CN105972935A - Method for separating methane from oxygen-bearing coal mine methane - Google Patents
Method for separating methane from oxygen-bearing coal mine methane Download PDFInfo
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- CN105972935A CN105972935A CN201610290014.0A CN201610290014A CN105972935A CN 105972935 A CN105972935 A CN 105972935A CN 201610290014 A CN201610290014 A CN 201610290014A CN 105972935 A CN105972935 A CN 105972935A
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- methane
- containing oxygen
- tail gas
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- coalbed methane
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0223—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
Abstract
The invention relates to a method for separating methane from oxygen-bearing coal mine methane and belongs to the technical field of treatment for the oxygen-bearing coal mine methane. The method comprises the steps that S1, the oxygen-bearing coal mine methane is compressed; S2, the compressed oxygen-bearing coal mine methane is subjected to desulfurization, decarbonation, dehydration and demercuration; S3, the purified oxygen-bearing coal mine methane is cooled; S4, the cooled oxygen-bearing coal mine methane is sent into a separation device for separating, and methane and tail gases are obtained; S5, the methane is reheated and output as a product; S6, the tail gases are reheated, and one part of the tail gases is discharged and the other part of the tails gases is supercharged; and S7, the supercharged tail gases are cooled and sent into the separation device. The method is simple in process procedure, low in operating pressure, good in safety, needless of special arrangement of a deoxygenation procedure or a refrigerating system, low in energy consumption and high in methane recovery rate and methane purity, and the method is a safe and economical separating method for the oxygen-bearing coal mine methane.
Description
Technical field
The invention belongs to coalbed methane containing oxygen processing technology field, a kind of method relating to coalbed methane containing oxygen separation of methane.
Background technology
Coal bed gas needs extraction coal bed gas in drive to guarantee while belonging to the associated gas in coal production, particularly coal mining
The safety of coal mining, the coal bed gas methane content that this mode extraction obtains is low, usual volume fraction more than 20%, remaining
Composition is mainly air.Owing to air content is higher, the most oxygen-containing, this kind of coal bed gas deals with dangerous property or warp
Ji property is the highest, so way for a long time is by the burning of this coalbed methane containing oxygen or directly to discharge, causes energy waste and pollution.
Methane is reclaimed significant to the economy improving coal bed gas use value and coal production from coalbed methane containing oxygen.Mesh
The front method for coalbed methane containing oxygen isolated methane typically has hydration method, pressure swing adsorption method, membrane separation process, cryogenic rectification method
Deng.Wherein hydrate can only carry out laboratory proofing at present due to technical limitations, it is impossible to carries out industrial applications.Pressure-variable adsorption
Method and membrane separation process require that coalbed methane containing oxygen has certain pressure differential and can be only achieved separating effect, and this just requires that coal bed gas has relatively
High pressure maybe must meet the requirement of pressure differential to device evacuation.Low-temperature liquefaction and cryogenic rectification method also require that coalbed methane containing oxygen
Having certain pressure, this process uses rectification mode simultaneously, processes energy consumption higher, needs to arrange special refrigeration system
And refrigerant storage or device for making technological process are complicated, number of devices is many.
For coalbed methane containing oxygen utilizes, safety and economy are key issues, the most under low pressure process it, and
And it is the lowest more good to process energy consumption.Coalbed methane containing oxygen pressure is the highest the most dangerous, this be limit absorption method, membrane separation process application one
Individual key issue；And energy consumption is high, technological process is complicated is then the main cause limiting the application of cryogenic rectification method.
Summary of the invention
In view of this, a kind of method that it is an object of the invention to provide coalbed methane containing oxygen separation of methane, the method whole process is in
Low-pressure state, safety is good, and during separation, minimum pressure can as little as 50kPaG, the 0.3MPaG required much smaller than current technical scheme
Above.In the case of coalbed methane containing oxygen methane volumetric mark 20%, process energy consumption and be less than often mark side's methane product 0.9KWh, if
Methane volumetric mark improves then energy consumption and declines.Whole technique stream need not ad hoc deoxidation step, special refrigeration system, institute need not be set
Chilling requirement only separated by coalbed methane containing oxygen after methane and tail gas provide.
For reaching above-mentioned purpose, the present invention provides following technical scheme:
A kind of method of coalbed methane containing oxygen separation of methane, the method comprises the following steps: S1: be compressed by coalbed methane containing oxygen；
S2: by the coalbed methane containing oxygen desulfurization after compression, carbon dioxide removal, dehydration, demercuration；S3: the coalbed methane containing oxygen after purifying is cold
But；S4: the coalbed methane containing oxygen after cooling is sent into segregation apparatus isolated methane and tail gas；S5: using after methane re-heat as
Output of products；S6: after tail gas re-heat, partial tail gas discharges, partial tail gas supercharging；S7: after the tail gas after supercharging is cooled down
Send into segregation apparatus.
Further, in the method, in handled coalbed methane containing oxygen, methane volumetric mark is more than 20%, and remaining is the most empty
Gas.
Further, coalbed methane containing oxygen enters the minimum pressure of segregation apparatus is 50kPaG.
Further, described segregation apparatus uses device for extraction and distillation, and tower top does not set condenser.
Further, before methane re-heat, it is depressured to below 20kPaG, as product after the methane re-heat of coalbed methane containing oxygen isolated
Output, its re-heat is simultaneously used for cooling down coalbed methane containing oxygen and tail gas.
Further, in step s 6, the pressure after tail gas supercharging is 2.5～3.5MPaG.
Further, in the step s 7, reducing pressure by regulating flow is answered to enter back into segregation apparatus after tail gas cooling, the tail gas pressure after reducing pressure by regulating flow
Should be than the high 10kPa of coal bed gas pressure entering segregation apparatus.
Further, in the product that this method finally gives, methane volumetric mark is not less than 99.5%, methane in the tail gas of final discharge
Volume fraction is not higher than 0.5%.
The beneficial effects of the present invention is: the method technological process that the present invention proposes is simple, operation pressure is low, and safety is good, no
Using ad hoc deoxidation step, need not set special refrigeration system, energy consumption is low, and methane recovery is high, and methane purity is high, is a kind of peace
Complete economic coalbed methane containing oxygen separation method.
Accompanying drawing explanation
In order to make the purpose of the present invention, technical scheme and beneficial effect clearer, the present invention provides drawings described below to illustrate:
Fig. 1 is the concrete steps of coalbed methane containing oxygen isolated methane in the present invention；
Fig. 2 is detailed process and the equipment schematic diagram of the embodiment of the present invention；
Wherein: 1, coalbed methane containing oxygen compression device；2, absorption tower；3, dehydrating tower A；4, dehydrating tower B；5, demercuration tower；6、
Heat exchanger；7, stripping tower；8, vaporizer at the bottom of tower；9, tail-gas compressor；10, tail gas choke valve；11, methane choke valve.
Detailed description of the invention
Below in conjunction with accompanying drawing, the preferred embodiments of the present invention are described in detail.
Fig. 1 is the concrete steps of coalbed methane containing oxygen isolated methane in the present invention, as it can be seen, this method specifically includes following
Step: S1: coalbed methane containing oxygen is compressed；S2: will compression after coalbed methane containing oxygen desulfurization, carbon dioxide removal, dehydration,
Demercuration；S3: the coalbed methane containing oxygen cooling after purifying；S4: the coalbed methane containing oxygen after cooling is sent into segregation apparatus isolated
Methane and tail gas；S5: using after methane re-heat as output of products；S6: after tail gas re-heat, partial tail gas discharges, part tail
Gas supercharging；S7: send into segregation apparatus after being cooled down by the tail gas after supercharging.
Specifically:
Coalbed methane containing oxygen is first fed into compressor boost, and the coalbed methane containing oxygen pressure after supercharging should ensure that and enters the oxygen-containing of segregation apparatus
Coal bed gas pressure is not less than 50kPaG.Conventional compression device can be used, such as coal bed gas extraction pump, helical-lobe compressor, piston pressure
Contracting machine etc..
Coalbed methane containing oxygen after supercharging carries out purified treatment according to desulfurization, carbon dioxide removal, dehydration, the order of demercuration.After process
Coal bed gas in mercury content less than 0.1umg/m3, hydrogen sulfide content is less than 1ppm, and carbon dioxide content is less than 50ppm, water content
Less than 1ppm.Conventional process, such as desulfurization and carbon dioxide removal can be used to use alkanolamine solution absorption process；Dehydration uses
Molecular sieve adsorption；Demercuration uses sulfur-bearing active carbon adsorption.
Coalbed methane containing oxygen after purification is sent into heat exchanger and is cooled to-140 DEG C～-165 DEG C, in this course, cool down oxygen-containing coal seam
Methane and tail gas that the cold of gas is flowed out by segregation apparatus provide.
Coalbed methane containing oxygen after cooling sends into segregation apparatus, and segregation apparatus is made up of vaporizer at the bottom of stripping tower and tower.Containing after cooling
Oxygen coal bed gas enters in the middle part of stripping tower.The separation unit overhead discharge methane content tail gas less than 0.5%, arranges bottom segregation apparatus
Put the methane content liquid methane more than 99.5%.
The liquid methane of segregation apparatus bottom discharge exports as product methane after entering heat exchanger re-heat, and liquid methane enters heat exchange
Before device, pressure is reduced to below 20kPaG by available choke valve.
The tail gas of separation unit overhead discharge flows out after entering heat exchanger re-heat, wherein partial tail gas emptying, another part tail gas quilt
Entering reducing pressure by regulating flow after heat exchanger is cooled to-155 DEG C to-175 DEG C after supercharging, the tail gas pressure ratio after throttling enters segregation apparatus
Coalbed methane containing oxygen pressure height 10kPa.Tail gas after throttling enters segregation apparatus stripping tower, and feed entrance point is higher than coalbed methane containing oxygen
Enter the position of stripping tower.
Particularly, for making full use of energy, the tail gas of separation unit overhead discharge can be lowered the temperature by expander, reclaims its pressure
Power energy.
By said method, in the product finally given, methane volumetric mark is not less than 99.5%, methane in the tail gas of final discharge
Volume fraction is not higher than 0.5%.
Embodiment:
In the present embodiment, methane volumetric mark 20%, nitrogen fraction 62.7%, oxygen purity about 17%, remaining group
Partial volume mark 0.3%, including for hydrargyrum, hydrogen sulfide, carbon dioxide, water coalbed methane containing oxygen as a example by illustrate.According to Fig. 1
Represented enforcement step, gives specific implementation process and equipment schematic diagram in Fig. 2.
Coalbed methane containing oxygen initially enters coalbed methane containing oxygen compression device 1 and carries out supercharging, and after supercharging, pressure is 80kPaG, subsequently into
Absorption tower 2 utilizes absorbent solution removing hydrogen sulfide and carbon dioxide, and in the coalbed methane containing oxygen after removing, hydrogen sulfide content is less than 1ppm,
Carbon dioxide content is less than 50ppm.
Coalbed methane containing oxygen after desulfurization and decarburization enters dehydrating tower A3.In dehydrating tower A3, filling 4A molecular sieve, is used for adsorbing oxygen-containing coal
Water in layer gas.From the coal bed gas that dehydrating tower A3 flows out, water content is less than 1ppm.Dehydrating tower B4 adsorbs for dehydrating tower A3
Use after saturated.
Coalbed methane containing oxygen after dehydration enters the demercuration tower 5 being filled with sulfur-bearing activated carbon.Coal bed gas mercury content after demercuration is less than
0.1umg/m3。
Coalbed methane containing oxygen pressure after purification is not less than 50kPaG entrance heat exchanger 6 and is cooled to-120 DEG C, steams subsequently at the bottom of tower
Send out the liquid that device 8 adds hot stripping tower 7 end and assembles, after self being further cooled to-150 DEG C, enter stripping tower 7 from middle part.
By carrying out the exchange of energy and material in stripping tower 7 by the methane separation in coalbed methane containing oxygen out.Stripping tower 7 end
Collected liquid, has certain liquid level, and at the bottom of tower, vaporizer 8 is soaked in liquid.The liquid at stripping tower 7 end is evaporated by the bottom of tower
After the heat evaporation of device 8 transmission, the nitrogen in liquid and oxygen volatilization, flow out methane content from stripping tower 7 end more than 99.5%
Liquid methane.Liquid methane is by becoming gas as product after entering heat exchanger 6 re-heat after methane choke valve 11 reducing pressure by regulating flow
Methane exports.
The tail gas that stripping tower 7 top is flowed out flows out after entering heat exchanger 6 re-heat, and partial tail gas directly discharges, another part tail gas
Entrance tail-gas compressor 9 is pressurized to 3MPaG entrance heat exchanger 6 and is cooled to-170 DEG C, is then throttled by tail gas choke valve 10
Enter stripping tower 7 from top after blood pressure lowering.
In the above-described example, in the tail gas of discharge, methane content is less than 0.5%, and in methane product, methane content is more than 99.5%, often
Obtaining 1 mark side's methane product needs the electric energy consumed to be 0.9KWh.
Finally illustrating, preferred embodiment above is only in order to illustrate technical scheme and unrestricted, although by above-mentioned
The present invention is described in detail by preferred embodiment, it is to be understood by those skilled in the art that can in form and
In details, it is made various change, without departing from claims of the present invention limited range.
Claims (8)
1. the method for a coalbed methane containing oxygen separation of methane, it is characterised in that: the method comprises the following steps:
S1: coalbed methane containing oxygen is compressed；
S2: by the coalbed methane containing oxygen desulfurization after compression, carbon dioxide removal, dehydration, demercuration；
S3: the coalbed methane containing oxygen cooling after purifying；
S4: the coalbed methane containing oxygen after cooling is sent into segregation apparatus isolated methane and tail gas；
S5: using after methane re-heat as output of products；
S6: after tail gas re-heat, partial tail gas discharges, partial tail gas supercharging；
S7: send into segregation apparatus after being cooled down by the tail gas after supercharging.
The method of a kind of coalbed methane containing oxygen separation of methane the most according to claim 1, it is characterised in that: in the method,
In handled coalbed methane containing oxygen, methane volumetric mark is more than 20%, and remaining is mainly air.
The method of a kind of coalbed methane containing oxygen separation of methane the most according to claim 1, it is characterised in that: coalbed methane containing oxygen enters
The minimum pressure entering segregation apparatus is 50kPaG.
The method of a kind of coalbed methane containing oxygen separation of methane the most according to claim 1, it is characterised in that: described segregation apparatus
Using device for extraction and distillation, tower top does not set condenser.
The method of a kind of coalbed methane containing oxygen separation of methane the most according to claim 1, it is characterised in that: drop before methane re-heat
Being pressed onto below 20kPaG, as output of products after the methane re-heat of coalbed methane containing oxygen isolated, its re-heat is simultaneously used for cooling
Coalbed methane containing oxygen and tail gas.
The method of a kind of coalbed methane containing oxygen separation of methane the most according to claim 1, it is characterised in that: in step s 6,
Pressure after tail gas supercharging is 2.5～3.5MPaG.
The method of a kind of coalbed methane containing oxygen separation of methane the most according to claim 1, it is characterised in that: in the step s 7,
Answering reducing pressure by regulating flow to enter back into segregation apparatus after tail gas cooling, the tail gas pressure after reducing pressure by regulating flow should be than the coal bed gas entering segregation apparatus
Pressure height 10kPa.
The method of a kind of coalbed methane containing oxygen separation of methane the most according to any one of claim 1 to 7, it is characterised in that:
In the product that this method finally gives, methane volumetric mark is not less than 99.5%, and in the tail gas of final discharge, methane volumetric mark is the highest
In 0.5%.
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| CN201610290014.0A CN105972935B (en) | 2016-05-04 | 2016-05-04 | A kind of method of coalbed methane containing oxygen separation of methane |
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| CN201610290014.0A CN105972935B (en) | 2016-05-04 | 2016-05-04 | A kind of method of coalbed methane containing oxygen separation of methane |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005221199A (en) * | 2004-02-09 | 2005-08-18 | Kobe Steel Ltd | Air separation device |
| CN1718680A (en) * | 2004-07-09 | 2006-01-11 | 西南化工研究设计院 | Technology of low temperature separation and concentration coal layer gas to produce methane |
| CN102206129A (en) * | 2011-04-02 | 2011-10-05 | 薛鲁 | Separation method for oxygen-containing coal bed gas |
| CN103267402A (en) * | 2013-06-08 | 2013-08-28 | 中煤科工集团重庆研究院 | Method for extracting methane contained in low-concentration oxygen-containing coal-seam gas |
| CN105296038A (en) * | 2015-11-27 | 2016-02-03 | 中煤科工集团重庆研究院有限公司 | Oxygen-bearing coal-bed gas low-temperature concentration method and device for implementing method |
-
2016
- 2016-05-04 CN CN201610290014.0A patent/CN105972935B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005221199A (en) * | 2004-02-09 | 2005-08-18 | Kobe Steel Ltd | Air separation device |
| CN1718680A (en) * | 2004-07-09 | 2006-01-11 | 西南化工研究设计院 | Technology of low temperature separation and concentration coal layer gas to produce methane |
| CN102206129A (en) * | 2011-04-02 | 2011-10-05 | 薛鲁 | Separation method for oxygen-containing coal bed gas |
| CN103267402A (en) * | 2013-06-08 | 2013-08-28 | 中煤科工集团重庆研究院 | Method for extracting methane contained in low-concentration oxygen-containing coal-seam gas |
| CN105296038A (en) * | 2015-11-27 | 2016-02-03 | 中煤科工集团重庆研究院有限公司 | Oxygen-bearing coal-bed gas low-temperature concentration method and device for implementing method |
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