Process for synthesizing LNG (Liquefied Natural Gas) and coproducing liquid ammonia by using methanol purge gas

A methanol degassing and methanol synthesis technology, applied in the preparation/separation of ammonia, petroleum industry, gas fuel, etc., can solve the problems of poor economic benefits and inability to use gas, achieve pure raw materials, reduce compression work loss, and reduce methane The effect of high content

Inactive Publication Date: 2016-07-06
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

Among these two methods, the economic benefits of the former are poor, and the latter cannot make full use of most of the gas in the purge gas at the same time.

Method used

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  • Process for synthesizing LNG (Liquefied Natural Gas) and coproducing liquid ammonia by using methanol purge gas

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0027] The methanol purge gas composition (vol%) in this example is: H276.79, CH42.97, CO3.39, CO24.04, N210.58, CH 3 OH2.1, H 2 O0.13. Methanol release gas volume is 30983Nm 3 / h, temperature 40°C, pressure 5.50MPa.

[0028] The above-mentioned methanol purge gas is directly preheated to 280°C and enters the primary methane synthesis reactor for reaction. The outlet temperature of the primary methane synthesis reactor is 640°C; a part of the outlet gas of the secondary methane synthesis reactor is recycled to the primary methane At the inlet of the synthesis reactor, the molar ratio of the recycle gas to the methanol purge gas entering the primary methane synthesis reactor in this embodiment is 0.3. The outlet composition (vol%) of the secondary methane synthesis reactor is: H242.9, CH48.6, CO5ppm, CO210ppm, N214.3, CH 3 OH7,H 2 O27.2.

[0029] Separation of methane: The purge gas after secondary methane synthesis enters the cryogenic separation device for cryogenic sep...

Embodiment 2

[0033] The methanol purge gas composition (vol%) in this example is: H275.04, CH42.97, CO4.92, CO24.04, N210.80, CH 3 OH2.1, H 2 O0.13. Methanol release gas volume is 30983Nm 3 / h, temperature 40°C, pressure 5.50MPa.

[0034]The above-mentioned methanol purge gas is directly preheated to 280°C and enters the primary methane synthesis reactor for reaction. The outlet temperature of the primary methane synthesis reactor is 650°C; a part of the outlet gas of the secondary methane synthesis reactor is recycled to the primary methane At the entrance of the synthesis reactor, the molar ratio of the recycle gas to the methanol purge gas entering the primary methane synthesis reactor in this embodiment is 0.25. The outlet composition (vol%) of the secondary methane synthesis reactor is: H240.9, CH49.2, CO8ppm, CO210ppm, N215.3, CH 3 OH7.2, H 2 O27.4.

[0035] Separation of methane: The purge gas after secondary methane synthesis enters the cryogenic separation device for cryogen...

Embodiment 3

[0039] The methanol purge gas composition (vol%) in this example is: H276.38, CH42.97, CO5.0, CO24.04, N29.58, CH 3 OH1.9, H 2 O0.13. Methanol release gas volume is 30983Nm 3 / h, temperature 40°C, pressure 5.50MPa.

[0040] The above-mentioned methanol purge gas is directly preheated to 280°C and enters the primary methane synthesis reactor for reaction. The outlet temperature of the primary methane synthesis reactor is 650°C; a part of the outlet gas of the secondary methane synthesis reactor is recycled to the primary methane At the entrance of the synthesis reactor, the molar ratio of the recycle gas to the methanol purge gas entering the primary methane synthesis reactor in this embodiment is 0.4. The outlet composition (vol%) of the secondary methane synthesis reactor is: H240.2, CH49.2, CO6ppm, CO210ppm, N213.3, CH 3 OH6.9, H 2 O30.4.

[0041] Separation of methane: The purge gas after secondary methane synthesis enters the cryogenic separation device for cryogenic...

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Abstract

The invention belongs to the field of energy and chemical industry, and discloses a process for synthesizing LNG and co-producing liquid ammonia by utilizing methanol purge gas. Under the action of a methane synthesis catalyst, the methanol purge gas produced from methanol synthesis is directly preheated to 250°C~350°C and enters the The methane synthesis unit performs a methane synthesis reaction. The obtained methane gas enters the cryogenic separation and liquefaction process after being cooled and dehydrated. Liquefied natural gas (LNG) is obtained in the bottom of the rectification tower. The yield of LNG is 95%~100%. Hydrogen gas and hydrogen-rich gas enter the pressure swing adsorption separation process after recovery of cooling capacity. The hydrogen-rich gas is separated from hydrogen, nitrogen and methane in the pressure swing adsorption separation device to obtain hydrogen, nitrogen and methane respectively, and then the nitrogen is pressurized and mixed with hydrogen to enter the ammonia synthesis process according to the hydrogen-nitrogen ratio of 2.9~3.1 , hydrogen and nitrogen that meet the conditions are mixed and then pressurized to 12.0MPa~30.0MPa to enter the ammonia synthesis tower to produce liquid ammonia.

Description

technical field [0001] The invention relates to an application technology of methanol purge gas, and provides a process for synthesizing LNG and co-producing liquid ammonia by using methanol purge gas. Background technique [0002] Natural gas is an efficient and clean energy, but due to the lack of natural gas resources in my country, its supply is far from meeting market demand. Coal-to-synthetic natural gas is an important way to alleviate the contradiction between supply and demand of natural gas, and it is a new coal chemical project supported by the country during the "Twelfth Five-Year Plan" period. [0003] On the other hand, my country's methanol production uses coal as the main raw material. During the methanol synthesis process of coal-to-methanol enterprises, a large amount of H 2 , CO, CO 2 , CH 4 and N 2 As the main component of Chi gas. According to each ton of methanol, 601.5Nm3 / h of purge gas can be produced. The typical composition of purge gas is show...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10L3/08C10L3/10C01C1/04
Inventor 吴琳朱艳芳徐本刚黄先亮张杰蔡进吴学其蔡成伟魏士新
Owner CHINA PETROLEUM & CHEM CORP
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