TWI825342B - Gas liquefaction apparatus - Google Patents
Gas liquefaction apparatus Download PDFInfo
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- TWI825342B TWI825342B TW109127377A TW109127377A TWI825342B TW I825342 B TWI825342 B TW I825342B TW 109127377 A TW109127377 A TW 109127377A TW 109127377 A TW109127377 A TW 109127377A TW I825342 B TWI825342 B TW I825342B
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- gas
- heat exchanger
- main heat
- pressure
- supply
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- 239000007789 gas Substances 0.000 claims abstract description 293
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 154
- 239000003345 natural gas Substances 0.000 claims abstract description 77
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 35
- 239000007788 liquid Substances 0.000 claims abstract description 33
- 239000003507 refrigerant Substances 0.000 claims abstract description 9
- 238000011084 recovery Methods 0.000 claims description 15
- 238000011144 upstream manufacturing Methods 0.000 claims description 15
- 230000006835 compression Effects 0.000 abstract description 8
- 238000007906 compression Methods 0.000 abstract description 8
- 238000000034 method Methods 0.000 abstract description 8
- 230000008569 process Effects 0.000 abstract description 5
- 238000000605 extraction Methods 0.000 abstract description 4
- 238000010586 diagram Methods 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000013535 sea water Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- -1 steam Substances 0.000 description 1
Classifications
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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
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0012—Primary atmospheric gases, e.g. air
- F25J1/0015—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
- F25J1/003—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
- 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"
- F25J1/0045—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 vaporising a liquid return stream
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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
- F25J1/008—Hydrocarbons
- F25J1/0082—Methane
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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
- F25J1/0224—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 in combination with an internal quasi-closed 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
- F25J1/02—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
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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.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
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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
- F25J2230/22—Compressor driver arrangement, e.g. power supply by motor, gas or steam turbine
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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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
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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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/90—Hot gas waste turbine of an indirect heated gas for power generation
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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
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
本發明係關於一種氣體液化裝置。 The invention relates to a gas liquefaction device.
專利文獻1記載有如下之構成：為了有效地製造液態氣體，於液化天然氣體(LNG)之接收及氣化基地，利用在使LNG蒸發時所釋放之冷熱能而冷卻氣體。 Patent Document 1 describes a structure in which, in order to efficiently produce liquid gas, at a receiving and gasification base for liquefied natural gas (LNG), the cold and heat energy released when LNG is evaporated is used to cool the gas.
專利文獻2記載有如下之方法：藉由利用LNG的冷能來壓縮氣體而得到高壓之氣體，藉由利用減壓閥將高壓氣體減壓而得到液態氣體。 Patent Document 2 describes a method in which a gas is compressed using the cold energy of LNG to obtain a high-pressure gas, and a liquid gas is obtained by depressurizing the high-pressure gas using a pressure reducing valve.
上述專利文獻1或2之技術，一般來說得以適用在LNG再氣化基地。在LNG再氣化基地使LNG蒸發，以將天然氣體供給至例如發電廠、都市氣體管路等。這些需求者所需的天然氣體壓力往往不同，但一般來說為了設備的簡化而專為高壓的需求者製造天然氣體，對於低壓的需求者則使該天然氣體膨脹後進行供給。 The technology of the above-mentioned Patent Document 1 or 2 is generally applicable to LNG regasification bases. LNG is evaporated at the LNG regasification base to supply natural gas to, for example, power plants, city gas pipelines, and the like. The natural gas pressure required by these consumers often differs, but in general, natural gas is produced specifically for high-pressure consumers to simplify equipment, and the natural gas is expanded and supplied to low-pressure consumers.
專利文獻3記載如下的方法：在膨脹時所能回收的能量係利用以膨脹渦輪使天然氣體膨脹時所得之動力來驅動發電機而作為電力進行回收、壓縮氣體。 Patent Document 3 describes a method in which the energy that can be recovered during expansion is used to drive a generator using the power obtained when natural gas is expanded with an expansion turbine, and is recovered as electric power to compress the gas.
然而，關於將如專利文獻3記載的所得到之電力或氣體壓縮動力於氣體液化裝置中利用，具體且可實現的方法並未被揭示或教示。 However, a specific and implementable method for utilizing the electric power or gas compression power obtained as described in Patent Document 3 in a gas liquefaction device has not been disclosed or taught.
進而，氣體液化裝置中，有著藉由有效地活用LNG冷能而有效地將氣體液化之必要性及需求，關於此方面在專利文獻3也並未揭示。 Furthermore, in the gas liquefaction device, there is a necessity and demand to effectively liquefy the gas by effectively utilizing the cold energy of LNG, and Patent Document 3 does not disclose this aspect either.
[先前技術文獻] [Prior technical literature]
[專利文獻] [Patent Document]
[專利文獻1]日本專利第4142559號公報 [Patent Document 1] Japanese Patent No. 4142559
[專利文獻2]日本專利第6087196號公報 [Patent Document 2] Japanese Patent No. 6087196
[專利文獻3]美國專利第9,903,232號公報(Fig.3之「opencycle」) [Patent Document 3] U.S. Patent No. 9,903,232 (Fig.3 "opencycle")
有鑑於上述實際情況，本發明之目的在於提供一種氣體液化裝置，其將利用渦輪機使天然氣體膨脹時之動力，利用於藉由液化天然氣體冷卻之處理氣體(process gas)之壓縮，可藉由有效地壓縮處理氣體而使液化效率提高。 In view of the above actual situation, the object of the present invention is to provide a gas liquefaction device that uses the power of a turbine to expand natural gas to compress the process gas cooled by the liquefied natural gas. Effectively compress processing gas to improve liquefaction efficiency.
本發明之氣體液化裝置其具備：供給管線(L1)，用以供給第一壓力(例如0.1MPa)之供給氣體(Feed gas)；第一氣體壓縮機(6)，配置於前述供給管線(L1)，將供給氣體壓縮至第二壓力(例如0.5MPa)；主熱交換器(1)，由前述第一氣體壓縮機(6)壓縮後之供給氣體(壓縮供給氣體)透過前述供給管線(L1)而被導入；低溫氣體昇壓機(7)，將自前述熱交換器(1)之中間(透過供給管線L1)導出之供給氣體昇壓至第三壓力(例如5MPa)；第一膨脹閥(2)，使由前述低溫氣體昇壓機(7)昇壓至第三壓力(例如5MPa)之昇壓後的供給氣體(昇壓供給氣體)(透過供給管線L1)於主熱交換器(1)進行熱交 換而導出後，減壓(膨脹)至第四壓力(例如0.5MPa)；分離器(3)，將由前述第一膨脹閥(2)減壓後之供給氣體(氣液混合氣體)分離成氣體成分與液體成分；第一取出管線(L2)，使自前述分離器(3)導出之第五壓力之液體成分(中壓液態氣體)，通過次冷卻器(4)，作為液化氣體(Liquefied gas)而取出；第二膨脹閥(5)，將自前述第一取出管線(L2)分歧之一部分之液體成分減壓至第六壓力(第二壓力>第六壓力>第一壓力)；第一循環管線(L21)，配置有前述第二膨脹閥(5)，且自前述第一取出管線(L2)分歧，用以使由前述第二膨脹閥(5)減壓後之氣體(低壓回收氣體)往前述次冷卻器(4)作為冷媒而使用後，送往前述主熱交換器(1)，然後往前述供給管線(L1)返回；第二循環管線(L3)，用以使自前述分離器(3)導出之第七壓力之氣體成分(中壓回收氣體，第七壓力>第二壓力)，在送往前述主熱交換器(1)後，往前述供給管線(L1)(之較前述第一氣體壓縮機(6)下游側)返回；天然氣體渦輪機(8)，與前述低溫氣體昇壓機(7)連結，用以提供用於進行驅動之動力；以及第二取出管線(L10)，將液化天然氣體(LNG)往前述主熱交換器(1)導入後，在前述天然氣體渦輪機(8)中使用後，作為天然氣體(NG)而取出。 The gas liquefaction device of the present invention is equipped with: a supply pipeline (L1) for supplying a first pressure (for example, 0.1MPa) feed gas (Feed gas); a first gas compressor (6) arranged in the aforementioned supply pipeline (L1) ), compressing the supply gas to a second pressure (for example, 0.5MPa); the main heat exchanger (1), the supply gas (compressed supply gas) compressed by the aforementioned first gas compressor (6) passes through the aforementioned supply pipeline (L1) ) is introduced; the low-temperature gas booster (7) boosts the supply gas derived from the middle of the aforementioned heat exchanger (1) (through the supply line L1) to a third pressure (for example, 5MPa); the first expansion valve (2) Make the pressurized supply gas (pressurized supply gas) pressurized to a third pressure (for example, 5 MPa) by the low-temperature gas booster (7) (through the supply line L1) in the main heat exchanger ( 1) Have hot sex After being replaced and exported, the pressure is reduced (expanded) to the fourth pressure (for example, 0.5MPa); the separator (3) separates the supply gas (gas-liquid mixed gas) decompressed by the aforementioned first expansion valve (2) into gas components and liquid components; the first take-out line (L2) allows the liquid component (medium pressure liquid gas) of the fifth pressure derived from the aforementioned separator (3) to pass through the secondary cooler (4) as liquefied gas (Liquefied gas) ) and take it out; the second expansion valve (5) decompresses a part of the liquid component branched from the first take-out line (L2) to the sixth pressure (second pressure>sixth pressure>first pressure); first The circulation line (L21) is equipped with the aforementioned second expansion valve (5) and branches from the aforementioned first take-out line (L2) to use the gas (low-pressure recovery gas) decompressed by the aforementioned second expansion valve (5). ) is used as refrigerant in the sub-cooler (4), then sent to the main heat exchanger (1), and then returned to the supply line (L1); the second circulation line (L3) is used to separate the The seventh pressure gas component (medium pressure recovery gas, seventh pressure > second pressure) derived from the device (3) is sent to the aforementioned main heat exchanger (1) and then to the aforementioned supply line (L1) (compared to The aforementioned first gas compressor (6) downstream side) returns; the natural gas turbine (8) is connected to the aforementioned low-temperature gas booster (7) to provide power for driving; and the second take-out pipeline (L10 ), liquefied natural gas (LNG) is introduced into the main heat exchanger (1), used in the natural gas turbine (8), and then taken out as natural gas (NG).
在上述處理中，作為原料之供給氣體與自次冷卻器(4)供給之低壓回收氣體合流，在第一氣體壓縮機(6)中被壓縮，經壓縮之供給氣體與自分離器(3)供給之中壓回收氣體合流後，在主熱交換器(1)中被冷卻後由低溫氣體昇壓機(7)壓縮，獲得高壓氣體。 In the above process, the supply gas as raw material is combined with the low-pressure recovery gas supplied from the subcooler (4), and is compressed in the first gas compressor (6). The compressed supply gas is separated from the separator (3) After the supplied medium-pressure recovery gases merge, they are cooled in the main heat exchanger (1) and then compressed by the low-temperature gas booster (7) to obtain high-pressure gas.
高壓氣體在主熱交換器(1)中被冷卻之後，在第一膨脹閥(2)膨脹，藉由分離器(3)而氣液分離。利用分離器(3)獲得之中壓液態氣體，由次冷卻器(4)冷卻後，一部分作為製品而導出。其餘的中壓液態氣體，在第二膨脹閥(5)中減壓後，作 為冷媒供給至次冷卻器(4)，進而在主熱交換器(1)中放出冷能後，在較第一氣體壓縮機(6)上游側與供給管線(L1)合流。 After the high-pressure gas is cooled in the main heat exchanger (1), it expands in the first expansion valve (2), and is separated into gas and liquid by the separator (3). The medium-pressure liquid gas is obtained by the separator (3), and after being cooled by the secondary cooler (4), a part of it is exported as a product. The remaining medium-pressure liquid gas is decompressed in the second expansion valve (5) and then The refrigerant is supplied to the sub-cooler (4), and then releases cooling energy in the main heat exchanger (1), and then merges with the supply line (L1) on the upstream side of the first gas compressor (6).
LNG在被供給至主熱交換器(1)而放出冷能後，從主熱交換器(1)的溫端被導出，至少其一部分藉由天然氣體渦輪機(8)而膨脹，驅動低溫氣體昇壓機(7)。 After LNG is supplied to the main heat exchanger (1) and releases cold energy, it is exported from the warm end of the main heat exchanger (1). At least part of it is expanded by the natural gas turbine (8), driving the low-temperature gas to rise. Press(7).
藉由此構成，不僅能夠活用藉由天然氣體渦輪機(8)所得之動力來進行氣體壓縮，還能藉由將氣體利用LNG冷能預冷後再進行氣體壓縮來大幅改善壓縮效率。 With this configuration, not only can the power obtained from the natural gas turbine (8) be utilized for gas compression, but the compression efficiency can also be significantly improved by precooling the gas using LNG cold energy and then compressing the gas.
在本發明中，氣體狀態、液體狀態、氣液混和狀態中的「高壓」為2MPa以上，「中壓」為0.2MPa以上未達2MPa，「低壓」為未達0.2MPa。 In the present invention, "high pressure" in a gas state, a liquid state, or a gas-liquid mixed state is 2 MPa or more, "medium pressure" is 0.2 MPa or more but less than 2 MPa, and "low pressure" is less than 0.2 MPa.
上述氣體液化裝置亦可進一步具備：第二氣體壓縮機(9)，配置於較前述第一氣體壓縮機(6)下游側之供給管線(L1)，將供給氣體壓縮至第八壓力(例如1MPa)。 The above-mentioned gas liquefaction device may further include: a second gas compressor (9), which is arranged in the supply line (L1) downstream of the first gas compressor (6) and compresses the supply gas to an eighth pressure (for example, 1 MPa). ).
前述第二循環管線(L3)亦可往較前述第一氣體壓縮機(6)下游側、且較前述第二氣體壓縮機(9)上游側之前述供給管線(L1)合流。為第八壓力<第三壓力之關係。第二氣體壓縮機(9)有效地壓縮第二循環管線(L3)供給之中壓回收氣體。 The second circulation line (L3) may merge with the supply line (L1) downstream of the first gas compressor (6) and upstream of the second gas compressor (9). It is the relationship between the eighth pressure and the third pressure. The second gas compressor (9) effectively compresses the medium-pressure recovery gas supplied from the second circulation line (L3).
在此構成中，將藉由第一氣體壓縮機(6)壓縮後之氣體與中壓回收氣體合流再利用第二壓縮機(9)進行壓縮，在利用主熱交換器(1)進行冷卻後利用低溫氣體昇壓機(7)進行昇壓藉此獲得高壓氣體。據此，即便在天然氣體的膨脹比有所限制而以天然氣體渦輪機(8)獲得之動力較少，亦能有效地將氣體壓縮到能將氣體液化的壓力程度。 In this structure, the gas compressed by the first gas compressor (6) and the medium-pressure recovery gas are combined and compressed by the second compressor (9), and then cooled by the main heat exchanger (1). The low-temperature gas booster (7) is used to boost the pressure to obtain high-pressure gas. According to this, even if the expansion ratio of the natural gas is limited and the natural gas turbine (8) obtains less power, the gas can be effectively compressed to a pressure level that can liquefy the gas.
上述氣體液化裝置亦可具備：第二氣體壓縮機(9)，配置於導入至前述主熱交換器(1)並自其途中導出後之位置之供給管線(L1)，將供給氣體壓縮至第九壓力。 The above-mentioned gas liquefaction device may also be equipped with: a second gas compressor (9), which is arranged in the supply line (L1) introduced into the aforementioned main heat exchanger (1) and led out from the middle, and compresses the supply gas to the third gas liquefaction device. Nine pressures.
上述氣體液化裝置亦可具備：中間冷卻器(10)，冷卻由前述第二氣體壓縮機 (9)壓縮後之供給氣體。 The above-mentioned gas liquefaction device may also be equipped with: an intercooler (10), which is cooled by the aforementioned second gas compressor. (9) Compressed supply gas.
第二氣體壓縮機(9)為從主熱交換器(1)之前段變更了配置至後段之構成。 The second gas compressor (9) has a structure in which the arrangement is changed from the front stage to the rear stage of the main heat exchanger (1).
第二氣體壓縮機(9)為低溫壓縮機，在與低溫氣體昇壓機(7)之間配置中間冷卻器(10)。第二氣體壓縮機(9)之吸入氣體，由主熱交換器(1)冷卻後供給，第二氣體壓縮機(9)之吐出氣體由中間冷卻器(10)冷卻後供給至低溫氣體昇壓機(7)。 The second gas compressor (9) is a low-temperature compressor, and an intercooler (10) is disposed between the second gas compressor (9) and the low-temperature gas booster (7). The suction gas of the second gas compressor (9) is cooled by the main heat exchanger (1) and supplied. The discharge gas of the second gas compressor (9) is cooled by the intercooler (10) and supplied to the low-temperature gas for boosting pressure. Machine(7).
作為其他實施形態，中間冷卻器(10)可與主熱交換器(1)組合，亦可分開設置，將LNG之一部分(透過管線L11)作為冷媒。亦可取代中間冷卻器(10)而利用主熱交換器(1)。 As other embodiments, the intercooler (10) can be combined with the main heat exchanger (1), or can be installed separately, using a part of the LNG (through the pipeline L11) as the refrigerant. It is also possible to use the main heat exchanger (1) instead of the intercooler (10).
上述氣體液化裝置亦可於天然氣體渦輪機(8)之下游側具備天然氣體加熱器(11)。 The above-mentioned gas liquefaction device may also be equipped with a natural gas heater (11) on the downstream side of the natural gas turbine (8).
天然氣體可藉由任意之壓縮機出口之高溫氣體或海等，或者發電機的排熱來加溫而供給至需求區域。例如，存在有天然氣體因在天然氣體渦輪機(8)(膨脹渦輪)膨脹而溫度下降，而未能滿足在下游之天然氣體管道所被要求之供給條件之情況。藉由本構成，即便天然氣體因膨脹而下降到不適當的溫度，亦能滿足下游管道之供給條件。 Natural gas can be heated by high-temperature gas or seawater from any compressor outlet, or by exhaust heat from a generator and supplied to the demand area. For example, there may be cases where the temperature of the natural gas drops due to expansion in the natural gas turbine (8) (expansion turbine), and the supply conditions required for the downstream natural gas pipeline are not met. With this structure, even if the natural gas drops to an inappropriate temperature due to expansion, it can still meet the supply conditions of the downstream pipeline.
上述天然氣體液化裝置亦可於天然氣體渦輪機(8)之入口側(上游側)具備天然氣體加熱器(11)。 The above-mentioned natural gas liquefaction device may also be equipped with a natural gas heater (11) on the inlet side (upstream side) of the natural gas turbine (8).
天然氣體藉由任意之壓縮機出口之高溫氣體、海水、蒸氣、天然氣體燃燒器、或者發電機的排熱來加溫。例如，若利用發電機之排熱，則可將天然氣體加溫至100℃左右，由於能夠使在膨脹時可回收之動力變大，因此可改善效率。 Natural gas is heated by high-temperature gas from any compressor outlet, sea water, steam, natural gas burner, or exhaust heat from a generator. For example, if the exhaust heat of a generator is used, the natural gas can be heated to about 100°C. This can increase the power that can be recovered during expansion, thereby improving efficiency.
上述氣體液化裝置亦可構成為，前述供給管線(L1)往前述主熱交換器(1)導入，自前述主熱交換器(1)之途中導出而往前述第一氣體壓縮機(6)引導供給氣體。 The gas liquefaction device may be configured such that the supply line (L1) is introduced into the main heat exchanger (1), is led out from the middle of the main heat exchanger (1), and is guided to the first gas compressor (6). Supply gas.
進而，前述第一循環管線(L21)亦可為以下構成，即，往前述主熱交換器(1) 導入，自前述主熱交換器(1)之途中導出，往前述供給管線(L1)(之較前述第一氣體壓縮機(6)上游側)合流。 Furthermore, the first circulation line (L21) may be configured as follows: It is introduced from the middle of the main heat exchanger (1) and merges into the supply line (L1) (upstream of the first gas compressor (6)).
在此構成中，第一氣體壓縮機(6)在低溫中被運用。供給氣體在由主熱交換器(1)冷卻後供給至第一氣體壓縮機(6)，低壓回收氣體從主熱交換器(1)以低溫之狀態被導出，供給至第一氣體壓縮機(6)。藉由此構成，能減少第一氣體壓縮機(6)之動力，進而改善效率(參照圖1B、2B、6等)。 In this configuration, the first gas compressor (6) is operated at low temperatures. The supply gas is cooled by the main heat exchanger (1) and supplied to the first gas compressor (6). The low-pressure recovery gas is led out from the main heat exchanger (1) in a low-temperature state and supplied to the first gas compressor (6). 6). With this structure, the power of the first gas compressor (6) can be reduced and the efficiency can be improved (see FIGS. 1B, 2B, 6, etc.).
1:主熱交換器 1: Main heat exchanger
2:第一膨脹閥 2: First expansion valve
3:分離器 3:Separator
4:次冷卻器 4: Secondary cooler
5:第二膨脹閥 5: Second expansion valve
6:第一氣體壓縮機 6: First gas compressor
7:低溫氣體昇壓機 7: Low temperature gas booster
8:天然氣體渦輪機(膨脹渦輪機) 8: Natural gas turbine (expansion turbine)
9:第二氣體壓縮機 9: Second gas compressor
10:中間冷卻器 10: Intercooler
11:天然氣體加熱器 11:Natural gas heater
L1:供給管線 L1: Supply pipeline
L10:第二取出管線 L10: Second extraction line
L11:管線 L11: Pipeline
L2:第一取出管線 L2: First take out the pipeline
L21:第一循環管線 L21: First circulation pipeline
L3:第二循環管線 L3: Second circulation pipeline
LNG:液化天然氣體 LNG: liquefied natural gas
NG:天然氣體 NG: natural gas
[圖1A]係表示實施形態1之氣體液化裝置之圖。 [Fig. 1A] is a diagram showing a gas liquefaction device according to Embodiment 1.
[圖1B]係表示實施形態1之變形例之氣體液化裝置之圖。 [Fig. 1B] is a diagram showing a gas liquefaction device according to a modified example of Embodiment 1.
[圖2A]係表示實施形態2之氣體液化裝置之圖。 [Fig. 2A] is a diagram showing a gas liquefaction device according to Embodiment 2.
[圖2B]係表示實施形態2之變形例之氣體液化裝置之圖。 [Fig. 2B] is a diagram showing a gas liquefaction device according to a modification of the second embodiment.
[圖3]係表示實施形態3之氣體液化裝置之圖。 [Fig. 3] is a diagram showing a gas liquefaction device according to Embodiment 3. [Fig.
[圖4]係表示實施形態4之氣體液化裝置之圖。 [Fig. 4] is a diagram showing a gas liquefaction device according to Embodiment 4.
[圖5]係表示實施形態5之氣體液化裝置之圖。 [Fig. 5] is a diagram showing a gas liquefaction device according to Embodiment 5. [Fig.
[圖6]係表示實施形態6之氣體液化裝置之圖。 [Fig. 6] is a diagram showing a gas liquefaction device according to Embodiment 6.
以下針對本發明之幾個實施形態進行說明。以下說明之實施形態係說明本發明之一例。本發明並未對以下之實施形態做任何限定，且也包含在不變更本發明之要旨之範圍內所實施之各種變形態樣。另外，以下說明之構成之全部並不限定為本發明之必要構成。 Several embodiments of the present invention will be described below. The embodiment described below is an example of the present invention. The present invention is not limited in any way to the following embodiments, and includes various modifications that can be implemented within the scope that does not change the gist of the present invention. In addition, all the structures described below are not limited to essential structures of the present invention.
<實施形態1> <Embodiment 1>
使用圖1說明關於實施形態1之氣體液化裝置。 The gas liquefaction device of Embodiment 1 will be described using FIG. 1 .
氣體液化裝置具備用以供給第1壓力(例如0.1MPa)之供給氣體(Feed gas)之供給管線L1。 The gas liquefaction device is provided with a supply line L1 for supplying a feed gas at a first pressure (for example, 0.1 MPa).
供給管線L1配置有第1氣體壓縮機6、低溫氣體昇壓機7，又構成為至少一次通過主熱交換器1，對供給氣體進行熱交換。 The supply line L1 is provided with a first gas compressor 6 and a low-temperature gas booster 7, and is configured to pass through the main heat exchanger 1 at least once to perform heat exchange on the supply gas.
第1氣體壓縮機6配置於供給管線L1，將供給氣體壓縮至第二壓力(例如0.5MPa)。 The first gas compressor 6 is disposed in the supply line L1 and compresses the supply gas to a second pressure (for example, 0.5 MPa).
主熱交換器1除了由第一氣體壓縮機6壓縮後之供給氣體(壓縮供給氣體)透過供給管線L1而導入之外，還導入後述之各種循環氣體、LNG以進行熱交換。 In addition to the supply gas compressed by the first gas compressor 6 (compressed supply gas) introduced through the supply line L1, the main heat exchanger 1 also introduces various circulating gases and LNG described below for heat exchange.
低溫氣體昇壓機7，從主熱交換器1之中間(中途)，將透過供給管線L1導出之供給氣體昇壓至第三壓力(例如5MPa)。 The low-temperature gas booster 7 boosts the supply gas led out through the supply line L1 from the middle (midway) of the main heat exchanger 1 to a third pressure (for example, 5 MPa).
第一膨脹閥2於使由低溫氣體昇壓機7昇壓至第三壓力(例如5MPa)之昇壓後的供給氣體(昇壓供給氣體)透過供給管線L1利用主熱交換器1進行熱交換而導出之後，減壓(膨脹)至第四壓力(例如0.5MPa)。 The first expansion valve 2 performs heat exchange with the main heat exchanger 1 by passing the pressurized supply gas (pressurized supply gas) pressurized to a third pressure (for example, 5 MPa) by the low-temperature gas booster 7 through the supply line L1. After being exported, the pressure is reduced (expanded) to the fourth pressure (for example, 0.5MPa).
分離器3將由第一膨脹閥2減壓後之供給氣體(氣液混合氣體)分離成氣體成分與液體成分。 The separator 3 separates the supply gas (gas-liquid mixed gas) decompressed by the first expansion valve 2 into a gas component and a liquid component.
第一取出管線L2，是用於使自分離器3導出之第五壓力之液體成分(中壓液態氣體)通過次冷卻器4，作為液化氣體(Liquefied gas)而取出之管線。 The first take-out line L2 is a line for taking out the liquid component (medium-pressure liquid gas) of the fifth pressure derived from the separator 3 through the sub-cooler 4 as liquefied gas (Liquefied gas).
第二膨脹閥5將自第一取出管線L2分歧之一部分之液體成分減壓至第六壓力(第二壓力>第六壓力>第一壓力)。 The second expansion valve 5 decompresses a portion of the liquid component branched from the first take-out line L2 to the sixth pressure (second pressure>sixth pressure>first pressure).
第一循環管線L21為如下之管線：配置有第二膨脹閥5，且自第一取出管線 L2分歧，用以使由第二膨脹閥5減壓後之氣體(低壓回收氣體)往次冷卻器4作為冷媒而使用後，送往主熱交換器(1)，接著往供給管線L1之較第一氣體壓縮機6上游側返回。 The first circulation pipeline L21 is a pipeline equipped with the second expansion valve 5 and is taken out from the first pipeline The L2 branch is used to allow the gas decompressed by the second expansion valve 5 (low-pressure recovery gas) to be used as refrigerant in the secondary cooler 4, then sent to the main heat exchanger (1), and then to the supply line L1. The upstream side of the first gas compressor 6 returns.
第二循環管線L3為如下之管線：用以在將自分離器3導出之第七壓力之氣體成分(中壓回收氣體，第七壓力>第二壓力)送往主熱交換器1後，往供給管線L1之較第一氣體壓縮機6下游側返回。 The second circulation line L3 is a pipeline used to send the seventh pressure gas component (medium pressure recovery gas, seventh pressure > second pressure) derived from the separator 3 to the main heat exchanger 1, and then to the main heat exchanger 1. The supply line L1 returns to the downstream side of the first gas compressor 6 .
天然氣體渦輪機8與低溫氣體昇壓機7連結，提供用於進行驅動之動力。 The natural gas turbine 8 is connected to the low-temperature gas booster 7 and provides power for driving.
第二取出管線L10，係用以使液化天然氣體(LNG)往主熱交換器1導入後，且於天然氣體渦輪機8使用後，作為天然氣體(NG)而取出之管線。 The second take-out line L10 is a line for introducing liquefied natural gas (LNG) into the main heat exchanger 1 and taking it out as natural gas (NG) after being used in the natural gas turbine 8 .
在本實施形態中，作為原料之供給氣體與自次冷卻器(4)供給之低壓回收氣體合流，在第一氣體壓縮機(6)被壓縮，經壓縮之供給氣體與自分離器(3)供給之中壓回收氣體合流後，在主熱交換器(1)被冷卻後藉由低溫氣體昇壓機(7)壓縮，得到高壓氣體。 In this embodiment, the supply gas as raw material is merged with the low-pressure recovery gas supplied from the subcooler (4), and is compressed in the first gas compressor (6). The compressed supply gas is separated from the separator (3) After the supplied medium-pressure recovery gas is combined, it is cooled in the main heat exchanger (1) and compressed by the low-temperature gas booster (7) to obtain high-pressure gas.
高壓氣體在由主熱交換器(1)冷卻後，在第一膨脹閥(2)膨脹，藉由分離器(3)而氣液分離。在分離器(3)所獲得之中壓液態氣體，藉由次冷卻器(4)冷卻後，一部分作為製品而導出。其餘之中壓液態氣體由第二膨脹閥(5)減壓後，作為冷媒供給至次冷卻器(4)，進一步在主熱交換器(1)釋放冷能後於較第一氣體壓縮機(6)上游側與供給管線(L1)合流。 After the high-pressure gas is cooled by the main heat exchanger (1), it expands in the first expansion valve (2), and is separated into gas and liquid by the separator (3). The medium-pressure liquid gas obtained in the separator (3) is cooled by the sub-cooler (4), and a part of it is exported as a product. The remaining medium-pressure liquid gas is decompressed by the second expansion valve (5) and then supplied to the secondary cooler (4) as refrigerant. It further releases cold energy in the main heat exchanger (1) and is compared with the first gas compressor (4). 6) The upstream side merges with the supply line (L1).
LNG在被供給至主熱交換器(1)並釋放冷能後，從主熱交換器(1)之溫端導出，至少其一部分藉由天然氣體渦輪機(8)而膨脹，而驅動低溫氣體昇壓機(7)。 After LNG is supplied to the main heat exchanger (1) and releases cold energy, it is exported from the warm end of the main heat exchanger (1). At least part of it is expanded by the natural gas turbine (8), driving the low-temperature gas to rise. Press(7).
藉由此構成，不僅能活用藉由天然氣體渦輪機(8)所得之動力來進行氣體壓縮，還能將氣體藉由LNG冷能進行預冷後進行氣體壓縮，藉此大幅地改善壓縮效 率。 With this configuration, not only can the power obtained by the natural gas turbine (8) be utilized for gas compression, but the gas can also be precooled by LNG cold energy and then compressed, thereby greatly improving the compression efficiency. Rate.
在上述各管線，亦可設有閥(例如閘閥、流量調整閥、壓力調整閥等)。 Each of the above pipelines may also be provided with valves (such as gate valves, flow regulating valves, pressure regulating valves, etc.).
<實施形態1之其他實施形態> <Other embodiments of embodiment 1>
使用圖1B說明關於其他實施形態之氣體液化裝置。針對與實施形態1之圖1A不同之構成進行說明，針對相同之構成則省略或簡化說明。 A gas liquefaction device according to another embodiment will be described using FIG. 1B. The structure different from that of FIG. 1A of Embodiment 1 will be described, and the description of the same structure will be omitted or simplified.
供給管線L1構成為往主熱交換器1導入，從主熱交換器1之途中導出而往第一氣體壓縮機6引導供給氣體。 The supply line L1 is introduced into the main heat exchanger 1 and is led out from the middle of the main heat exchanger 1 to guide the supply gas to the first gas compressor 6 .
第一循環管線L21係往主熱交換器1導入，從主熱交換器1之途中導出，往供給管線L1之較第一氣體壓縮機6上游側合流之構成。 The first circulation line L21 is introduced into the main heat exchanger 1 , is led out from the middle of the main heat exchanger 1 , and merges with the supply line L1 upstream of the first gas compressor 6 .
<實施形態2> <Embodiment 2>
使用圖2A說明關於實施形態2之氣體液化裝置。針對與實施形態1(圖1A)不同之構成進行說明，針對相同之構成則省略或簡化說明。 The gas liquefaction device of Embodiment 2 will be described using FIG. 2A. Configurations different from those in Embodiment 1 (FIG. 1A) will be described, and descriptions of the same configurations will be omitted or simplified.
第二氣體壓縮機9配置於較第一氣體壓縮機6下游側之供給管線L1，將供給氣體壓縮至第八壓力(例如1MPa)。 The second gas compressor 9 is disposed in the supply line L1 downstream of the first gas compressor 6 and compresses the supply gas to an eighth pressure (for example, 1 MPa).
第二循環管線L3往較第一氣體壓縮機6下游側，且較第二氣體壓縮機9上游側之供給管線L1合流。第八壓力<第三壓力之關係成立。 The second circulation line L3 merges with the supply line L1 on the downstream side of the first gas compressor 6 and upstream of the second gas compressor 9 . The relationship of eighth pressure < third pressure is established.
<實施形態2之其他實施形態> <Other embodiments of embodiment 2>
使用圖2B說明關於其他實施形態之氣體液化裝置。針對與實施形態2之圖2A不同之構成進行說明，針對相同之構成則省略或簡化說明。 A gas liquefaction device according to another embodiment will be described using FIG. 2B. The structure different from that in FIG. 2A of Embodiment 2 will be described, and the description of the same structure will be omitted or simplified.
供給管線L1構成為往主熱交換器1導入，從主熱交換器1之途中導出而往第 一氣體壓縮機6引導供給氣體。 The supply line L1 is introduced into the main heat exchanger 1 and is led out from the main heat exchanger 1 to the third A gas compressor 6 conducts the supply gas.
第一循環管線L21係往主熱交換器1導入，從主熱交換器1之途中導出而往供給管線L1之較第一氣體壓縮機6上游側合流之構成。 The first circulation line L21 is introduced into the main heat exchanger 1 , is led out from the middle of the main heat exchanger 1 , and merges with the supply line L1 upstream of the first gas compressor 6 .
<實施形態3> <Embodiment 3>
使用圖3說明關於實施形態3之氣體液化裝置。針對與實施形態1、2(圖1A、2A)不同之構成進行說明，針對相同之構成則省略或簡化說明。 The gas liquefaction device of Embodiment 3 will be described using FIG. 3 . Configurations different from those of Embodiments 1 and 2 (Figs. 1A and 2A) will be described, and descriptions of the same configurations will be omitted or simplified.
於實施形態3中，在實施形態2中配置於主熱交換器1之上游側的第二氣體壓縮機9配置於主熱交換器1之後段。 In Embodiment 3, the second gas compressor 9 arranged on the upstream side of main heat exchanger 1 in Embodiment 2 is arranged in the subsequent stage of main heat exchanger 1 .
第二氣體壓縮機9配置於導入至主熱交換器1並從主熱交換器1之中斷(途中)導出後之位置之供給管線L1，將第二氣體壓縮機9之下游側之供給氣體壓縮至第九壓力(例如1MPa)。 The second gas compressor 9 is disposed in the supply line L1 at a position introduced into the main heat exchanger 1 and led out from the main heat exchanger 1 to compress the supply gas on the downstream side of the second gas compressor 9 to the ninth pressure (eg 1MPa).
中間冷卻器10配置於供給管線L1，對由第二氣體壓縮機9壓縮後之供給氣體進行冷卻。由中間冷卻器10冷卻後之供給氣體，被送往其後段之低溫氣體昇壓機7。供給氣體藉由低溫氣體昇壓機7壓縮成為高壓氣體，在由主熱交換器1冷卻後，被送往第一膨脹閥2進行膨脹。其後，進行與實施形態1同樣之處理。 The intercooler 10 is disposed in the supply line L1 and cools the supply gas compressed by the second gas compressor 9 . The supply gas cooled by the intercooler 10 is sent to the low-temperature gas booster 7 in the subsequent stage. The supply gas is compressed into high-pressure gas by the low-temperature gas booster 7, and after being cooled by the main heat exchanger 1, is sent to the first expansion valve 2 for expansion. Thereafter, the same processing as in Embodiment 1 is performed.
在本實施形態中，第二氣體壓縮機9作為低溫壓縮機發揮功能。第二氣體壓縮機9之吸入氣體，由主熱交換器1冷卻後供給，第二氣體壓縮機9之吐出氣體由中間冷卻器10冷卻後供給至低溫氣體昇壓機7。在本實施形態中，中間冷卻器10之冷媒係將LNG之一部分透過管線L11而供給。 In this embodiment, the second gas compressor 9 functions as a low-temperature compressor. The suction gas of the second gas compressor 9 is cooled by the main heat exchanger 1 and supplied, and the discharge gas of the second gas compressor 9 is cooled by the intercooler 10 and supplied to the low-temperature gas booster 7 . In this embodiment, a part of the LNG is supplied as the refrigerant to the intercooler 10 through the line L11.
<實施形態3之其他實施形態> <Other embodiments of embodiment 3>
針對與實施形態3之圖3不同之構成進行說明，針對相同之構成則省略或簡化說明。 The structure different from that in FIG. 3 of Embodiment 3 will be described, and the description of the same structure will be omitted or simplified.
供給管線L1構成為，往主熱交換器1導入，從主熱交換器1之途中導出而往第一氣體壓縮機6引導供給氣體。第一循環管線L21係往主熱交換器1導入，從主熱交換器1之途中導出，往供給管線L1之較第一氣體壓縮機6上游側合流之構成。 The supply line L1 is introduced into the main heat exchanger 1 and led out from the middle of the main heat exchanger 1 to guide the supply gas to the first gas compressor 6 . The first circulation line L21 is introduced into the main heat exchanger 1 , is led out from the middle of the main heat exchanger 1 , and merges with the supply line L1 upstream of the first gas compressor 6 .
<實施形態4> <Embodiment 4>
使用圖4說明關於實施形態4之氣體液化裝置。針對與實施形態3(圖3)不同之構成進行說明，針對相同之構成則省略或簡化說明。 The gas liquefaction device of Embodiment 4 will be described using FIG. 4 . Configurations different from those in Embodiment 3 (Fig. 3) will be described, and descriptions of the same configurations will be omitted or simplified.
天然氣體加熱器11配置於天然氣體渦輪機8之下游側之第二取出管線L10。 The natural gas heater 11 is arranged in the second take-out line L10 on the downstream side of the natural gas turbine 8 .
<實施形態4之其他實施形態> <Other embodiments of embodiment 4>
針對與實施形態4之圖4不同之構成進行說明，針對相同之構成則省略或簡化說明。 The structure different from that in FIG. 4 of Embodiment 4 will be described, and the description of the same structure will be omitted or simplified.
供給管線L1構成為往主熱交換器1導入，從主熱交換器1之途中導出而往第一氣體壓縮機6引導供給氣體。第一循環管線L21係往主熱交換器1導入，從主熱交換器1之途中導出，往供給管線L1之較第一氣體壓縮機6上游側合流之構成。 The supply line L1 is introduced into the main heat exchanger 1 and is led out from the middle of the main heat exchanger 1 to guide the supply gas to the first gas compressor 6 . The first circulation line L21 is introduced into the main heat exchanger 1 , is led out from the middle of the main heat exchanger 1 , and merges with the supply line L1 upstream of the first gas compressor 6 .
<實施形態5> <Embodiment 5>
使用圖5說明關於實施形態5之氣體液化裝置。針對與實施形態3(圖3)不同之構成進行說明，針對相同之構成則省略或簡化說明。 The gas liquefaction device of Embodiment 5 will be described using FIG. 5 . Configurations different from those in Embodiment 3 (Fig. 3) will be described, and descriptions of the same configurations will be omitted or simplified.
天然氣體加熱器11配置於天然氣體渦輪機8之入口側(上游側)之第二取出管線L10。 The natural gas heater 11 is arranged in the second take-out line L10 on the inlet side (upstream side) of the natural gas turbine 8 .
<實施形態6> <Embodiment 6>
使用圖6說明關於實施形態6之氣體液化裝置。針對與實施形態5(圖5)不同之 構成進行說明，針對相同之構成則省略或簡化說明。 The gas liquefaction device of Embodiment 6 will be described using FIG. 6 . Regarding the differences from Embodiment 5 (Fig. 5) The structure will be described, and the description of the same structure will be omitted or simplified.
供給管線L1構成為往主熱交換器1導入，從主熱交換器1之途中導出而往第一氣體壓縮機6引導供給氣體。第一循環管線L21係往主熱交換器1導入，從主熱交換器1之途中導出，往供給管線L1之較第一氣體壓縮機6上游側合流之構成。 The supply line L1 is introduced into the main heat exchanger 1 and is led out from the middle of the main heat exchanger 1 to guide the supply gas to the first gas compressor 6 . The first circulation line L21 is introduced into the main heat exchanger 1 , is led out from the middle of the main heat exchanger 1 , and merges with the supply line L1 upstream of the first gas compressor 6 .
(實施例1) (Example 1)
更具體地說明上述實施形態1(圖1)之裝置。 The device of the above-mentioned Embodiment 1 (Fig. 1) will be described more specifically.
在此，將氮氣作為供給氣體。 Here, nitrogen gas is used as the supply gas.
作為原料之供給氣體係以0.12MPa、20℃、1000Nm3/h供給，與自次冷卻器4供給之低壓回收氣體(230Nm3/h)合流，而由第一氣體壓縮機6壓縮至0.77MPa。 The supply gas system as the raw material is supplied at 0.12MPa, 20°C, and 1000Nm 3 /h. It is combined with the low-pressure recovery gas (230Nm 3 /h) supplied from the sub-cooler 4 and compressed to 0.77MPa by the first gas compressor 6 .
經壓縮後之供給氣體，與自分離器3供給之中壓回收氣體(416Nm3/h)合流之後，由主熱交換器1冷卻至-104℃後藉由低溫氣體昇壓機7壓縮至5.0MPa，得到高壓氣體。 After the compressed supply gas is combined with the medium-pressure recovery gas (416Nm 3 /h) supplied from the separator 3, it is cooled to -104°C by the main heat exchanger 1 and then compressed to 5.0 by the low-temperature gas booster 7 MPa to obtain high-pressure gas.
所得到之高壓氣體在由主熱交換器1冷卻至-156℃後，由第一膨脹閥2膨脹至0.77MPa，且藉由分離器3而氣液分離。 The obtained high-pressure gas is cooled to -156°C by the main heat exchanger 1, expanded to 0.77MPa by the first expansion valve 2, and separated into gas and liquid by the separator 3.
於分離器3所得到之中壓液態氣體(1230Nm3/h)，藉由次冷卻器4冷卻至-194℃後，液化氣體(1000Nm3/h)作為製品被導出。其餘的中壓液態氣體(230Nm3/h)由第二膨脹閥5減壓至0.13MPa後，作為冷媒被供給至次冷卻器4，進一步地在主熱交換器1放出冷能後被供給至第一氣體壓縮機6。 The medium-pressure liquid gas (1230Nm 3 /h) obtained in the separator 3 is cooled to -194°C by the sub-cooler 4, and the liquefied gas (1000Nm 3 /h) is exported as a product. The remaining medium-pressure liquid gas (230Nm 3 /h) is decompressed to 0.13MPa by the second expansion valve 5 and then supplied to the sub-cooler 4 as refrigerant. It is further supplied to the main heat exchanger 1 after releasing cold energy. First gas compressor 6.
LNG係以7.3MPa、-155℃、3700Nm3/h之條件被供給至主熱交換器1而在放出冷能後從主熱交換器1之溫端以7.1MPa、10℃之條件導出，其總量為藉由天然氣體渦輪機8膨脹至0.7MPa而作為天然氣體取出。天然氣體渦輪機8驅動低溫氣體昇壓機7。 LNG is supplied to the main heat exchanger 1 under the conditions of 7.3MPa, -155°C, and 3700Nm 3 /h, and after releasing the cold energy, it is derived from the warm end of the main heat exchanger 1 under the conditions of 7.1MPa, 10°C. The total amount is expanded to 0.7MPa by the natural gas turbine 8 and taken out as natural gas. The natural gas turbine 8 drives the cryogenic gas booster 7 .
在本實施形態1之處理中，能一邊對在天然氣體之膨脹時所放出 之能量進行回收，且一邊有效利用LNG冷能而使氣體液化。 In the processing of this embodiment 1, it is possible to control the gas released during the expansion of natural gas. The energy is recovered and the cold energy of LNG is effectively utilized to liquefy the gas.
<優越性評價> <Evaluation of superiority>
將相當於實施形態1~5之實施例1~6之優越性，與比較例做比較來進行說明。 The advantages of Examples 1 to 6 corresponding to Embodiments 1 to 5 will be explained by comparing them with Comparative Examples.
比較例：專利文獻1(日本特許第4142559號公報) Comparative example: Patent Document 1 (Japanese Patent No. 4142559)
實施例1：實施形態1(圖1A) Example 1: Embodiment 1 (Fig. 1A)
實施例2：實施形態2(圖2A) Example 2: Embodiment 2 (Fig. 2A)
實施例3：實施形態3(圖3) Example 3: Embodiment 3 (Fig. 3)
實施例4：實施形態4(圖4) Example 4: Embodiment 4 (Fig. 4)
實施例5：實施形態5(圖5) Example 5: Embodiment 5 (Fig. 5)
實施例6：實施形態6(圖6) Example 6: Embodiment 6 (Fig. 6)
將實施例1與比較例進行比較。 Compare Example 1 with Comparative Examples.
作為比較例，為在專利文獻1(日本特許第4142559號)之處理中將氮進行液化之構成，與本實施例1進行比較評量。 As a comparative example, a structure in which nitrogen is liquefied in the process of Patent Document 1 (Japanese Patent No. 4142559) is compared with Example 1 and evaluated.
在比較例中，將0.9MPa之LNG供給至裝置而使其蒸發，在得到0.7MPa之天然氣體之情形時，利用回收之冷能而得到液態氮時之液化原單位約為0.3kWh/Nm3。相較之下，在本實施例中，於將LNG自0.9MPa昇壓至7.3MPa時必須有23kW之能量，但由於利用天然氣體渦輪機8(膨脹渦輪機)回收123kW之能量而利用於氣體之壓縮(低溫氣體昇壓機7)，因此整體上能削減100kW之能量。 In the comparative example, when 0.9 MPa of LNG is supplied to the device and evaporated, and 0.7 MPa of natural gas is obtained, the liquefaction original unit when liquid nitrogen is obtained by utilizing the recovered cold energy is approximately 0.3 kWh/Nm 3 . In comparison, in this embodiment, 23 kW of energy is required to increase the pressure of LNG from 0.9 MPa to 7.3 MPa. However, the natural gas turbine 8 (expansion turbine) is used to recover 123 kW of energy and use it for gas compression. (Low temperature gas booster 7), therefore the overall energy can be reduced by 100kW.
在實施例1中，得到1000Nm3/h之液態氮，在液化原單位能削減0.1kWh/Nm3，相對於比較例能有約0.33%之效率改善。 In Example 1, 1000Nm 3 /h of liquid nitrogen is obtained, which can reduce the liquefaction unit by 0.1kWh/Nm 3 and improve the efficiency by about 0.33% compared to the comparative example.
實施例2與實施例1相比，係於第一氣體壓縮機6之吐出管線(L1)追加有第二氣體壓縮機9之構成。藉由此構成，即便是在天然氣體渦輪機8(膨脹渦輪機)能回收之動力小之情況，亦能將氣體昇壓至對於液化而言充分的壓力。 Compared with Example 1, Example 2 has a structure in which a second gas compressor 9 is added to the discharge line (L1) of the first gas compressor 6. With this configuration, even when the power that can be recovered by the natural gas turbine 8 (expansion turbine) is small, the gas can be pressurized to a pressure sufficient for liquefaction.
實施例3與實施例2相比，係對往第二氣體壓縮機9供給之吸入氣體以主熱交換器1進行冷卻，且將自第二氣體壓縮機9吐出之吐出氣體以中間冷卻器10(LNG冷能)冷卻後，於低溫氣體昇壓機7供給供給氣體。藉由此構成，與與實施例2相同地，即便是在天然氣體渦輪機8(膨脹渦輪機)能回收之動力小之情況，亦能將氣體昇壓至對於液化而言充分的壓力。 Compared with Example 2, Example 3 cools the suction gas supplied to the second gas compressor 9 with the main heat exchanger 1 and cools the discharge gas discharged from the second gas compressor 9 with the intercooler 10 (LNG cold energy) is cooled, and then the supply gas is supplied to the low-temperature gas booster 7 . With this configuration, like Embodiment 2, even when the power that can be recovered by the natural gas turbine 8 (expansion turbine) is small, the gas can be pressurized to a pressure sufficient for liquefaction.
實施例4與實施例3相比，係在天然氣體渦輪機8(膨脹渦輪機)之吐出側具備有天然氣體加熱器11之構成。一般而言，於供給至天然氣體管道之天然氣體溫度，有例如-10℃以上之溫度範圍的限制。假如天然氣體以膨脹比10倍由天然氣體渦輪機8(膨脹渦輪機)進行膨脹，由於溫度降低70℃左右，所以即便能將天然氣體從主熱交換器1以10℃導出，也有可能在天然氣體渦輪機8(膨脹渦輪機)出口變為-60℃，而無法滿足在下游所要求之規格，但藉由實施形態4之天然氣體加熱器11能夠解決此問題，且即便使天然氣體膨脹後也能進行供給。 Compared with Example 3, Example 4 is configured to include a natural gas heater 11 on the discharge side of the natural gas turbine 8 (expansion turbine). Generally speaking, the temperature of the natural gas supplied to the natural gas pipeline is limited to a temperature range of -10° C. or higher. If the natural gas is expanded by the natural gas turbine 8 (expansion turbine) at an expansion ratio of 10 times, the temperature drops by about 70°C. Therefore, even if the natural gas can be exported from the main heat exchanger 1 at 10°C, it is possible that the natural gas turbine 8 8 (expansion turbine) outlet becomes -60°C, which cannot meet the specifications required downstream. However, the natural gas heater 11 of Embodiment 4 can solve this problem, and the natural gas can be supplied even after it is expanded. .
實施例5與實施例3相比，係在天然氣體渦輪機8(膨脹渦輪機)之吸入側具備有天然氣體加熱器11之構成。例如，若將藉由天然氣體加熱器11膨脹之前之天然氣體，從實施例1之10℃設為100℃，則能夠將能回收之能量自123kW增加至183kW，進而能提高氣體壓縮之效率。 Compared with Example 3, Example 5 is configured to include a natural gas heater 11 on the suction side of the natural gas turbine 8 (expansion turbine). For example, if the natural gas before expansion by the natural gas heater 11 is changed from 10°C in Embodiment 1 to 100°C, the energy that can be recovered can be increased from 123kW to 183kW, thereby improving the efficiency of gas compression.
實施例6與實施例5相比，係第一氣體壓縮機6作為低溫壓縮機發揮功能，且供給氣體由主熱交換器1冷卻後供給至第一氣體壓縮機6。藉由第一循環管線L21，低壓回收氣體從主熱交換器1以低溫導出，供給至第一氣體壓縮機6。藉由此構成，能減低第一氣體壓縮機6之動力，而能進一步地改善效率。第一氣體壓縮機6之動力為84kW，在實施例1中為110kW，也就是能削減27kW(25%)之能量。 Example 6 is compared with Example 5 in that the first gas compressor 6 functions as a low-temperature compressor, and the supply gas is cooled by the main heat exchanger 1 and then supplied to the first gas compressor 6 . Through the first circulation line L21, the low-pressure recovery gas is led out from the main heat exchanger 1 at low temperature and supplied to the first gas compressor 6. With this configuration, the power of the first gas compressor 6 can be reduced, and the efficiency can be further improved. The power of the first gas compressor 6 is 84kW, which is 110kW in Embodiment 1, that is, the energy can be reduced by 27kW (25%).
實施例6之構成亦可適用於實施例1~4的任一者。 The structure of Embodiment 6 can also be applied to any one of Embodiments 1 to 4.
<其他實施形態> <Other embodiments>
雖未特別明示，但也可於各管線設置壓力調整裝置、流量控制裝置等，以進行壓力調整或流量調整。 Although not specifically stated, a pressure adjustment device, a flow control device, etc. may also be installed in each pipeline to perform pressure adjustment or flow adjustment.
1:主熱交換器 1: Main heat exchanger
2:第一膨脹閥 2: First expansion valve
3:分離器 3:Separator
4:次冷卻器 4: Secondary cooler
5:第二膨脹閥 5: Second expansion valve
6:第一氣體壓縮機 6: First gas compressor
7:低溫氣體昇壓機 7: Low temperature gas booster
8:天然氣體渦輪機(膨脹渦輪機) 8: Natural gas turbine (expansion turbine)
L1:供給管線 L1: Supply pipeline
L10:第二取出管線 L10: Second extraction line
L2:第一取出管線 L2: First take out the pipeline
L21:第一循環管線 L21: First circulation pipeline
L3:第二循環管線 L3: Second circulation pipeline
LNG:液化天然氣體 LNG: liquefied natural gas
NG:天然氣體 NG: natural gas
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| KR20210036826A (en) | 2021-04-05 |
| TW202129210A (en) | 2021-08-01 |
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| JP7355979B2 (en) | 2023-10-04 |
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