JP6093457B2 - Natural gas liquefaction method and apparatus - Google Patents
Natural gas liquefaction method and apparatus Download PDFInfo
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- JP6093457B2 JP6093457B2 JP2015562962A JP2015562962A JP6093457B2 JP 6093457 B2 JP6093457 B2 JP 6093457B2 JP 2015562962 A JP2015562962 A JP 2015562962A JP 2015562962 A JP2015562962 A JP 2015562962A JP 6093457 B2 JP6093457 B2 JP 6093457B2
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 42
- 239000003345 natural gas Substances 0.000 title claims description 18
- 238000000034 method Methods 0.000 title claims description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 101
- 239000002826 coolant Substances 0.000 claims description 74
- 229910052757 nitrogen Inorganic materials 0.000 claims description 51
- 239000007789 gas Substances 0.000 claims description 42
- 239000007788 liquid Substances 0.000 claims description 35
- 238000001816 cooling Methods 0.000 claims description 26
- 239000003949 liquefied natural gas Substances 0.000 claims description 21
- 238000004781 supercooling Methods 0.000 claims description 15
- 230000006835 compression Effects 0.000 claims description 9
- 238000007906 compression Methods 0.000 claims description 9
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 9
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 7
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 6
- 238000005194 fractionation Methods 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 239000002737 fuel gas Substances 0.000 claims description 4
- 239000001273 butane Substances 0.000 claims description 3
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 3
- 239000001294 propane Substances 0.000 claims description 3
- 239000008246 gaseous mixture Substances 0.000 claims 1
- 238000011084 recovery Methods 0.000 description 6
- 239000000356 contaminant Substances 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003507 refrigerant 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
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0291—Refrigerant compression by combined gas compression and liquid pumping
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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"
- F25J1/0042—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 liquid expansion with extraction of work
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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
- F25J1/0047—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 an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/005—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 an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
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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
- F25J1/0047—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 an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—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 an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
- F25J1/0055—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 an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream originating from an incorporated cascade
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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
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/007—Primary atmospheric gases, mixtures thereof
- F25J1/0072—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
- 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
- F25J1/0211—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 a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0214—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 a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle
- F25J1/0215—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 a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a dual level refrigeration cascade with at least one MCR cycle with one SCR cycle
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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
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
- F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
- F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
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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
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
- F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
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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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
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Description
本発明は、ガスとその混合物の液化に関連し、天然ガス処理中に使用できる。 The present invention relates to the liquefaction of gases and mixtures thereof and can be used during natural gas processing.
現状の技術は、北極海沿岸或いは近海での天然ガス液化方法（ロシア特許公報第２３４４３５９号、ＣＩ．Ｆ２５Ｊ１／００、２００９年１月２０日）を含む。前記方法は、混入物、重質炭化水素、および窒素の除去によるガス精製用で、なおかつ、それに続くガス液化用の回路はもちろん、分配装置において、圧縮され、冷却された冷却剤の、１：１９〜１：３３の比率の２つの流れへの分配が行われる冷却回路との、２つの回路を備える装置の使用によって実施される。前記冷却剤のより大きな流れは冷却目的の熱交換器（ＨＥ）に送られ、（絞り弁を通過する）より小さな流れは回収塔の反応セクションに送られる。それらの圧力が平衡した後、両方の冷却剤が一緒に混合される。この方法の不都合は電力消費が大きいことである。 Current technology includes a natural gas liquefaction method (Russian Patent Publication No. 2344359, CI.F25J1 / 00, January 20, 2009) on or near the Arctic Ocean. The method is for gas purification by removal of contaminants, heavy hydrocarbons, and nitrogen, and in the distribution apparatus as well as the circuit for the subsequent gas liquefaction, 1: This is done by the use of a device with two circuits, with a cooling circuit in which a distribution of 19 to 1:33 in two streams takes place. The larger stream of the coolant is sent to a heat exchanger (HE) for cooling purposes, and the smaller stream (passing through the throttle valve) is sent to the reaction section of the recovery tower. After their pressures equilibrate, both coolants are mixed together. The disadvantage of this method is high power consumption.
出願人が試作として採用した最も近い既存技術は、天然ガス液化方法とその装置（ロシア特許公報第２３４４３６０号、ＣＩ．Ｆ２５Ｊ１／００、２００９年１月２０日）である。 The closest existing technology adopted by the applicant as a prototype is a natural gas liquefaction method and apparatus (Russian Patent Publication No. 2344360, CI.F25J1 / 00, January 20, 2009).
この方法は、混入物、重質炭化水素、および窒素の除去によるガス精製用で、なおかつ、それに続くガス液化用の回路はもちろん、分配装置において、圧縮され、冷却された冷却剤の、１：１９〜１：３３の比率の２つの流れへの分配が行われる冷却回路との、２つの回路を備える装置の使用によって実施される。前記冷却剤のより大きな流れは冷却目的の熱交換器（ＨＥ）に送られ、（絞り弁を通過する）より小さな流れは回収塔の反応セクションに送られる。それらの圧力が平衡した後、両方の冷却剤が一緒に混合される。前記天然ガス液化装置は、混入物、重質炭化水素、および窒素の除去によるガス精製用で、なおかつ、それに続くガス液化用の回路はもちろん、冷却回路とからなる。液化天然ガス用の前記分配装置は、ミキサーで合流する第１および第２液化ラインに接続される２つの流出口を有する。前記第１液化ラインは第１ＨＥを通過し、前記第２液化ラインは第２ＨＥを通過する。両方のラインはバルブと、液化ガスミキサーでの混合より前に、前記第１および第２冷却ライン内の液化ガスの圧力の平衡を確保する圧力計と、を備え、当該液化ガスミキサーの流出口は第１分離器に接続され、当該第１分離器の頭頂部は、第１ＨＥを通過する第３液化ラインを通って、前記回収塔に接続される。前記回収塔の頭頂部はパイプラインで前記第２ＨＥに接続され、前記回収塔の底部は過冷却ＨＥを通過する第４液化ラインに接続される。前記冷却回路は第１および第２冷却ラインに接続される２つの流出口を有する圧縮冷却分離器を備え、当該第１および第２冷却ラインは第１冷却ミキサーで合流する。前記第１冷却ラインは第３ＨＥを通過し、前記第２冷却ラインは第３絞り弁と前記回収塔の反応セクションを通過する。両方のラインはバルブと、前記第１冷却ミキサーでの混合より前に、前記第１および第２冷却ライン内の前記冷却剤の圧力の平衡を確保する圧力計と、を備える。 This method is for gas purification by removal of contaminants, heavy hydrocarbons, and nitrogen, and of the compressed and cooled coolant in the distributor as well as the circuit for the subsequent gas liquefaction, 1: This is done by the use of a device with two circuits, with a cooling circuit in which a distribution of 19 to 1:33 in two streams takes place. The larger stream of the coolant is sent to a heat exchanger (HE) for cooling purposes, and the smaller stream (passing through the throttle valve) is sent to the reaction section of the recovery tower. After their pressures equilibrate, both coolants are mixed together. The natural gas liquefying apparatus is for gas purification by removing contaminants, heavy hydrocarbons, and nitrogen, and further includes a cooling circuit as well as a subsequent gas liquefying circuit. The distributor for liquefied natural gas has two outlets connected to the first and second liquefaction lines that merge at the mixer. The first liquefaction line passes through the first HE, and the second liquefaction line passes through the second HE. Both lines comprise a valve and a pressure gauge that ensures a balance of the pressure of the liquefied gas in the first and second cooling lines before mixing in the liquefied gas mixer, and the outlet of the liquefied gas mixer Is connected to the first separator, and the top of the first separator is connected to the recovery tower through a third liquefaction line passing through the first HE. The top of the recovery tower is connected to the second HE by a pipeline, and the bottom of the recovery tower is connected to a fourth liquefaction line passing through the supercooling HE. The cooling circuit includes a compression cooling separator having two outlets connected to first and second cooling lines, and the first and second cooling lines are joined by a first cooling mixer. The first cooling line passes through the third HE, and the second cooling line passes through the third throttle valve and the reaction section of the recovery tower. Both lines comprise a valve and a pressure gauge that ensures a balance of the pressure of the coolant in the first and second cooling lines prior to mixing in the first cooling mixer.
上記の方法と装置の使用は、電力消費が大きいことを特徴とする。 The use of the above method and apparatus is characterized by high power consumption.
本発明の応用を通じて到達する技術的な成果は、天然ガス液化処理中に必要とされる電力消費の低下である。 The technical result achieved through the application of the present invention is the reduction in power consumption required during the natural gas liquefaction process.
天然ガス液化の処理フローダイアグラムは、図面に以下のように示される。 The process flow diagram for natural gas liquefaction is shown in the drawing as follows.
本天然ガス液化方法の本質は、前処理済乾燥ガスが、予冷ＨＥにおいて、摂氏マイナス５２〜マイナス５４度の間の範囲の温度まで冷却され、そして、濃縮されることである。それから、分別目的用に供給される液状エタンの留分を除去することによって、前記前処理済乾燥ガスは分離され、そして、第１分離器からのガス流が、液化ＨＥにおいて摂氏マイナス１２０〜マイナス１２５度まで引き続いて冷却され、過冷却熱交換器において摂氏マイナス１５０〜マイナス１６０度まで、気体窒素によって冷却される。過冷却された液化天然ガス（ＬＮＧ）の圧力は、液体膨張器において０．１１〜０．１３ＭＰａになるまで低下させられる。前記過冷却されたＬＮＧは分離目的で供給され、それからＬＮＧ貯蔵タンクに供給される。前記分離されたガスは燃料ガス系に供給され、前記予冷ＨＥからの、窒素、メタン、エタン、プロパン、ブタンおよびペンタンを包含する混合冷却剤は３．０〜３．１ＭＰａになるまで圧縮され、摂氏２６〜３０度に冷却され、そして、重液体冷却剤と軽気体冷却剤に分離される。前記重液体冷却剤は、直前の分離器からの重液体冷却剤と混和するために吸い出される。前記重液体混合冷却剤と前記軽気体混合冷却剤は、重冷却剤と軽冷却剤の低圧（ＬＰ）の混合対向流を注入することによって摂氏マイナス５２〜マイナス５４度へ冷却されるために供給される。それから、前記重液体混合冷却剤は、前記予冷ＨＥにおいて過冷却され、０．２５〜０．２７ＭＰａになるまでスロットルで調整され、そして、前記予冷ＨＥの配管を冷却するために、前記液化ＨＥからの前記軽混合冷却剤と共に供給される。前記軽混合冷却剤は、前記予冷ＨＥと前記液化ＨＥにおいて、濃縮され、そして引き続いて過冷却される。前記液化ＨＥの流出口において生じた過冷却された液化軽混合冷却剤は０．２５〜０．２７ＭＰａになるまでスロットルで調整され、それから、配管を冷却する。窒素ＨＥからのＬＰ気体窒素はターボ膨張圧縮機において１．２〜１．４ＭＰａになるまで、そして、各窒素圧縮機において３．５〜３．７ＭＰａになるまで圧縮され、そして続けて、各空気冷却器において摂氏２６〜３０度まで、そして、窒素ＨＥにおいてＬＰ窒素冷却剤対向流を通じて摂氏マイナス１０７〜マイナス１０９度まで冷却される。その後窒素は、膨張器において０．８〜１．０ＭＰａになるまで膨張され、ＬＮＧ流を冷却するために過冷却ＨＥに送られ、窒素ＨＥにおいて高圧（ＨＰ）窒素によって摂氏２２〜２４度まで加熱され、そして、ターボ膨張圧縮機吸込み口に帰還する。 The essence of the natural gas liquefaction method is that the pretreated dry gas is cooled and concentrated in pre-cooled HE to a temperature in the range between minus 52 and minus 54 degrees Celsius. The pre-treated dry gas is then separated by removing the fraction of liquid ethane supplied for fractionation purposes, and the gas stream from the first separator is minus 120 to minus Celsius in the liquefied HE. It is subsequently cooled to 125 degrees and cooled with gaseous nitrogen to minus 150 to minus 160 degrees Celsius in a supercooling heat exchanger. The pressure of the supercooled liquefied natural gas (LNG) is reduced to 0.11 to 0.13 MPa in the liquid expander. The supercooled LNG is supplied for separation purposes and then supplied to the LNG storage tank. The separated gas is supplied to a fuel gas system, and the mixed coolant including nitrogen, methane, ethane, propane, butane, and pentane from the precooled HE is compressed to 3.0 to 3.1 MPa, It is cooled to 26-30 degrees Celsius and separated into a heavy liquid coolant and a light gas coolant. The heavy liquid coolant is aspirated for mixing with the heavy liquid coolant from the previous separator. The heavy liquid mixed coolant and the light gas mixed coolant are supplied to be cooled to minus 52 to minus 54 degrees Celsius by injecting a low pressure (LP) mixed counter flow of heavy and light coolant. Is done. The heavy liquid mixed coolant is then subcooled in the precooled HE, adjusted with a throttle until it reaches 0.25 to 0.27 MPa, and from the liquefied HE to cool the precooled HE piping. Of the light mixed coolant. The light mixed coolant is concentrated and subsequently supercooled in the precooled HE and the liquefied HE. The supercooled liquefied light mixed coolant generated at the outlet of the liquefied HE is adjusted with a throttle until it becomes 0.25 to 0.27 MPa, and then the pipe is cooled. LP gaseous nitrogen from nitrogen HE is compressed to 1.2-1.4 MPa in a turbo expansion compressor and 3.5-3.7 MPa in each nitrogen compressor, and then each air Cooled to 26-30 degrees Celsius in the cooler and to minus 107-109 degrees Celsius through LP nitrogen coolant counterflow in nitrogen HE. Nitrogen is then expanded to 0.8-1.0 MPa in an expander, sent to supercooled HE to cool the LNG stream, and heated to 22-24 degrees Celsius with high pressure (HP) nitrogen in nitrogen HE. And return to the suction port of the turbo expansion compressor.
本方法の実施のために使用される本天然ガス液化装置の本質は、予冷ＨＥ、５つの分離器、２つの絞り弁、液化ＨＥ、混合冷却剤圧縮用の３つの圧縮機、５つの空気冷却器、２つのポンプ、液体膨張器、過冷却ＨＥ、ターボ膨張器装置（作動用膨張器と圧縮機を備える）、および２つの窒素圧縮機の各機器からなる装置であることである。 The essence of the natural gas liquefier used for carrying out the method consists of precooled HE, 5 separators, 2 throttle valves, liquefied HE, 3 compressors for mixed coolant compression, 5 air cooling. A pump, a liquid expander, a supercooling HE, a turbo expander device (including an operating expander and a compressor), and two nitrogen compressors.
前記予冷ＨＥの流入口は、天然ガスの取り込み用である。前記予冷ＨＥの第１流出口は第１分離器の流入口に接続され、当該第１分離器のガス流出口は前記液化ＨＥの第１流入口に接続され、当該液化ＨＥの第１流出口は前記過冷却ＨＥの流入口に接続され、当該過冷却ＨＥの第１流出口は前記液体膨張器を経由して第２分離器の流入口に接続され、当該第２分離器の分離ガス流出口は燃料ガス系への送り出し用である。 The inlet of the precooled HE is for taking in natural gas. The first outlet of the precooled HE is connected to the inlet of the first separator, the gas outlet of the first separator is connected to the first inlet of the liquefied HE, and the first outlet of the liquefied HE Is connected to the inlet of the supercooling HE, the first outlet of the supercooling HE is connected to the inlet of the second separator via the liquid expander, and the separation gas flow of the second separator is The outlet is for delivery to the fuel gas system.
前記第２分離器の液化ガス流出口はＬＮＧ貯蔵タンクに接続される。前記第１分離器の液体エタン流出口は分別装置の流入口に接続される。前記予冷ＨＥの混合冷却剤流出口は第１圧縮機の流入口に接続され、当該第１圧縮機の流出口は前記空気冷却器の流入口に接続され、当該空気冷却器は、重液体冷却剤流と軽気体混合冷却剤流を生じる分離器の流入口に接続される。上述の第１圧縮機、空気冷却器、および分離器は、少なくとも三段階の圧縮段の、第１段階を構成し、当該圧縮段の全段階は同一である。第ｉ段階（ｉ＝１，２
とする）の分離器の軽気体混合冷却剤用の流出口は、前記三段階の圧縮段の第ｉ＋１段階
の圧縮機の流入口に接続される。最終段階の分離器の軽気体混合冷却剤用の流出口は、前記予冷ＨＥの第２流入口に接続される。第１段階および第２段階の分離器の重液体冷却剤用の流出口は、それぞれに、第１および第２ポンプを通過して、前記予冷ＨＥの第３流入口に混合物を供給するために、第３段階の分離器の重液体冷却剤用の流出口と結合される。前記予冷ＨＥの第２流出口は、前記液化ＨＥの第２流入口に接続され、当該液化ＨＥの第２流出口は、第２絞り弁を通じて配管冷却用の前記液化ＨＥの流入口に接続される。前記予冷ＨＥの第３流出口は、配管冷却用に前記予冷ＨＥ内に混合物を供給するために、第１絞り弁を通じて前記液化ＨＥの第３流出口と結合される。前記過冷却ＨＥの第２流出口は、窒素ＨＥの流入口に接続され、当該窒素ＨＥの第１および第２流出口は、それぞれに、膨張器とターボ膨張圧縮機の流入口に接続され、当該膨張器とターボ膨張圧縮機の流出口は、それぞれに、前記過冷却ＨＥのＬＮＧ流の冷却用の流入口と第２窒素圧縮機の流入口に接続される。後者の流出口は、直列に接続された第５空気冷却器、第１窒素圧縮機および第４空気冷却器に接続され、当該第４空気冷却器流出口は、前記窒素ＨＥの別の流入口へのＨＰ窒素供給用である。
The liquefied gas outlet of the second separator is connected to an LNG storage tank. The liquid ethane outlet of the first separator is connected to the inlet of the fractionation device. The precooled HE mixed coolant outlet is connected to the inlet of the first compressor, the outlet of the first compressor is connected to the inlet of the air cooler, and the air cooler is cooled by heavy liquid cooling. Connected to the inlet of the separator that produces the agent stream and the light gas mixed coolant stream. The first compressor, the air cooler, and the separator described above constitute the first stage of at least three compression stages, and all stages of the compression stage are the same. I-th stage (i = 1, 2
The outlet for the light gas mixed coolant of the separator is connected to the inlet of the compressor in the i + 1th stage of the three-stage compression stage. The outlet for the light gas mixed coolant of the final stage separator is connected to the second inlet of the precooled HE. The outlets for the heavy liquid coolant of the first stage and second stage separators pass through the first and second pumps, respectively, to supply the mixture to the third inlet of the precooled HE. , Coupled to the outlet for the heavy liquid coolant of the third stage separator. The second outlet of the pre-cooled HE is connected to the second inlet of the liquefied HE, and the second outlet of the liquefied HE is connected to the inlet of the liquefied HE for cooling the pipe through a second throttle valve. The The third outlet of the precooled HE is coupled to the third outlet of the liquefied HE through a first throttle valve to supply a mixture into the precooled HE for pipe cooling. The second outlet of the supercooling HE is connected to an inlet of nitrogen HE, and the first and second outlets of the nitrogen HE are connected to the inlet of the expander and the turbo expansion compressor, respectively. The outlets of the expander and the turbo expansion compressor are respectively connected to an inlet for cooling the LNG flow of the supercooling HE and an inlet of the second nitrogen compressor. The latter outlet is connected to a fifth air cooler, a first nitrogen compressor, and a fourth air cooler connected in series, and the fourth air cooler outlet is another inlet for the nitrogen HE. For supplying HP nitrogen.
前記天然ガス液化装置は、
‐ 混合冷却剤回路と、
‐ 窒素冷却剤回路の、
２つの回路を備える。
The natural gas liquefaction device is:
-Mixed coolant circuit;
-Of the nitrogen coolant circuit,
Two circuits are provided.
前記天然ガス液化装置は、
‐ 予冷ＨＥ（１）と、
‐ 第１〜第５分離器（２，２０，８，１１，１４）と、
‐ 第１および第２絞り弁（３，５）と、
‐ 液化ＨＥ（４）と、
‐ 混合冷却剤圧縮用の、第１〜第３圧縮機（６，９，１２）と、
‐ 第１〜第５空気冷却器（７，１０，１３，２３，２５）と、
‐ 第１および第２ポンプ（１５，１６）と、
‐ 液体膨張器（１９）と、
‐ 過冷却ＨＥ（１７）と、
‐ 窒素ＨＥ（１８）と、
‐ 作動用膨張器（２１）と圧縮機（２２）を備えるターボ膨張器装置と、
‐ ２つの窒素圧縮機（２４，２６）と、
‐ 分別装置（２７）と、
‐ ＬＮＧ貯蔵タンク（２８）の、
各機器と各ブロックを備える。
The natural gas liquefaction device is:
-Pre-cooled HE (1),
-The first to fifth separators (2, 20, 8, 11, 14);
-First and second throttle valves (3, 5);
-Liquefied HE (4);
-First to third compressors (6, 9, 12) for mixed coolant compression;
-First to fifth air coolers (7, 10, 13, 23, 25);
-First and second pumps (15, 16);
-A liquid inflator (19);
-Supercooled HE (17);
-Nitrogen HE (18);
A turbo-expander device comprising an actuating expander (21) and a compressor (22);
-Two nitrogen compressors (24, 26);
-A sorting device (27);
-Of the LNG storage tank (28),
Each device and each block are provided.
前処理済乾燥ガスが液化目的で供給され、それから混合冷却剤によって、予冷ＨＥ（１）において摂氏マイナス５２〜マイナス５４度まで冷却される。二相の流れが、エタンの留分の除去が行われる第１分離器（２）を通過し、それから、前記第１分離器からの液体が、分別目的で送り込まれる。ガス流は液化ＨＥ（４）に供給され、摂氏マイナス１２０〜マイナス１２５度まで冷却される。 Pretreated dry gas is supplied for liquefaction purposes and then cooled to minus 52 to minus 54 degrees Celsius in precooled HE (1) by a mixed coolant. The two-phase stream passes through a first separator (2) where ethane fraction removal takes place, from which the liquid from the first separator is sent for fractionation purposes. The gas stream is supplied to liquefied HE (4) and cooled to minus 120 to minus 125 degrees Celsius.
液化天然ガス（ＬＮＧ）はその後過冷却ＨＥ（１７）において摂氏マイナス１５０〜マイナス１６０度まで、気体窒素によって冷却される。 The liquefied natural gas (LNG) is then cooled with gaseous nitrogen to minus 150 to minus 160 degrees Celsius in supercooled HE (17).
過冷却ＨＥ（１７）から出ていく冷却されたＬＮＧの圧力は、液体膨張器（１９）において０．１１〜０．１３ＭＰａになるまで低下させられる。前記低圧化したＬＮＧは分離器（２０）に、それからＬＮＧ貯蔵タンクに供給される。液体膨張器（１９）は、液化ガス膨張エネルギーのおかげで、液化処理中の消費電力を低減することが可能になる。 The pressure of the cooled LNG exiting from the supercooled HE (17) is reduced to 0.11 to 0.13 MPa in the liquid expander (19). The reduced pressure LNG is fed to the separator (20) and then to the LNG storage tank. The liquid expander (19) can reduce power consumption during the liquefaction process thanks to the liquefied gas expansion energy.
混合冷却剤回路 Mixed coolant circuit
混合冷却剤は、窒素、メタン、エタン、プロパン、ブタンおよびペンタンからなる。 The mixed coolant consists of nitrogen, methane, ethane, propane, butane and pentane.
前記混合冷却剤は、コンプレッサ（６，９，１２）において、３．０〜３．１ＭＰａになるまで圧縮される。各圧縮段階の間に、前記混合冷却剤は、空気冷却器（７，１０，１３）において、摂氏２６〜３０度に冷却される。二相の流れが、重液体混合冷却剤流と軽気体混合冷却剤流への分離用の混合冷却剤分離器（８，１１，１４）に供給される。分離器（８，１１）からの前記重液体混合冷却剤流は、ポンプ（１５，１６）によって、分離器（１４）からの前記液体との混合のために供給される。段階毎の重液体混合冷却剤の成分および量は、混合冷却剤成分に依存し、当該混合冷却剤成分は、ある周囲温度における天然ガスの液化中の、最小冷却剤消費を確保するような方法で選択される。 The mixed coolant is compressed in a compressor (6, 9, 12) until it reaches 3.0 to 3.1 MPa. During each compression stage, the mixed coolant is cooled to 26-30 degrees Celsius in an air cooler (7, 10, 13). The two-phase stream is fed to a mixed coolant separator (8, 11, 14) for separation into a heavy liquid mixed coolant stream and a light gas mixed coolant stream. The heavy liquid mixed coolant stream from the separator (8, 11) is supplied by the pump (15, 16) for mixing with the liquid from the separator (14). The composition and amount of the heavy liquid mixed coolant at each stage depends on the mixed coolant component, and the mixed coolant component is a method that ensures minimum coolant consumption during liquefaction of natural gas at a certain ambient temperature. Selected.
重および軽混合冷却剤流は、ＬＰ重および軽混合冷却剤の対向流を通じて、ＨＥ（１）において摂氏マイナス５２〜マイナス５４度まで冷却される。 The heavy and light mixed coolant streams are cooled to minus 52 to minus 54 degrees Celsius in HE (1) through the counter flow of LP heavy and light mixed refrigerants.
重混合冷却剤は、ＨＥ（１）において冷却され、０．２５〜０．２７ＭＰａになるまで絞り弁（３）によって調整され、そして、ＨＥ（１）の配管を冷却するために、液化ＨＥ（４）からの軽混合冷却剤と一緒にＨＥ（１）の配管スペース内に供給される。 The heavy mixed coolant is cooled in HE (1), adjusted by a throttle valve (3) until 0.25 to 0.27 MPa, and liquefied HE ( It is fed into the piping space of HE (1) together with the light mixed coolant from 4).
軽混合冷却剤は、ＨＥ（１）および（４）において濃縮され、冷却される。その後過冷却され液化された軽混合冷却剤は、０．２５〜０．２７ＭＰａになるまで絞り弁（５）によって調整され、配管を冷却するために液化ＨＥ（４）の配管スペース内に供給される。 The light mixed coolant is concentrated and cooled in HE (1) and (4). Thereafter, the light mixed coolant that has been supercooled and liquefied is adjusted by the throttle valve (5) until it reaches 0.25 to 0.27 MPa, and is supplied into the piping space of the liquefied HE (4) to cool the piping. The
ＬＰ重および軽混合冷却剤流は、一緒に混和されて、配管を冷却するためにＨＥ（１）の配管スペースに帰還する。 The LP heavy and light mixed coolant streams are mixed together and returned to the piping space of HE (1) to cool the piping.
ＬＰ混合冷却剤は、ＨＥ（１）から摂氏２６〜３０度の蒸気として出ていき、当該蒸気は再循環のために供給される。前記混合冷却剤は、ガス流を摂氏マイナス１２０〜マイナス１２５度まで冷却するために使用される。 The LP mixed coolant exits HE (1) as steam at 26-30 degrees Celsius, and the steam is supplied for recirculation. The mixed coolant is used to cool the gas stream to minus 120 to minus 125 degrees Celsius.
窒素冷却剤回路 Nitrogen coolant circuit
ＬＰ気体窒素は、ターボ膨張器装置内で膨張器（２１）によって駆動される圧縮機（２２）において、１．２〜１．４ＭＰａになるまで、そして、窒素圧縮機（２４）および（２６）において、３．５〜３．７ＭＰａになるまで圧縮される。それから、それは空気冷却器（２３）および（２５）において摂氏２６〜３０度まで冷却され、窒素ＨＥ（１８）においてＬＰ窒素対向流を通じて摂氏マイナス１０７〜マイナス１０９度まで冷却される。 LP gaseous nitrogen is 1.2 to 1.4 MPa in the compressor (22) driven by the expander (21) in the turboexpander apparatus, and then the nitrogen compressors (24) and (26) , It is compressed to 3.5 to 3.7 MPa. It is then cooled to 26-30 degrees Celsius in air coolers (23) and (25), and cooled to minus 107-109 degrees Celsius through LP nitrogen countercurrent in nitrogen HE (18).
それから窒素は、膨張器（２１）において０．８〜１．０ＭＰａになるまで膨張され、ＬＮＧ流を冷却するために過冷却ＨＥ（１７）に供給され、窒素ＨＥ（１８）においてＨＰ窒素によって摂氏２２〜２４度まで加熱され、そして、圧縮機吸込み口に帰還する。 The nitrogen is then expanded to 0.8-1.0 MPa in the expander (21) and fed to the supercooled HE (17) to cool the LNG stream, and in nitrogen HE (18) by HP nitrogen in degrees Celsius. Heated to 22-24 degrees and returned to compressor inlet.
天然ガス液化処理の間に消費される電力の削減は、予冷および液化段階における混合冷却剤の使用はもちろん、過冷却段階における窒素循環からも生じる。 The reduction in power consumed during the natural gas liquefaction process arises from nitrogen circulation in the supercooling stage as well as the use of mixed coolant in the precooling and liquefaction stage.
Claims (2)
前処理済乾燥ガスが、予冷熱交換器において、摂氏マイナス５２〜マイナス５４度の間の範囲の温度まで冷却され、
それから、分別目的用に供給される液状エタンの留分を除去する第１分離器を通過することによって、前記前処理済乾燥ガスは分離され、そして、第１分離器からのガス流が、液化熱交換器において摂氏マイナス１２０〜マイナス１２５度まで引き続いて冷却され、
過冷却熱交換器において摂氏マイナス１５０〜マイナス１６０度まで、気体窒素によって冷却され、
過冷却された液化天然ガスの圧力が、液体膨張器において０．１１〜０．１３ＭＰａになるまで低下させられ、
そして、前記過冷却された液化天然ガスは第２分離器に分離目的で供給され、そしてそれから、液化天然ガス貯蔵タンクに供給され、
分離されたガスは燃料ガス系に送られ、
前記予冷熱交換器からの、窒素、メタン、エタン、プロパン、ブタンおよびペンタンを包含する混合冷却剤は３．０〜３．１ＭＰａになるまで圧縮され、摂氏２６〜３０度に冷却され、そして、第３分離器、第４分離器、第５分離器に供給され重液体混合冷却剤と軽気体混合冷却剤に分離され、
第３分離器、第４分離器からの前記重液体混合冷却剤は、第５分離器からの重液体混合冷却剤と混和するために吸い出され、
重液体混合冷却剤と軽気体混合冷却剤は、重液体混合冷却剤と軽気体混合冷却剤の投入によって摂氏マイナス５２〜マイナス５４度まで冷却するために供給され、
それから、前記重液体混合冷却剤は前記予冷熱交換器において過冷却され、０．２５〜０．２７ＭＰａになるまでスロットルで調整され、そして、前記予冷熱交換器の配管を冷却するために、前記液化熱交換器からの前記軽気体混合冷却剤と共に供給され、
前記軽気体混合冷却剤は、前記予冷熱交換器と前記液化熱交換器において、濃縮され、そして引き続いて過冷却され、
前記液化熱交換器の流出口において生じた過冷却された液化軽気体混合冷却剤は０．２５〜０．２７ＭＰａになるまでスロットルで調整され、それから、前記液化熱交換器の配管を冷却するために供給され、
窒素熱交換器からの低圧気体窒素はターボ膨張圧縮機において１．２〜１．４ＭＰａになるまで、そして、各窒素圧縮機において３．５〜３．７ＭＰａになるまで圧縮され、各空気冷却器において摂氏２６〜３０度まで、そして、窒素熱交換器において低圧窒素冷却剤により摂氏マイナス１０７〜マイナス１０９度まで冷却され、
そしてそれから、窒素は、膨張器において０．８〜１．０ＭＰａになるまで膨張され、液化天然ガス流を冷却するために過冷却熱交換器に送られ、窒素熱交換器において高圧窒素によって摂氏２２〜２４度まで加熱され、そして、ターボ膨張圧縮機吸込み口に帰還することを特徴とする天然ガス液化方法。 A natural gas liquefaction method comprising:
The pretreated dry gas is cooled in a pre-cooling heat exchanger to a temperature in the range between minus 52 and minus 54 degrees Celsius ;
The pretreated dry gas is then separated by passing through a first separator that removes a fraction of liquid ethane supplied for fractionation purposes, and the gas stream from the first separator is liquefied. In the heat exchanger, it is continuously cooled to minus 120 to minus 125 degrees Celsius,
Cooled by gaseous nitrogen to minus 150 to minus 160 degrees Celsius in a supercooling heat exchanger,
The pressure of the supercooled liquefied natural gas is reduced to 0.11 to 0.13 MPa in the liquid expander,
And the supercooled liquefied natural gas is supplied to the second separator for separation purposes, and then supplied to the liquefied natural gas storage tank,
The separated gas is sent to the fuel gas system,
The mixed coolant including nitrogen, methane, ethane, propane, butane and pentane from the pre-cooling heat exchanger is compressed to 3.0-3.1 MPa, cooled to 26-30 degrees Celsius, and Supplied to the third separator, the fourth separator, and the fifth separator and separated into a heavy liquid mixed coolant and a light gas mixed coolant;
The heavy liquid mixed coolant from the third separator, the fourth separator is sucked out to mix with the heavy liquid mixed coolant from the fifth separator;
Heavy liquid mixing coolant and light gaseous mixture coolant is supplied to cool to Celsius 52 to minus 54 degrees by the introduction of heavy liquid mixture coolant and light gas mixed coolant,
Then, the heavy liquid mixed coolant is subcooled in the precooling heat exchanger and adjusted with a throttle until it reaches 0.25 to 0.27 MPa, and in order to cool the piping of the precooling heat exchanger, Supplied with the light gas mixed coolant from the liquefied heat exchanger,
The light gas mixed coolant is concentrated and subsequently subcooled in the precooling heat exchanger and the liquefied heat exchanger,
The supercooled liquefied light gas mixed coolant generated at the outlet of the liquefied heat exchanger is adjusted with a throttle until it reaches 0.25 to 0.27 MPa, and then the piping of the liquefied heat exchanger is cooled. Supplied to
The low pressure gaseous nitrogen from the nitrogen heat exchanger is compressed to 1.2 to 1.4 MPa in the turbo expansion compressor and to 3.5 to 3.7 MPa in each nitrogen compressor , and each air cooler Cooled to 26 to 30 degrees Celsius, and cooled to minus 107 to 109 degrees Celsius with a low pressure nitrogen coolant in a nitrogen heat exchanger,
And then, the nitrogen is expanded to 0.8-1.0 MPa in the expander and sent to a supercooling heat exchanger to cool the liquefied natural gas stream, and 22 degrees Celsius with high pressure nitrogen in the nitrogen heat exchanger. A natural gas liquefaction method, characterized in that it is heated to ˜24 degrees and then returned to the inlet of the turbo expansion compressor.
予冷熱交換器と、５つの分離器と、２つの絞り弁と、液化熱交換器と、混合冷却剤を圧縮するための３つの圧縮器と、５つの空気冷却器と、２つのポンプと、液体膨張器と、過冷却熱交換器と、作動用膨張器（２１）と圧縮機（２２）を備えるターボ膨張器装置と、２つの窒素圧縮機と、を備え、
前記予冷熱交換器の流入口は、天然ガスの取り込み用であり、
当該予冷熱交換器の第１流出口は第１分離器の流入口に接続され、
当該第１分離器のガス流出口は液化熱交換器の第１流入口に接続され、
当該液化熱交換器の第１流出口は前記過冷却熱交換器の流入口に接続され、
当該過冷却熱交換器の第１流出口は前記液体膨張器を経由して第２分離器の流入口に接続され、
当該第２分離器の分離ガス流出口は燃料ガス系への送り出し用であり、
そして、前記第２分離器の液化ガス流出口は液化天然ガス貯蔵タンクに接続され、
前記第１分離器の液状エタン流出口は分別装置の流入口に接続され、
前記予冷熱交換器の混合冷却剤流出口は第１圧縮機の流入口に接続され、
当該第１圧縮機の流出口は空気冷却器の流入口に接続され、
当該空気冷却器は重液体混合冷却剤流と軽気体混合冷却剤流を生じる分離器の流入口に接続され、
上述の第１圧縮機、空気冷却器、および分離器は、少なくとも三段階の圧縮段の、第１段階を構成し、
ｉ＝１，２として、第ｉ段階の分離器の軽気体混合冷却剤用の流出口は、前記三段階の圧縮段の第ｉ＋１段階の圧縮機の流入口に接続されるものとし、
最終段階の分離器の軽気体混合冷却剤用の流出口は、前記予冷熱交換器の第２流入口に接続され、
第１段階および第２段階の分離器の重液体混合冷却剤用の流出口は、それぞれに、第１および第２ポンプを通過して、前記予冷熱交換器の第３流入口に混合物を供給するために、第３段階の分離器の重液体混合冷却剤用の流出口と結合され
前記予冷熱交換器の第２流出口は、前記液化熱交換器の第２流入口に接続され、
前記液化熱交換器の第２流出口は、第２絞り弁を通じて前記液化熱交換器の配管冷却用の流入口に接続され
前記予冷熱交換器の第３流出口は、前記予冷熱交換器内に配管冷却用に混合物を供給するために、第１絞り弁を通じて前記液化熱交換器の第３流出口と結合され、
前記過冷却熱交換器の第２流出口は、窒素熱交換器の流入口に接続され、
当該窒素熱交換器の第１および第２流出口は、それぞれに、膨張器とターボ膨張圧縮機の流入口に接続され、
当該膨張器とターボ膨張圧縮機の流出口は、それぞれに、前記過冷却熱交換器の液化天然ガス流の冷却用の流入口と第２窒素圧縮機の流入口に接続され、
そして、後者の流出口は、直列に接続された第５空気冷却器、第１窒素圧縮機および第４空気冷却器に接続され、
当該第４空気冷却器の流出口は、前記窒素熱交換器の別の流入口への高圧窒素供給用であることを特徴とする装置。 An apparatus used for carrying out the method according to claim 1, comprising:
A precooling heat exchanger, five separators, two throttle valves, a liquefied heat exchanger, three compressors for compressing the mixed coolant, five air coolers, two pumps, A liquid expander, a supercooling heat exchanger, a turboexpander device comprising an actuating expander (21) and a compressor (22), and two nitrogen compressors,
The inlet of the pre-cooling heat exchanger is for taking in natural gas;
The first outlet of the precooling heat exchanger is connected to the inlet of the first separator;
The gas outlet of the first separator is connected to the first inlet of the liquefied heat exchanger,
A first outlet of the liquefied heat exchanger is connected to an inlet of the supercooling heat exchanger;
A first outlet of the supercooling heat exchanger is connected to an inlet of the second separator via the liquid expander;
The separation gas outlet of the second separator is for sending out to the fuel gas system,
And the liquefied gas outlet of the second separator is connected to a liquefied natural gas storage tank,
The liquid ethane outlet of the first separator is connected to the inlet of the fractionation device;
A mixed coolant outlet of the precooling heat exchanger is connected to an inlet of the first compressor;
The outlet of the first compressor is connected to the inlet of the air cooler;
The air cooler is connected to a separator inlet that produces a heavy liquid mixed coolant stream and a light gas mixed coolant stream;
The first compressor, air cooler, and separator described above constitute a first stage of at least three stages of compression stages ;
Assuming that i = 1, 2, the outlet for the light gas mixed coolant of the i-th stage separator is connected to the inlet of the compressor of the i + 1-th stage of the three-stage compression stage,
The outlet for the light gas mixed coolant of the final stage separator is connected to the second inlet of the precooling heat exchanger,
The outlets for the heavy liquid mixed coolant of the first stage and second stage separators respectively pass the first and second pumps to supply the mixture to the third inlet of the precooling heat exchanger A second outlet of the precooling heat exchanger is connected to a second inlet of the liquefied heat exchanger, coupled to an outlet for the heavy liquid mixed coolant of the third stage separator,
The second outlet of the liquefied heat exchanger is connected to an inlet for cooling the pipe of the liquefied heat exchanger through a second throttle valve, and the third outlet of the precooling heat exchanger is in the precooling heat exchanger. To supply a mixture for cooling the pipe to the third outlet of the liquefied heat exchanger through a first throttle valve,
A second outlet of the supercooling heat exchanger is connected to an inlet of the nitrogen heat exchanger;
The first and second outlets of the nitrogen heat exchanger are connected to the inlets of the expander and the turbo expansion compressor, respectively.
The outlet of the expander and the turbo expansion compressor are respectively connected to an inlet for cooling the liquefied natural gas stream of the supercooling heat exchanger and an inlet of the second nitrogen compressor,
The latter outlet is connected to a fifth air cooler, a first nitrogen compressor and a fourth air cooler connected in series,
The outlet of the fourth air cooler is for supplying high-pressure nitrogen to another inlet of the nitrogen heat exchanger.
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