CN101614464B - Method for liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas - Google Patents
Method for liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas Download PDFInfo
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- CN101614464B CN101614464B CN2008100635235A CN200810063523A CN101614464B CN 101614464 B CN101614464 B CN 101614464B CN 2008100635235 A CN2008100635235 A CN 2008100635235A CN 200810063523 A CN200810063523 A CN 200810063523A CN 101614464 B CN101614464 B CN 101614464B
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 147
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 105
- 239000003345 natural gas Substances 0.000 title claims abstract description 49
- 238000000034 method Methods 0.000 title claims abstract description 25
- 229910001873 dinitrogen Inorganic materials 0.000 title claims abstract description 19
- 238000005057 refrigeration Methods 0.000 claims abstract description 27
- 238000001816 cooling Methods 0.000 claims abstract description 18
- 239000007789 gas Substances 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract 2
- 229910052757 nitrogen Inorganic materials 0.000 claims description 64
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 14
- 238000003303 reheating Methods 0.000 abstract 1
- 238000004781 supercooling Methods 0.000 abstract 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- JVFDADFMKQKAHW-UHFFFAOYSA-N C.[N] Chemical compound C.[N] JVFDADFMKQKAHW-UHFFFAOYSA-N 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
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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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
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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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/24—Multiple compressors or compressor stages in parallel
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
- F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
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- 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 discloses a method for liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas, which comprises the followings steps: pressurizing and cooling the nitrogen gas to obtain high-pressure nitrogen gas of 2.2 to 3.6 MPa; introducing the high-pressure nitrogen gas and raw natural gas into a main heat exchanger so that the gas is cooled to a temperature of between 70 DEG C below zero and 30 DEG C below zero by using low-pressure nitrogen gas at the outlet of a low-temperature expander, then extracting one stream of the cooled gas and introducing the cooled gas into a high-temperature expander for expansion refrigeration, and then returning the gas to a position of which the temperature is between 100 DEG C below zero and 80 DEG C below zero in the main heat exchanger; and continuously cooling the other stream of the gas to a temperature of between 110 DEG C below zero and 70 DEG C below zero, then introducing the gas into the low-temperature expander for expansion refrigeration, returning the gas into the main heat exchanger to reheat the gas to a temperature of between 100 DEG C below zero and 80 DEG C below zero, joining the gas with the nitrogen gas after the expansion refrigeration by the high-temperature expander, continuously reheating the mixed gas out of the main heat exchanger, and simultaneously cooling and liquefying the raw natural gas by the low-pressure nitrogen gas, and taking the raw natural gas out of the main heat exchanger after super cooling; and throttling and separating the raw natural gas getting out of the main heat exchanger to obtain the liquid state natural gas. The method is suitable for high-low temperature areas, and has high liquefaction rate which can reach 100 percent.
Description
Technical field
The present invention relates to a kind of natural gas liquefaction, relate in particular to a kind of method for liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas.
Background technology
Along with the development of society, the petroleum storage amount is reducing, and greenhouse effects are more and more obvious; People are also more and more strong to the requirement of green energy resource, so natural gas has obtained extensive use.Be gaseous state but natural gas extraction is come out, may transport hardly, so just restricted its widely and used.The liquefaction ratio of natural gas is 591, if natural gas liquefaction, and 591 times of volume-diminished, transportation just becomes possibility, so a large amount of natural gas liquefaction devices just occurred.The liquefaction process of natural gas mainly contains nitrogen swell refrigeration flow process, nitrogen-methane swell refrigeration flow process, mixed working fluid cooling flow etc.Here mainly introduce the liquefying high-low pressure nitrogen double-expansion natural gas flow process.
Wherein nitrogen swell refrigeration flow process is divided into according to user's output and pressure difference again: nitrogen list swell refrigeration flow process (being mainly used in output less than 30 tons/day), refrigerator adds nitrogen list swell refrigeration flow process (being mainly used in output is 30 ~ 100 tons/day), and nitrogen double-expansion system flow process (being mainly used in output is 100 ~ 600 tons/day) is cold.But also be not used in the liquefaction flow path of the promptly two warm areas of high low temperature, mainly introduce the liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas flow process here, this flow process is a kind of of nitrogen double-expansion system flow process.
Summary of the invention
The purpose of this invention is to provide a kind of method for liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas, solved problems of the prior art.
The technical solution adopted in the present invention is that method for liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas comprises the steps:
A, nitrogen are compressed to 1.5～2.5MPa, are cooled to 30～45 ℃;
The nitrogen part that b, step a obtain enters the pressurized end of high temperature pressurised machine, 2.2～3.6MPa the high pressure nitrogen that obtains is cooled to 30～45 ℃ through first aftercooler, another part enters the pressurized end of low temperature supercharger, and the 2.2～3.6MPa high pressure nitrogen that obtains is cooled to 30～45 ℃ through second aftercooler;
C, entered 0.6～1.0MPa low-pressure nitrogen cooling that main heat exchanger is exported by cryogenic expansion machine by cooled all high pressure nitrogens of step b and 1.0MPa～10Mpa raw natural gas, high pressure nitrogen is extracted one out after being cooled to-70～-30 ℃, return on ℃ temperature position, main heat exchanger-100～-80 after sending into high temperature decompressor swell refrigeration, obtain 0.6～1.0MPa low-pressure nitrogen after sending into the cryogenic expansion machine swell refrigeration after another strand continues to be cooled to-110～-70 ℃, 0.6～1.0MPa low-pressure nitrogen returns the main heat exchanger re-heat, re-heat to-100～-80 ℃ with high temperature decompressor swell refrigeration after nitrogen converge the back and continue to be gone out main heat exchanger by re-heat, 1.0MPa～10Mpa raw natural gas is continued cooling by low-pressure nitrogen simultaneously, liquefaction, cross and go out main heat exchanger after cold;
D, go out main heat exchanger raw natural gas through the choke valve throttling, after separate to irritate separating, obtain liquified natural gas and send into storage tank, gas returns main heat exchanger and reclaims cold.
Because method provided by the invention adopts high temperature pressurised machine and the supercharging of low temperature supercharger, so high temperature decompressor and cryogenic expansion machine swell refrigeration are applicable to high low-temperature space.And the liquefied fraction height can reach 100%.
Description of drawings
Fig. 1 is a principle schematic of the present invention.
The specific embodiment
The present invention is described in detail below in conjunction with the drawings and specific embodiments.
The invention provides a kind of method for liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas, comprise the steps:
A, nitrogen are compressed to 1.5～2.5MPa through recycle compressor, cool off to 30～45 ℃ through recirculated water again;
The nitrogen part that b, step a obtain enters the pressurized end of high temperature pressurised machine 1,2.2～3.6MPa the high pressure nitrogen that obtains is cooled to 30～45 ℃ through first aftercooler 3, another part enters the pressurized end of low temperature supercharger 2, and the 2.2～3.6MPa high pressure nitrogen that obtains is cooled to 30～45 ℃ through second aftercooler 4;
C, entered 0.6～1.0MPa low-pressure nitrogen cooling that main heat exchanger 9 is exported by cryogenic expansion machine 6 by cooled all high pressure nitrogens of step b and 1.0MPa～10Mpa raw natural gas, high pressure nitrogen is extracted one out after being cooled to-70～-30 ℃, send into high temperature decompressor 5, in expansion ratio is 2～3, high pressure 3.0MPa, after high temperature-50 ℃ following the expansion, return on ℃ temperature position, main heat exchanger-100～-80, after continuing to be cooled to-110～-70 ℃, another strand send into cryogenic expansion machine 6, in expansion ratio is 2～3, high pressure 3.0MPa, obtain 0.6～1.0MPa low-pressure nitrogen behind the low temperature-90 ℃ following swell refrigeration, 0.6～1.0MPa low-pressure nitrogen returns the main heat exchanger re-heat, re-heat to-100～-80 ℃ with high temperature decompressor 5 swell refrigerations after nitrogen converge the back and continue to be gone out main heat exchanger 9 by re-heat, 1.0MPa～10Mpa raw natural gas is continued cooling by 0.6～1.0MPa low-pressure nitrogen simultaneously, liquefaction, cross and go out main heat exchanger after cold;
D, go out main heat exchanger 1.0MPa～10Mpa raw natural gas through choke valve 7 throttlings, separate to irritate 8 separate after, to obtain pressure be the liquified natural gas of 0.6MPa～1.0Mpa and send into storage tank, gas returns main heat exchanger and reclaims cold.
A, nitrogen are compressed to 1.5MPa through recycle compressor, cool off to 30 ℃ through recirculated water again;
The nitrogen part that b, step a obtain enters the pressurized end of high temperature pressurised machine 1, the 2.2MPa high pressure nitrogen that obtains is cooled to 30 ℃ through first aftercooler 3, the pressurized end that another part enters low temperature supercharger 2 obtains the 2.2MPa high pressure nitrogen, is cooled to 30 ℃ through second aftercooler 4;
C, entered the 0.6MPa low-pressure nitrogen cooling that main heat exchanger 9 is exported by cryogenic expansion machine 6 by cooled all high pressure nitrogens of step b and 1.0MPa raw natural gas, high pressure nitrogen is extracted one out after being cooled to-30 ℃, send into high temperature decompressor 5, in expansion ratio is 2, high pressure 3.0MPa, after high temperature-50 ℃ following the expansion, return on the main heat exchanger-80 ℃ temperature position, after continuing to be cooled to-70 ℃, another strand send into cryogenic expansion machine 6, in expansion ratio is 2, high pressure 3.0MPa, obtain the 0.6MPa low-pressure nitrogen behind the low temperature-90 ℃ following swell refrigeration, 0.6MPa low-pressure nitrogen returns the main heat exchanger re-heat, re-heat to-80 ℃ with high temperature decompressor 5 swell refrigerations after nitrogen converge the back and continue to be gone out main heat exchanger 9 by re-heat, raw natural gas is continued cooling by the 0.6MPa low-pressure nitrogen simultaneously, liquefaction, cross and go out main heat exchanger after cold;
D, go out main heat exchanger raw natural gas through choke valve 7 throttlings, separate to irritate 8 separate after, to obtain pressure be the liquified natural gas of 0.6Mpa and send into storage tank, gas returns main heat exchanger and reclaims cold.
A, nitrogen are compressed to 2.5MPa through recycle compressor, cool off to 45 ℃ through recirculated water again;
The nitrogen part that b, step a obtain enters the pressurized end of high temperature pressurised machine 1, the 3.6MPa high pressure nitrogen that obtains is cooled to 45 ℃ through first aftercooler 3, another part enters the pressurized end of low temperature supercharger 2, and the 3.6MPa high pressure nitrogen that obtains is cooled to 45 ℃ through second aftercooler 4;
C, entered the 1.0MPa low-pressure nitrogen cooling that main heat exchanger 9 is exported by cryogenic expansion machine 6 by cooled all high pressure nitrogens of step b and 10Mpa raw natural gas, high pressure nitrogen is extracted one out after being cooled to-70 ℃, sending into high temperature decompressor 5 is 3 in expansion ratio, high pressure 3.0MPa, after high temperature-50 ℃ following the expansion, return on the main heat exchanger-100 ℃ temperature position, after continuing to be cooled to-110 ℃, another strand send into cryogenic expansion machine 6, in expansion ratio is 3, high pressure 3.0MPa, behind the low temperature-90 ℃ following swell refrigeration, return the main heat exchanger re-heat, re-heat to-100 ℃ with high temperature decompressor 5 swell refrigerations after nitrogen converge the back and continue to be gone out main heat exchanger 9 by re-heat, the 10Mpa raw natural gas is continued cooling by the 1.0MPa low-pressure nitrogen simultaneously, liquefaction, cross and go out main heat exchanger after cold;
D, go out main heat exchanger raw natural gas through choke valve 7 throttlings, separate to irritate 8 separate after, to obtain pressure be the liquified natural gas of 1.0Mpa and send into storage tank, gas returns main heat exchanger and reclaims cold.
Embodiment 3
A, nitrogen are compressed to 2MPa through recycle compressor, cool off to 40 ℃ through recirculated water again;
The nitrogen part that b, step a obtain enters the pressurized end of high temperature pressurised machine 1, the 3.0MPa high pressure nitrogen that obtains is cooled to 40 ℃ through first aftercooler 3, another part enters the pressurized end of low temperature supercharger 2, and the 3.0MPa high pressure nitrogen that obtains is cooled to 40 ℃ through second aftercooler 4;
C, entered the 0.7MPa low-pressure nitrogen cooling that main heat exchanger 9 is exported by cryogenic expansion machine 6 by cooled all high pressure nitrogens of step b and 1.6Mpa raw natural gas, high pressure nitrogen is extracted one out after being cooled to-40 ℃, sending into high temperature decompressor 5 is 3 in expansion ratio, high pressure 3.0MPa, behind the high temperature-50 ℃ following swell refrigeration, return on the main heat exchanger-90 ℃ temperature position, after continuing to be cooled to-80 ℃, another strand send into cryogenic expansion machine, in expansion ratio is 3, high pressure 3.0MPa, behind the low temperature-90 ℃ following swell refrigeration, return the main heat exchanger re-heat, re-heat to-90 ℃ with high temperature decompressor 5 swell refrigerations after nitrogen converge the back and continue to be gone out main heat exchanger 9 by re-heat, the 1.6Mpa raw natural gas is continued cooling by the 0.7MPa low-pressure nitrogen simultaneously, liquefaction, cross and go out main heat exchanger after cold;
D, go out main heat exchanger raw natural gas through choke valve 7 throttlings, separate to irritate 8 separate after, to obtain pressure be the liquified natural gas of 0.7Mpa and send into storage tank, gas returns main heat exchanger and reclaims cold.
Embodiment 4
A, nitrogen are compressed to 2.2MPa through recycle compressor, cool off to 35 ℃ through recirculated water again;
The nitrogen part that b, step a obtain enters the pressurized end of high temperature pressurised machine 1, the 2.8MPa high pressure nitrogen that obtains is cooled to 35 ℃ through first aftercooler 3, another part enters the pressurized end of low temperature supercharger 2, and the 2.8MPa high pressure nitrogen that obtains is cooled to 35 ℃ through second aftercooler 4;
C, entered the 0.8MPa low-pressure nitrogen cooling that main heat exchanger 9 is exported by cryogenic expansion machine 6 by cooled all high pressure nitrogens of step b and 5Mpa raw natural gas, high pressure nitrogen is extracted one out after being cooled to-60 ℃, sending into high temperature decompressor 5 is 2 in expansion ratio, high pressure 3.0MPa, behind the high temperature-50 ℃ following swell refrigeration, return on the main heat exchanger-90 ℃ temperature position, after continuing to be cooled to-90 ℃, another strand send into cryogenic expansion machine, in expansion ratio is 2, high pressure 3.0MPa, behind the low temperature-90 ℃ following swell refrigeration, return the main heat exchanger re-heat, re-heat to-90 ℃ with high temperature decompressor 5 swell refrigerations after nitrogen converge the back and continue to be gone out main heat exchanger 9 by re-heat, the 5Mpa raw natural gas is continued cooling by the 0.8MPa low-pressure nitrogen simultaneously, liquefaction, cross and go out main heat exchanger after cold;
D, go out main heat exchanger raw natural gas through choke valve 7 throttlings, separate to irritate 8 separate after, to obtain pressure be the liquified natural gas of 0.9Mpa and send into storage tank, gas returns main heat exchanger and reclaims cold.
Claims (5)
1. method for liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas is characterized in that comprising the steps:
A, nitrogen are compressed to 1.5～2.5MPa, are cooled to 30～45 ℃;
The nitrogen part that b, step a obtain enters the pressurized end of high temperature pressurised machine (1), 2.2～3.6MPa the high pressure nitrogen that obtains is cooled to 30～45 ℃ through first aftercooler (3), another part enters the pressurized end of low temperature supercharger (2), and the 2.2～3.6MPa high pressure nitrogen that obtains is cooled to 30～45 ℃ through second aftercooler (4);
C, entered main heat exchanger (9) by 0.6～1.0MPa low-pressure nitrogen cooling of cryogenic expansion machine (6) outlet by cooled described all high pressure nitrogens of step b and raw natural gas, high pressure nitrogen is extracted one out after being cooled to-70～-30 ℃, return on ℃ temperature position, main heat exchanger-100～-80 after sending into high temperature decompressor (5) swell refrigeration, obtain 0.6～1.0MPa low-pressure nitrogen after sending into cryogenic expansion machine (6) swell refrigeration after another strand continues to be cooled to-110～-70 ℃, 0.6～1.0MPa low-pressure nitrogen returns the main heat exchanger re-heat, re-heat to-100～-80 ℃ with high temperature decompressor (5) swell refrigeration after nitrogen converge the back and continue to be gone out main heat exchanger (9) by re-heat, raw natural gas is continued cooling by 0.6～1.0MPa low-pressure nitrogen simultaneously, liquefaction, cross and go out main heat exchanger after cold;
D, go out main heat exchanger raw natural gas through choke valve (7) throttling, separate to irritate after (8) separate, obtain liquified natural gas and send into storage tank, gas returns main heat exchanger and reclaims cold.
2. method for liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas according to claim 1, it is characterized in that described high temperature decompressor (5) is in ℃ expansion down of high pressure 3.0MPa high temperature-50, expansion ratio is 2～3, cryogenic expansion machine (6) is in ℃ expansion down of high pressure 3.0MPa low temperature-90, and expansion ratio is 2～3.
3. method for liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas according to claim 1 is characterized in that, the pressure of raw natural gas is 1.0MPa～10Mpa.
4. method for liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas according to claim 3 is characterized in that, the pressure of raw natural gas is 1.6MPa～5Mpa.
5. method for liquefying natural gas through double-expansion of high-temperature and low-temperature nitrogen gas according to claim 1 is characterized in that, the liquid natural atmospheric pressure is 0.6MPa～1.0Mpa.
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| CN101858683A (en) * | 2010-04-30 | 2010-10-13 | 浙江大学 | System for producing liquefied natural gas by utilizing liquid nitrogen cold energy |
| EP2893275A1 (en) * | 2012-09-07 | 2015-07-15 | Keppel Offshore&Marine Technology Centre Pte Ltd | System and method for natural gas liquefaction |
| CN106338182B (en) * | 2016-08-25 | 2018-11-06 | 重庆朝阳气体有限公司 | A kind of energy-saving control method of air-seperation system |
| CN110487023B (en) * | 2019-08-12 | 2024-02-23 | 盈德气体工程(浙江)有限公司 | Method for producing liquid nitrogen by utilizing LNG cold energy |
| JP7355979B2 (en) * | 2019-09-26 | 2023-10-04 | レール・リキード－ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | gas liquefaction equipment |
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| FR2116116A5 (en) * | 1970-11-28 | 1972-07-07 | Chiyoda Chem Eng Construct Co | |
| CN87103872A (en) * | 1986-05-02 | 1987-11-18 | 英国氧气集团公司 | Gas liquefaction method and device |
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| WO2007011155A1 (en) * | 2005-07-19 | 2007-01-25 | Shinyoung Heavy Industries Co., Ltd. | Lng bog reliquefaction apparatus |
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| CN101614464A (en) | 2009-12-30 |
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