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Method for producing isopropylbenzene by using benzene and propylene

A technology of cumene and propylene, which is applied in the field of producing cumene from benzene and propylene, can solve the problem of high n-propylbenzene content, achieve the effect of reducing content 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

[0006] 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 from benzene and propylene is provided

Method used

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  • Method for producing isopropylbenzene by using benzene and propylene
  • Method for producing isopropylbenzene by using benzene and propylene
  • Method for producing isopropylbenzene by using benzene and propylene

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0030] according to figure 1 The technological process, the catalyst bed of the alkylation reactor is divided into four sections, loaded with 170 grams of shaped catalyst containing MCM-22 zeolite, the four sections are equipped with 35, 40, 45, 50 grams in turn, and propylene is fed in four sections . The reaction conditions of the alkylation reactor are: 130°C of reaction temperature, 2.5MPa of reaction pressure, 550 g / hour of benzene feed (stream 12) entering the alkylation reactor, 110 g / hour of propylene feed, four sections The amount of propylene fed in sequence is 20, 25, 30, 35 g / h.

[0031] The transalkylation reactor uses two fixed-bed reactors connected in series. The first transalkylation reaction zone is loaded with 40 grams of shaped catalyst containing Beta zeolite, and the second transalkylation reaction zone is loaded with 50 grams of shaped catalyst containing PSH-3 zeolite. The reaction conditions of the first transalkylation reactor are: 150 DEG C of rea...

Embodiment 2

[0038] Same as [Example 1], except that the catalyst bed of the alkylation reactor is divided into four sections, loaded with 200 grams of molded catalyst containing MCM-22 zeolite, and the four sections are successively equipped with 45, 50, 50, 55 grams, propylene fraction Four stage feeding. The reaction conditions of the alkylation reactor are: 150°C of reaction temperature, 2.5MPa of reaction pressure, 550 grams / hour of benzene feed (stream 12) entering the alkylation reactor, 160 grams / hour of propylene feed, four The amount of propylene fed into the stage successively is 35, 40, 40, 45 g / h.

[0039] The transalkylation reactor uses two fixed-bed reactors connected in series. Wherein the first transalkylation reactor is loaded with 80 grams of shaped catalyst containing Beta zeolite, and the second transalkylation reactor is loaded with 30 grams of shaped catalyst containing PSH-3 zeolite. The reaction conditions of the first transalkylation reactor are: 150 DEG C of r...

Embodiment 3

[0046] Same as [Example 1], except that the catalyst bed of the alkylation reactor is divided into four sections, and 170 grams of shaped catalysts containing SHY-1 zeolite are loaded, and 45, 50, 50, and 55 grams of propylene are loaded in the four sections successively. Four stage feeding. The reaction conditions of the alkylation reactor are: reaction temperature 130°C, reaction pressure 2.5MPa, 550 g / hour of benzene feed (stream 12) entering the alkylation reactor, 160 g / hour of propylene feed, four sections The amount of propylene fed in sequence is 35, 40, 40, 45 g / h.

[0047] The transalkylation reactor uses two fixed-bed reactors connected in series. Wherein the first transalkylation reactor is loaded with 80 grams of shaped catalyst containing Beta zeolite, and the second transalkylation reactor is loaded with 30 grams of shaped catalyst containing SHY-2 zeolite. The reaction conditions of the first transalkylation reactor are: 150 DEG C of reaction temperature, 40 ...

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Abstract

The invention relates to a method for producing isopropylbenzene by using benzene and propylene and mainly solves the problem of high content of n-propylbenzene existing in an isopropylbenzene product of 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 first stream of benzene material flow 12 and propylene enter an alkylation reactor to react, thereby material flow 19 comprising benzene, propylene, isopropylbenzene and polyisopropylbenzene is obtained; (b) the material flow 19 is separated to obtain material flow 23 containing polyisopropylbenzene; (c) after the material flow 23 is separated by a rectifying tower, material flow 13 is obtained at the tower top, and material flow 14 is obtained in the middle part of the tower; (d) a second stream of material flow 10 and the material flow 13 enter a first alkyl group transfer reaction zone for carrying out alkyl group transfer reaction to obtain a material flow 20; the material flow 20, a third stream of material flow 11 and the material flow 14 enter a second alkyl group transfer reaction zone for carrying out alkyl group transfer reaction to obtain material flow 22; and the material flow 21 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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Patent Type & Authority Applications(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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