Method for producing light olefins

A low-carbon olefin and regenerant technology, which is applied in the production of bulk chemicals, processing of hydrocarbon oil, and hydrocarbon cracking to produce hydrocarbons, etc., can solve the problems of low olefin yield, low coke yield, and high coke yield, and achieve olefin low yield effect

Active Publication Date: 2021-04-06
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0012] The purpose of the present invention is to overcome the defect that the olefin yield is not high and the coke yield is relatively high in the production of ethylene-based olefin products in the prior art, and to provide an olefin yield under the premise of ensuring low energy consumption A method with higher coke yield and lower coke yield to produce mainly ethylene from raw materials containing heavy oil, with by-products of propylene and triphenylaromatics

Method used

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  • Method for producing light olefins
  • Method for producing light olefins
  • Method for producing light olefins

Examples

Experimental program
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specific Embodiment approach

[0043] The raw material oil 2 and water vapor 1 are introduced into the first cracking reaction zone 3 containing the first contact agent through the pipeline for cracking reaction, and then the steam 1 and the stream in the first cracking reaction zone 3 are introduced into the second contacting The cracking reaction is carried out in the second cracking reaction zone 4 of the agent; then the stream after the cracking reaction obtained on the top or top of the second cracking reaction zone 4 is condensed to obtain gaseous substances, liquid substances and carbon deposition contact agents, and cracked products 10 out of the reaction system; the carbon-deposited catalyst is introduced into the regenerator 7 containing oxygen-containing gas 5 through the pipeline for coking treatment to obtain the regenerant, and the flue gas 11 produced in the regenerator 7 is discharged from the top of the regenerator 7 Draw out the reaction system; and introduce part of the regenerant directly...

Embodiment 1

[0055] According to this embodiment figure 1 The process route shown is carried out, specifically, in the present embodiment:

[0056] The raw oil and water vapor enter the first cracking reaction zone after preheating, the contact agent is MFC-2, and the process conditions are: reaction temperature 500°C, water-oil ratio 0.10, weight hourly space velocity 4h -1 , pressure 0.15MPa. The stream after the cracking reaction and part of the water vapor from the external pipeline enter the second cracking reaction zone. The process conditions are: reaction temperature 700°C, water-to-oil ratio 0.5, weight hourly space velocity 20h -1 , pressure 0.15MPa. The coke contact agent obtained after the contact cracking reaction enters the settler for stripping and then enters the regenerator for charring treatment. The process conditions are: the temperature in the dense-phase bed is 750 ° C, and the air is charred. Part of the regenerated agent after charring enters the second cracking ...

Embodiment 2

[0059] According to this embodiment figure 1 The process route shown is carried out, specifically, in the present embodiment:

[0060] The raw oil and water vapor enter the first cracking reaction zone after preheating, the contact agent is MFC-1, and the process conditions are: reaction temperature 540°C, water-oil ratio 0.20, weight hourly space velocity 12h -1 , pressure 0.28MPa. The stream after the cracking reaction and part of the water vapor from the external pipeline enter the second cracking reaction zone. The process conditions are: reaction temperature 620°C, water-to-oil ratio 0.9, weight hourly space velocity 40h -1 , pressure 0.28MPa. The coke contact agent obtained after the contact cracking reaction enters the settler for stripping and then enters the regenerator for charring treatment. The process conditions are: the temperature in the dense-phase bed is 700 ° C, and the air is charred. Part of the regenerated agent after charring enters the second cracking...

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Abstract

The invention relates to the field of production of low-carbon olefins, and discloses a method for producing low-carbon olefins. The method comprises: sequentially introducing raw material oil and water vapor into a first cracking reaction zone and a second cracking reaction zone to perform a cracking reaction; obtaining Coke contact agent; then coking the coke catalyst to obtain regenerant; and introducing part of the regenerant directly into the second cracking reaction zone, and introducing the remaining part of the regenerant into the first cracking reaction zone after heat exchange In the reaction zone, the weight ratio of the regeneration agent introduced into the first cracking reaction zone and the second cracking reaction zone is 1: (1-8), and the cracking reaction temperature of the first cracking reaction zone is higher than that of the second cracking reaction zone The temperature of the cracking reaction is low. The method for producing low-carbon olefins provided by the present invention can mainly produce ethylene from raw materials containing heavy oil with higher olefin yield and lower coke yield under the premise of ensuring lower energy consumption, while by-product propylene and triphenylaromatics.

Description

technical field [0001] The invention relates to the field of production of low-carbon olefins, in particular to a method for producing low-carbon olefins. Background technique [0002] Low-carbon olefins such as ethylene and propylene are important organic chemical raw materials. At present, the industrial production of ethylene and propylene mainly includes steam cracking and catalytic cracking. [0003] The steam cracking method uses a high-temperature method for cracking. The range of raw materials includes gaseous hydrocarbons, light oil (naphtha), kerosene, light diesel oil, and heavy diesel oil. The cracking temperature is generally 750-900°C. The reaction is carried out in a furnace tube, and the reacted product is rapidly cooled at the outlet of the furnace to terminate its reaction, and then separated by a fractionating tower to obtain cracked gas, cracked gasoline, cracked diesel and cracked tar. The yield of ethylene in the light olefins obtained by steam cracki...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G51/02C07C4/04C07C11/02C07C11/04C07C15/02
CPCC07C4/04C10G51/02C10G2400/20C07C11/04C07C11/02C07C15/02Y02P20/52Y02P20/584
Inventor 张书红龙军李延军申海平李子锋任磊
Owner CHINA PETROLEUM & CHEM CORP
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