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Method for prodn. of phenol and acetone by acid-catalysed cleavage of cumen hydroperoxide

A technology of cumene hydroperoxide and cumene hydroperoxide, which is applied in the preparation of oxygen-containing compounds, chemical instruments and methods, and the preparation of organic compounds, and can solve problems such as the negative impact of selectivity and yield

Inactive Publication Date: 2004-07-07
石碳酸化学股份有限公司
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

However, when CHP is cleaved, AMS undergoes a polymerization reaction or an addition reaction between AMS and phenol, these reactions lead to the formation of high boilers (poly-α-methylstyrene and cumylphenol), the result of which is the selectivity of the entire process and yields are negatively affected

Method used

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  • Method for prodn. of phenol and acetone by acid-catalysed cleavage of cumen hydroperoxide

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Experimental program
Comparison scheme
Effect test

Embodiment 1

[0027] Embodiment 1 (comparative example):

[0028] In a basic structure such as figure 1 In the cracking equipment of the present invention, the CHP content is 67% (weight) technical grade CHP reaction to the residual content in the CHP cracking product is the degree of 1.0% (weight). The cycle ratio λ is set to 17 here. Add an appropriate amount of sulfuric acid as a catalyst to match this.

[0029] Three tube-bundle heat exchangers connected in series ( figure 1 The reactor 1) in is used as a CHP cracking reactor; the reaction temperature is 50°C. The reaction pressure is 1×10 5 Pa (1 bar) (absolute).

[0030] The resulting cleavage product contained 0.21% by weight of high boilers (mainly polymerized AMS and cumylphenol). CHP lysis was followed by DCP lysis.

Embodiment 2

[0031] Embodiment 2 (according to the present invention)

[0032] Except that the circulation ratio is 7, the CHP cracking of Example 1 is carried out under other identical conditions; after adding an appropriate amount of acid, the residual CHP concentration in the CHP cracking product is specified as 0.25% (weight). The cleavage product likewise contained 0.21% by weight of high boilers.

[0033] In this case, by reducing the circulation ratio, although the lower residual CHP concentration has also been achieved, the same selectivity as in Comparative Example 1 can be achieved, but in Example 1, the only way to achieve a lower residual CHP concentration is to increase the acid concentration. The amount of addition, and this will promote the formation of by-products. The size of the cleavage reactor and piping can be correspondingly smaller. In addition, lower residual CHP content is more beneficial to the safety of downstream equipment.

Embodiment 3

[0034] Embodiment 3 (according to the present invention)

[0035] The circulation ratio was set to 7, and then under the same conditions, including the residual CHP concentration in the cleavage product being 1.0% by weight, the CHP cleavage of Example 1 was implemented. The content of high boilers in the cleavage product was 0.16% by weight. Compared with Example 1, the selectivity was significantly increased by reducing the recycle ratio. Compared with Example 2, it is shown that the selectivity can be improved by increasing the residual CHP concentration at low circulation ratio.

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Abstract

In the production of phenol and acetone by acid-catalyzed homogeneous cracking of cumene hydroperoxide (CHP) in reactor(s) with tube flow characteristics, in which part of the cracked stream is recycled and combined with the CHP feed stream, the weight ratio of recycled cracked stream to CHP stream (recycling ratio) is less than 10.

Description

technical field [0001] The present invention relates to an improved process for the selective cleavage of cumene hydroperoxide (CHP) to phenol and acetone under the action of an acid. Background technique [0002] Internationally, phenol is mainly prepared from cumene. Cumene is first oxidized to cumene hydroperoxide (abbreviated as CHP), and due to selectivity, the conversion rate of cumene usually reaches 20-30% (by weight). In the next step called concentration, the CHP content of the oxide feed is usually concentrated to 65-90% by weight. So-called industrial grade CHP is produced. In subsequent cleavage, technical grade CHP reacts with an acid, usually sulfuric acid, to produce phenol and acetone. After the cleavage products have been neutralized, the products are separated from the cleavage products, mainly by distillation in the so-called work-up section of the phenol plant. [0003] Both oxidation and cleavage reactions are accompanied by the formation of unwante...

Claims

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Application Information

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IPC IPC(8): C07B61/00C07C27/12C07C27/22C07C27/26C07C37/08C07C39/04B01J27/04C07C45/53C07C49/08
CPCC07C45/53C07C37/08Y02P20/52C07C49/08C07C39/04C07C27/26
Inventor M·韦伯O·格尔里希M·克莱尼-波伊曼W·波姆佩茨基R·西格C·米查利克J·沃尔克
Owner 石碳酸化学股份有限公司
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