CN105890282A - Device for separating methane from oxygen-bearing coalbed methane - Google Patents
Device for separating methane from oxygen-bearing coalbed methane Download PDFInfo
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- CN105890282A CN105890282A CN201610288308.XA CN201610288308A CN105890282A CN 105890282 A CN105890282 A CN 105890282A CN 201610288308 A CN201610288308 A CN 201610288308A CN 105890282 A CN105890282 A CN 105890282A
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- methane
- heat exchanger
- stripping tower
- containing oxygen
- vaporizer
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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
-
- 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
-
- 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
-
- 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
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to a device for separating methane from oxygen-bearing coalbed methane, and belongs to the technical field of oxygen-bearing coalbed methane processing. The device comprises a striping tower, an evaporator, a heat exchanger, a flow regulating valve and a tail gas compressor, wherein the striping tower and the evaporator are used for jointly completing the separation of methane in the oxygen-bearing coalbed methane; the heat exchanger is used for heat exchange between cold materials and hot materials; the flow regulating valve is used for regulating the flow of materials and reducing the pressure and temperature of the materials; and the compressor is used for pressurizing the materials. The device can work under a relatively low operating pressure, is simple in process, good in safety and reasonable in use of cold energy, is simple and convenient to operate and has strong working condition adaptability and high recovery rate of methane.
Description
Technical field
The invention belongs to coalbed methane containing oxygen processing technology field, relate to the device of a kind of 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.
From coalbed methane containing oxygen, separate and recover methane the economy of extension and the use value of raising coal bed gas and coal production is had
Significance.The most disclosed device for coalbed methane containing oxygen separation of methane is mostly provided with special deoxygenation system or refrigeration
System and refrigerant storage charging system, flow process is complicated, and heat transmission equipment is many, and number of devices is many, processes energy consumption high, simultaneously will
Ask coal bed gas to have certain pressure and could realize preferably separation, but pressure is the lowest more safe for coalbed methane containing oxygen, institute
In economy and safety, certain problem is all there is with said apparatus.
Summary of the invention
In view of this, it is an object of the invention to provide the device of a kind of coalbed methane containing oxygen separation of methane, this device can be at oxygen-containing coal
Running under layer gas low-pressure state, safety is good, during separation minimum pressure can as little as 50kPaG, far below at present other matching requirements
The operation pressure of more than 0.3MPaG.In the case of coalbed methane containing oxygen methane volumetric mark 20%, process energy consumption less than often marking
Side's methane product 0.9KWh, if methane volumetric mark improves, energy consumption declines.This device need not ad hoc deoxygenation system, need not set specially
Door refrigeration system, institute's chilling requirement only separated by coalbed methane containing oxygen after methane and tail gas provide, use stripping tower realize oxygen-containing coal
The separation of methane in layer gas, methane recovery is high, and methane product purity is high, is the coalbed methane containing oxygen separation first of a kind of safety economy
The device of alkane.
For reaching above-mentioned purpose, the present invention provides following technical scheme:
The device of a kind of coalbed methane containing oxygen separation of methane, this device includes stripping tower, vaporizer, heat exchanger, choke valve and tail gas
Compressor；Described stripping tower jointly completes methane in coalbed methane containing oxygen and separates with vaporizer；Described heat exchanger is used for hot and cold thing
Heat exchange between material；Described choke valve is lowered the temperature for material reducing pressure by regulating flow；Described compressor is for the supercharging of material；
Described heat exchanger is connected with vaporizer, and coalbed methane containing oxygen enters vaporizer after heat exchanger flows out；Described vaporizer is positioned over
Stripping tower bottom is soaked by the liquid of stripping tower bottom, and is connected in the middle part of stripping tower, and coalbed methane containing oxygen flows out laggard from vaporizer
Enter in the middle part of stripping tower；Described stripping tower bottom is connected with heat exchanger, after the liquid methane reducing pressure by regulating flow cooling that stripping tower bottom flows out
Enter heat exchanger re-heat and become gases methane product；Described stripping top of tower is connected with heat exchanger, the tail gas that stripping top of tower flows out
Enter heat exchanger re-heat；Described heat exchanger is also connected with described tail-gas compressor, the tail gas part emptying discharge of outflow heat exchanger；
Being partly into tail-gas compressor supercharging, the tail gas after supercharging enters heat exchanger cooling；Described heat exchanger also with stripping tower top phase
Even, the tail gas reducing pressure by regulating flow cooling after supercharging cooling is directly entered stripping tower top.
Further, the coalbed methane containing oxygen pressure entering this device is less than 50 DEG C higher than 50kPaG, temperature, and wherein methane volumetric divides
Number is more than 20%, and hydrargyrum volume fraction is less than 0.1umg/m3, hydrogen sulfide volume fraction is less than 1ppm, and carbon dioxide volume fraction is less than
50ppm, water volume fraction is less than 1ppm.
The beneficial effects of the present invention is: the present invention can run under coalbed methane containing oxygen low-pressure state, and safety is good, during separation
Low-pressure can as little as 50kPaG, far below the operation pressure of more than the 0.3MPaG of at present other matching requirements.At coalbed methane containing oxygen
In the case of methane volumetric mark 20%, process energy consumption and be less than often mark side's methane product 0.9KWh, if methane volumetric mark improves,
Energy consumption declines.This device need not ad hoc deoxygenation system, special refrigeration system need not be set, institute's chilling requirement is only divided by coalbed methane containing oxygen
Methane and tail gas after from provide, and use stripping tower to realize the separation of methane in coalbed methane containing oxygen, and methane recovery is high, and methane produces
Product purity is high, is the device of the coalbed methane containing oxygen separation of methane of a kind of safety economy.
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 structural representation of device of the present invention；
Wherein: 1, heat exchanger；2, vaporizer；3, stripping tower；4, tail-gas compressor；5, tail gas choke valve；6, 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 structural representation of device of the present invention, as it can be seen, device include stripping tower, vaporizer, heat exchanger,
Choke valve, tail-gas compressor totally 5 kinds of capital equipments.Stripping tower jointly completes methane in coalbed methane containing oxygen and separates with vaporizer；
Heat exchanger heat exchange between hot and cold material；Choke valve is lowered the temperature for material reducing pressure by regulating flow；Compressor is for the increasing of material
Pressure.
Described heat exchanger is joined directly together with vaporizer, and coalbed methane containing oxygen enters after heat exchanger is cooled and is directly entered vaporizer.
Described vaporizer is joined directly together in the middle part of stripping tower, and coalbed methane containing oxygen enters after vaporizer is cooled and is directly entered stripping tower
Middle part；Wherein vaporizer is positioned over stripping tower bottom and is soaked by the liquid of stripping tower bottom.
Described stripping tower bottom is connected with heat exchanger, enters heat exchange after the liquid methane reducing pressure by regulating flow cooling that stripping tower bottom flows out
Device re-heat becomes gases methane product.
Described stripping top of tower is connected with heat exchanger, and the tail gas that stripping top of tower flows out enters heat exchanger re-heat.
Described heat exchanger is connected with tail-gas compressor, the tail gas part emptying discharge of outflow heat exchanger；It is partly into tail gas
Compressor boost, the tail gas after supercharging enters heat exchanger cooling.
Described heat exchanger is connected with stripping tower top, and the tail gas reducing pressure by regulating flow cooling after supercharging cooling is directly entered stripping tower top,
Especially tail gas enters the position of stripping tower and enters the position of stripping tower higher than coalbed methane containing oxygen.
Final from the methane that this device obtains, methane volumetric mark is more than 99.5%, and in the tail gas of discharge, methane volumetric mark is less than
0.5%.Often obtain the energy consumption of 1 mark side's methane less than 0.9KWh.
Embodiment:
In the present embodiment, with methane volumetric mark 35%, nitrogen fraction 52.5%, oxygen purity about 11.5%, its
Remaining component be hydrargyrum, hydrogen sulfide, carbon dioxide, water coalbed methane containing oxygen as a example by illustrate.Fig. 1 gives the concrete of device
Implementation process and equipment schematic diagram.
Before coalbed methane containing oxygen enters this device, temperature is 40 DEG C, and pressure 50kPaG initially enters heat exchanger 1 and is cooled to
-120 DEG C, it is further cooled to-150 DEG C subsequently into vaporizer 2, then enters stripping tower 3 from middle part.
Coalbed methane containing oxygen is through the exchange of matter and energy in stripping tower 3, and methane therein is separated and with the shape of liquid
Formula is gathered in bottom stripping tower 3.Vaporizer 2 is immersed in the liquid bottom stripping tower 3 simultaneously, utilizes and enters vaporizer 2
Liquid bottom stripping tower 3 is heated by coalbed methane containing oxygen so that it is in non-methane component evaporate to obtain methane volumetric mark
Liquid methane more than 99.5%.
Liquid methane bottom stripping tower 3 by methane choke valve 6 expenditure and pressure to 20kPaG, subsequently into heat exchanger 1 re-heat
To 35 DEG C, become gases methane as output of products.
Coalbed methane containing oxygen is through the exchange of matter and energy in stripping tower 3, and the i.e. tail gas of non-methane component therein is separated,
And exit into heat exchanger 1 re-heat to 35 DEG C from stripping tower 3 top.A tail gas part directly emptying after re-heat, a part is entered
Enter tail-gas compressor 4 and be supercharged to 3.1MPaG, by tail gas choke valve 5 after being cooled to-170 DEG C subsequently into heat exchanger 1
Reducing pressure by regulating flow is to 60kPaG, and enters stripping tower 3 top.
In the present embodiment, the process energy consumption often obtaining 1 mark side's methane product is 0.5KWh.
In this device, coalbed methane containing oxygen is directly entered the most available gases methane product of this device, simultaneously after discharge separation of methane
The tail gas obtained.For cooling down the cold of coalbed methane containing oxygen and tail gas by the liquid methane after reducing pressure by regulating flow and stripping tower 3 top
The tail gas flowed out provides, and need not arrange special deoxygenation system and refrigeration system.
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 (2)
1. the device of a coalbed methane containing oxygen separation of methane, it is characterised in that: this device include stripping tower, vaporizer, heat exchanger,
Choke valve and tail-gas compressor；Described stripping tower jointly completes methane in coalbed methane containing oxygen and separates with vaporizer；Described heat exchanger
Heat exchange between hot and cold material；Described choke valve is lowered the temperature for material reducing pressure by regulating flow；Described compressor is for material
Supercharging；
Described heat exchanger is connected with vaporizer, and coalbed methane containing oxygen enters vaporizer after heat exchanger flows out；Described vaporizer is positioned over
Stripping tower bottom is soaked by the liquid of stripping tower bottom, and is connected in the middle part of stripping tower, and coalbed methane containing oxygen flows out laggard from vaporizer
Enter in the middle part of stripping tower；Described stripping tower bottom is connected with heat exchanger, after the liquid methane reducing pressure by regulating flow cooling that stripping tower bottom flows out
Enter heat exchanger re-heat and become gases methane product；Described stripping top of tower is connected with heat exchanger, the tail gas that stripping top of tower flows out
Enter heat exchanger re-heat；Described heat exchanger is also connected with described tail-gas compressor, the tail gas part emptying discharge of outflow heat exchanger；
Being partly into tail-gas compressor supercharging, the tail gas after supercharging enters heat exchanger cooling；Described heat exchanger also with stripping tower top phase
Even, the tail gas reducing pressure by regulating flow cooling after supercharging cooling is directly entered stripping tower top.
The device of a kind of coalbed methane containing oxygen separation of methane the most according to claim 1, it is characterised in that: enter this device
Coalbed methane containing oxygen pressure is higher than 50kPaG, and temperature is less than 50 DEG C, and wherein methane volumetric mark is more than 20%, and hydrargyrum volume fraction is little
In 0.1umg/m3, hydrogen sulfide volume fraction is less than 1ppm, and carbon dioxide volume fraction is less than 50ppm, and water volume fraction is less than
1ppm。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610288308.XA CN105890282B (en) | 2016-05-04 | 2016-05-04 | A kind of device of coalbed methane containing oxygen separation of methane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610288308.XA CN105890282B (en) | 2016-05-04 | 2016-05-04 | A kind of device of coalbed methane containing oxygen separation of methane |
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| Publication Number | Publication Date |
|---|---|
| CN105890282A true CN105890282A (en) | 2016-08-24 |
| CN105890282B CN105890282B (en) | 2018-06-05 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201610288308.XA Active CN105890282B (en) | 2016-05-04 | 2016-05-04 | A kind of device of coalbed methane containing oxygen separation of methane |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN101456556A (en) * | 2008-12-31 | 2009-06-17 | 中国科学院广州能源研究所 | Carbon dioxide industrial-scale separation and purification system and method in mixture gas by hydrate method |
| CN102206129A (en) * | 2011-04-02 | 2011-10-05 | 薛鲁 | Separation method for oxygen-containing coal bed gas |
| CN103277978A (en) * | 2013-06-08 | 2013-09-04 | 中国科学院理化技术研究所 | Device for extracting methane in low-concentration oxygen-containing coal-bed gases |
| US20160054055A1 (en) * | 2010-10-26 | 2016-02-25 | Kirtikumar N. Patel | Process for separating and recovering NGLs from hydrocarbon streams |
-
2016
- 2016-05-04 CN CN201610288308.XA patent/CN105890282B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN101456556A (en) * | 2008-12-31 | 2009-06-17 | 中国科学院广州能源研究所 | Carbon dioxide industrial-scale separation and purification system and method in mixture gas by hydrate method |
| US20160054055A1 (en) * | 2010-10-26 | 2016-02-25 | Kirtikumar N. Patel | Process for separating and recovering NGLs from hydrocarbon streams |
| CN102206129A (en) * | 2011-04-02 | 2011-10-05 | 薛鲁 | Separation method for oxygen-containing coal bed gas |
| CN103277978A (en) * | 2013-06-08 | 2013-09-04 | 中国科学院理化技术研究所 | Device for extracting methane in low-concentration oxygen-containing coal-bed gases |
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| CN105890282B (en) | 2018-06-05 |
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