CN202382517U - Cryogenic separation system of using coke-oven gas to produce liquefied natural gas - Google Patents
Cryogenic separation system of using coke-oven gas to produce liquefied natural gas Download PDFInfo
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- CN202382517U CN202382517U CN201120516619XU CN201120516619U CN202382517U CN 202382517 U CN202382517 U CN 202382517U CN 201120516619X U CN201120516619X U CN 201120516619XU CN 201120516619 U CN201120516619 U CN 201120516619U CN 202382517 U CN202382517 U CN 202382517U
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Abstract
The utility model discloses a cryogenic separation system of using coke-oven gas to produce liquefied natural gas, which comprises a methane-hydrogen rectifying column, a methane-nitrogen rectifying column, a feed gas cooler, a nitrogen subcooler, a first overhead condenser for the methane-hydrogen rectifying column, a second overhead condenser for the methane-nitrogen rectifying column and a bottom reboiler for the methane-nitrogen rectifying column, so that a natural gas cryogenic separation pipeline system, a hydrogen-rich recovery pipeline system and a nitrogen-rich pipeline system are formed. The cryogenic separation system further comprises a twin-stage nitrogen expansion refrigerating circulation loop for providing refrigerating capacity for the feed gas cooler and the nitrogen subcooler. The cryogenic separation system of using coke-oven gas to produce liquefied natural gas is low in cost, small in investment, stable in system, simple in operation and high in recovery rate of natural gas.
Description
Technical field
The utility model relates to the system of oven gas preparing liquefied natural gas, especially a kind of cryogenic separation system of oven gas preparing liquefied natural gas.
Background technology
Contain components such as carbon monoxide, methane, hydrogen, nitrogen in the oven gas, calorific value gas in belonging to.Main component after methanation is handled in the oven gas is methane, hydrogen, nitrogen and a small amount of ethane; The cost of producing natural gas with oven gas has bigger competitiveness than coal preparing natural gas; The energy policy that had both met country; Can fully, rationally utilize industrial discharge gas resource, reduce greenhouse gas emission, can bring huge economic benefit for enterprise again simultaneously.In the prior art, cryogenic separation natural gas from oven gas is to adopt the azeotrope kind of refrigeration cycle, and azeotrope need increase storage, the transportation system of each cryogen, and cryogen compressor cost is higher.
The utility model content
The purpose of the utility model is: a kind of cryogenic separation system of oven gas preparing liquefied natural gas is provided, and low, the small investment of cost, the rate of recovery of system stability, simple to operate, natural gas is high.
For realizing above-mentioned purpose, the utility model can be taked following technical proposals:
The cryogenic separation system of a kind of oven gas preparing liquefied natural gas of the utility model; Comprise methane-hydrogen rectifying column; Methane-nitrogen rectifying column; Feed gas chiller, nitrogen subcooler, the overhead condenser one of methane-hydrogen rectifying column; The overhead condenser two of methane-nitrogen rectifying column; And the tower bottom reboiler of methane-nitrogen rectifying column, the unstripped gas that obtains through methanation processing and preliminary treatment is successively through second cooling line of the cooling line of first cooling line of said feed gas chiller, tower bottom reboiler, feed gas chiller, methane-hydrogen rectifying column inlet, methane-hydrogen rectifying Tata bottom outlet, pressure-reducing valve one, methane-nitrogen rectifying column inlet, the heating pipe line of tower bottom reboiler, the 3rd cooling line, pressure-reducing valve three and the natural gas storage tank of feed gas chiller; Constitute the cryogenic separation pipe-line system of natural gas, wherein the outlet of the heating pipe line of tower bottom reboiler also is communicated with ascending air inlet at the bottom of the tower of methane-nitrogen rectifying column; The tower top outlet of methane-hydrogen rectifying column is communicated with the cooling line of overhead condenser one, the first re-heat pipeline of nitrogen subcooler, the first re-heat pipeline and the hydrogen rich gas recovery tube of feed gas chiller successively; Constitute hydrogen rich gas reclaim line system, wherein the outlet of the cooling line of overhead condenser one also is communicated with the overhead reflux liquid inlet of methane-hydrogen rectifying column; The tower top outlet of methane-nitrogen rectifying column is communicated with the cooling line of overhead condenser two, the second re-heat pipeline of nitrogen subcooler, the second re-heat pipeline and the rich nitrogen tube of feed gas chiller successively; Constitute rich nitrogen pipeline system, wherein the outlet of the cooling line of overhead condenser two also is communicated with the overhead reflux liquid inlet of methane-nitrogen rectifying column; Also being included as feed gas chiller and nitrogen subcooler provides the twin-stage nitrogen swell refrigeration closed circuit of cold.
Said twin-stage nitrogen swell refrigeration closed circuit comprises the circulating nitrogen gas compressor, cold junction booster expansion turbine, hot junction booster expansion turbine and J/T valve; Low-pressure nitrogen is divided into two strands through the circulating nitrogen gas compressor boost and after being cooled to room temperature; One gets into the pressurized end supercharging of hot junction booster expansion turbine; Get into the 4th cooling line cooling of unstripped gas heat exchanger then; Extract the expanding end that most of nitrogen gets into said cold junction booster expansion turbine out from unstripped gas heat exchanger middle part, from the 4th re-heat pipeline re-heat of expanding end outlet entering unstripped gas heat exchanger, for feed gas chiller provides cold; Extract cooling line cooling, liquefaction that fraction nitrogen gets into the nitrogen subcooler out from unstripped gas heat exchanger middle part; Through J/T valve decompression refrigeration; Low-temperature receiver as the overhead condenser two of the overhead condenser one of methane-hydrogen rectifying column and methane-nitrogen rectifying column; Said overhead condenser one is respectively methane-hydrogen rectifying column with overhead condenser two, methane-nitrogen rectifying column provides required phegma; After the liquid nitrogen vaporization successively through the 3rd re-heat pipeline of nitrogen subcooler and the 5th re-heat pipeline re-heat of feed gas chiller, for nitrogen subcooler and feed gas chiller provide cold; Another strand gets into the pressurized end supercharging of cold junction booster expansion turbine; Get into the 5th cooling line cooling of unstripped gas heat exchanger then; Get into the expanding end of cold junction booster expansion turbine then; From the 3rd re-heat pipeline re-heat of expanding end outlet entering unstripped gas heat exchanger, for feed gas chiller provides cold; From the nitrogen of the 3rd, the 4th and the 5th re-heat pipeline of feed gas chiller, import the inlet of circulating nitrogen gas compressor, get into kind of refrigeration cycle next time.
Be provided with nitrogen in the said twin-stage nitrogen swell refrigeration closed circuit and replenish mouth, said nitrogen replenishes mouth and links to each other with circulating nitrogen gas suction port of compressor pipeline.
Compared with prior art the beneficial effect of the utility model is: because the utility model utilizes backflow nitrogen, rich nitrogen, hydrogen rich gas of low pressure to provide cold to provide cold to cool off unstripped gas and supercharging nitrogen to feed gas chiller; Utilize backflow nitrogen, rich nitrogen, hydrogen rich gas of low pressure to provide cold to cool off liquid nitrogen for the nitrogen subcooler; Reduced the energy consumption of whole system, again because the mode that has adopted circulation of twin-stage nitrogen swell refrigeration and liquid nitrogen throttling refrigeration to combine makes the equipment investment of separating natural gas reduce greatly; And further reduced the energy consumption of whole system; System stability is good, and is simple to operate, and the rate of recovery of natural gas is high.
Description of drawings
Fig. 1 is the structural representation of cryogenic separation system of the oven gas preparing liquefied natural gas of the utility model.
The specific embodiment
As shown in Figure 1, the cryogenic separation system of a kind of oven gas preparing liquefied natural gas of the utility model comprises methane-hydrogen rectifying column T-101; Methane-nitrogen rectifying column T-102, feed gas chiller E-201, nitrogen subcooler E-202; Overhead condenser one E-104 of methane-hydrogen rectifying column T-101, overhead condenser two E-105 of methane-nitrogen rectifying column T-102, the tower bottom reboiler E-106 of methane-nitrogen rectifying column T-102; Circulating nitrogen gas compressor C-101, hot junction booster expansion turbine ET-101, cold junction booster expansion turbine ET-102; J/T valve V-102, pressure-reducing valve one V-101 and pressure-reducing valve three V-103;
The unstripped gas that obtains through methanation processing and preliminary treatment; Successively through the second cooling line LY-2 of the cooling line of the first cooling line LY-1 of said feed gas chiller E-201, tower bottom reboiler E-106, feed gas chiller E-201, methane-hydrogen rectifying column T-101 inlet, methane-hydrogen rectifying column T-101 tower bottom outlet, pressure-reducing valve one V-101, methane-nitrogen rectifying column T-102 inlet, the heating pipe line of tower bottom reboiler E-106, the 3rd cooling line LY-3, pressure-reducing valve three V-103 and the natural gas storage tank of feed gas chiller E-201; Constitute the cryogenic separation pipe-line system of natural gas, wherein the outlet of the heating pipe line of tower bottom reboiler E-106 also is communicated with uprising gas inlet at the bottom of the tower of methane-nitrogen rectifying column T-102;
The tower top outlet of methane-hydrogen rectifying column T-101 is communicated with the cooling line of overhead condenser one E-104, the first re-heat pipeline FD-1 of nitrogen subcooler E-202, the first re-heat pipeline FY-1 and the hydrogen rich gas recovery tube of feed gas chiller E-201 successively; Constitute hydrogen rich gas reclaim line system, wherein the outlet of the cooling line of overhead condenser one E-104 also is communicated with the overhead reflux liquid inlet of methane-hydrogen rectifying column T-101;
The tower top outlet of methane-nitrogen rectifying column T-102 is communicated with the cooling line of overhead condenser two E-105, the second re-heat pipeline FD-2 of nitrogen subcooler E-202, the second re-heat pipeline FY-2 and the rich nitrogen tube of feed gas chiller E-201 successively; Constitute rich nitrogen pipeline system, wherein the outlet of the cooling line of overhead condenser two E-105 also is communicated with the overhead reflux liquid inlet of methane-nitrogen rectifying column T-102;
Also being included as feed gas chiller E-201 and nitrogen subcooler E-202 provides the twin-stage nitrogen swell refrigeration closed circuit of cold.Said twin-stage nitrogen swell refrigeration closed circuit comprises circulating nitrogen gas compressor C-101, hot junction booster expansion turbine ET-101, cold junction booster expansion turbine ET-102 and J/T valve V-102; Low-pressure nitrogen is divided into two strands through the C-101 supercharging of circulating nitrogen gas compressor and after being cooled to room temperature; One gets into the pressurized end supercharging of hot junction booster expansion turbine ET-101; Get into the 4th cooling line LY-4 cooling of unstripped gas heat exchanger E-201 then; Extract the expanding end that most of nitrogen gets into said hot junction booster expansion turbine ET-101 out from unstripped gas heat exchanger E-201 middle part; From the 4th re-heat pipeline FY-4 re-heat that the expanding end outlet gets into unstripped gas heat exchanger E-201, E-201 provides cold for feed gas chiller; Extract cooling line LD-1 cooling, liquefaction that fraction nitrogen gets into nitrogen subcooler E-202 out from unstripped gas heat exchanger E-201 middle part; Through J/T valve V-102 decompression refrigeration; Low-temperature receiver as overhead condenser two E-105 of overhead condenser one E-104 of methane-hydrogen rectifying column T-101 and methane-nitrogen rectifying column T-102; Said overhead condenser one E-104 and overhead condenser two E-105 are respectively methane-hydrogen rectifying column T-101, methane-nitrogen rectifying column T-102 provides required phegma; After the liquid nitrogen vaporization successively through the 5th re-heat pipeline FY-5 re-heat of the 3rd re-heat pipeline FD-3 and the feed gas chiller E-201 of nitrogen subcooler E-202, for nitrogen subcooler E-202 and feed gas chiller E-201 provide cold; Another strand gets into the pressurized end supercharging of cold junction booster expansion turbine ET-102; Get into the 5th cooling line LY-5 cooling of unstripped gas heat exchanger E-201 then; Get into the expanding end of cold junction booster expansion turbine ET-102 then; From the 3rd re-heat pipeline FY-3 re-heat that the expanding end outlet gets into unstripped gas heat exchanger E-201, E-201 provides cold for feed gas chiller; From the 3rd, the 4th and the 5th re-heat pipeline FY-3 of feed gas chiller E-201,4 and 5 nitrogen, import the inlet of circulating nitrogen gas compressor C-101, get into kind of refrigeration cycle next time.
As preferably, be provided with nitrogen in the said twin-stage nitrogen swell refrigeration closed circuit and replenish mouth, said nitrogen replenishes mouth and links to each other with the entrance pipe of circulating nitrogen gas compressor C-101.
The utility model deep cooling separating method is following:
Step 1: oven gas obtains main component after methanation processing and preliminary treatment be that the pressure of methane, hydrogen, nitrogen and a small amount of ethane is the unstripped gas of 1.7～2.1Mpa; After the first cooling line LY-1 that said unstripped gas is imported feed gas chiller E-201 is cooled to-120～-126 ℃; Extract out from said feed gas chiller E-201 middle part; Import the thermal source of tower bottom reboiler E-106 then as this tower bottom reboiler E-106; The second cooling line LY-2 that imports feed gas chiller E-201 then continues to be cooled to-140～-150 ℃; The unstripped gas that contains small amount of liquid that comes out from feed gas chiller E-201 imports methane-hydrogen rectifying column T-101, obtains the tower bottom liquid product of cat head hydrogen-rich gas and-150～-160 ℃ after the rectifying, and the main component of this tower bottom liquid product is nitrogen, methane and hydrogen;
Step 2: with said cat head hydrogen-rich gas successively through the cooling line of overhead condenser one E-104, the first re-heat pipeline FD-1 of nitrogen subcooler E-202, the first re-heat pipeline FY-1 of feed gas chiller E-201; For said nitrogen subcooler E-202 and feed gas chiller E-201 provide cold, return behind re-heat to the normal temperature methanation reaction device or through PSA purify high-purity hydrogen; Said tower bottom liquid product is imported methane-nitrogen rectifying column T-102 after pressure-reducing valve one V-101 is decompressed to 0.3～0.42Mpa, obtains methane production and the rich nitrogen of cat head at the bottom of the tower after the rectifying; The rich nitrogen of said cat head is that nitrogen subcooler E-202 and feed gas chiller E-201 provide cold through cooling line, the second re-heat pipeline FD-2 of nitrogen subcooler E-202, the feed gas chiller E-201 second re-heat pipeline FY-2 of overhead condenser two E-105 successively; Methane production after the 3rd cooling line LY-3 of the heating pipe line of tower bottom reboiler E-106, feed gas chiller E-201 crosses cold 6～8 ℃, pressure-reducing valve three V-103 and is decompressed to required pressure, imports natural gas storage tank successively at the bottom of the said tower;
Said feed gas chiller E-201 and nitrogen subcooler E-202 adopt the circulation of twin-stage nitrogen swell refrigeration: pressure is that the low-pressure nitrogen of 0.28～0.36Mpa is divided into two strands through the C-101 supercharging of circulating nitrogen gas compressor and after being cooled to room temperature; One pressurized end that gets into hot junction booster expansion turbine ET-101 is pressurized to 2.2～2.4Mpa; The 4th cooling line LY-4 that gets into unstripped gas heat exchanger E-201 then is cooled to-25 ℃; Extract the expanding end that most of nitrogen gets into said hot junction booster expansion turbine ET-101 out from unstripped gas heat exchanger E-201 middle part; The pressure that exports out from expanding end is that 0.3～0.4Mpa, temperature are-165 ℃ nitrogen; Get into i.e. the 4th re-heat pipeline FY-4 re-heat of low-pressure nitrogen passage of unstripped gas heat exchanger E-201, E-201 provides cold for feed gas chiller; From the cooling line LD-1 of unstripped gas heat exchanger E-201 middle part extraction fraction nitrogen entering nitrogen subcooler E-202, liquefy, be cooled to-170～-180 ℃; Through J/T valve V-102 decompression refrigeration; Low-temperature receiver as overhead condenser two E-105 of overhead condenser one E-104 of methane-hydrogen rectifying column T-101 and methane-nitrogen rectifying column T-102; Said overhead condenser one E-104 is that methane-hydrogen rectifying column T-101 provides required phegma; Said overhead condenser two E-105 are that methane-nitrogen rectifying column T-102 provides required phegma; The main component of said phegma is nitrogen, methane and hydrogen, after the liquid nitrogen vaporization successively through the 5th re-heat pipeline FY-5 re-heat of the 3rd re-heat pipeline FD-3 and the feed gas chiller E-201 of nitrogen subcooler E-202, for nitrogen subcooler E-202 and feed gas chiller E-201 provide cold; The pressurized end that another strand gets into cold junction booster expansion turbine ET-102 is pressurized to 1.7～1.85Mpa; The 5th cooling line LY-5 that gets into unstripped gas heat exchanger E-201 then is cooled to-110～-120 ℃; Get into the expanding end of ET-102 then; From i.e. the 3rd re-heat pipeline FY-3 re-heat of low-pressure nitrogen passage that the expanding end outlet gets into unstripped gas heat exchanger E-201, E-201 provides cold for feed gas chiller; From the 3rd, the 4th and the 5th re-heat pipeline FY-3 of feed gas chiller E-201,4 and 5 nitrogen, import the inlet of circulating nitrogen gas compressor C-101, get into kind of refrigeration cycle next time.
As preferably, in the nitrogen of said twin-stage nitrogen swell refrigeration circulation, add 5%～15% methane gas, purpose is to optimize heat exchange, cuts down the consumption of energy.
Use the obtainable liquefied natural gas purity of the utility model about 92%, ethane content is about 7%, yield 99%; The yield of byproduct recycle hydrogen about 99%; Specific energy consumption is 0.65kw.h/Nm3 LNG.
The utility model is not limited to the above-mentioned specific embodiment, and any technical scheme that is equal to mutually with the utility model, or the simple replacement that the utility model is carried out are all at the protection domain of the utility model.
Claims (3)
1. the cryogenic separation system of an oven gas preparing liquefied natural gas comprises methane-hydrogen rectifying column (T-101), methane-nitrogen rectifying column (T-102); Feed gas chiller (E-201); Nitrogen subcooler (E-202), the overhead condenser one (E-104) of methane-hydrogen rectifying column (T-101), the overhead condenser two (E-105) of methane-nitrogen rectifying column (T-102); And the tower bottom reboiler (E-106) of methane-nitrogen rectifying column (T-102)
The unstripped gas that obtains through methanation processing and preliminary treatment; Successively through second cooling line (LY-2) of the cooling line of first cooling line (LY-1) of said feed gas chiller (E-201), tower bottom reboiler (E-106), feed gas chiller (E-201), methane-hydrogen rectifying column (T-101) inlet, methane-hydrogen rectifying column (T-101) tower bottom outlet, pressure-reducing valve one (V-101), methane-nitrogen rectifying column (T-102) inlet, the heating pipe line of tower bottom reboiler (E-106), the 3rd cooling line (LY-3), pressure-reducing valve three (V-103) and the natural gas storage tank of feed gas chiller (E-201); Constitute the cryogenic separation pipe-line system of natural gas, wherein the outlet of the heating pipe line of tower bottom reboiler (E-106) also is communicated with ascending air inlet at the bottom of the tower of methane-nitrogen rectifying column (T-102);
The tower top outlet of methane-hydrogen rectifying column (T-101) is communicated with the cooling line of overhead condenser one (E-104), the first re-heat pipeline (FD-1) of nitrogen subcooler (E-202), the first re-heat pipeline (FY-1) and the hydrogen rich gas recovery tube of feed gas chiller (E-201) successively; Constitute hydrogen rich gas reclaim line system, wherein the outlet of the cooling line of overhead condenser one (E-104) also is communicated with the overhead reflux liquid inlet of methane-hydrogen rectifying column (T-101);
The tower top outlet of methane-nitrogen rectifying column (T-102) is communicated with the cooling line of overhead condenser two (E-105), the second re-heat pipeline (FD-2) of nitrogen subcooler (E-202), the second re-heat pipeline (FY-2) and the rich nitrogen tube of feed gas chiller (E-201) successively; Constitute rich nitrogen pipeline system, wherein the outlet of the cooling line of overhead condenser two (E-105) also is communicated with the overhead reflux liquid inlet of methane-nitrogen rectifying column (T-102);
It is characterized in that: also be included as the twin-stage nitrogen swell refrigeration closed circuit that feed gas chiller (E-201) and nitrogen subcooler (E-202) provide cold.
2. the cryogenic separation system of a kind of oven gas preparing liquefied natural gas according to claim 1; It is characterized in that: said twin-stage nitrogen swell refrigeration closed circuit; Comprise circulating nitrogen gas compressor (C-101); Hot junction booster expansion turbine (ET-101), cold junction booster expansion turbine (ET-102) and J/T valve (V-102); Low-pressure nitrogen is divided into two strands through (C-101) supercharging of circulating nitrogen gas compressor and after being cooled to room temperature; One gets into the pressurized end supercharging of hot junction booster expansion turbine (ET-101); Get into the 4th cooling line (LY-4) cooling of unstripped gas heat exchanger (E-201) then; Extract the expanding end that most of nitrogen gets into said hot junction booster expansion turbine (ET-101) out from unstripped gas heat exchanger (E-201) middle part; From the 4th re-heat pipeline (FY-4) re-heat that the expanding end outlet gets into unstripped gas heat exchanger (E-201), (E-201) provides cold for feed gas chiller; Extract cooling line (LD-1) cooling, liquefaction that fraction nitrogen gets into nitrogen subcooler (E-202) out from unstripped gas heat exchanger (E-201) middle part; Through J/T valve (V-102) decompression refrigeration; Low-temperature receiver as the overhead condenser two (E-105) of the overhead condenser one (E-104) of methane-hydrogen rectifying column (T-101) and methane-nitrogen rectifying column (T-102); Said overhead condenser one (E-104) and overhead condenser two (E-105) are respectively methane-hydrogen rectifying column (T-101), methane-nitrogen rectifying column (T-102) provides required phegma; After the liquid nitrogen vaporization successively through the 3rd re-heat pipeline (FD-3) of nitrogen subcooler (E-202) and the 5th re-heat pipeline (FY-5) re-heat of feed gas chiller (E-201), for nitrogen subcooler (E-202) and feed gas chiller (E-201) provide cold; Another strand gets into the pressurized end supercharging of cold junction booster expansion turbine (ET-102); Get into the 5th cooling line (LY-5) cooling of unstripped gas heat exchanger (E-201) then; Get into the expanding end of cold junction booster expansion turbine (ET-102) then; From the 3rd re-heat pipeline (FY-3) re-heat that the expanding end outlet gets into unstripped gas heat exchanger (E-201), (E-201) provides cold for feed gas chiller;
From the nitrogen of the 3rd, the 4th and the 5th re-heat pipeline (FY-3,4 and 5) of feed gas chiller (E-201), import the inlet of circulating nitrogen gas compressor (C-101), get into kind of refrigeration cycle next time.
3. the cryogenic separation system of a kind of oven gas preparing liquefied natural gas according to claim 2; It is characterized in that: be provided with nitrogen in the said twin-stage nitrogen swell refrigeration closed circuit and replenish mouth, said nitrogen replenishes mouth and links to each other with circulating nitrogen gas compressor (C-101) entrance pipe.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201120516619XU CN202382517U (en) | 2011-12-13 | 2011-12-13 | Cryogenic separation system of using coke-oven gas to produce liquefied natural gas |
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| CN201120516619XU CN202382517U (en) | 2011-12-13 | 2011-12-13 | Cryogenic separation system of using coke-oven gas to produce liquefied natural gas |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102435044A (en) * | 2011-12-13 | 2012-05-02 | 杭州中泰深冷技术股份有限公司 | Cryogenic separating system for preparing liquefied natural gas with oven gas |
| CN103776238A (en) * | 2012-10-18 | 2014-05-07 | 林德股份公司 | Method and equipment for separating methane from synthesis gas |
| CN103983086A (en) * | 2014-05-19 | 2014-08-13 | 杭州杭氧股份有限公司 | Synthesis gas separation system suitable for methyl alcohol making device by coal and cryogenic separation method for making LNG (liquefied natural gas) |
| CN104293402A (en) * | 2014-09-26 | 2015-01-21 | 成都赛普瑞兴科技有限公司 | Method of separating and purifying methane gas containing hydrogen gas and carbon monoxide to prepare liquefied natural gas |
| CN109028756A (en) * | 2018-05-23 | 2018-12-18 | 上海交通大学 | A method of coke-stove gas is separated using helium swell refrigeration |
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2011
- 2011-12-13 CN CN201120516619XU patent/CN202382517U/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102435044A (en) * | 2011-12-13 | 2012-05-02 | 杭州中泰深冷技术股份有限公司 | Cryogenic separating system for preparing liquefied natural gas with oven gas |
| CN102435044B (en) * | 2011-12-13 | 2014-05-07 | 杭州中泰深冷技术股份有限公司 | Cryogenic separating system for preparing liquefied natural gas with oven gas |
| CN103776238A (en) * | 2012-10-18 | 2014-05-07 | 林德股份公司 | Method and equipment for separating methane from synthesis gas |
| CN103983086A (en) * | 2014-05-19 | 2014-08-13 | 杭州杭氧股份有限公司 | Synthesis gas separation system suitable for methyl alcohol making device by coal and cryogenic separation method for making LNG (liquefied natural gas) |
| CN103983086B (en) * | 2014-05-19 | 2016-03-30 | 杭州杭氧股份有限公司 | A kind of method being applicable to synthesis gas piece-rate system in ammonia from coal device and cryogenic separation LNG |
| CN104293402A (en) * | 2014-09-26 | 2015-01-21 | 成都赛普瑞兴科技有限公司 | Method of separating and purifying methane gas containing hydrogen gas and carbon monoxide to prepare liquefied natural gas |
| CN109028756A (en) * | 2018-05-23 | 2018-12-18 | 上海交通大学 | A method of coke-stove gas is separated using helium swell refrigeration |
| CN109028756B (en) * | 2018-05-23 | 2019-09-27 | 上海交通大学 | A method of coke-stove gas is separated using helium swell refrigeration |
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Granted publication date: 20120815 |