WO2016139702A1 - 天然ガスの液化システム及び液化方法 - Google Patents
天然ガスの液化システム及び液化方法 Download PDFInfo
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- WO2016139702A1 WO2016139702A1 PCT/JP2015/001138 JP2015001138W WO2016139702A1 WO 2016139702 A1 WO2016139702 A1 WO 2016139702A1 JP 2015001138 W JP2015001138 W JP 2015001138W WO 2016139702 A1 WO2016139702 A1 WO 2016139702A1
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- gas
- heat exchanger
- refrigerant
- natural gas
- raw material
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 106
- 239000003345 natural gas Substances 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title description 6
- 239000007789 gas Substances 0.000 claims abstract description 164
- 239000003507 refrigerant Substances 0.000 claims abstract description 66
- 230000002378 acidificating effect Effects 0.000 claims abstract description 28
- 238000001816 cooling Methods 0.000 claims abstract description 26
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 18
- 238000010438 heat treatment Methods 0.000 claims abstract description 16
- 239000002994 raw material Substances 0.000 claims description 65
- 239000002253 acid Substances 0.000 claims description 29
- 230000006837 decompression Effects 0.000 claims description 14
- 229930195733 hydrocarbon Natural products 0.000 claims description 8
- 150000002430 hydrocarbons Chemical class 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 5
- 238000010521 absorption reaction Methods 0.000 description 12
- 239000007788 liquid Substances 0.000 description 9
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 4
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 238000007710 freezing Methods 0.000 description 3
- 230000008014 freezing Effects 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 239000008096 xylene Substances 0.000 description 2
- GIAFURWZWWWBQT-UHFFFAOYSA-N 2-(2-aminoethoxy)ethanol Chemical compound NCCOCCO GIAFURWZWWWBQT-UHFFFAOYSA-N 0.000 description 1
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 1
- 229940058020 2-amino-2-methyl-1-propanol Drugs 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- GSEJCLTVZPLZKY-UHFFFAOYSA-N Triethanolamine Chemical compound OCCN(CCO)CCO GSEJCLTVZPLZKY-UHFFFAOYSA-N 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- CBTVGIZVANVGBH-UHFFFAOYSA-N aminomethyl propanol Chemical compound CC(C)(N)CO CBTVGIZVANVGBH-UHFFFAOYSA-N 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- LVTYICIALWPMFW-UHFFFAOYSA-N diisopropanolamine Chemical compound CC(O)CNCC(C)O LVTYICIALWPMFW-UHFFFAOYSA-N 0.000 description 1
- 229940043276 diisopropanolamine Drugs 0.000 description 1
- -1 for example Chemical compound 0.000 description 1
- 150000004677 hydrates Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
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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
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/263—Drying gases or vapours by absorption
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
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- 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
- F25J1/0047—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
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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
- F25J1/0087—Propane; Propylene
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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
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- 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
- F25J1/0216—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 using a C3 pre-cooling 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
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0296—Removal of the heat of compression, e.g. within an inter- or afterstage-cooler against an ambient heat sink
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/06—Heat exchange, direct or indirect
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/44—Deacidification step, e.g. in coal enhancing
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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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- 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
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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
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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
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
Definitions
- the present invention relates to a natural gas liquefaction system and a liquefaction method for producing natural gas by cooling natural gas.
- Natural gas collected from gas fields and the like is liquefied at a liquefaction base or the like, and is handled as LNG (liquefied natural gas) for storage and transportation.
- LNG cooled to about ⁇ 162 ° C. has an advantage that the volume is greatly reduced compared to natural gas (gas) and it is not necessary to store at high pressure.
- moisture, acid gas components such as carbon dioxide and hydrogen sulfide, and other impurities such as mercury are removed in advance, and a heavy component having a relatively high freezing point (benzene). , Toluene, xylene, pentane or higher C5 + hydrocarbons, etc.) are removed, and the raw material gas is liquefied by heat exchange with the refrigerant.
- natural gas in a natural gas liquefaction system, as a method for removing acid gas components from natural gas, for example, natural gas can be obtained by bringing an absorbing liquid (such as an amine-based solution) that absorbs acid gas into contact with natural gas.
- an absorbing liquid such as an amine-based solution
- separates acidic gas from the absorption liquid is known (refer patent document 1).
- a method of separating the liquefied heavy portion in the natural gas in a distillation tower is generally used, but the natural gas to be liquefied has a relatively high pressure (for example, when the pressure exceeds 80 barA), it is difficult to separate methane and heavy components in the distillation operation, so it is necessary to reduce the natural gas to a predetermined pressure in advance.
- the temperature range for example, 35 ° C. to 40 ° C.
- the temperature range for example, 35 ° C. to 40 ° C.
- such a tendency is conspicuous when the natural gas having a high pressure (for example, 100 barA or more) is decompressed.
- natural gas is converted to acidic gas by heat exchange with natural gas downstream of the relatively high temperature (for example, before or after removing moisture after removing acid gas) or by heating with a heater. It is conceivable that the temperature is raised to a temperature range suitable for removing the components.
- heat exchange with natural gas before moisture removal hydrates that cause blockage of piping and the like may be generated due to the presence of moisture in the natural gas, and more downstream (after moisture removal) Natural gas may not be able to secure the temperature and flow rate required for temperature rise. Further, heater heating requires a large amount of energy.
- the present invention has been devised in view of such problems of the prior art, and does not require (or suppress) the addition of energy from the outside, and the raw material gas after depressurization is converted into an acidic gas.
- the main object of the present invention is to provide a natural gas liquefaction system and a liquefaction method capable of raising the temperature when removing components.
- a first aspect of the present invention is a natural gas liquefaction system (1) for cooling a raw material gas containing natural gas to produce a liquefied natural gas, and a decompression device (2) for reducing the pressure of the raw material gas
- the acidic gas removing device (3) for removing the gas component and the source gas after the acidic gas component has been removed by the acidic gas removing device are cooled by heat exchange with the refrigerant whose temperature has been lowered.
- the raw material gas that has been lowered in temperature by being decompressed by the decompression device is heated by heat exchange with the refrigerant in the first heat exchanger, energy from the outside is used. Therefore, it is possible to increase the temperature of the decompressed raw material gas when removing the acidic gas component without requiring (or suppressing) the addition. Moreover, since the cold of natural gas by decompression is used for cooling the refrigerant, there is also an advantage that the energy efficiency in the refrigerant cycle can be increased.
- a heating device (8) for heating the source gas supplied from the first heat exchanger to the acidic gas removal device, with respect to the first aspect.
- the temperature of the raw material gas supplied to the acidic gas removal device is reliably controlled within an appropriate range even when the raw material gas is not sufficiently heated by the first heat exchanger. Is possible.
- the third aspect of the present invention relates to the first or second aspect described above, and is provided between the acid gas removal device and the second heat exchanger and removes heavy hydrocarbons in the raw material gas. It further comprises a mass removing device (5).
- heavy hydrocarbons in the second heat exchanger are removed by removing heavy hydrocarbons (heavy content) of the raw material gas supplied to the second heat exchanger. Troubles such as solidification can be avoided.
- the first heat exchanger and the second heat exchanger pre-cool the raw material gas supplied to the liquefaction device, according to any of the first to third aspects.
- a compressor (11) that constitutes a pre-cooling refrigerant cycle and compresses the refrigerant used in the second heat exchanger; and in the refrigerant cycle, the first heat exchanger and the second heat exchanger And an expansion valve (15) that is provided between them to squeeze and expand the refrigerant.
- the refrigerant cooled by heat exchange with the source gas in the first heat exchanger is supplied to the second heat exchanger as a lower temperature refrigerant through the expansion valve. For this reason, it is possible to reduce the load on the compressor in the refrigerant cycle with a simple configuration.
- a natural gas liquefaction method for producing a liquefied natural gas by cooling a raw material gas containing natural gas, wherein the pressure reducing step reduces the pressure of the raw material gas, A first heat exchange step of heating the source gas after being depressurized by heat exchange with a refrigerant, and an acid gas removal step of removing an acid gas component from the source gas after being heated by the first heat exchange step And a second heat exchange step for cooling the raw material gas after the acid gas component is removed by the acid gas removal step by heat exchange with the refrigerant whose temperature has been lowered, and the second heat exchange step. And a liquefaction step for producing a liquefied natural gas by cooling the raw material gas after being cooled by the step (a).
- FIG. 1 is a schematic configuration diagram of a natural gas liquefaction system 1 according to an embodiment of the present invention.
- the liquefaction system 1 generates LNG (liquefied natural gas) by cooling a raw material gas containing natural gas.
- the liquefaction system 1 includes a decompression device 2 that decompresses the raw material gas to a predetermined pressure, an acidic gas removal device 3 that removes acidic gas contained in the raw material gas, and a moisture removal device 4 that removes moisture contained in the raw material gas.
- a heavy component removing device 5 for removing heavy components in the raw material gas here, heavy hydrocarbons such as benzene, toluene, xylene, pentane or higher C5 + hydrocarbons
- the raw material gas as a refrigerant
- It is mainly provided with a liquefaction device 6 that generates LNG by cooling by heat exchange with a liquefaction refrigerant ”.
- the liquefaction system 1 is provided with a precooling system 7 for precooling the raw material gas supplied to the liquefaction device 6 by heat exchange with a refrigerant (hereinafter referred to as “precooling refrigerant”).
- the acid gas removing device 3 is provided with a heater (heating device) 8 that maintains the supplied source gas in an appropriate temperature range by heating the source gas upstream of the acid gas removing device 3. Yes.
- source gas in the present specification does not mean that the gas is strictly in a gaseous state, but refers to an object of liquefaction treatment flowing in the liquefaction system 1 (a partially liquefied state during the treatment). Included).
- the raw material gas processed in the liquefaction system 1 is not particularly limited, and natural gas collected from a known gas field can be used.
- a source gas having a relatively high pressure (at least a pressure exceeding 80 barA, more preferably a pressure exceeding 100 barA) is a target.
- Such a raw material gas has a high pressure to be collected and has a small pressure drop until it is supplied to the liquefaction system 1 after the collection, or is pressurized at the time of collection (for example, FPSO (Floating Production, Storage and Offloading system ) Is supplied to the liquefaction system 1 in a high-pressure state for reasons such as gas separated from crude oil.
- FPSO Floating Production, Storage and Offloading system
- the decompression device 2 is a known expander that lowers the pressure of the raw material gas by isentropic expansion of the flowing raw material gas.
- the raw material gas supplied to the liquefaction system 1 (here, the decompression device 2) has a temperature of about 20 ° C., a pressure of 150 to 200 barA, and a flow rate of about 500,000 kg / hr.
- the temperature, pressure and flow rate of the raw material gas can be changed as necessary.
- the raw material gas is depressurized to a predetermined pressure (here, 70 to 80 barA) by the depressurization device 2 so that appropriate processing can be performed in the heavy component removal device 5 described in detail later.
- the source gas decompressed in the decompression device 2 is heated by heat exchange (heating) with the refrigerant in the refrigerant cooler 14 described in detail later, and further heated to a predetermined temperature by the heating of the heater 8. Later, it is introduced into the acid gas removing device 3.
- the temperature range of the raw material gas introduced into the acid gas removing device 3 is about 25 to 60 ° C., more preferably 35 to 40 ° C. If the temperature of the raw material gas is less than 20 ° C, the fluidity of the acidic gas absorption medium will be reduced, causing problems in the operation of the equipment. If the raw material gas temperature exceeds 60 ° C, the acid gas removal efficiency will be reduced. The problem arises. *
- the decompression device 2 is not limited to an expander as long as the source gas can be decompressed to a desired pressure, and other known devices (for example, expansion valves) may be used.
- the heater 8 various known heat sources can be used as long as the temperature of the source gas can be raised to a desired temperature.
- the acid gas removal device 3 is composed of an absorption tower that removes the acid gas contained in the raw material gas based on the chemical absorption method.
- the acid gas removal device 3 further includes a regeneration tower that regenerates the absorption liquid used in the absorption tower. (Not shown) is attached.
- the absorption tower is a plate tower in which shelves are provided at regular intervals inside the tower and absorbs acid gas components (such as carbon dioxide) by bringing the absorption liquid into countercurrent contact with the supplied raw material gas. Absorb in liquid.
- an alkanolamine aqueous solution can be used, for example, monoethanolamine, diethanolamine, triethanolamine, methyldiethanolamine, diisopropanolamine, diglycolamine, 2-amino-2-methyl-1-propanol, and the like.
- the regeneration tower treats the absorption liquid at a predetermined pressure (here, 1 to 2 barA) and temperature (here, 130 ° C to 140 ° C) and absorbs the regenerated absorption liquid by separating the acid gas component from the absorption liquid. Circulate to the tower.
- the raw material gas from which the acidic gas component has been removed in the acidic gas removing device 3 is sent to the moisture removing device 4.
- the moisture removing device 4 is composed of a dehydrating tower filled with a moisture absorbent (here, molecular sieve) that physically adsorbs moisture.
- a moisture absorbent here, molecular sieve
- the water content in the raw material gas is preferably dehydrated so that the water content is preferably less than 0.1 ppmv (parts per million by volume).
- the moisture removing device 4 other known devices (or configurations) can be adopted as long as moisture in the raw material gas can be removed to a desired ratio or less.
- the raw material gas from which moisture has been removed by the moisture removing device 4 is sent to the heavy component removing device 5.
- the heavy component removing device 5 is composed of a rectifying column having a plurality of shelves inside, and removes a heavy component having a relatively high freezing point contained in the raw material gas (that is, each component constituting the heavy component is removed). Reduce to below desired concentration).
- a liquid containing a relatively high concentration of heavy components is discharged from the bottom of the column.
- a raw material gas (light component) mainly composed of methane, which is a low boiling point component is separated as a column top distillate. The separated source gas is cooled (precooled) by heat exchange with the refrigerant in the refrigerant evaporator 16 described in detail later, and then introduced into the liquefying device 6.
- the liquefying device 6 is a main heat exchanger that liquefies the raw material gas from which unnecessary components such as acid gas and heavy components are removed as described above by heat exchange with the mixed refrigerant.
- the liquefying device 6 is composed of a spool-type heat exchanger in which a heat transfer tube (tube bundle) for flowing a raw material gas and a mixed refrigerant is wound in a coil shape and is housed in a shell.
- a heat transfer tube tube bundle
- a mixed refrigerant is wound in a coil shape and is housed in a shell.
- plate fin heat exchange can be used as long as at least the liquefaction treatment of the source gas is possible.
- the low temperature (about ⁇ 162 ° C.) source gas (LNG) liquefied by the liquefying device 6 is sent to an LNG storage facility (not shown) and stored.
- a mixed refrigerant for cooling the raw material gas is a mixture of hydrocarbons containing methane, ethane and propane with nitrogen added, but is not limited to this and ensures a desired cooling capacity.
- a refrigerant composed of other known components may be employed.
- the liquefying device 6 is provided with equipment (such as a compressor and a condenser) for realizing a known refrigerant cycle (refrigeration cycle) for the mixed refrigerant.
- the precooling system 7 includes a compressor 11 that compresses the precooling refrigerant, a condenser 12 that condenses the precooling refrigerant, a subcooler 13 that supercools the precooling refrigerant, and heat exchange between the precooling refrigerant and the source gas.
- a cooling device (first heat exchanger) 14 that cools by a refrigerant, an expansion valve 15 that squeezes and expands the refrigerant, and an evaporator (second heat exchanger) 16 that cools the raw material gas by heat exchange with the raw material gas.
- a refrigerant cycle for precooling the raw material gas liquefied by the liquefying device 6 is realized.
- propane is used as the precooling refrigerant.
- the present invention is not limited to this, and other known components may be employed.
- the compressor 11 is a centrifugal compressor that compresses the mixed refrigerant after the raw material gas is cooled in the evaporator 16.
- the flow rate of the mixed refrigerant introduced into the compressor 11 (that is, used in the refrigerant cycle) is about 800,000 kg / hr
- the temperature and pressure of the refrigerant compressed by the compressor 11 are about 70 ° C. and about 30 barA. It is.
- the precooling refrigerant compressed by the compressor 11 is condensed in the condenser 12 and further subcooled to about 30 ° C. by air or water in the subcooler 13. Thereafter, the precooling refrigerant is sent from the subcooler 13 to the cooler 14, and heat exchange with the raw material gas is performed in the cooler 14.
- the heat exchange in the cooler 14 cools the precooling refrigerant to about ⁇ 10 ° C., while the raw material gas is heated to about 25 ° C. by the heat from the precooling refrigerant.
- the precooling refrigerant is sent from the cooler 14 to the expansion valve 15, and becomes a low-temperature and low-pressure state (temperature is about ⁇ 50 ° C., pressure is about 3.5 barA) due to the expansion of the expansion valve 15. Further, the precooling refrigerant is sent from the expansion valve 15 to the evaporator 16, and heat exchange with the raw material gas is performed in the evaporator 16. The heat exchange in the evaporator 16 evaporates the precooling refrigerant to about 10 ° C. due to heat from the source gas, while the source gas is cooled to about ⁇ 40 ° C. The precooling refrigerant from the evaporator 16 is circulated by being sent to the compressor 11 again.
- the decompression device 2 since the low-temperature source gas decompressed by the decompression device 2 is heated by heat exchange with the precooling refrigerant in the cooler 14, it is necessary to add energy from the outside. Without (or while suppressing), it is possible to raise the temperature of the decompressed raw material gas when removing the acidic gas component.
- the cold heat of the natural gas whose pressure is reduced on the upstream side is used for cooling the precooling refrigerant for cooling the raw material gas on the downstream side (here, after removing the heavy component).
- the load of 11 can be reduced and the energy efficiency in the refrigerant cycle can be increased.
- the sub-cooler 13 can be omitted.
- the processing amount of natural gas in the liquefaction system 1 (that is, the production amount of LNG) can be increased.
- the heater 8 can be downsized, and in some cases, the heater 8 can be omitted.
- the raw material supplied to the acidic gas removal device 3 is obtained even when the temperature rise of the raw material gas in the cooler 14 is not sufficient by using both the temperature rise by heat exchange with the precooling refrigerant and the heating by the heater 8. There is an advantage that the gas temperature can be reliably controlled within an appropriate range by heating the heater 8.
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Abstract
Description
2 減圧装置
3 酸性ガス除去装置
5 重質分除去装置
6 液化装置
7 予冷システム
8 ヒータ(加熱装置)
11 コンプレッサ(圧縮機)
14 冷却器(第1熱交換器)
15 膨張弁
16 蒸発器(第2熱交換器)
Claims (5)
- 天然ガスを含む原料ガスを冷却して液化天然ガスを生成する天然ガスの液化システムであって、
前記原料ガスの圧力を低下させる減圧装置と、
前記減圧装置によって減圧された後の前記原料ガスを冷媒との熱交換によって加熱する第1熱交換器と、
前記第1熱交換器によって加熱された後の前記原料ガスから酸性ガス成分を除去する酸性ガス除去装置と、
前記酸性ガス除去装置によって前記酸性ガス成分が除去された後の前記原料ガスを、温度を低下させた前記冷媒との熱交換によって冷却する第2熱交換器と、
前記第2熱交換器によって冷却された後の前記原料ガスを冷却することにより、液化天然ガスを生成する液化装置と
を備えたことを特徴とする天然ガスの液化システム。 - 前記第1熱交換器から前記酸性ガス除去装置に供給される前記原料ガスを加熱する加熱装置を更に備えたことを特徴とする請求項1に記載の天然ガスの液化システム。
- 前記酸性ガス除去装置と第2熱交換器との間に設けられ、前記原料ガス中の重質炭化水素を除去する重質分除去装置を更に備えたことを特徴とする請求項1または請求項2に記載の天然ガスの液化システム。
- 前記第1熱交換器および前記第2熱交換器は、前記液化装置に供給される前記原料ガスを予冷する予冷用の冷媒サイクルを構成し、
前記第2熱交換器で用いられた前記冷媒を圧縮する圧縮機と、
前記冷媒サイクルにおいて、前記第1熱交換器および前記第2熱交換器の間に設けられ、前記冷媒を絞り膨張させる膨張弁と
を更に備えたことを特徴とする請求項1から請求項3のいずれかに記載の天然ガスの液化システム。 - 天然ガスを含む原料ガスを冷却して液化天然ガスを生成する天然ガスの液化方法であって、
前記原料ガスの圧力を低下させる減圧工程と、
前記減圧工程によって減圧された後の前記原料ガスを冷媒との熱交換によって加熱する第1熱交換工程と、
前記第1熱交換工程によって加熱された後の前記原料ガスから酸性ガス成分を除去する酸性ガス除去工程と、
前記酸性ガス除去工程によって前記酸性ガス成分が除去された後の前記原料ガスを、温度を低下させた前記冷媒との熱交換によって冷却する第2熱交換工程と、
前記第2熱交換工程によって冷却された後の前記原料ガスを冷却することにより、液化天然ガスを生成する液化工程と
を有することを特徴とする天然ガスの液化方法。
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GB1716299.1A GB2553705B (en) | 2015-03-04 | 2015-03-04 | Natural gas liquefaction system and method |
RU2017133520A RU2677023C1 (ru) | 2015-03-04 | 2015-03-04 | Способ и система сжижения природного газа |
PCT/JP2015/001138 WO2016139702A1 (ja) | 2015-03-04 | 2015-03-04 | 天然ガスの液化システム及び液化方法 |
AU2015385052A AU2015385052B2 (en) | 2015-03-04 | 2015-03-04 | Natural gas liquefaction system and method |
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Cited By (2)
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CN109628181A (zh) * | 2018-11-22 | 2019-04-16 | 天津市振津石油天然气工程有限公司 | 一种撬装天然气液化装置的新型布置结构 |
RU2823002C1 (ru) * | 2023-12-27 | 2024-07-17 | Общество с ограниченной ответственностью научно-исследовательский и проектный институт "ПЕГАЗ" | Комплекс сжижения природного газа |
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2015
- 2015-03-04 WO PCT/JP2015/001138 patent/WO2016139702A1/ja active Application Filing
- 2015-03-04 AU AU2015385052A patent/AU2015385052B2/en active Active
- 2015-03-04 RU RU2017133520A patent/RU2677023C1/ru active
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US3503220A (en) * | 1967-07-27 | 1970-03-31 | Chicago Bridge & Iron Co | Expander cycle for natural gas liquefication with split feed stream |
US4012212A (en) * | 1975-07-07 | 1977-03-15 | The Lummus Company | Process and apparatus for liquefying natural gas |
JP2010532796A (ja) * | 2007-07-09 | 2010-10-14 | エルエヌジー テクノロジー ピーティーワイ リミテッド | 液化天然ガスの生成方法およびシステム |
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CN109628181A (zh) * | 2018-11-22 | 2019-04-16 | 天津市振津石油天然气工程有限公司 | 一种撬装天然气液化装置的新型布置结构 |
RU2823002C1 (ru) * | 2023-12-27 | 2024-07-17 | Общество с ограниченной ответственностью научно-исследовательский и проектный институт "ПЕГАЗ" | Комплекс сжижения природного газа |
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GB2553705B (en) | 2021-01-06 |
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AU2015385052A1 (en) | 2017-10-05 |
AU2015385052B2 (en) | 2018-11-08 |
GB201716299D0 (en) | 2017-11-22 |
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