Method for producing propylene oxide

A technology of propylene oxide and epoxidation reaction, which is applied in the direction of organic chemistry, can solve the problem of rising reaction temperature and achieve the effect of improving selectivity

Inactive Publication Date: 2015-04-29
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0010] The technical problem to be solved by this invention is that in the prior art, the reaction process of cumene hydroperoxide and propylene epoxidation to propylene oxide has a higher reaction temperatur...

Method used

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  • Method for producing propylene oxide

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Experimental program
Comparison scheme
Effect test

Embodiment 1

[0037] according to figure 1 In the technical scheme shown, the raw material contains a mixture of cumene hydroperoxide with a concentration of 35% wt, and the flow rate is 101166.1 kg / h. It is divided into two shares in proportion and enters a two-stage adiabatic fixed-bed reactor respectively. The raw material propylene is 10812.7 kg / hour, circulating propylene 92993.1 kg / hour, circulating epoxidation reaction product 51243 kg / hour, mixed with the cumene hydroperoxide mixture entering the first catalyst bed layer, circulating epoxidation reaction product 85404.5 kg / hour and entering The mixture of cumene hydroperoxide in the second catalyst bed is mixed with Ti / SiO 2 Catalyst contact, liquid phase epoxidation reaction to generate propylene oxide, dimethyl benzyl alcohol and other by-products; the reactants flowing out of the first catalyst bed and the mixture of cumene hydroperoxide entering the second catalyst bed, circulation The streams are mixed, the temperature is con...

Embodiment 2

[0040] Same as [Example 1], only change the flow rate of the recycle stream: the recycle propylene flow rate is 61995.4 kg / h, the cyclic epoxidation reaction product entering the first catalyst bed is 43493.6 kg / h, enters the recycle loop of the second catalyst bed layer Oxidation reaction product 72489.3 kilograms / hour, other is with [embodiment 1]. Cumene hydroperoxide weight space velocity 4.5hr -1 , the mol ratio of total propylene and cumene hydroperoxide is 7.1, the mol ratio of propylene and cumene hydroperoxide of the first catalyst bed layer and the second catalyst bed inlet then reaches 20.6 and 18.5, the first catalyst bed The outlet temperatures of the bed and the second catalyst bed were 83.1°C and 79.3°C respectively, the total conversion rate of cumene hydroperoxide was 99.2%, and the molar selectivity to propylene oxide was 96.1%.

[0041]

Embodiment 3

[0043] Same as [Example 1], only the reactor form is changed: two single-bed adiabatic fixed-bed reactors are connected in series, and the others are the same as [Example 1]. Cumene hydroperoxide weight space velocity 4.5hr -1 , the mol ratio of total propylene and cumene hydroperoxide is 10.2, and the mol ratio of propylene and cumene hydroperoxide at the inlet of the first catalyst bed and the second catalyst bed then reaches 29.6 and 27.2, the first catalyst The outlet temperatures of the bed and the second catalyst bed were 78.2°C and 75.3°C respectively, the total conversion rate of cumene hydroperoxide was 99.3%, and the molar selectivity to propylene oxide was 96.4%.

[0044]

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Abstract

The invention relates to a method for producing propylene oxide. The method is mainly used for solving the problem of relatively high reaction temperature rise and the problem that a relatively high molar ratio of propylene to cumyl hydroperoxide is needed for keeping relatively high reaction efficiency in the prior art. The method comprises the following steps: enabling raw materials namely cumyl hydroperoxide and a propylene liquid phase to enter a multi-section adiabatic reaction area with at least two sections, and performing contact reaction on the raw materials and a Ti-silicon dioxide catalyst to prepare propylene oxide under the conditions that the epoxidation reaction temperature is 15-160 DEG C, the pressure is 1.0-12.0MPa and a total molar ratio of propylene to cumyl hydroperoxide is 2-30, wherein the raw material namely cumyl hydroperoxide enters each catalyst bed layer of the multi-section adiabatic reaction area in a sectional mode; and an epoxidation reaction product containing propylene oxide, obtained from an outlet of the multi-section adiabatic reaction area, is partially circulated to an inlet of each catalyst bed layer of the multi-section adiabatic reaction area. By adopting such a technical scheme, the problem of relatively high reaction temperature rise and the problem that the relatively high molar ratio of propylene to cumyl hydroperoxide is needed for keeping relatively high reaction efficiency can be relatively well solved; and the method disclosed by the invention can be applied to the industrial production of preparing propylene oxide from cumyl hydroperoxide and propylene by virtue of epoxidation.

Description

technical field [0001] The present invention relates to a method for producing propylene oxide. Background technique [0002] Propylene oxide is an important basic chemical raw material and the third largest propylene derivative after polypropylene and acrylonitrile. It is mainly used in the production of polyether and propylene glycol. It is also the main raw material of the fourth-generation detergent non-ionic surfactant, oil field demulsifier, pesticide emulsifier, etc. Propylene oxide derivatives are widely used in industries such as automobiles, construction, food, tobacco, medicine and cosmetics. Nearly 100 kinds of downstream products have been produced, which are important raw materials for fine chemical products. [0003] The traditional production process of propylene oxide is the chlorohydrin process, which includes three steps: chloroalcoholization of propylene and hypochlorous acid solution, saponification of chloropropanol and milk of lime, and product refi...

Claims

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Application Information

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IPC IPC(8): C07D301/19C07D303/04
CPCC07D301/19C07D303/04
Inventor 邵百祥黄云群
Owner CHINA PETROLEUM & CHEM CORP
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