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Method for preparing butyraldehyde from propylene and synthesis gas

A synthesis gas and propylene technology, applied in carbon monoxide reaction preparation, organic chemistry, etc., can solve the problems of low conversion rate and production capacity of the second reactor, short catalyst life cycle, high production cost, etc.

Active Publication Date: 2014-01-01
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0003] The technical problem to be solved by the present invention is that there are problems in the prior art that the conversion rate and production capacity of the second reactor are low, the service life of the catalyst is short, and the production cost is high, and a new method for preparing butyraldehyde from propylene and synthesis gas is provided

Method used

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  • Method for preparing butyraldehyde from propylene and synthesis gas
  • Method for preparing butyraldehyde from propylene and synthesis gas
  • Method for preparing butyraldehyde from propylene and synthesis gas

Examples

Experimental program
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Effect test

Embodiment 1

[0024] according to figure 2 In the process shown, the stream I containing propylene, synthesis gas and catalyst enters the first reactor 1, after the reaction, the vapor phase stream II is obtained at the top of the tower, and the liquid phase stream III is obtained at the bottom of the tower. Stream III enters the intermediate separation unit 3, and after separation, vapor phase stream IV and liquid phase stream V are obtained. Stream Ⅴ enters the follow-up process as a crude product. Stream II, stream IV, supplementary synthesis gas 4 and supplementary catalyst 5 enter the second reactor, and after the reaction, liquid phase stream VI containing butyraldehyde and tail gas 6 are obtained. Logistics Ⅵ is output as a product, and tail gas 6 is discharged out of bounds or enters the subsequent process.

[0025] The operating conditions of the first reactor are: pressure 1900KPa, temperature 90°C, residence time 3 hours. The weight ratio of propylene, synthesis gas and catal...

Embodiment 2

[0038] Flow process and operating conditions are the same as [Example 1], but the amount of feed is different.

[0039] The reaction result is: the conversion rate of the first reactor is 77%, and the conversion rate of the second reactor is 83%. See Table 4 and Table 5 for details.

[0040] Table 4

[0041]

[0042] table 5

[0043]

[0044] Under the premise of not changing the structure, size and size of the two reactors, the production capacity of the reaction system is increased by 10%. Nascent butyraldehyde increased from 395kmol / h to 435kmol / h. If there is a margin of more than 10% in the subsequent separation equipment, then only a small amount of equipment can be added to expand the capacity by 10%.

Embodiment 3

[0046] according to image 3 In the process shown, the stream I containing propylene, synthesis gas and catalyst enters the first reactor 1, after the reaction, the vapor phase stream II is obtained at the top of the tower, and the liquid phase stream III is obtained at the bottom of the tower. Stream III enters the intermediate separation unit 3, and after separation, vapor phase stream IV and liquid phase stream V are obtained. Stream Ⅴ enters the follow-up process as a crude product. Stream II, stream IV, supplementary synthesis gas 4 and supplementary catalyst 5 enter the second reactor, and after the reaction, stream VI containing butyraldehyde and tail gas 6 are obtained. Stream V and stream VI enter separation unit 7, using synthesis gas as stripping gas (stream 8), and after separation, vapor phase stream VII containing propylene and synthesis gas, liquid phase stream VIII containing catalyst and product butyraldehyde stream IX are obtained. Among them, stream VII is...

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Abstract

The invention relates to a method for preparing butyraldehyde from propylene and synthesis gas, and mainly solves the problems that a second reactor has low conversion rate and capacity and a catalyst has short life cycle and high production cost in the prior art. The method comprises the following steps of: a) allowing material flow I containing propylene, synthesis gas and a catalyst to enter a first reactor, and reacting to obtain vapor phase material flow II on the tower top and liquid phase material flow III on the tower bottom; b) allowing the material flow III to enter a middle separation unit, separating to obtain vapor phase material flow IV and liquid phase material flow V, and allowing the liquid phase material flow V serving as a crude product to enter a subsequent process; and c) allowing the material flow II, the material flow IV, make-up synthesis gas and a make-up catalyst to enter a second reactor, and reacting to obtain material flow VI containing the butyraldehyde. The method better solves the problems and can be applied to industrial production of preparing butyraldehyde from propylene and synthesis gas.

Description

technical field [0001] The invention relates to a method for preparing butyraldehyde from propylene and synthesis gas. Background technique [0002] Butyraldehyde is an important organic chemical raw material. At present, it is mainly produced industrially from propylene, carbon monoxide and hydrogen through oxo synthesis. The literature "Simulation Research on Propylene Carbonylation Process for Butyraldehyde Synthesis, Natural Gas Chemical Industry, 2009(34): 20-24" discloses a process flow for preparing butyraldehyde by carbonylation of propylene and synthesis gas. In this process, propylene and syngas are used as raw materials, which pass through two series-connected reactors in sequence to obtain the product butyraldehyde. Then the product enters the downstream separation section. Through two evaporations, propylene and catalyst are recycled as much as possible. Part of the butyraldehyde is recycled as a reaction solvent, and part of it is sent to the downstream butano...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C47/02C07C45/50
Inventor 李真泽陈迎印立峰马伟丽
Owner CHINA PETROLEUM & CHEM CORP
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