CN201199120Y - Separated liquefaction equipment of air conditioner back heating type mine gas - Google Patents
Separated liquefaction equipment of air conditioner back heating type mine gas Download PDFInfo
- Publication number
- CN201199120Y CN201199120Y CNU200820111400XU CN200820111400U CN201199120Y CN 201199120 Y CN201199120 Y CN 201199120Y CN U200820111400X U CNU200820111400X U CN U200820111400XU CN 200820111400 U CN200820111400 U CN 200820111400U CN 201199120 Y CN201199120 Y CN 201199120Y
- Authority
- CN
- China
- Prior art keywords
- gas
- heat exchanger
- liquefaction
- fractionating column
- refrigeration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model relates to mine gas separation and liquefaction equipment which comprises a compressing and purification device, a refrigeration device, a liquefaction and separation device and an auxiliary device, wherein, the liquefaction and separation device comprises a heat exchanger and a fractionating tower; a feed gas output pipeline of the compressing and purification device is connected with a feed gas input channel of the heat exchanger of the liquefaction and separation device; a refrigeration pipeline of the refrigeration device is connected with a refrigeration channel of the heat exchanger of the liquefaction and separation device; a feed gas output pipe of the heat exchanger of the liquefaction and separation device is connected with a feed gas input port in the middle part of the fractionating tower the top of which is provided with a condenser and a gas pipeline which can guide low-temperature air into the heat exchanger; and the bottom of the fractionating tower is provided with an evaporator and a liquified natural gas eduction pipeline. The mine gas separation and liquefaction equipment can prevent the generation of nitrogen in low temperature, adopts a method of air heat return, has simple structure and reduces the energy consumption and the cost, thus being more beneficial to large-scale popularization.
Description
Technical field
The utility model relates to a kind of gas and separates liquefaction method and apparatus, particularly a kind of separation liquefaction device of mine gas gas of air backheating type.
Background technology
The coal bed gas of extraction is a mine gas gas in the coal mining process, because pressure is low, methane content is low, wherein is mixed with air, has brought difficulty for the processing and the transportation of this gas, all is that it is discharged in the atmosphere usually.This has not only caused serious atmosphere pollution, also causes the very big wasting of resources.If the coal bed gas in this Device in Gas (mainly being methane) and air separation is come out and will purify after coal gas gasification, this will make transportation and utilize and all becomes very convenient.
Conventional separation method has absorption process, absorption method, film permeation method and cryogenic rectification method etc.The front several method, the purity of separation is difficult to reach requirement, and the rate of recovery that has is low, and what have also needs heating, and the Device in Gas that is mixed with air is explosive at high temperature, has potential safety hazard, does not therefore have and can be applied.A kind of technology has been invented by U.S. BCCK engineering company, be that the mine gas air pressure that will be mixed with air earlier contracts, with contact oxidation method wherein oxygen removed then, remove hydrogen sulfide and carbon dioxide then, remove moisture again, last method of separating with throttling refrigeration again removes nitrogen.This process equipment more complicated, product is a gases methane.As producing liquid methane, also to further increase liquefaction device.The content that proposes respectively in May, 2006 and July is in several the Chinese patent application of " containing air coal gas gasification Processes and apparatus ", and (patent No. is: 200610080889.4 to have described the technology of a kind of twin-stage rectifying and single-stage rectifying respectively; 200620115881.2; 200610103425.0; 200620122543.1), above-mentioned Processes and apparatus is simpler than the technology of U.S. BCCK, and can directly produce the methane of liquid.But because above-mentioned technology all needs to isolate at low temperatures nitrogen, so the required energy consumption of its process equipment is still higher.
Summary of the invention
Technical problem to be solved in the utility model provides a kind of air backheating type mine gas gas and separates liquefaction device, and it can adopt the method for Cryogenic air backheat to reclaim cold, and does not produce nitrogen, and technology is more simple, and energy consumption is also lower.
For solving the problems of the technologies described above, the utility model provides a kind of separation liquefaction device of mine gas gas of air backheating type,
It comprises compression cleaning equipment, refrigeration plant, liquefaction separation equipment and auxiliary equipment;
Described liquefaction separation equipment includes heat exchanger and a fractionating column, the unstripped gas input channel of the heat exchanger in the unstripped gas output pipe of compression cleaning equipment and the separation equipment that liquefies is connected, the refrigeration pipe of refrigeration plant is connected with the refrigerating channel of the heat exchanger of liquefaction separation equipment, and the unstripped gas output channel of the heat exchanger of described liquefaction separation equipment links to each other with the unstripped gas input port that is positioned at the fractionating column middle part;
The fractionating column top has condenser, and simultaneously its top also is provided with gas piping and Cryogenic air is drawn gets back in the heat exchanger; The fractionating column bottom has evaporimeter, and the bottom is provided with the liquified natural gas introduction pipe simultaneously.
Further, the gas piping at described fractionating column top with Cryogenic air draw get back to heat exchanger after, also can be connected to decompressor, and then be connected to heat exchanger.
Further, be input to the temperature of unstripped gas (mine gas gas) of unstripped gas input port at fractionating column middle part below negative 82.5 degree Celsius.
Further, the evaporimeter heating pipe line of described fractionating column is connected with the precooling pipeline of refrigerant.
Further, the condenser refrigeration pipe of described fractionating column is connected with the refrigerant pipeline of heat exchanger.
Further, the evaporimeter heating pipe line of described fractionating column also can be connected with unstripped gas precooling pipeline.
Further, described refrigeration plant is gas swell refrigeration equipment or mix refrigerant refrigeration plant.
Further, can comprise compressor and raw material gas purifying device in the described compression cleaning equipment; Described raw material gas purifying device can be the cleaning equipment of molecular sieve adsorption, also the cleaning system that can be made up of amine absorption tower and regenerator.
Further, described auxiliary equipment is the equipment of making nitrogen, for example THE PRESSURE SWING ADSORPTION NITROGEN GENERATING DEVICE.
The refrigerant pipeline of the condenser of described fractionating column is communicated with the refrigeration air pipe of refrigeration plant; The liquid line of fractionating column bottom can insert the liquid in the liquid storage groove.
Described refrigeration plant can be nitrogen expansion refrigeration or nitrogen, methane swell refrigeration, includes compressor, decompressor etc., also can freeze with mix refrigerant, includes hybrid refrigeration compressor, cooler, gas-liquid separator etc.; Described auxiliary equipment can be varying-voltage adsorption nitrogen machine, the nitrogen export pipeline of varying-voltage adsorption nitrogen machine and the regeneration pipeline of cleaning equipment, also has the nitrogen pipeline of nitrogen refrigeration system to be connected.
Technical scheme in the utility model and application number are that 200610080889.4 invention is compared, this invention need be set up the two-stage fractionating column, and need mine gas gas is decomposed into nitrogen, oxygen-enriched air and liquified natural gas three parts, its complex process, cost height, power consumption are greatly; And the utility model adopts single fractionation column, and does not need to decomposite from mine gas gas nitrogen and oxygen-enriched air, has the beneficial effect that manufacturing process is simple, cost is low, power consumption is little.
Technical scheme in the utility model and application number are that 200610103425.0 invention is compared, though the single fractionation column structure has been adopted in this invention, but still need from mine gas gas, to decomposite nitrogen and oxygen-enriched air, a plurality of different temperature provinces need be set in fractionating column, and the shunt conduit that nitrogen, oxygen-enriched air are drawn respectively, and for separation of nitrogen needs also will provide lower temperature, so it still exists the defective that technology is complicated, cost is higher, power consumption is bigger.By comparison, because the utility model does not need to decomposite nitrogen and oxygen-enriched air from mine gas gas, need in fractionating column, not set up different temperatures interval, many places, and the shunt conduit that nitrogen, oxygen-enriched air are drawn respectively, therefore, the utility model obviously has beneficial effect simple in structure, that construction cost is low, fractionating efficiency is higher, power consumption is little.
In sum, the beneficial effect of the method and apparatus in the utility model is: the utility model mine gas gas separates liquefaction device and has avoided producing at low temperatures nitrogen, and adopt the method for air backheating, it is simple in structure, thereby reduced energy consumption, reduce cost, more helped large-scale promotion.
Description of drawings
Fig. 1 is the compression cleaning equipment schematic diagram of the utility model embodiment 1;
Fig. 2 is refrigeration plant and the liquefaction separation equipment schematic diagram of the utility model embodiment 1.
Fig. 3 is refrigeration plant and the liquefaction separation equipment schematic diagram of the utility model embodiment 2.
Fig. 4 is the structural representation of fractionating column in the utility model.
The specific embodiment
Embodiment 1
Consult Fig. 1, be the compression cleaning equipment schematic diagram of the utility model embodiment 1.Comprise filter 1, gas-liquid separator 2, compressor 3, cooler 4, gas-liquid separator 5, molecular sieve purification equipment group, described molecular sieve purification equipment group comprises two molecular sieve drying machines 6,7, when 6 work of first molecular sieve drying machine, second molecular sieve drying machine 7 thermal regeneration, cooling are standby, switch once in per 12 hours.This molecular sieve drying equipment is mainly used to remove water, carbon dioxide.Filter 8 is arranged after the molecular sieve equipment group, go back having heaters 9.In addition, also have a varying-voltage adsorption nitrogen machine 10 that nitrogen is provided, be used for the gas of displacement purge equipment.
The concrete technological process that compression purifies is as follows:
1, the next mine gas gas unstripped gas of self-discharging pipeline at first removes dust through filter 1;
2, after the mine gas gas after the dedusting entered gas-liquid separator 2 gas-liquid separations, gas entered compressor 3 compressions;
3, compression is after cooler 4 coolings are removed free water through gas-liquid separator 5 then.
4, mine gas gas enters molecular sieve drying equipment 6, deviates from water and carbon dioxide, the nitrogen that varying-voltage adsorption nitrogen machine 10 provides, be introduced into 7, displacement Device in Gas wherein is heated to 240-250 ℃ with the pure air heater via 9 that produces in the flow process then, is used for the regeneration of mole sieve drier 7; After thermal regeneration is finished, pure air without heating, is directly imported drier 7, the cooling molecular sieve, the temperature of reduction molecular sieve drying machine 7, and then with the air in the nitrogen replacement molecular sieve 7, standby;
6, the unstripped gas that removes water, carbon dioxide and oxygen through molecular sieve drying equipment again through filter 8 can enter refrigeration, separation equipment liquefies.
Consult Fig. 2, be refrigeration plant and the liquefaction separation equipment schematic diagram of the utility model embodiment 1.The liquefaction separation equipment comprises level Four heat exchanger 11,12,13,17 and fractionating column 15; Condenser 16 is arranged at the fractionating column top, and evaporimeter 14 is arranged at the fractionating column bottom, and the refrigeration piping of condenser 16 links to each other with the pipeline of refrigeration system, and the water back of evaporimeter 14 links to each other with the pipeline of refrigeration gas between heat exchanger 11,12; The unstripped gas pipeline links to each other with heat exchanger 11,12,13 successively, and the unstripped gas pipeline of heat exchanger 13 cold junctions links to each other with the middle part of fractionating column 15; Fractionating column 15 tops have gas pipeline to link to each other with heat exchanger 17, decompressor 18, heat exchanger 13,12,11 successively; The fractionating column bottom also has liquid line that liquid natural gas is connected to heat exchanger 17, is connected to output valve then.
Refrigeration plant is the compression-expansion refrigeration system, has adopted the turbo-expander 23 of a compressor 19, cooler 20,22, band supercharger 21.The refrigeration feed channel links to each other with the water back of evaporimeter 14 between heat exchanger 9,10, and the gas exhaust piping of decompressor 23 links to each other with the refrigeration piping of condenser 16, links to each other with heat exchanger 13,12,11 successively then.
The liquefying separation process step is as follows:
1, the mine gas unstripped gas of compressed purification (methane 45%, air 55%) enters cooled gas cooled in the heat exchanger 11,12,13, reduces temperature and reaches-175 ℃ approximately.
2, the unstripped gas after temperature descends enters the middle part of fractionating column 15, its liquid flows through column plate from top to bottom, the part of unstripped gas liquid is evaporated to gas in the evaporimeter 14 of fractionating column 15 bottoms, heating-up temperature is about-140 ℃, and the gas that is evaporated upwards flows and the liquid that flows downward carries out heat, matter exchange.
3, the gas that upwards flows arrives the fractionating column top, and by condenser 16 condensations at fractionating column top, wherein a part is condensed into liquid again, refluxes downwards, carries out heat, matter exchange again with gas equally again.The condensation temperature of condenser 16 is about-180 ℃.
4, the gas of emitting from the top of fractionating column is clean air, flow is 55% of a unstripped gas, this part gas contains methane content less than 0.1%, temperature is about-178 ℃, through heat exchanger 17 the liquid coal bed gas is further cooled off earlier, then, expanded through decompressor 18 again, enter heat exchanger 13,12,11 backheats more successively, to reclaim cold.
What 6, emit from fractionating column 12 bottoms is exactly the very high liquefaction coal bed gas of purity.Flow is 45% of a unstripped gas, and purity reaches more than 99.9%, and temperature is about-143 ℃.
1, before refrigeration system starts, is full of nitrogen in the system as refrigeration gas.
2, start refrigeration system, earlier compressed machine 19 compressions of refrigeration gas, 21 superchargings of turbine supercharger are passed through in cooling again in cooler 20, through cooler 22 coolings, enter 11 precoolings of first heat exchanger again, and temperature is reduced to-128 ℃.
3, refrigeration gas is further cooled to-142 ℃ through the pipeline (temperature is for-143 ℃) of evaporimeter 14 again, and the gas that freezes then enters second heat exchanger 12, is further cooled to-150 ℃, enters turbo-expander 23 swell refrigerations again.
4, the refrigeration temperature degree after expanding from turbo-expander 23 be-182 ℃, and it is introduced into the refrigeration piping of condenser 16, and for condenser 16 provides low-temperature receiver, subsequently, the temperature degree that freezes is elevated to-179 ℃, backflows to enter the 3rd heat exchanger 13 and be used for cooling off unstripped gas again.
5, the refrigeration gas that comes out from the hot junction of heat exchanger 13 enters heat exchanger 12,11 more successively, as the low-temperature receiver of heat exchanger.After the refrigerant gas re-heat, return the suction port of compressor, compression again, supercharging, cooling, swell refrigeration, so circulation.
Embodiment 2
Referring to Fig. 3, be refrigeration plant and the liquefaction separation equipment schematic diagram of the utility model embodiment 2.Its heat exchanger, fractionating column that separates the liquefaction part is substantially the same manner as Example 1, no longer repeat specification.Difference is, makes unstripped gas be cooled to 0 ℃ to-50 ℃ by heat exchanger 24 earlier, and the evaporimeter 27 of process fractionating column bottom is for evaporimeter provides heat then, and unstripped gas itself obtains precooling simultaneously.Therefore, on equipment, the heating pipe line of the evaporimeter 27 of fractionating column is connected with the unstripped gas pipeline, and unstripped gas is cooled to-150 ℃～-180 ℃ through heat exchanger 25,26 more then, makes most of mine gas gas be cooled to liquid, enters the middle part of fractionating column 28 again.Difference is more in addition, refrigeration system has adopted the method for mix refrigerant refrigeration, mixed refrigerant systems is made up of mix refrigerant compressor assembly 32, low temperature gas-liquid separator 33 and several throttle, and this is ripe prior art, does not need narration here.Just on equipment, the refrigerant pipeline of the condenser 29 of fractionating column is to be communicated with the refrigeration pipe of mix refrigerant refrigeration plant, rather than as embodiment 1, is connected with the decompressor gas exhaust piping of nitrogen refrigeration.
Figure 4 shows that the structural representation of fractionating column among embodiment 1 and the embodiment 2, the top of fractionating column 15 is provided with condenser 16 among the figure, and the bottom of fractionating column 15 is provided with evaporimeter 14.
Claims (9)
1. an air backheating type mine gas gas separates liquefaction device, comprises compression cleaning equipment, refrigeration plant, liquefaction separation equipment and auxiliary equipment;
Described liquefaction separation equipment includes heat exchanger and a fractionating column, the unstripped gas input channel of the heat exchanger in the unstripped gas output pipe of compression cleaning equipment and the separation equipment that liquefies is connected, the refrigeration pipe of refrigeration plant is connected with the refrigerating channel of the heat exchanger of liquefaction separation equipment, and the unstripped gas output channel of the heat exchanger of described liquefaction separation equipment links to each other with the unstripped gas input port that is positioned at the fractionating column middle part;
The fractionating column top has condenser, and simultaneously its top also is provided with gas piping and Cryogenic air is drawn gets back in the heat exchanger; The fractionating column bottom has evaporimeter, and the bottom is provided with the liquified natural gas introduction pipe simultaneously.
2. a kind of air backheating type mine gas gas according to claim 1 separates liquefaction device, it is characterized in that, the gas piping at described fractionating column top with Cryogenic air draw get back to heat exchanger after, be connected to decompressor, and then be connected to heat exchanger.
3. a kind of air backheating type mine gas gas according to claim 1 separates liquefaction device, it is characterized in that, the temperature of unstripped gas of unstripped gas input port that is input to the fractionating column middle part is below negative 82.5 degree Celsius.
4. separate liquefaction device according to claim 1 or 2 or 3 described a kind of air backheating type mine gas gas, it is characterized in that the evaporimeter heating pipe line of described fractionating column is connected with the precooling pipeline of refrigerant.
5. separate liquefaction device according to claim 1 or 2 or 3 described a kind of air backheating type mine gas gas, it is characterized in that the condenser refrigeration pipe of described fractionating column is connected with the refrigerant pipeline of heat exchanger.
6. separate liquefaction device according to claim 1 or 2 or 3 described a kind of air backheating type mine gas gas, it is characterized in that the evaporimeter heating pipe line of described fractionating column is connected with unstripped gas precooling pipeline.
7. separate liquefaction device according to claim 1 or 2 or 3 described a kind of air backheating type mine gas gas, it is characterized in that described refrigeration plant is gas swell refrigeration equipment or mix refrigerant refrigeration plant.
8. separate liquefaction device according to claim 1 or 2 or 3 described a kind of air backheating type mine gas gas, it is characterized in that, cleaning equipment in the described compression cleaning equipment is the molecular sieve adsorption clarifier, or the cleaning system of being made up of amine absorption tower and regenerator.
9. separate liquefaction device according to claim 1 or 2 or 3 described a kind of air backheating type mine gas gas, it is characterized in that described auxiliary equipment is the equipment of making nitrogen.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU200820111400XU CN201199120Y (en) | 2007-10-12 | 2008-04-18 | Separated liquefaction equipment of air conditioner back heating type mine gas |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200720178398.3 | 2007-10-12 | ||
| CN200720178398 | 2007-10-12 | ||
| CNU200820111400XU CN201199120Y (en) | 2007-10-12 | 2008-04-18 | Separated liquefaction equipment of air conditioner back heating type mine gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201199120Y true CN201199120Y (en) | 2009-02-25 |
Family
ID=40005074
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2008100936533A Pending CN101270952A (en) | 2007-10-12 | 2008-04-18 | Air backheating type mine gas separation and liquefaction method and apparatus |
| CNU200820111400XU Expired - Lifetime CN201199120Y (en) | 2007-10-12 | 2008-04-18 | Separated liquefaction equipment of air conditioner back heating type mine gas |
Family Applications Before (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2008100936533A Pending CN101270952A (en) | 2007-10-12 | 2008-04-18 | Air backheating type mine gas separation and liquefaction method and apparatus |
Country Status (1)
| Country | Link |
|---|---|
| CN (2) | CN101270952A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101818984A (en) * | 2010-04-21 | 2010-09-01 | 中国石油大学(北京) | Full liquefying separation process for air-containing coal bed gas |
| CN102321494A (en) * | 2011-05-24 | 2012-01-18 | 北京惟泰安全设备有限公司 | Coal bed gas separating system and process |
| CN102321493A (en) * | 2011-05-24 | 2012-01-18 | 北京惟泰安全设备有限公司 | Coal bed gas separating system and process utilizing catalyst to deoxidize |
| CN103256786A (en) * | 2013-06-08 | 2013-08-21 | 中煤科工集团重庆研究院 | Flame-suppression and explosion-suppression cryogenic liquefaction device for low-concentration coal bed gas |
| CN111249852A (en) * | 2020-02-13 | 2020-06-09 | 中国科学院理化技术研究所 | Regenerative oil gas VOCs condensation recovery system for mixed working medium refrigeration |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101476485B (en) * | 2009-02-09 | 2011-01-26 | 宁波鲍斯压缩机有限公司 | Large coal bed gas recovery apparatus set |
| EP2641042A1 (en) * | 2010-11-16 | 2013-09-25 | Praxair Technology, Inc. | System and method for cryogenic cooling of a process stream with enhanced recovery of refrigeration |
| CN102504900B (en) * | 2011-10-20 | 2016-08-17 | 辽宁哈深冷气体液化设备有限公司 | The Apparatus and method for of liquified natural gas is produced from coke-stove gas |
| CN103175380B (en) * | 2013-04-07 | 2015-09-02 | 中煤科工集团重庆研究院有限公司 | Low concentration coal-bed gas produces LNG device containing oxygen cryogenic liquefying |
| CN103175381B (en) * | 2013-04-07 | 2015-09-16 | 中国科学院理化技术研究所 | Low concentration coal-bed gas produces LNG technique containing oxygen cryogenic liquefying |
| CN103267402B (en) * | 2013-06-08 | 2015-09-09 | 中煤科工集团重庆研究院有限公司 | Extract the method for methane in low concentration coalbed methane containing oxygen |
| CN107606876A (en) * | 2017-08-29 | 2018-01-19 | 中国科学院理化技术研究所 | Air-seperation system |
-
2008
- 2008-04-18 CN CNA2008100936533A patent/CN101270952A/en active Pending
- 2008-04-18 CN CNU200820111400XU patent/CN201199120Y/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101818984A (en) * | 2010-04-21 | 2010-09-01 | 中国石油大学(北京) | Full liquefying separation process for air-containing coal bed gas |
| CN102321494A (en) * | 2011-05-24 | 2012-01-18 | 北京惟泰安全设备有限公司 | Coal bed gas separating system and process |
| CN102321493A (en) * | 2011-05-24 | 2012-01-18 | 北京惟泰安全设备有限公司 | Coal bed gas separating system and process utilizing catalyst to deoxidize |
| CN102321493B (en) * | 2011-05-24 | 2013-11-27 | 北京惟泰安全设备有限公司 | Coal bed gas separating system and process utilizing catalyst to deoxidize |
| CN103256786A (en) * | 2013-06-08 | 2013-08-21 | 中煤科工集团重庆研究院 | Flame-suppression and explosion-suppression cryogenic liquefaction device for low-concentration coal bed gas |
| CN103256786B (en) * | 2013-06-08 | 2015-09-09 | 中煤科工集团重庆研究院有限公司 | Combustion and explosion suppression type low concentration coal-bed gas cryogenic liquefying device |
| CN111249852A (en) * | 2020-02-13 | 2020-06-09 | 中国科学院理化技术研究所 | Regenerative oil gas VOCs condensation recovery system for mixed working medium refrigeration |
| CN111249852B (en) * | 2020-02-13 | 2022-04-26 | 中国科学院理化技术研究所 | Regenerative oil gas VOCs condensation recovery system for mixed working medium refrigeration |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101270952A (en) | 2008-09-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN201199120Y (en) | Separated liquefaction equipment of air conditioner back heating type mine gas | |
| CN109838975B (en) | Low-energy-consumption liquid nitrogen preparation device and process | |
| CN100404988C (en) | Air-contained coal gas gasification and separation process and equipment | |
| CN108061428B (en) | Pure nitrogen preparation device and process | |
| US20080245101A1 (en) | Integrated Method and Installation for Cryogenic Adsorption and Separation for Producing Co2 | |
| CN201377961Y (en) | Multi-operating mode air separation equipment | |
| CN109140903B (en) | Air separation system and air separation method utilizing cold energy of liquefied natural gas | |
| CN109173558B (en) | Low-energy-consumption carbon dioxide capturing and sealing technology and system | |
| CN115069057B (en) | Method for purifying and recovering carbon dioxide by low-temperature rectification | |
| CN103123203A (en) | Method of preparing pure nitrogen by using exhaust gas with nitrogen to carry out once-more cryogenic distillation | |
| CN105716370A (en) | System and method of preparing hydrogen rich gas and carbon monoxide from synthesis gas | |
| AU2010291532B2 (en) | Method and device for treating a carbon dioxide-containing gas flow, wherein the energy of the vent gas (work and cold due to expansion) is used | |
| CN103523751A (en) | Device and method for performing cryogenic separation and purification on carbon monoxide and hydrogen | |
| CN104807290A (en) | Device and method for preparing low-pressure nitrogen gas by using single-tower double-backflow expansion | |
| CN101929791B (en) | Large-tonnage high-purity nitrogen equipment | |
| JPH028235B2 (en) | ||
| EP1612496A1 (en) | Air separator | |
| CN1952569A (en) | Process and equipment for liquefying air-containing coal-bed gas | |
| CN200952872Y (en) | Air-containing coal seam gas liquifying separating equipment | |
| CN207365553U (en) | A kind of device for producing high pure oxygen and High Purity Nitrogen | |
| CN202204239U (en) | Device for producing high-purity nitrogen and low-purity oxygen with pressure | |
| CN101493277B (en) | Low temperature separation method and apparatus for mine gas | |
| CN115790076B (en) | Device and method for recycling carbon dioxide and nitrogen in flue gas | |
| CN2898737Y (en) | Liquefier containing coal-seam gas | |
| CN201359420Y (en) | Low temperature separation equipment of mine gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20090225 |