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Method and reactor for catalytic cracking for producing propylene using fluid bed

A fluidized bed reactor and catalytic cracking technology, applied in the field of chemical engineering, can solve the problems of large pore size and low propylene selectivity, and achieve the effects of improving selectivity, reducing back mixing and improving total yield

Active Publication Date: 2007-05-16
CHINA NAT CHEM ENG GRP CORP LTD +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

However, due to the large pore size of the ZSM-5 molecular sieve, more high-carbon hydrocarbons with more than C4 are generated, resulting in relatively low selectivity of ethylene and propylene.

Method used

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  • Method and reactor for catalytic cracking for producing propylene using fluid bed
  • Method and reactor for catalytic cracking for producing propylene using fluid bed
  • Method and reactor for catalytic cracking for producing propylene using fluid bed

Examples

Experimental program
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Effect test

Embodiment 1

[0065] Methanol is used as a raw material, SAPO-34 / silica gel particles are used as a catalyst, and the content of the active component SAPO-34 in the catalyst is 30%. The process flow shown in Figure 1 is adopted. The reaction system includes two reactors: 104 is the main reactor for raw material cracking; 101 is the olefin conversion reactor for C 2- with C 4+ transform. The products of the two reactors merge into the gas separation system and are separated into C 2- , Propylene, Propane, C 4+ , unconverted raw materials and water, where C 2- with C 4+ After releasing 1% (percentage by weight), they are returned to 101 olefin conversion reactors, and unconverted raw materials are returned to 104 main reactors. The reaction temperature in the main reactor is 400°C, the pressure is 0.1MPa, and the weight space velocity of the feed (including circulating raw materials) is 10hr -1 ;The reaction temperature in the olefin conversion reactor is 600°C, the pressure is 0.1MPa,...

Embodiment 2

[0067] The mixture of methanol and ethanol is used as a raw material, SAPO-34 / silica gel particles are used as a catalyst, and the content of the active component SAPO-34 in the catalyst is 80%. The process flow shown in Figure 2 is adopted. The reaction system includes three reactors: 102 for C 2 Olefin Conversion Reactor for C 2- Conversion; 104 is the main reactor for dimethyl ether cracking; 106 is C 4+ Olefin Conversion Reactor for C 4+ transform. The products of the three reactors merge into the gas separation system and are separated into C 2- , Propylene, Propane, C 4+ , dimethyl ether and water, where C 2- with C 4+ After releasing 2%, they are returned to 102 and 106 olefin conversion reactors respectively, and unconverted raw materials are returned to 104 main reactor. The reaction temperature in the main reactor 104 is 350°C, the pressure is 1MPa, and the weight space velocity of the feed (including circulating raw materials) is 0.5hr -1 ;C 2 The reaction...

Embodiment 3

[0069] Dimethyl ether is used as a raw material, ZSM-5 / silica gel particles are used as a catalyst, and the content of the active component ZSM-5 in the catalyst is 10%. The process flow shown in Figure 3 is adopted. The reaction system includes three reactors: 102 for C 2 Olefin Conversion Reactor for C 2- Conversion; 104 is the main reactor for dimethyl ether cracking; 106 is C 4+ Olefin Conversion Reactor for C 4+ transform. The products of the three reactors merge into the gas separation system and are separated into C 2- , Propylene, Propane, C 4+ , dimethyl ether and water, where C 2- with C 4+ After releasing 2%, they return to 102 and 106 olefin conversion reactors respectively, and the unconverted dimethyl ether returns to 104 main reactor. The reaction temperature in the main reactor 104 is 400 ° C, the pressure is 1 MPa, and the weight space velocity of the feed (including circulating dimethyl ether) is 10 hr -1 ;C 2 The reaction temperature in the olefin ...

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Abstract

The invention discloses a manufacturing method of propylene and multi-layer fluid bed reactor structure as main reacting region or olefin transmitting region, which is characterized by the following: separating C2 and component less than C2, C4 and component less than C4 with object product propylene; circulating; returning to fluid bed in the catalytic crack reacting device; transmitting olefin; controlling operating condition to manufacture propylene selectively; avoiding inert component from accumulating.

Description

technical field [0001] The invention relates to a method and a device for producing propylene by catalytic cracking, especially suitable for the process of producing propylene by catalytic cracking of alcohol and ether, and belongs to the technical field of chemical engineering. Background technique [0002] Ethylene and propylene are two basic organic chemical raw materials that are widely used and in great demand. At present, the production of ethylene and propylene mainly relies on co-production of steam cracking unit and by-product of refinery. In recent years, with the rapid increase in demand for propylene derivatives (such as polypropylene, acrylonitrile, acrylic acid, propylene oxide, etc.), the world's propylene demand has shown a strong growth trend, and its growth rate has exceeded that of ethylene. In the future, the world may face a shortage of propylene resources. [0003] Steam cracking co-production of propylene is currently the most important source of pro...

Claims

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Application Information

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IPC IPC(8): C07C1/20C07C7/00C07C11/06B01J8/18
Inventor 王垚魏飞钱震袁学民周华群刘家强
Owner CHINA NAT CHEM ENG GRP CORP LTD
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