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A kind of preparation method and preparation device of substitute natural gas

A technology for substituting natural gas and preparation device, which is applied in the field of substituting natural gas preparation and synthesis gas preparation substituting natural gas, can solve the problems of catalyst wear and consumption, low CH4 selectivity, etc., to reduce wear and consumption, improve CO conversion rate and product The effect of CH4 yield and yield increase

Active Publication Date: 2021-04-30
PETROCHINA CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

The synthesis gas first enters the slurry bed reaction, and most of the methanation reaction with strong exotherm is carried out in the slurry bed. The slurry bed methanation reactor is in a state of high space velocity, which will inevitably cause wear and consumption of the catalyst; the slurry bed Reactor tail gas produces side reactions, generating some low-carbon hydrocarbons and a small amount of oxygen-containing compounds; the slurry bed is at the front end of the combined process, and the temperature of the slurry bed is 270-380 ° C; the fixed bed is at the rear end, and the temperature of the fixed bed is higher at 350-500 ℃, the methanation reaction is a strong exothermic reaction, and high temperature is not conducive to the conversion to CH 4 The direction of generation proceeds, so CO conversion, CH 4 Not very selective

Method used

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  • A kind of preparation method and preparation device of substitute natural gas

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0056] Preparation of nickel-based catalyst:

[0057] Prepare a nickel nitrate solution with a cation concentration of 0.5g / ml, and add 10 to 40 meshes of γ-Al to it according to the composition of the catalyst 2 o 3 The carrier powder is impregnated for 22 hours under stirring conditions. After the impregnation, the suspension is heated and concentrated in a water bath at 60°C, then calcined at 450°C for 10 hours, and ground to 10-40 meshes after calcining.

[0058] In the nickel-based catalyst, the mass ratio of nickel nitrate to aluminum oxide is 14:9.

[0059] The nickel-based catalyst is reduced to generate a nickel catalyst 1 for use in the subsequent first methanation reaction in the first solid-state bed reactor.

Embodiment 2

[0061] Preparation of nickel-based catalyst:

[0062] Prepare a nickel nitrate solution with a cation concentration of 0.9g / ml, and add 10 to 40 meshes of γ-Al to it according to the composition of the catalyst 2 o 3 The carrier powder is impregnated for 12 hours under stirring conditions. After the impregnation, the suspension is heated and concentrated in a water bath at 70°C, then calcined at 550°C for 7 hours, and ground to 10-40 mesh after calcining.

[0063] In the nickel-based catalyst, the mass ratio of nickel nitrate to aluminum oxide is 16:9.

[0064] The nickel-based catalyst is reduced to generate a nickel catalyst 2, which is used in the subsequent second methanation reaction in the second solid-state bed reactor.

Embodiment 3

[0066] Preparation of nickel-based catalyst:

[0067] Prepare a nickel nitrate solution with a cation concentration of 0.8g / ml, and add 10 to 40 meshes of γ-Al to it according to the composition of the catalyst 2 o 3 The carrier powder is impregnated for 24 hours under stirring conditions. After the impregnation, the suspension is heated and concentrated in a water bath at 80°C, then calcined at 450°C for 10 hours, and ground to 10-40 meshes after calcining.

[0068] In the nickel-based catalyst, the mass ratio of nickel nitrate to aluminum oxide is 12:8.

[0069] The nickel-based catalyst is reduced to generate nickel catalyst 3, which is used in the third methanation reaction and the fourth methanation reaction in the first slurry bed reactor and the second slurry bed reactor.

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Abstract

The invention provides a preparation method and a preparation device for a substitute natural gas. The method includes the following steps: 1) After part of the raw material gas enters the first fixed-bed reactor for the first methanation reaction, the first reaction gas is generated, and the first reaction gas passes through After the first heat exchange, the first low-temperature gas is generated; 2) After the first low-temperature gas and the remaining raw material gas enter the second fixed-bed reactor for the second methanation reaction, the second reaction gas is generated, and the second reaction gas undergoes the second exchange process. After heating, the second low temperature gas is generated; 3) part of the second low temperature gas enters the first slurry bed reactor for the third methanation reaction to generate the third reaction gas, and the remaining second low temperature gas enters the second slurry bed reactor for The fourth methanation reaction generates a fourth reaction gas; 4) combining the third reaction gas and the fourth reaction gas to generate a mixed reaction gas, and performing a gas-liquid separation operation on the mixed reaction gas to obtain a substitute natural gas. The invention reduces equipment investment and corresponding energy consumption in the reaction process, and improves the conversion rate of carbon monoxide.

Description

technical field [0001] The invention relates to a technology for preparing a substitute natural gas from synthetic gas, in particular to a preparation method and a preparation device for a substitute natural gas, and belongs to the technical field of natural gas. Background technique [0002] Alternative natural gas (also known as coal-to-natural gas) is one of the key areas of modern coal chemical industry development in my country. According to data released by the National Bureau of Statistics, my country's coal-to-natural gas output reached 820 million cubic meters from January to July 2016, a year-on-year increase of 21.1%. . The core of the coal-to-natural gas process is the methanation of syngas. However, as a strongly exothermic reaction, each percent CO conversion during methanation can cause an adiabatic temperature rise of 74 °C. Therefore, how to effectively control the reaction bed temperature in the methanation process, so as to prevent catalyst deactivation c...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10L3/08
Inventor 展江宏张晓飞刘键林春兴王云娟许磊樊金龙魏书梅陈蓝天陈季敏张力贺春梅冯丽梅裴蓓
Owner PETROCHINA CO LTD
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