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Method for dehydrogenation of CO raw material in virtue of oxidation reaction

An oxidation reaction and fluidized bed reactor technology, applied in the direction of carbon monoxide, etc., can solve the problems of poor catalyst selectivity, high CO loss rate, and difficult temperature control.

Inactive Publication Date: 2012-08-29
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0006] The main problems of the technology involved in the above literature are that the temperature is difficult to control, the catalyst selectivity is poor, and the CO loss rate is high.

Method used

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  • Method for dehydrogenation of CO raw material in virtue of oxidation reaction
  • Method for dehydrogenation of CO raw material in virtue of oxidation reaction

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0018] use figure 1In a fluidized bed reactor, the vertical distance between the terminator injection port and the bottom of the riser is 1 / 5 of the length of the riser, the inner diameter of the riser is 1 / 10 of the outer diameter of the dense phase zone, and the height of the riser is 1 / 4 of the height of the phase area. The vertical distance between the regeneration inclined pipe of the fluidized bed reactor and the connection port of the dense phase area is 1 / 5 of the vertical height of the dense phase area from the bottom of the dense phase area, and the vertical height of the transition area of ​​the fluidized bed reactor is 1 / 5 of the vertical height of the dense phase area / 10. A palladium-loaded alumina fluidized bed catalyst with a palladium content of 0.5% has an average particle diameter of 80 microns, water is used as a terminator, and a CO mixed gas with a hydrogen content of 10% is used as a raw material, and the weight ratio of the raw material to the terminat...

Embodiment 2

[0020] use figure 1 In a fluidized bed reactor, the vertical distance between the terminator injection port and the bottom of the riser is 1 / 8 of the length of the riser, the inner diameter of the riser is 1 / 12 of the outer diameter of the dense phase zone, and the height of the riser is 1 / 2 of the height of the phase area. The vertical distance between the regeneration inclined pipe of the fluidized bed reactor and the connection port of the dense phase area is 1 / 3 of the vertical height of the dense phase area from the bottom of the dense phase area, and the vertical height of the transition area of ​​the fluidized bed reactor is 1 / 3 of the vertical height of the dense phase area / 5. A palladium-supported alumina fluidized bed catalyst with a platinum content of 0.2% has an average particle diameter of 120 microns, water is used as a terminator, and CO mixed gas with a hydrogen content of 10% is used as a raw material, and the weight ratio of the raw material to the termina...

Embodiment 3

[0022] use figure 1 In a fluidized bed reactor, the vertical distance between the terminator injection port and the bottom of the riser is 1 / 15 of the length of the riser, the inner diameter of the riser is 1 / 6 of the outer diameter of the dense phase zone, and the height of the riser is 1 / 3 of the height of the phase area. The vertical distance between the regeneration inclined pipe of the fluidized bed reactor and the connection port of the dense phase zone is 1 / 8 of the vertical height of the dense phase zone from the bottom of the dense phase zone, and the vertical height of the transition zone of the fluidized bed reactor is 1 / 8 of the vertical height of the dense phase zone / 6. A palladium-loaded alumina fluidized bed catalyst with a platinum content of 0.3% has an average particle diameter of 180 microns, water is used as a terminator, and CO mixed gas with a hydrogen content of 5% is used as a raw material, and the weight ratio of the raw material to the terminator is...

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Abstract

The invention relates to a method for dehydrogenation of CO raw material in virtue of oxidation reaction and mainly solves the technical problems of low hydrogen desorbing rate and high CO loss rate in reaction process of oxidative dehydrogenation of CO gas raw material in the prior art. In the invention, by adopting mixture gas containing CO and hydrogen as raw material, and under the conditions that water is selected as a termination agent, the reaction temperature ranges from 80 to 260 DEG C, the volume space velocity is 100 to 10,000 hours<-1>, the molar ratio of oxygen / hydrogen is (0.5-10) : 1, the reaction pressure is 0.08 below zero to 5.0 MPa, and the weight ratio of the raw material and the termination agent is (5-100) : 1, the invention adopts the technical scheme that the raw material is in contact reaction with a catalyst inside a reactor so as to generate an effluent containing water, and the reactor is a fluidized bed reactor with an external cyclone separator. Therefore, the problems are well solved, and the method can be used in industrial production of dehydrogenation of CO raw material in virtue of oxidation reaction.

Description

technical field [0001] The invention relates to a method for dehydrogenating CO raw material by means of oxidation reaction, in particular to the use of an external cyclone separator, which is practical for the oxidative dehydrogenation reaction process of CO gas raw material. Background technique [0002] Oxalate is an important organic chemical raw material, which is widely used in the fine chemical industry to produce various dyes, medicines, important solvents, extractants and various intermediates. In the 21st century, oxalate, as a degradable and environmentally friendly engineering plastic monomer, has received extensive international attention. In addition, oxalic acid can be obtained by normal pressure hydrolysis of oxalate, and oxalamide can be obtained by normal pressure ammonia solution. Oxalate can also be used as a solvent to produce pharmaceutical and dye intermediates, etc., such as various condensation reactions with fatty acid esters, cyclohexylacetophenon...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C01B31/18C01B32/40
Inventor 刘俊涛孙凤侠李蕾
Owner CHINA PETROLEUM & CHEM CORP