Synthesis gas methanation reaction method

A technology of methanation reactor and gas methane, which is applied in the direction of gas fuel, petroleum industry, fuel, etc., and can solve problems such as complex process, low conversion rate of methanation reaction, and many heat exchange equipment

Active Publication Date: 2013-12-04
CHINA PETROLEUM & CHEM CORP +1
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  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0008] The technical problem to be solved by the present invention is the problems of low methanation reaction conversion rate, many heat exchange equipment, complicated process and high energy consumption of compressors existing in the previous syngas-to-SNG technology, and a new syngas-to-SNG method is provided. The method has the advantages of high methanation reaction conversion rate, less heat exchange equipment, simple flow process and low compressor energy consumption

Method used

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Effect test

Embodiment 1

[0023] 2 billion Nm 3 / year synthetic gas methanation to substitute natural gas plant (annual operating hours 8,000 hours), using figure 1 With advanced technology, the raw syngas is divided into three shares evenly at a pressure of 3.3MPa and a temperature of 30°C. The circulating gas from the compressor has a pressure of 3.3MPa and a temperature of 49°C. It is divided into three streams according to the ratio of 4:4:2, and is mixed with the raw material synthesis gas to enter the third-stage catalyst bed of the fixed-bed reactor, so that the temperature of the mixed gas entering the middle-stage catalyst bed is The temperature of the mixed gas entering the lower catalyst bed is 438°C. The mixed gas entering the upper catalyst bed first exchanges heat with the reaction gas in the heat exchanger, and then rises to 300°C before entering the catalyst bed. After the reaction product comes out of the reactor at 552°C, heat the mixed gas as mentioned above, the temperature of the ...

Embodiment 2

[0026] 2 billion Nm 3 / year synthetic gas methanation to replace natural gas installations, using figure 1 The process technology, the reaction gas is divided into two streams, 11% of the reaction gas is used as the feed of the lower methanation reactor, and 89% of the reaction gas is used as the cycle gas to mix with the raw synthesis gas. The temperature of the mixed gas entering the middle catalyst bed is 323°C, the temperature of the mixed gas entering the lower catalyst bed is 406°C, and the temperature of the methanation reaction gas product is 510°C. Other conditions are with embodiment 1. The conversion rate of the methanation reaction of this device is 77.0%, and the energy consumption of the compressor is 6585KW.

[0027]

Embodiment 3

[0029] 2 billion Nm 3 / year synthetic gas methanation to replace natural gas installations, using figure 1 The raw material synthesis gas is divided into three shares on average at 5.5MPa and 20°C, and the circulating gas exits the compressor at a temperature of 25°C and a pressure of 5.5MPa. Each catalyst bed of the stage fixed bed reactor makes the temperature of the mixed gas entering the middle catalyst bed be 379°C, the temperature of the mixture entering the lower stage catalyst bed is 448°C, and the product temperature of the methanation reactor is 567°C. Other process conditions are with embodiment 1.

[0030] The conversion rate of the methanation reaction of this device is 73.2%, and the energy consumption of the compressor is 2996KW.

[0031]

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Abstract

The present invention relates to a synthesis gas methanation reaction method, wherein problems of low methanation reaction conversion rate, more heat exchange equipment, complex process and high compressor energy consumption in the prior art are mainly solved with the present invention. The method comprises the following steps that: at a temperature of 20-60 DEG C under a pressure of 3.0-5.5 MPa, synthesis gas is divided into a plurality of parts, the plurality of the parts are mixed with circulation gas from a methanation reactor, and the obtained mixing gases are introduced into various bed layers of a multi-stage fixed bed reactor filled with a methanation catalyst, wherein a temperature of the mixed gas is controlled to 300-400 DEG C, and the mixed gas comprises the mixing gas and the reaction gas discharged from various catalyst bed layers; outlet gas comprising CH4, H2O, unconverted CO, unconverted CO2 and unconverted H2 is obtained from the reactor outlet; the mixing gas entering the first stage catalyst bed layer and the outlet gas of the methanation reactor are subjected to heat exchange to be heated to a temperature of 260-450 DEG C; and the methanation reactor outlet gas is divided into two parts, the one part is adopted as the circulation gas, and the other part enters the next stage methanation reactor. With the technical scheme, the problems are well solved, and the method can be used for industrial production of substitute natural gas preparation through synthesis gas.

Description

technical field [0001] The invention relates to a method for producing substitute natural gas (SNG) by methanation of synthesis gas. Background technique [0002] Natural gas is a low-pollution, high-calorific-value clean energy that can make up for the increasingly scarce oil resources to a certain extent. However, my country's natural gas reserves are small and the demand for natural gas is growing rapidly. It is estimated that my country's current natural gas gap is about 20 billion m3 . my country is rich in coal resources, so the methanation of synthetic gas from coal gasification to substitute natural gas (SNG) can effectively alleviate my country's demand for natural gas. [0003] The main components of syngas are CO, CO 2 and H 2 , a large amount of methane is produced through the methanation reaction, and the reaction equation is: [0004] [0005] The methanation reaction is a strongly exothermic reaction, depending on the initial methane content, the single-...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10L3/08
Inventor 刘文杰郭毅
Owner CHINA PETROLEUM & CHEM CORP
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