connected in series. The first transalkylation reaction zone was loaded with 40 grams of shaped catalyst of Beta zeolite, and the second transalkylation reaction zone was loaded with 40 grams of shaped catalyst of MCM-49 zeolite. The reaction conditions in the first transalkylation reaction zone are: 151°C of reaction temperature, 80 grams / hour of benzene flow (stream 6), 40 grams / hour of multi-substituted cumene (stream 8), and diisopropyl in stream 8. The benzene content is 98%. The reaction conditions in the second transalkylation reaction zone are: 171°C of reaction temperature, 1.5MPa of the second reaction zone outlet pressure, 50 grams / hour of multi-substituted cumene (streaming 9) flow rate, and 5% triisopropylbenzene content in the stream 9 . Continuous reaction for 5 days.

[0035] The operatin...

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Abstract

The invention relates to a method for producing isopropylbenzene and mainly solves the problem of high content of n-propylbenzene existing in the prior art. The method better solves the problem and can be applied to the industrial production of isopropylbenzene by adopting the technical scheme which comprises the following steps of: (1) a material flow 12 containing polysubstituted isopropylbenzene enters a polysubstituted isopropylbenzene tower, after rectifying seperation is carried out on the material flow 12, a material flow 8 is obtained at the tower top, a material flow 9 is obtained in the middle part of the tower, and a heavy component material flow 11 containing oil tar is obtained in the tower bottom and enters a follow-up process; (b) a raw material benzene material flow 6 and the material flow 8 enter a first alkyl group transfer reaction zone from the top to contact with a catalytic agent for carrying out alkyl group transfer reaction, and a material flow 7 containing isopropylbenzene is obtained after reaction; (c) the material flow 7 and the material flow 9 enter a second alkyl group transfer reaction zone from the top to contact with the catalytic agent for carrying out alkyl group transfer reaction, and a material flow 10 containing isopropylbenzene is obtained after reaction; and the material flow 10 enters the follow-up refining process, thereby the isopropylbenzene product is obtained.

Description

technical field [0001] The invention relates to a method for producing cumene from benzene and propylene. Background technique [0002] Cumene is an important organic chemical raw material and the main intermediate compound in the production of phenol, acetone and α-methylstyrene. Industrially, cumene is prepared by the alkylation reaction of propylene and benzene, and its by-product is mainly polycumene. As early as 1945, UOP announced the method of preparing cumene by reacting propylene and benzene in the presence of an acidic catalyst (SPA method) (USP2382318). The SPA method uses solid phosphoric acid as an alkylation catalyst, because solid phosphoric acid cannot catalyze Transalkylation reaction, so there is no transalkylation part in the process flow. Therefore, the SPA method can only operate under the condition of high styrene molar ratio (5-7), and the yield of cumene is only about 95%. In the 1980s, Monsanto developed AlCl 3 The production process of cumene as...

Claims

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Application Information

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IPC IPC(8): C07C15/085C07C6/12
Inventor 高焕新周斌魏一伦顾瑞芳方华季树芳姚晖
Owner CHINA PETROLEUM & CHEM CORP
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