A method for synthesizing methane by adiabatic cooling type methanation

A methanation and chemical synthesis technology, applied in the petroleum industry, gas fuels, fuels, etc., can solve the problems of high energy consumption for isothermal methanation and high investment in adiabatic methanation, prolong service life, reduce side reactions of methanation, ensure effect of life

Inactive Publication Date: 2017-03-15
四川月新达科新能源科技有限公司
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  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0005] The object of the present invention is: Based on the above problems, adiabatic cooling type methanation synthesis methane process is proposed, so as to solve the problems of high energy consumption and high investment of adiabatic methanation in isothermal methanation

Method used

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  • A method for synthesizing methane by adiabatic cooling type methanation
  • A method for synthesizing methane by adiabatic cooling type methanation
  • A method for synthesizing methane by adiabatic cooling type methanation

Examples

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Effect test

Embodiment 1

[0034] The technical flow of the low-pressure high-carbon monoxide raw material gas adiabatic cooling type methanation to synthesize methane in this embodiment is as follows:

[0035] Process such as figure 1 shown. In this embodiment, the raw material gas is a low-pressure high-carbon monoxide gas, the raw material gas pressure is ~0.93MPa(G), the temperature is normal temperature, and the flow rate is ~51000 Nm 3 / h, the main composition of the gas is CO: 20%, CO2: 3%, H2: 74%, CH4: 1.4%. It enters the heat exchanger E3 and exchanges heat with the gas at the outlet of the hot water tower. The raw gas is heated to ~110°C. Then it is divided into two parts: ~40% raw material gas is mixed with the same flow rate after heating, CO: ~10%, CO2: ~2%, H2: ~45.7%, CH4: ~38.5% after mixing, enter the saturation tower T1, the temperature of the raw material gas from the saturation tower T1 is ~129°C, the water content is ~26.5%, and it enters the heat exchanger E1 to exchange heat wi...

Embodiment 2

[0040] The low-pressure feed gas adiabatic cooling type methanation synthesis methane production process of LNG in this embodiment is as follows:

[0041] Process such as figure 2 shown. The raw material gas in this example is a low-pressure raw material gas, the raw material gas pressure is ~0.93MPa(G), the temperature is normal temperature, and the flow rate is ~60000 Nm 3 / h, the main composition of the gas is CO: 8.6%, CO2: 3%, H2: 60%, CH4: 24%, enters the heat exchanger E3 and exchanges heat with the gas at the outlet of the hot water tower T2, and the raw gas is heated to ~113°C , and then enter the saturation tower T1, the temperature of the raw material gas from the saturation tower T1 is ~123°C, the water content is ~22%, enter the heat exchanger E1 and exchange heat with the reaction gas coming out of the adiabatic cooling type methanation reactor R1, and the raw gas is heated to ~250°C enters the adiabatic cooling type methanation reactor R1, the temperature of ...

Embodiment 3

[0046] The flow process of the medium-pressure high-carbon monoxide raw material gas adiabatic cooling type methanation synthesis methane to LNG in this embodiment is as follows:

[0047] Process such as image 3 shown. In this example, the raw material gas is a medium-pressure high carbon monoxide gas, the raw material gas pressure is ~2.0MPa(G), the temperature is normal temperature, and the flow rate is ~51000 Nm 3 / h, the main composition of the gas is CO: 20%, CO2: 3%, H2: 74%, CH4: 1.4%, enters the heat exchanger E3 and exchanges heat with the gas at the outlet of the hot water tower T2, and the raw gas is heated to ~142°C , and then divided into two parts: ~45% raw material gas is mixed with the same flow rate after heating, after mixing CO: ~10%, CO2: ~2.1%, H2: ~45%, CH4: ~40%, enter saturation Tower T1, the temperature of the feed gas coming out of the saturated tower T1 is ~148°C, the water content is ~22%, and it enters the heat exchanger E1 to exchange heat with...

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Abstract

The invention discloses an adiabatic cooling type methanation synthesis method for methane and belongs to natural gas synthesis technologies in the field of chemical engineering. The method includes setting a saturation tower and a hot water tower, using the hot water tower for recovering a great quantity of steam condensing heat contained in high-temperature gas after methanation reaction, then using the saturation tower for evaporating water in the heat recovered by the hot water tower to enable the heat, subjected to water evaporation, to enter feed gas, increasing water vapor content in the feed gas entering a methanator, controlling methanation equilibrium temperature and inhibiting side reaction, wherein the methanator is an adiabatic cooling type reactor. When a concentration sum of carbon monoxide and carbon dioxide in the feed gas is not less than 12%, a circulation machine is set to return the gas after the methanation reaction circularly, and the methanation adiabatic reaction equilibrium temperature is controlled to protect catalysts from being damaged by high temperature; two adiabatic cooling type reactors in series connection are set, and the feed gas is divided into two parts to enter the two adiabatic cooling type reactors respectively. The adiabatic cooling type methanation synthesis method for the methane is used for solving the problems of high equal-temperature methanation energy consumption and high adiabatic methanation investment.

Description

technical field [0001] The invention belongs to the synthetic natural gas technology in the field of chemical industry. Background technique [0002] At present, the methane synthesis process mainly includes adiabatic methanation process with circulation and isothermal methanation process without circulation. [0003] Using the isothermal methanation synthesis process without circulation, due to the fast methanation reaction speed, the reaction hot spot temperature will be close to the equilibrium temperature. For the raw material gas with high carbon monoxide and carbon dioxide content, the methanation hot spot temperature will be very high, and it is easy to occur at this time The carbon evolution reaction causes the methanation catalyst to fail. Although it is possible to directly add a large amount of steam to the feed gas to dilute the concentration of carbon monoxide and carbon dioxide in the feed gas to control the temperature of the methanation hot spot, due to the n...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10L3/08
Inventor 不公告发明人
Owner 四川月新达科新能源科技有限公司
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