CN101445755B - Method for purifying and liquefying coalbed gas - Google Patents
Method for purifying and liquefying coalbed gas Download PDFInfo
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- CN101445755B CN101445755B CN2008102299991A CN200810229999A CN101445755B CN 101445755 B CN101445755 B CN 101445755B CN 2008102299991 A CN2008102299991 A CN 2008102299991A CN 200810229999 A CN200810229999 A CN 200810229999A CN 101445755 B CN101445755 B CN 101445755B
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- deoxidation
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Abstract
The invention relates to a method for purifying and liquefying coalbed gas, the method is used for purifying and liquefying the exhausted oxygen-containing mixed coalbed gas of worked-out areas and mining areas, and the method is mainly realized through the following process: raw material coalbed gas-deoxidation-pressure boosting-decarburization-dehydration-denitrification-storage and transportation, wherein, the dioxidation is carried out as follows: the sulfur-tolerant catalytic deoxidation process mixes the raw material coalbed gas with part of deoxidizing circulating gas in a gas cabinet at 70KPa, the mixed gas enters a reactor after pre-heating by a pre-heater, methane and oxygen are reacted in a catalyst bed within a certain temperature range to generate CO2 and H2O; then the pressure boosting is carried out, the MEA plus MDEA decarburization process is adopted for decarburization, the physical absorption method is utilized for dehydration, the mixed refrigerant process is adopted for denitrification, and the storage and the transportation are carried out according to the standards. The method solves the problems that the deoxidization after pressure boosting is unsafe and the daily processing capacity of the raw material layer for production is small of the prior art. The method can be widely used for purifying and liquefying the exhausted oxygen-containing mixed coalbed gas of the worked-out areas and the mining areas.
Description
Technical field:
The present invention relates to goaf, moving exploiting field pump drainage contains oxygen and mixes coal bed gas and purify a kind of method for purifying and liquefying coalbed gas of liquefaction usefulness.
Background technology:
Present domestic coalbed methane containing oxygen purifying and liquefying research ground zero; In July, 2007; Beijing agrees with the International Investment Company and Co., Ltd of YangQuan Mine group to build up first coalbed methane containing oxygen purifying and liquefying device in Yangquan, Shanxi; This device day output is 5000 cubic metres, and its technological process is: supercharging-decarburization, sulphur-dehydration-liquefaction denitrogenation, deoxidation-accumulating.Existing coalbed methane containing oxygen purifying and liquefying technological process is deoxidation after the first supercharging, and the problem that this kind method exists is dangerous, and day processing raw material coal seam production capacity is little, has satisfied not the production needs.
The utility model content:
The purpose of this invention is to provide a kind of method for purifying and liquefying coalbed gas, after this method has solved the first supercharging that exists in the prior art deoxidation dangerous, it is little day to handle raw material coal seam production capacity, has satisfied not the problem of production needs.
The technical solution adopted for the present invention to solve the technical problems is: a kind of method for purifying and liquefying coalbed gas, this method are to solve the safety problem of mixing the coal bed gas compression: with oxygen, nitrogen, carbon dioxide safe separating.Purpose is to bring up to more than 95% by 30% mixing coal bed gas concentration, improves GAS QUALITY, extended hybrid coal bed gas approaches and methods, and method and technology main points of the present invention are: deoxidation before supercharging, the safety of assurance supercharging; The sulfur-tolerant type Catalytic processes is adopted in deoxidation, has anti-sulphur property, saves desulfurization link expense, and its operating cost descends 20% than coke method; Adopt ripe MEA+MDEA decarbonization process, the physisorphtion in the solid drier absorption method is adopted in dehydration, and sorbing material adopts the 4A molecular sieve; Mixed refrigeration process is selected in denitrogenation for use: because N in the raw material coal bed gas
2Content is very high, so when design adds denitrification column, utilizes the falling liquid film separation principle to remove N a large amount of in the coal bed gas
2, have higher calorific value to guarantee product LCBM; Strengthen daily handling ability, suitable with conventional gas LNG ability.
Method for purifying and liquefying coalbed gas is realized through following technology: raw material coal bed gas-deoxidation-supercharging-decarburization-dehydration-denitrogenation-accumulating.Deoxidation: the sulfur-tolerant type catalytic deoxidation process be the raw material coal bed gas under 70Kpa with gas holder in part deoxidation circulating air mix, after the preheater preheating, get into reactor, in 500 ℃ of-700 ℃ of temperature ranges, methane and oxygen generate CO at the beds internal reaction
2And H
2O; High temperature deoxidation gas entering preheater and reactor feed gas produce the Steam Recovery heat through waste heat boiler after the heat handing-over, after cooling, get into gas holder; Supercharging: the coal bed gas after the deoxidation at first gets into coal bed gas and divides flow container, and the liquid that is produced in the course of conveying is removed from coal bed gas; Deliver to filter again particle diameter is removed greater than 5 microns liquid and solid, bring supercharger into, supercharger is caused damage to avoid liquid; Coal bed gas after the filtration gets into supercharger and is compressed to 1.05Mpa, after cooler is cooled to 35 ℃, gets into decarburization then; Decarburization: adopt ripe monoethanolamine MEA+ methyl diethanolamine MDEA decarbonization process flow process, at 35 ℃, 1.05Mpa gets into CO down to coal bed gas after filtering, compressing
2Absorb at the bottom of the Tata, with the MEA solution counter current contacting of self-absorption column overhead entering, to absorb the CO in the coal bed gas
2Eject the coal bed gas of coming from the absorption tower and get into the cat head filter, the entrained liquid greater than 5 microns is removed, get into dehydration then; From absorbing rich amine aqueous solution at the bottom of the Tata, throttling is after after the poor rich liquid heat exchanger heating, get into the amine regenerator; Amine regenerator cat head gas phase is cooled to 60 ℃-70 ℃ through cooler, and the gas after the separation advances blowdown system, and liquid refluxes and all returns the amine regenerator, and from amine liquid heater heating at the bottom of regenerator of amine regenerator, gas phase is returned regenerator; Liquid phase gets into poor amine booster pump earlier after rich amine/poor amine heat exchanger cooling; Get into the top, absorption tower, begin a new circulation; Dehydration: adopt the physisorphtion in the solid drier absorption method, sorbing material is selected the 4A molecular sieve for use, 35 ℃ of adsorption temps, pressure 1.0Mpa, 8 hours time; 300 ℃ of regeneration temperatures, pressure 1.05Mpa, 5.5 hours time; 2.5 hours cold blowing time; Denitrogenation: adopt mixed refrigeration process, it is to utilize in many mixture the characteristic of condensation behind the condensation of heavy component elder generation, the light component, with their condensations successively, throttling; Evaporation obtains the cold of different temperatures level, makes component condensation corresponding in the natural gas and final all liquefaction; Select for use cold-producing medium to be selected from following two kinds: a kind of is by N
2, C
1, C
2And C
3The mix refrigerant of forming; Another kind is the ammonia auxiliary refrigerant, through the raw material coal bed gas of deoxidation through under 35 ℃, 1.0Mpa, obtaining-154 ℃ through auxiliary cooling, hybrid refrigeration respectively, the LCBM of 0.896Mpa after separating and filtering, compression, carbon dioxide removal, the dehydration; Obtain-153.8 ℃ through the throttling step-down again, the product LCBM of 0.3Mpa; For guaranteeing that transportation LCBM does not gasify, product is crossed cold 0.6 ℃ and is sent into the LCBM storage tank; Accumulating: the pressure store according to the LNG product can be divided into normal pressure storage and the storage of band pressure with storage mode, takes all factors into consideration the terms and conditions of this project product LCBM and selects for use the band pressure to store the tank wagon means of transportation.
The invention has the beneficial effects as follows: compressing secure is guaranteed, and before cooling, separating is in technological process, and especially the cooled compressed gas purity is outside explosion limit; Disposal ability is strong, and a day processing improves an one magnitude, the suitable conventional gas LNG of daily handling ability; The gas emptying improves the gas exhaust utilization rate to the pollution of atmosphere in the minimizing coal mining process; But mass development utilizes the old man to remain gas, enlarges the transportation of mixing coal bed gas and utilizes radius.
Description of drawings:
Fig. 1 is a sulfur-tolerant type catalyst deoxidization technique sketch among the present invention.
Fig. 2 is a mixed refrigeration process sketch map among the present invention.
The specific embodiment:
In Fig. 1; Technology in a kind of method for purifying and liquefying coalbed gas; Deoxidation: the sulfur-tolerant type catalytic deoxidation process be the raw material coal bed gas under 70Kpa with gas holder in part deoxidation circulating air mix; After the preheater preheating, get into reactor, in 500 ℃ of-700 ℃ of temperature ranges, methane and oxygen generate CO at the beds internal reaction
2And H
2O; High temperature deoxidation gas entering preheater and reactor feed gas produce the Steam Recovery heat through waste heat boiler after the heat handing-over, after cooling, get into gas holder;
In Fig. 2, method for purifying and liquefying coalbed gas is realized through following technology: raw material coal bed gas-deoxidation-supercharging-decarburization-dehydration-denitrogenation-accumulating: from Fig. 1, carry out supercharging after the deoxidation again; Supercharging: the coal bed gas after the deoxidation at first gets into coal bed gas and divides flow container, and the liquid that is produced in the course of conveying is removed from coal bed gas; Deliver to filter again particle diameter is removed greater than 5 microns liquid and solid, bring supercharger into, supercharger is caused damage to avoid liquid; Coal bed gas after the filtration gets into supercharger and is compressed to 1.05Mpa, after cooler is cooled to 35 ℃, gets into decarburization then; Decarburization: adopt ripe monoethanolamine MEA+ methyl diethanolamine MDEA decarbonization process flow process: at 35 ℃, 1.05Mpa gets into CO down to coal bed gas after filtering, compressing
2Absorb at the bottom of the Tata, with the MEA solution counter current contacting of self-absorption column overhead entering, to absorb the CO in the coal bed gas
2Eject the coal bed gas of coming from the absorption tower and get into the cat head filter, the entrained liquid greater than 5 microns is removed, get into dehydration then; From absorbing rich amine aqueous solution at the bottom of the Tata, throttling is after after the heating of rich or poor solution heat exchanger, get into the amine regenerator; Amine regenerator cat head gas phase is cooled to 60 ℃-70 ℃ through cooler, and the gas after the separation advances blowdown system, and liquid refluxes and all returns the amine regenerator, and from amine liquid heater heating at the bottom of regenerator of amine regenerator, gas phase is returned regenerator; Liquid phase gets into poor amine booster pump earlier after rich amine/poor amine heat exchanger cooling; Get into the top, absorption tower, begin a new circulation; Dehydration: adopt the physisorphtion in the solid drier absorption method, sorbing material is selected the 4A molecular sieve for use, 35 ℃ of adsorption temps, pressure 1.0Mpa, 8 hours time; 300 ℃ of regeneration temperatures, pressure 1.05Mpa, 5.5 hours time; 2.5 hours cold blowing time; Denitrogenation: adopt mixed refrigeration process, it is to utilize in many mixture the characteristic of condensation behind the condensation of heavy component elder generation, the light component, with their condensations successively, throttling; Evaporation obtains the cold of different temperatures level, makes component condensation corresponding in the natural gas and final all liquefaction; Select for use cold-producing medium to be selected from following two kinds: a kind of is by N
2, C
1, C
2And C
3The mix refrigerant of forming; Another kind is the ammonia auxiliary refrigerant, through the raw material coal bed gas of deoxidation through under 35 ℃, 1.0Mpa, obtaining-154 ℃ through auxiliary cooling, hybrid refrigeration respectively, the LCBM of 0.896Mpa after separating and filtering, compression, carbon dioxide removal, the dehydration; Obtain-153.8 ℃ through the throttling step-down again, the product LCBM of 0.3Mpa; For guaranteeing that transportation LCBM does not gasify, product is crossed cold 0.6 ℃ and is sent into the LCBM storage tank; Accumulating: the pressure store according to the LNG product can be divided into normal pressure storage and the storage of band pressure with storage mode, takes all factors into consideration the terms and conditions of this project product LCBM and selects for use the band pressure to store the tank wagon means of transportation.
Claims (1)
1. method for purifying and liquefying coalbed gas; It is characterized in that this method realizes through following technology: raw material coal bed gas-deoxidation-supercharging-decarburization-dehydration-denitrogenation-accumulating: deoxidation: the sulfur-tolerant type catalytic deoxidation process be the raw material coal bed gas under 70Kpa with gas holder in part deoxidation circulating air mix; After the preheater preheating, get into reactor; In 500 ℃ of-700 ℃ of temperature ranges, methane and oxygen generate CO at the beds internal reaction
2And H
2O; High temperature deoxidation gas entering preheater and reactor feed gas produce the Steam Recovery heat through waste heat boiler after the heat handing-over, after cooling, get into gas holder; Supercharging: the coal bed gas after the deoxidation at first gets into coal bed gas and divides flow container, and the liquid that is produced in the course of conveying is removed from coal bed gas; Deliver to filter again particle diameter is removed greater than 5 microns liquid and solid, bring supercharger into, supercharger is caused damage to avoid liquid; Coal bed gas after the filtration gets into supercharger and is compressed to 1.05Mpa, after cooler is cooled to 35 ℃, gets into decarburization then; Decarburization: adopt ripe monoethanolamine MEA+ methyl diethanolamine MDEA decarbonization process flow process: at 35 ℃, 1.05Mpa gets into CO down to coal bed gas after filtering, compressing
2Absorb at the bottom of the Tata, with the MEA solution counter current contacting of self-absorption column overhead entering, to absorb the CO in the coal bed gas
2Eject the coal bed gas of coming from the absorption tower and get into the cat head filter, the entrained liquid greater than 5 microns is removed, get into dehydration then; From absorbing rich amine aqueous solution at the bottom of the Tata, throttling is after after the poor rich liquid heat exchanger heating, get into the amine regenerator; Amine regenerator cat head gas phase is cooled to 60 ℃-70 ℃ through cooler, and the gas after the separation advances blowdown system, and liquid refluxes and all returns the amine regenerator, and from amine liquid heater heating at the bottom of regenerator of amine regenerator, gas phase is returned regenerator; Liquid phase gets into poor amine booster pump earlier after rich amine/poor amine heat exchanger cooling; Get into the top, absorption tower, begin a new circulation; Dehydration: adopt the physisorphtion in the solid drier absorption method, sorbing material is selected the 4A molecular sieve for use, 35 ℃ of adsorption temps, pressure 1.0Mpa, 8 hours time; 300 ℃ of regeneration temperatures, pressure 1.05Mpa, 5.5 hours time; 2.5 hours cold blowing time; Denitrogenation: adopt mixed refrigeration process, it is to utilize in many mixture the characteristic of condensation behind the condensation of heavy component elder generation, the light component, with their condensations successively, throttling; Evaporation obtains the cold of different temperatures level, makes component condensation corresponding in the natural gas and final all liquefaction; Select for use cold-producing medium to be selected from following two kinds: a kind of is by N
2, C
1, C
2And C
3The mix refrigerant of forming; Another kind is the ammonia auxiliary refrigerant, through the raw material coal bed gas of deoxidation through under 35 ℃, 1.0Mpa, obtaining-154 ℃ through auxiliary cooling, hybrid refrigeration respectively, the LCBM of 0.896Mpa after separating and filtering, compression, carbon dioxide removal, the dehydration; Obtain-153.8 ℃ through the throttling step-down again, the product LCBM of 0.3Mpa; For guaranteeing that transportation LCBM does not gasify, product is crossed cold 0.6 ℃ and is sent into the LCBM storage tank; Accumulating: the pressure store according to the LNG product can be divided into normal pressure storage and the storage of band pressure with storage mode, takes all factors into consideration the terms and conditions of this project product LCBM and selects for use the band pressure to store the tank wagon means of transportation.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008102299991A CN101445755B (en) | 2008-12-22 | 2008-12-22 | Method for purifying and liquefying coalbed gas |
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| CN2008102299991A CN101445755B (en) | 2008-12-22 | 2008-12-22 | Method for purifying and liquefying coalbed gas |
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| CN101445755B true CN101445755B (en) | 2012-11-28 |
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Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101818984B (en) * | 2010-04-21 | 2012-05-30 | 中国石油大学(北京) | Full liquefying separation process for air-containing coal bed gas |
| CN102538398B (en) * | 2012-02-09 | 2013-11-06 | 杭州杭氧股份有限公司 | Process and system for purifying, separating and liquefying nitrogen-and-oxygen-containing coal mine methane (CMM) |
| CN102839028B (en) * | 2012-09-18 | 2014-03-19 | 新地能源工程技术有限公司 | Energy-saving method of deoxidizing coalbed methane |
| CN103740430B (en) * | 2013-12-27 | 2015-05-13 | 中国矿业大学(北京) | Low-rank coal alcoholysis deoxidization method |
| CN106440658A (en) * | 2016-09-27 | 2017-02-22 | 上海安恩吉能源科技有限公司 | Combination process for preparing liquefied natural gas (LNG) through high-oxygen-content and high-nitrogen-content coalbed methane |
| CN106621692A (en) * | 2017-03-06 | 2017-05-10 | 成都赛普瑞兴科技有限公司 | Joint regeneration purifying system and purifying method |
| CN113108551A (en) * | 2021-05-17 | 2021-07-13 | 中石化中原石油工程设计有限公司 | Process and device for extracting high-purity helium in liquefied natural gas production process |
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| US5388645A (en) * | 1993-11-03 | 1995-02-14 | Amoco Corporation | Method for producing methane-containing gaseous mixtures |
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| CN101250449A (en) * | 2008-04-17 | 2008-08-27 | 西南化工研究设计院 | Catalytic conversion deoxidation method of coal-bed gas |
| CN101285639A (en) * | 2008-06-05 | 2008-10-15 | 上海交通大学 | Pre-cooled type coal bed gas nitrogen dilated and liquefied process taking advantage of variable pressure for adsorbing residual pressure |
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2008
- 2008-12-22 CN CN2008102299991A patent/CN101445755B/en not_active Expired - Fee Related
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|---|---|---|---|---|
| US5388645A (en) * | 1993-11-03 | 1995-02-14 | Amoco Corporation | Method for producing methane-containing gaseous mixtures |
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Address after: 124010 Xinglongtai, Liaoning Province, oil street, No. 96, No. Applicant after: Chinese Petroleum Group Changcheng Drilling Engineering Co., Ltd. Address before: 100724 No. 6, Kang Street, six, Xicheng District, Beijing Applicant before: Chinese Petroleum Group Changcheng Drilling Engineering Co., Ltd. |
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Granted publication date: 20121128 Termination date: 20131222 |