CN103043609A - Liquid nitrogen washing device with function of producing natural gas - Google Patents
Liquid nitrogen washing device with function of producing natural gas Download PDFInfo
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- CN103043609A CN103043609A CN2012105640626A CN201210564062A CN103043609A CN 103043609 A CN103043609 A CN 103043609A CN 2012105640626 A CN2012105640626 A CN 2012105640626A CN 201210564062 A CN201210564062 A CN 201210564062A CN 103043609 A CN103043609 A CN 103043609A
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- liquid
- gas
- output terminal
- washing device
- natural gas
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 162
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 94
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 81
- 239000007788 liquid Substances 0.000 title claims abstract description 53
- 238000005406 washing Methods 0.000 title claims abstract description 43
- 239000003345 natural gas Substances 0.000 title claims abstract description 33
- 239000007789 gas Substances 0.000 claims abstract description 82
- 235000009508 confectionery Nutrition 0.000 claims description 26
- 239000007791 liquid phase Substances 0.000 claims description 26
- 239000012071 phase Substances 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 238000010992 reflux Methods 0.000 claims description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 12
- 230000015572 biosynthetic process Effects 0.000 abstract description 8
- 238000002309 gasification Methods 0.000 abstract description 8
- 238000003786 synthesis reaction Methods 0.000 abstract description 8
- 229910021529 ammonia Inorganic materials 0.000 abstract description 7
- 239000003245 coal Substances 0.000 abstract description 5
- 238000000034 method Methods 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 12
- 239000002737 fuel gas Substances 0.000 description 5
- 238000007670 refining Methods 0.000 description 5
- 241000282326 Felis catus Species 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000007710 freezing Methods 0.000 description 3
- 230000008014 freezing Effects 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 210000000689 upper leg Anatomy 0.000 description 3
- 239000000470 constituent Substances 0.000 description 2
- NMJORVOYSJLJGU-UHFFFAOYSA-N methane clathrate Chemical compound C.C.C.C.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O NMJORVOYSJLJGU-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 208000001408 Carbon monoxide poisoning Diseases 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000002595 cold damage Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000005304 joining Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a liquid nitrogen washing device with a function of producing natural gas, which comprises a first feed gas cooler 1, a second feed gas cooler 2, a nitrogen washing tower 3, a purifying synthesis gas pipe and a demethanizer 3, wherein the purifying synthesis gas pipe runs through the first feed gas cooler 1 and the second feed gas cooler 2 in sequence; the demethanizer 3 is provided with an air inlet end, an air outlet end and a fraction output end; the purifying synthesis gas pipe is communicated with the air inlet end after running through the second feed gas cooler; and the air outlet end is communicated with the nitrogen washing tower 3 through a pipe. The liquid nitrogen washing device with the function of producing natural gas is capable of recycling methane generated during the process of coal gasification and manufacturing the methane into natural gas, which not only realizes the goal of obtaining clean natural gas containing about 99% of methane while producing refined ammonia synthesis gas, but also adds a new product variety and increases the business opportunity of a factory.
Description
Technical field
The present invention relates to coal chemical technology, be used for the synthetic gas process for refining of synthetic ammonia processed, relate in particular to the liquid nitrogen washing device that a kind of double system is produced Sweet natural gas.
Background technology
Coal obtains raw gas through gasification workshop section, raw gas enters low temperature washing device for methanol behind conversion section, be purified synthetic gas after low temperature washing device for methanol removes sour gas, decontaminating syngas enters liquid nitrogen washing device and removes the material synthesis gas that obtains synthetic ammonia behind trace amounts of CO etc.
At present, domestic " liquid nitrogen washing device " for coal chemical technology, the refining synthetic gas of synthetic ammonia processed all is for the CO that removes decontaminating syngas.But when washing CO, CH
4Also washed with Ar, and with excessive liquid N
2Mix, this mixture after re-heat all as the fuel gas of factory.Contain higher CO in this fuel gas.
There is following problem in prior art:
1. common, if the methane concentration in the decontaminating syngas of feed liquor nitrogen cleaning device≤1%, liquid nitrogen washing device can safe handling; If the stifled phenomenon of ice that CH4 freezes to solidify then very easily under-180 ℃ or lower temperature, occurs in methane concentration 〉=1% or when higher, and cause the parking of device and factory be forced to stop.
Under normal pressure, pure CH
4-182 ℃ of boiling point-162 ℃, freezing points (or claiming solidification point).In low temperature and pressurization namely under the operational condition in liquid nitrogen washing, CH
4Then begin liquefaction from-127 ℃ (very causing in also having from-92 ℃) and (depend primarily on CH the decontaminating syngas of the working pressure of system and feed liquor nitrogen cleaning device
4Concentration), its freezing point temperature also can raise with the increase of working pressure.
Yet feeding gas generally is about-186 ℃ in the service temperature that goes out the final stage plate-fin heat exchanger of liquid nitrogen washing device (being the present invention the second feed gas chiller E04305).At that time improper at underload or operation control especially, surplus can appear in the cold in the system, thereby just the CH in the feeding gas occurs very easily
4, in the final stage plate-fin heat exchanger, solidify freezing its passage that blocks.Thereby, forcing the parking of factory because of the parking of liquid nitrogen washing device, its similar accident had generation in certain factory.、
2. if still adopt the way of former liquid nitrogen cleaning device, not with CH
4Remove separately, CH can not occur even suppose it
4Ice stifled, then can be excessive because of fuel quantity, can occur that supply exceed demand; The extraction part is made domestic fuel and is then contained higher CO (CO content can surpass the safety standards of domestic fuel), and also should not do.Certainly also be not suitable for carrying by pipe network this its, otherwise the effusion that CO can occur causes the security incident of " carbon monoxide poisoning ".
3. large-scale gasification factory (especially contains cut CH in raw gas in the technique of the refining ammonia synthesis gas of liquid nitrogen washing
4When higher), if the fuel gas cut that liquid nitrogen washing device is discharged is all delivered to the fuel gas system of factory, can cause too greatly a large amount of burning and exhaustings of accident flare system in factory because of tolerance.Thereby, not only can cause the waste of the energy, also increased CO
2Quantity discharged.
Summary of the invention
Purpose of the present invention solve exactly when CH4 content 〉=1% in the decontaminating syngas or when higher (contain in the raw gas of making such as lurgi pressure gasification, KBR pressurized gasification or other gasification process etc. about 2% (butt meter) and more than methane), methane solidifies frozen block in the ice chest of liquid nitrogen washing device, cause the problem that liquid nitrogen washing device can't normal running, simultaneously can realize the by-product high-purity methane, high-purity methane is clean fuel---and Sweet natural gas is " LNG " (natural gas liquids) after the liquefaction.
The system of holding concurrently is produced the liquid nitrogen washing device of Sweet natural gas, comprise the first feed gas chiller 1, the second feed cooler 2, nitrogen wash column 3 and decontaminating syngas pipeline, described decontaminating syngas pipeline flow through successively the first feed gas chiller 1 and the second feed cooler 2, also comprise demethanizing tower 5, described demethanizing tower 5 is established inlet end, outlet side and cut output terminal, and described decontaminating syngas pipeline is flowed through after the second feed cooler and to be connected middle part, top and the bottom that described inlet end, outlet side, cut output terminal lay respectively at described demethanizing tower 5 with described inlet end.
Described double system is produced the liquid nitrogen washing device of Sweet natural gas, also comprise elevated pressure nitrogen water cooler 4 and tower reactor cut separator 6, described tower reactor cut separator 6 is provided with the first separator input terminus, the first liquid phase output terminal and the first gas phase output terminal, described the first separator input terminus connects described cut output terminal by pipeline, described the first liquid phase output terminal be connected the gas phase output terminal and connect the Sweet natural gas delivery conduit, described Sweet natural gas delivery conduit flow through successively the first feed gas chiller 1, the second feed cooler 2 and elevated pressure nitrogen water cooler 4.
Described double system is produced the liquid nitrogen washing device of Sweet natural gas, also comprise trim the top of column separator 7, described trim the top of column separator 7 is established the second separator input terminus, second liquid phase output terminal and the second gas phase output terminal, described the second separator input terminus is by the described outlet side of pipeline connection, and described the second gas phase output terminal is by the described nitrogen wash column 3 of pipeline connection; Described demethanizing tower is established the liquid-phase reflux end, and described second liquid phase output terminal is by the described liquid-phase reflux end of pipeline connection.
Described liquid-phase reflux end is positioned at the top of described demethanizing tower.
Establish liquid phase on described second liquid phase output terminal and the pipeline that the liquid-phase reflux end is communicated with pump 9.
The pipeline that described outlet side is communicated with the second separator input terminus described the second feed cooler 2 of flowing through, the pipeline that described the second gas phase output terminal is communicated with nitrogen wash column 3 described the second feed cooler 2 of flowing through.
Described demethanizing tower 5 tower reactors are provided with reboiler 8.
Described reboiler 8 is established still liquid recycle pump 10.
Described decontaminating syngas pipeline flow through successively the first feed gas chiller 1, reboiler, the first feed gas chiller 1, the second feed gas chiller 2.
The present invention is owing to being provided with demethanizing tower in ice chest, utilize the cold in traditional liquid nitrogen washing, separate before before-180 ℃, the methane in the feeding gas (containing methane 〉=5%) being advanced nitrogen wash column, therefore situation that just there will be no the stifled device channels of solid-state methane ice under-180 ℃ the low-temperature condition in rear system, occurs being lower than, middlely situation that just there will be no the stifled device channels of solid-state methane ice under-180 ℃ the low-temperature condition occurs being lower than, guarantee that the safety in production of factory and long period produce continuously.
Because the methane fraction of separating meets the national standard of Sweet natural gas, sell pipe network therefore can directly send into weather; In addition CH
4After cut is in time separated separately, effectively avoid methane under zero pour, solidify the long period stable operation that ice had blocked up, guaranteed ice chest.
The present invention holds concurrently and makes the liquid nitrogen washing device of producing Sweet natural gas, the methane recovery that generates in the coal gasification course is made Sweet natural gas, can realize in refining ammonia synthesis gas, also obtaining containing approximately 99% clean Sweet natural gas of methane, also make factory increase by a new range of product, increase the business opportunity of factory.
Description of drawings
Fig. 1 is the schematic diagram that the double system of the present invention is produced the liquid nitrogen washing device of Sweet natural gas.
Description of reference numerals:
1 is the first feed gas chiller among the figure, and 2 is the second feed cooler, and 3 is nitrogen wash column, and 4 is the elevated pressure nitrogen water cooler, and 5 is demethanizing tower, and 6 is tower reactor cut separator, and 7 is the trim the top of column separator, and 8 is reboiler, and 9 are the liquid phase pump, and 10 is still liquid recycle pump.
Embodiment
Embodiment 1
Decontaminating syngas is introduced in the molecular sieve adsorber in the liquid nitrogen washing device, the CO of its contained trace
2And CH
3OH is adsorbed in adsorber.Afterwards, decontaminating syngas (3-001 flows thigh) then enters the first feed gas chiller in " ice chest ", is cooled to approximately-128 ℃ by several bursts of re-heat logistics; Then entering the second feed gas chiller continues to be cooled to approximately-155 ℃ and the middle part of extracting, deliver to demethanizing tower from the middle part of the second feed gas chiller out by several bursts of re-heat logistics again and enters tower.At this moment, enter the tower logistics near the bubble point state and contain a small amount of liquid phase: vapor phase stream is to cat head, and liquid phase then flows to tower reactor.
Enter tower reactor cut separator after tower reactor cut (the being Sweet natural gas) decompression, the gas/liquid two-phase of separation is the water cooler re-heat to 30 ℃ of normal temperature and delivers to natural gas storage tank or gas distributing system outside the battery limit (BL).3-011 stream thigh during its gaseous constituent and quantity see attached list.
The tower reactor of demethanizing tower is provided with reboiler, and the thermal source system of reboiler is provided by the hot logistics in the first feed gas chiller (from the decontaminating syngas of low-temperature rectisol, seeing schema), and returns demethanizing tower by still liquid recycle pump pump circulation.The overhead gas of demethanizing tower is sent in the second feed gas chiller, continue by several bursts of re-heat logistics then to deliver to the trim the top of column separator of demethanizing tower after approximately-158 ℃ being cooled to approximately-178 ℃, extract out from the second feed gas chiller again.In the trim the top of column separator, gas/liquid two is separated: liquid phase is sent into demethanizing tower with pump pressure and is made phegma; Gas phase (contains CH
4Be about: 1%) be synthetic gas after the demethanizing then send back to again the second feed gas chiller continue to be cooled to approximately-187 ℃ by several bursts of re-heat logistics after (because of CH
4Content only 1% is owing to there being the N of considerable part
2Liquefaction, and the ice that can not occur condensing is stifled), as the feeding gas of nitrogen wash column (C04301) bottom.
The structure of demethanizing tower and size: Φ 1600-1100; H (tangent line height) approximately 30000; Theoretical plate number: 12; Plate efficiency: 0.33; Tower tray form: 25 * 25 square float valves.
Gas after the demethanizing of the bottom of nitrogen wash column rises along tower, by from its contained CO and Ar etc. under the liquid nitrogen washing of cat head.
Discharge purified gas from the top of nitrogen wash column, it contains C0≤3ppm, and temperature approximately-189 ℃ first through the second feed gas chiller re-heat, makes its H through joining nitrogen mixing tank (SP04301) again
2/ N
2Than being divided into two strands after being about 3/1: one returns cold to low temperature washing device for methanol again, and another thigh then ℃ is sent ice chest through the re-heat to 30 of elevated pressure nitrogen water cooler.Two strands of gases converge outside ice chest, join nitrogen through essence again and make its H
2/ N
2Than being 3/1, arriving afterwards subsequent processing---ammonia synthesis.
Go out the pressure of the refining synthetic gas of liquid nitrogen washing: 2.85Mpa, temperature: 30 ℃, and very clean.Its gaseous constituent and quantity are as follows: the 3-040 stream number of share of stock certificate in seeing attached list.
The liquid phase of discharging from the still section of nitrogen wash column enters the tower reactor separator.At the tower reactor separator, be divided into the gas/liquid two-phase: gas phase is the H of dissolving
2Through the second feed gas chiller, the first feed gas chiller and the re-heat to 30 of elevated pressure nitrogen water cooler ℃, send ice chest and to the recycle gas compressor pressurization of low temperature washing device for methanol; (the excessive liquid N of CO+Ar+ of liquid phase system
2) etc. ℃ send ice chest and to the fuel gas pipe network of factory through the second feed gas chiller, the first feed gas chiller and the re-heat to 30 of elevated pressure nitrogen water cooler.
The elevated pressure nitrogen that liquid nitrogen washing is used is available pressure both: 5.0Mpa, temperature: approximately 40 ℃, and also available pressure: 3.0Mpa, temperature: approximately 40 ℃.Different is: if use pressure: 3.0Mpa, temperature: about 40 ℃ nitrogen then than using pressure: 5.0Mpa, temperature: approximately the required cold of confessing to ice chest of 40 ℃ nitrogen is more, and namely more to the liquid nitrogen that system replenishes, this is high pressure N
2Incorporate H into
2The result of Shi Fasheng J-T effect.
Native system is selected the pressure of elevated pressure nitrogen: 5.0Mpa, temperature: approximately 40 ℃.
Elevated pressure nitrogen by elevated pressure nitrogen water cooler, the first feed gas chiller and part by the second feed gas chiller be as cold as-186 ℃ become liquid nitrogen after, send the top of nitrogen wash column, as the washings of nitrogen wash column; By the second feed gas chiller cooling, namely extract out from the outlet of the first feed gas chiller, flow through and join nitrogen mixing tank (SP04301), come gas to mix with cat head from nitrogen wash column, and make the H in the gas mixture
2/ N
2Be about 3/1 than reaching.
The cold of system is not enough, then provides by liquid nitrogen and keeps balance.
(pressure is this liquid nitrogen: 0.25Mpa) be from air separation facility.
Liquid nitrogen is introduced into tower reactor cut separator, and gas/liquid then enters respectively the second feed gas chiller, the first feed gas chiller and elevated pressure nitrogen water cooler afterwards.Its pressure is: gasification under the 0.20Mpa, heating, surrender cold after, about 0.15Mpa can deliver to the low pressure N2 gas pipe network of full factory.
When high pressure nitrogen was selected the pressure of 5.0Mpa, the amount of liquid nitrogen that native system (the cold damage that comprises system) will replenish: 4740Kg/h namely needed external system for cold to be: 550Kw
Claims (10)
1. the system of holding concurrently is produced the liquid nitrogen washing device of Sweet natural gas, comprise the first feed gas chiller (1), the second feed cooler (2), nitrogen wash column (3) and decontaminating syngas pipeline, described decontaminating syngas pipeline flow through successively the first feed gas chiller (1) and the second feed cooler (2), characterized by further comprising demethanizing tower (5), described demethanizing tower (5) is established inlet end, outlet side and cut output terminal, described decontaminating syngas pipeline is flowed through and is communicated with described inlet end after the second feed cooler, and described outlet side and described nitrogen wash column (3) pass through pipeline connection.
2. double system according to claim 1 is produced the liquid nitrogen washing device of Sweet natural gas, it is characterized in that described inlet end, outlet side, cut output terminal lay respectively at middle part, top and the bottom of described demethanizing tower (5).
3. double system according to claim 1 is produced the liquid nitrogen washing device of Sweet natural gas, characterized by further comprising elevated pressure nitrogen water cooler (4) and tower reactor cut separator (6), described tower reactor cut separator (6) is provided with the first separator input terminus, the first liquid phase output terminal and the first gas phase output terminal, described the first separator input terminus connects described cut output terminal by pipeline, described the first liquid phase output terminal be connected the gas phase output terminal and connect the Sweet natural gas delivery conduit, described Sweet natural gas delivery conduit the first feed gas chiller (1) of flowing through successively, the second feed cooler (2) and elevated pressure nitrogen water cooler (4).
According to claim 2 or 3 described double systems produce the liquid nitrogen washing device of Sweet natural gases, characterized by further comprising trim the top of column separator (7), described trim the top of column separator (7) is established the second separator input terminus, second liquid phase output terminal and the second gas phase output terminal, described the second separator input terminus is by the described outlet side of pipeline connection, and described the second gas phase output terminal is by the described nitrogen wash column of pipeline connection (3); Described demethanizing tower is established the liquid-phase reflux end, and described second liquid phase output terminal is by the described liquid-phase reflux end of pipeline connection.
5. double system according to claim 4 is produced the liquid nitrogen washing device of Sweet natural gas, it is characterized in that described liquid-phase reflux end is positioned at the top of described demethanizing tower.
6. double system according to claim 4 is produced the liquid nitrogen washing device of Sweet natural gas, it is characterized in that establishing liquid phase usefulness pump (9) on described second liquid phase output terminal and the pipeline that the liquid-phase reflux end is communicated with.
7. double system according to claim 4 is produced the liquid nitrogen washing device of Sweet natural gas, it is characterized in that pipeline that described outlet side is communicated with the second separator input terminus described the second feed cooler (2) of flowing through, the pipeline that described the second gas phase output terminal is communicated with nitrogen wash column (3) described the second feed cooler (2) of flowing through.
According to claim 2 or 3 described double systems produce the liquid nitrogen washing device of Sweet natural gases, it is characterized in that described demethanizing tower (5) tower reactor is provided with reboiler (8).
9. double system according to claim 8 is produced the liquid nitrogen washing device of Sweet natural gas, it is characterized in that described reboiler (8) establishes still liquid recycle pump (10).
10. double system according to claim 8 is produced the liquid nitrogen washing device of Sweet natural gas, it is characterized in that described decontaminating syngas pipeline flow through successively the first feed gas chiller (1), reboiler, the first feed gas chiller (1), the second feed gas chiller (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210564062.6A CN103043609B (en) | 2012-12-24 | 2012-12-24 | Liquid nitrogen washing device with function of producing natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210564062.6A CN103043609B (en) | 2012-12-24 | 2012-12-24 | Liquid nitrogen washing device with function of producing natural gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103043609A true CN103043609A (en) | 2013-04-17 |
| CN103043609B CN103043609B (en) | 2015-01-21 |
Family
ID=48056502
Family Applications (1)
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|---|---|---|---|
| CN201210564062.6A Active CN103043609B (en) | 2012-12-24 | 2012-12-24 | Liquid nitrogen washing device with function of producing natural gas |
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| CN (1) | CN103043609B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105157348A (en) * | 2015-08-17 | 2015-12-16 | 杭州中泰深冷技术股份有限公司 | Liquid nitrogen washing device for recycling LNG and method for liquid nitrogen washing device |
| CN106185801A (en) * | 2016-07-04 | 2016-12-07 | 华陆工程科技有限责任公司 | A kind of scrubbing with liquid nitrogen devices and methods therefor that can reclaim methane |
| CN106642988A (en) * | 2016-12-07 | 2017-05-10 | 中科瑞奥能源科技股份有限公司 | System of utilizing liquid nitrogen wash to produce syngas for synthetic ammonia and LNG |
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| CN102353233A (en) * | 2011-08-03 | 2012-02-15 | 成都蜀远煤基能源科技有限公司 | Process method and device for cryogenically separating and liquefying gas obtained after coal gas methanation |
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| DE3801712A1 (en) * | 1988-01-21 | 1989-07-27 | Linde Ag | Process for purifying a gas mixture |
| US4917716A (en) * | 1988-01-28 | 1990-04-17 | Linde Aktiengesellschaft | Process for purifying a gaseous mixture |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105157348A (en) * | 2015-08-17 | 2015-12-16 | 杭州中泰深冷技术股份有限公司 | Liquid nitrogen washing device for recycling LNG and method for liquid nitrogen washing device |
| CN105157348B (en) * | 2015-08-17 | 2017-06-23 | 杭州中泰深冷技术股份有限公司 | The liquid nitrogen washing device and its method of a kind of recovery LNG |
| CN106185801A (en) * | 2016-07-04 | 2016-12-07 | 华陆工程科技有限责任公司 | A kind of scrubbing with liquid nitrogen devices and methods therefor that can reclaim methane |
| CN106642988A (en) * | 2016-12-07 | 2017-05-10 | 中科瑞奥能源科技股份有限公司 | System of utilizing liquid nitrogen wash to produce syngas for synthetic ammonia and LNG |
| CN106642988B (en) * | 2016-12-07 | 2022-07-05 | 中科瑞奥能源科技股份有限公司 | System for utilize liquid nitrogen to wash and prepare synthetic ammonia feed gas and LNG |
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| Publication number | Publication date |
|---|---|
| CN103043609B (en) | 2015-01-21 |
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