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Light olefins hydroformylation method

A technology for hydroformylation of carbon olefins and low-carbon olefins, which is applied in the field of hydroformylation of low-carbon olefins, and can solve the problems of high investment cost of stirring equipment, equipment failure, affecting the safe and stable operation of reactors, etc.

Active Publication Date: 2014-09-10
SINOPEC SHANGHAI ENG +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 that the existing technology has high investment cost of stirring equipment, which is prone to equipment failure, affects the safe and stable operation of the reactor, the circulating reaction liquid with heat removal interferes with the stirring effect, and the bubble column reactor is easy to form a concentration The problem of gradient and temperature inhomogeneity, providing a new method for the hydroformylation of light olefins

Method used

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  • Light olefins hydroformylation method

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Effect test

Embodiment 1

[0031] use figure 1 The jet reactor shown includes a gas outlet 1, a liquid inlet 2, a liquid injection device 3, a gas distributor 4, an air inlet 5, a liquid outlet 6 and a baffle 7; wherein, the gas outlet 1 and the inlet The liquid port 2 is placed at the top of the reactor, the gas inlet 5 is placed at the lower side of the reactor, the liquid outlet 6 is placed at the bottom of the reactor, and the gas distributor 4 is located between the liquid injection device 3 and the baffle 7 . The liquid injection device is a reduced-bore tube type, the baffle has a skirt, and the gas distributor is a double-ring gas distributor.

[0032] Among them, the relationship between the reactor liquid level H and the reactor diameter D is H / D=1.75, the distance between the baffle and the bottom of the reactor a=0.25D, the distance between the gas distributor and the baffle b=0.1D, and the liquid injection device The distance from the liquid level H is c=0.25D, the diameter of the liquid i...

Embodiment 2

[0037] Same as [Example 1], except that the relationship between the reactor liquid level H and the reactor diameter D is H / D=1.5, the distance between the baffle and the bottom of the reactor a=0.25D, and the distance between the gas distributor and the baffle b= 0.1D, the distance c=0.25D between the liquid injection device and the liquid level H, the diameter of the liquid injection device d=0.05D, the diameter of the baffle is 0.9 of the diameter of the reactor, the diameter of the air outlet on the baffle is 7 mm, and the diameter of the baffle The number of openings is 10. The height of the skirt is 100 mm and the skirt is at 45° to the main body of the fender. The ratio of the outer diameter of the double-ring gas distributor to the diameter of the reactor is 0.7, the ratio of the inner diameter to the diameter of the reactor is 0.4, and the number of openings is 300.

[0038] The above reactor is used in the carbonylation of mixed butenes to produce valeraldehyde, the...

Embodiment 3

[0042] Same as [Example 1], except that the relationship between the reactor liquid level H and the reactor diameter D is H / D=2, the distance between the baffle and the bottom of the reactor a=0.25D, and the distance between the gas distributor and the baffle b= 0.1D, the distance c=0.25D between the liquid injection device and the liquid level H, the diameter of the liquid injection device d=0.05D, the diameter of the baffle is 0.9 of the diameter of the reactor, the diameter of the air outlet on the baffle is 7 mm, and the diameter of the baffle The number of openings is 10. The height of the skirt is 100 mm and the skirt is at 45° to the main body of the fender. The ratio of the outer diameter of the double-ring gas distributor to the diameter of the reactor is 0.7, the ratio of the inner diameter to the diameter of the reactor is 0.4, and the number of openings is 300.

[0043] The above reactor is used in the carbonylation of mixed butenes to produce valeraldehyde, the f...

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Abstract

The invention relates to a light olefins hydroformylation method, which solves the problems that the stirring equipment investment is high, fault is easily generated, a heat-dissipating cycle reaction solution interferes the stirring effect, and unevenness of concentration gradient and temperature is easily formed by a bubble column reactor. According to the invention, light olefins as well as hydrogen and CO-containing synthetic gas respectively pass through a liquid inlet 2 and an air inlet 5, and then are supplied to a jet reactor; the jet reactor comprises a gas outlet 1, a liquid inlet 2, at least one liquid jet apparatus 3, at least one gas distributor 4, an air inlet 5, a liquid outlet 6 and a baffle plate 7; wherein, the gas outlet 1 and the liquid inlet 2 are arranged at top of the reactor, the air inlet 5 is arranged at the lower part at side of the reactor, the liquid outlet 6 is placed at bottom of the reactor, the gas distributor 4 is positioned between the liquid jet apparatus 3 and the baffle plate 7, so that the technical scheme better solves the problems, and can be used for industrial production of aldehyde by light olefins hydroformylation.

Description

technical field [0001] The invention relates to a method for hydroformylation of light olefins. Background technique [0002] Hydroformylation of alkenes with H 2 / CO mixture (synthesis gas) at a certain temperature and pressure, in the presence or absence of a catalyst containing phosphorus, arsenic, antimony or nitrogen ligands in a homogeneous solution containing at least one cobalt, rhodium or ruthenium element in the reaction medium , The process of reacting low-carbon olefins with carbon monoxide and hydrogen. [0003] Low-pressure oxo synthesis is currently the main method for producing aldehydes from light olefins. The industrial process of producing aldehydes from low-carbon olefins mostly uses a rhodium-phosphine complex catalytic system, which belongs to the field of so-called "homogeneous catalysis". Large-scale industrial production adopts continuous operation mode, raw material H 2 / CO and olefins are directly passed into the catalyst solution, and certain ...

Claims

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Application Information

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IPC IPC(8): C07C47/02C07C45/50
CPCC07C45/50C07C47/02
Inventor 陈迎许慎艳张艺贾微贾震
Owner SINOPEC SHANGHAI ENG
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