Method for producing isopropylbenzene

A production method and technology of cumene, applied in the direction of chemical instruments and methods, hydrocarbons, hydrocarbons, etc., 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: 2013-12-04
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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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

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Experimental program
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Effect test

Embodiment 1

[0023] according to figure 1 The technical process, the first transalkylation reactor is loaded with the shaped catalyst of 20 grams of Beta zeolite, and the second transalkylation reactor is loaded with the shaped catalyst of 50 grams of MCM-22 zeolite. The reaction condition of the first transalkylation reactor is: 150 ℃ of reaction temperature, reaction pressure 1.2MPa, the first benzene flow rate (stream 7) 40 grams / hour, many substituted cumene (stream 13) feed rate 20 grams / hour Hours, the content of dicumylbenzene in stream 13 was 98%. The second transalkylation reactor reaction condition is: 180 ℃ of reaction temperature, reaction pressure 1.5MPa, the second benzene flow (stream 8) 80 grams / hour, many substituted cumene (stream 12) flow 80 grams / hour, Triisopropylbenzene content in stream 12 is 10%. Continuous reaction for 5 days.

[0024] The operating conditions of the multi-substituted cumene tower are: tower top temperature 132°C, tower bottom temperature 215°C,...

Embodiment 2

[0027] according to figure 1 The process flow, the first transalkylation reactor is loaded with the shaped catalyst of 30 grams of Beta zeolite, and the second transalkylation reactor is loaded with the shaped catalyst of 40 grams of MCM-22 zeolite. The reaction conditions of the first transalkylation reactor are: 143°C of reaction temperature, 1.2MPa of reaction pressure, 60 g / hour of the first stream of benzene flow (stream 7), and 20 g / h of multi-substituted cumene (stream 13) feed rate Hours, the content of dicumyl in stream 13 was 99%. The second transalkylation reactor reaction condition is: 175 ℃ of reaction temperature, reaction pressure 1.5MPa, the second benzene flow (stream 8) 60 grams / hour, many substituted cumene (stream 12) flow 40 grams / hour, The content of triisopropylbenzene in stream 12 is 8%. Continuous reaction for 5 days.

[0028] The operating conditions of the multi-substituted cumene tower are: tower top temperature 128°C, tower bottom temperature 20...

Embodiment 3

[0031] according to figure 1The technical process, the first transalkylation reactor is loaded with the shaped catalyst of 50 grams of Beta zeolite, and the second alkylation reactor is loaded with the shaped catalyst of 40 grams of SHY-1 zeolite. The reaction conditions of the first transalkylation reactor are: 150 DEG C of reaction temperature, 1.2MPa of reaction pressure, 100 grams / hour of the first stream of benzene flow (stream 7), 60 grams / hour of multi-substituted cumene (stream 13) feeding rate Hours, the content of dicumylbenzene in stream 13 was 98%. The second transalkylation reactor reaction condition is: 180 ℃ of reaction temperature, reaction pressure 1.5MPa, the second benzene flow (stream 8) 80 grams / hour, many substituted cumene (stream 12) flow 80 grams / hour, The content of triisopropylbenzene in stream 12 is 5%. Continuous reaction for 5 days.

[0032] The operating conditions of the multi-substituted cumene tower are: tower top temperature 132°C, tower b...

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Abstract

The invention relates to a method for producing isopropylbenzene. The problem that the content of n-propylbenzene is high in the prior art is solved. The method comprises the following steps that: a) a material flow which contains multi-substituted isopropylbenzene enters a multi-substituted isopropylbenzene tower, after distillation separation, a material flow 13 is obtained from the top of the tower, a material flow 12 is obtained from the middle part of the tower, and a heavy component material flow which contains tar is obtained from a tower kettle, wherein in the material flow 13, the content of diisopropylbenzene is at least more than 95 weight percent, and in the material flow 12, the content of triisopropylbenzene is at least more than 0.5 percent; b) a first benzene material flow and the material flow 13 enter a first alkyl transfer reactor from the top to be contacted with a catalyst to perform an alkyl transference reaction, and a material flow 9 which contains the isopropylbenzene is obtained at the bottom; c) a second benzene material flow and the material flow 12 enter a second alkyl transference reactor from the top to be contacted with a catalyst to perform an alkyl transference reaction, and a material flow 10 which contains the isopropylbenzene is obtained at the bottom; and d) the material flow 9 and the material flow 10 enter a subsequent refining process to produce the product, namely the isopropylbenzene. The problem is better solved through the technical scheme and the method can be applied to the industrial production of the isopropylbenzene.

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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Patent Type & Authority Patents(China)
IPC IPC(8): C07C15/085C07C2/66
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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