US20110146341A1 - Gas supply system for gas engines - Google Patents
Gas supply system for gas engines Download PDFInfo
- Publication number
- US20110146341A1 US20110146341A1 US12/991,098 US99109809A US2011146341A1 US 20110146341 A1 US20110146341 A1 US 20110146341A1 US 99109809 A US99109809 A US 99109809A US 2011146341 A1 US2011146341 A1 US 2011146341A1
- Authority
- US
- United States
- Prior art keywords
- gas
- supply system
- gas supply
- pump
- heat exchanger
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- 239000007789 gas Substances 0.000 claims abstract description 59
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 45
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 22
- 238000010438 heat treatment Methods 0.000 claims abstract description 17
- 239000000446 fuel Substances 0.000 claims abstract description 7
- 230000010354 integration Effects 0.000 claims abstract description 5
- 238000000605 extraction Methods 0.000 claims abstract description 4
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 3
- 239000000284 extract Substances 0.000 claims abstract 2
- 239000012267 brine Substances 0.000 claims description 17
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 238000011144 upstream manufacturing Methods 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 6
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 4
- 239000004215 Carbon black (E152) Substances 0.000 claims description 2
- 229930195733 hydrocarbon Natural products 0.000 claims description 2
- 150000002430 hydrocarbons Chemical class 0.000 claims description 2
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 2
- 239000007788 liquid Substances 0.000 claims description 2
- 239000003507 refrigerant Substances 0.000 claims description 2
- 238000000034 method Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 239000006200 vaporizer Substances 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 3
- 229910000746 Structural steel Inorganic materials 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000004172 nitrogen cycle Methods 0.000 description 1
- 230000010349 pulsation Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
- F02M21/00—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form
- F02M21/02—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
- F02M21/06—Apparatus for de-liquefying, e.g. by heating
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02D—CONTROLLING COMBUSTION ENGINES
- F02D19/00—Controlling engines characterised by their use of non-liquid fuels, pluralities of fuels, or non-fuel substances added to the combustible mixtures
- F02D19/06—Controlling engines characterised by their use of non-liquid fuels, pluralities of fuels, or non-fuel substances added to the combustible mixtures peculiar to engines working with pluralities of fuels, e.g. alternatively with light and heavy fuel oil, other than engines indifferent to the fuel consumed
- F02D19/0639—Controlling engines characterised by their use of non-liquid fuels, pluralities of fuels, or non-fuel substances added to the combustible mixtures peculiar to engines working with pluralities of fuels, e.g. alternatively with light and heavy fuel oil, other than engines indifferent to the fuel consumed characterised by the type of fuels
- F02D19/0642—Controlling engines characterised by their use of non-liquid fuels, pluralities of fuels, or non-fuel substances added to the combustible mixtures peculiar to engines working with pluralities of fuels, e.g. alternatively with light and heavy fuel oil, other than engines indifferent to the fuel consumed characterised by the type of fuels at least one fuel being gaseous, the other fuels being gaseous or liquid at standard conditions
- F02D19/0647—Controlling engines characterised by their use of non-liquid fuels, pluralities of fuels, or non-fuel substances added to the combustible mixtures peculiar to engines working with pluralities of fuels, e.g. alternatively with light and heavy fuel oil, other than engines indifferent to the fuel consumed characterised by the type of fuels at least one fuel being gaseous, the other fuels being gaseous or liquid at standard conditions the gaseous fuel being liquefied petroleum gas [LPG], liquefied natural gas [LNG], compressed natural gas [CNG] or dimethyl ether [DME]
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
- F02M21/00—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form
- F02M21/02—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
- F02M21/0203—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels characterised by the type of gaseous fuel
- F02M21/0215—Mixtures of gaseous fuels; Natural gas; Biogas; Mine gas; Landfill gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
- F02M21/00—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form
- F02M21/02—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
- F02M21/0218—Details on the gaseous fuel supply system, e.g. tanks, valves, pipes, pumps, rails, injectors or mixers
- F02M21/0227—Means to treat or clean gaseous fuels or fuel systems, e.g. removal of tar, cracking, reforming or enriching
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
- F02M21/00—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form
- F02M21/02—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
- F02M21/0218—Details on the gaseous fuel supply system, e.g. tanks, valves, pipes, pumps, rails, injectors or mixers
- F02M21/029—Arrangement on engines or vehicle bodies; Conversion to gaseous fuel supply systems
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
- F25J1/0025—Boil-off gases "BOG" from storages
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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
- F25J1/003—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
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/007—Primary atmospheric gases, mixtures thereof
- F25J1/0072—Nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—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
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0235—Heat exchange integration
- F25J1/0242—Waste heat recovery, e.g. from heat of compression
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
- F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
- F25J1/0264—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams
- F25J1/0265—Arrangement of heat exchanger cores in parallel with different functions, e.g. different cooling streams comprising cores associated exclusively with the cooling of a refrigerant stream, e.g. for auto-refrigeration or economizer
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
- F25J1/0277—Offshore use, e.g. during shipping
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
- F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2265/00—Effects achieved by gas storage or gas handling
- F17C2265/03—Treating the boil-off
- F17C2265/032—Treating the boil-off by recovery
- F17C2265/037—Treating the boil-off by recovery with pressurising
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C2265/00—Effects achieved by gas storage or gas handling
- F17C2265/06—Fluid distribution
- F17C2265/066—Fluid distribution for feeding engines for propulsion
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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
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
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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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- 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
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
- F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
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- 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
- F25J2230/30—Compression 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T10/00—Road transport of goods or passengers
- Y02T10/10—Internal combustion engine [ICE] based vehicles
- Y02T10/30—Use of alternative fuels, e.g. biofuels
Definitions
- the present invention relates to a gas supply system for engines such as dual-fuel or gas engines for vessels transporting liquefied gas as liquefied nature gas (LNG).
- LNG liquefied nature gas
- LNG-vessels have traditionally used steam-turbine propulsion but are now changing to slow speed-diesel, dual-fuel or gas propulsion machinery.
- the new concept covers primarily a “stand alone” evaporator (evaporator) provided with an intermediate closed loop and in addition an integration of an evaporator (optimizer) into the BOG reliquefaction plant in order to utilize the cold duty in vaporized LNG to be feed into the engines for propulsion of the vessel. Utilization of the cold duty in the LNG will result in a reduction of the overall power consumption. If the BOG reliquefaction plant is stopped, the stand alone evaporator will feed the gas engines.
- Condensate from the BOG reliquefaction plant or LNG from the cargo tanks being supplied with the cargo pumps is sent to at least one high pressure (HP) pump for feeding the evaporator.
- the LNG normally above the supercritical pressure is heated to “gas” in a heat exchanger.
- This heat exchanger is referred to as an evaporator or vaporizer, respectively; see e.g. FIGS. 1 and 2 .
- the high pressure gas is delivered to the propulsion engines or gas turbines, not shown in the drawings.
- the discharge pressure of the high pressure pump is typically be up to 30 MPa (300 bar) at design case.
- the LNG temperature is typically from ⁇ 140 to ⁇ 150° C. LNG at high pressure is supercritical and it is not possible to distinguish between liquid and gas phase. Nevertheless, the heating of LNG to ambient temperature at high pressure is referred to as evaporation in this document.
- the discharge pressure of the high pressure pump is typically 30 MPa (300 bar) at design case.
- the LNG temperature is typically from ⁇ 140 to ⁇ 150° C.
- the system is based on an evaporation of LNG at high pressure with a heating source.
- a closed loop with intermediate medium is used to heat the LNG.
- the intermediate media could be a brine mixture, glycol mixture, hydrocarbon mixture or a refrigerant and is hereinafter referred to as “brine”.
- the closed loop comprises a LNG-vaporizer, i.e. the evaporator, a brine pump, and a heating source being denoted steam/hot water steamer in the drawings. This prevents the danger of getting LNG to machine room in case of internal leakage in the vaporizer. Another main reason for using an intermediate loop is that this is a more safe system due to the possibility of freezing.
- the evaporator and its closed loop including can be installed in the Cargo Compressor Room (CCR) together with the BOG reliquefaction plant, in a separate location or in the engine room.
- CCR Cargo Compressor Room
- LNG at typically ⁇ 160° C. and approximately 2-5 bar is pressurized in a cryogenic reciprocating pump (HP pump) to typically 300 bar.
- the LNG is then evaporated and heated to typically +45° C. in a heat exchanger, i.e. the evaporator. If required a pulsation damper will be installed at the outlet of the pump and/or the evaporator, not illustrated in the drawings.
- a typically configurations are two HP pump in parallel, each with 1 ⁇ 100% capacity, one in operation and one stand by, or 3 ⁇ 50%, two in operation and one in stand by.
- LNG is heated with the brine.
- the brine is heated with hot water from the engine (jacket water), steam, e.g. machinery room, cooling water from process equipment in a steam/hot water heater.
- steam e.g. machinery room
- cooling water from process equipment in a steam/hot water heater.
- intermediate media sea water can also be a heating source.
- the brine enters the evaporator at typically 90° C. and leaves at typically 30° C. If the heating agent is jacket water, the brine enters the heat exchanger at typically 75° C. and leaves at atypically 30° C. If cooling water from the process equipments is used, the temperature level is lower.
- the intermediate flow (brine) is pumped to a heat exchanger for heating to typically 90° C., alternatively 75° C.
- This heat exchanger where the brine is heated is the heat source referred to as “steam/hot water, heater” in the drawings.
- Steam can be used as heating source for the evaporator and saturated steam is assumed. Steam condition depends on what is available on the LNG vessel. In the closed loop steam is condensing and sub-cooled in the heater for brine before it is returned to the boilers condensate/feed water tank.
- a gas supply system for dual-fuel or gas engines adapted for integration with a boil-off gas reliquefaction plant comprising a cryogenic heat exchanger, a boil-off gas compressor having a boil-off gas preheater, and a nitrogen loop with a compander, the gas being in the form of liquefied natural gas from cargo tanks or condensate from the reliquefaction plant.
- the system For utilizing in the reliquefation plant cold duty from gas to be combusted by the engines the system is provided with an evaporator (optimizer) extracting the cold duty and/or an evaporator being arranged in a closed loop comprising of at least one pump and a heating source for an intermediate medium used to optimize the cold duty extraction.
- evaporator optically extracting the cold duty and/or an evaporator being arranged in a closed loop comprising of at least one pump and a heating source for an intermediate medium used to optimize the cold duty extraction.
- the evaporator (optimizer) is used to optimize the cold duty extraction.
- the preheater can be replaced or supplemented by a precooler.
- the compander is understood to be a unit having compressor/expander unit, for instance.
- FIG. 1 shows a process description for a LNG reliquefation plant including a gas supply system for dual-fuel or gas engines, the gas supply system not being connected to the reliquefation plant;
- FIG. 2 illustrates the gas supply system in FIG. 1 ;
- FIGS. 3 to 5 depict embodiments according to the present invention in which cold duty extracted in an evaporator (optimizer) is transferred into the reliquefation plant upstream a cryogenic heat exchanger, in parallel with a BOG preheater, or in parallel with the cryogenic heat exchanger, respectively; and
- FIG. 6 shows an embodiment minimizing the use of an external heating source for the HP LNG.
- cold duty in a LNG evaporator is removed from the LNG during heating and evaporization thereof and is utilized in a BOG reliquefaction plant in order to reduce the overall power consumption.
- the cold duty is taken out in the LNG evaporator (optimizer) and put into the BOG reliquefaction plant.
- the most efficient solution would have been to add an extra pass in a cryogenic heat exchanger, i.e. the cold box. Since the maximum design pressure for the state of the art cold boxes is limited, this solution is not cost efficient today. If BOG or nitrogen is precooled with LNG, less production of cooling duty for liquefying the BOG is required. This means that the compressor work will be reduced for operational modes where the optimizer is in operation.
- the cold duty can be transferred into the BOG cycle upstream the cold box, in parallel with the cold box or integrated with the cold box or into the nitrogen cycle upstream or down stream the cold box, in parallel with the cold box or integrated with the cold box.
- the closed intermediate loop illustrated in FIG. 2 is hereinafter referred to as a “brine loop” and the LNG is evaporating in the “LNG evaporizer”.
- the heat exchanger integrated with the BOG reliquefaction plant is referred to as an “optimizer”. Typical solutions are shown in process flow diagrams; see FIGS. 3 to 5 but the energy integrations are not limited to these figures.
- the LNG vaporizer and optimizer can be installed in parallel as shown in FIG. 3 , or in series.
- FIG. 3 shows a process flow diagram where the BOG is precooled upstream the cold box.
- the LNG is vaporizing while the BOG is precooled.
- An alternative solution is to utilize the cold duty in parallel or integrated in the cold box on the BOG side.
- the Boil-off gas is compressed in the BOG compressor and cooled in an aftercooler to ambient condition.
- the boil-off gas is further cooled upstream or in parallel with the cold box by heat exchanging with the compressed LNG.
- the compressed LNG is at cryogenic condition (typically ⁇ 140 to 160 C) and is heated up by the boil-off gas.
- the available cold duty in the LNG will therefore be utilized in the nitrogen loop. Utilizing of the cold duty results in reduced power consumption for the compander.
- the separator in the figures will operate as a suction drum for the pump. If required, a low pressure pump (LP pump) will be installed upstream the high pressure pump (HP-pump) in order to secure sufficient net positive suction head (NPSH) for the HP pump.
- the LP pump will function as a booster pump to the HP pump.
- the fuel gas system can be fed with both liquefied boil-off gas from the reliquefaction system and LNG from the cargo tanks.
- FIG. 4 illustrates a process flow diagram where the optimizer is installed in parallel to the BOG preheater.
- nitrogen at ambient condition is precooled while the LNG is evaporizing in the optimizer.
- Precooled nitrogen is mixed with the nitrogen flow from the BOG preheater, sent into the cold box and mixed with nitrogen cooled in the cold box.
- the nitrogen is further cooled in the cold box before it is expanded to almost compressor suction pressure in the expander.
- the precooled nitrogen can also be introduced into the cold box in a separate connection, precooled further in the cold box and expanded in the expander. Precooling of nitrogen by using high-pressure LNG will result in reduced power consumption for the system.
- FIG. 5 discloses a process flow diagram where the optimizer is in parallel with the cold box. This means that part of the nitrogen at ambient condition is cooled in heat exchanging with LNG in the optimizer. The nitrogen stream is cooled to the inlet expander temperature and mixed with the nitrogen from the cold box. The nitrogen is further expanded to almost compressor suction pressure in the expander.
- warm nitrogen gas can be taken from one of the compressor stages upstream intercoolers or aftercooler. Then, warm nitrogen from the compressor stages is to be mixed with nitrogen from the after-cooler before entering the optimizer.
- nitrogen upstream one of the compressor stage coolers can be sent to a separate heat exchanger after the optimizer. The chilled nitrogen is returned downstream the cooler/heat exchanger unit where the Nitrogen is fetched.
- the embodiment in FIG. 6 is minimizing the use of external heat in the steam/hot water heater as to reduce costs. If the heat gained from the nitrogen is insufficiently, more heat could be extracted ahead of the coolers. A typical situation exists when little BOG is available and the ship is using large quantities of fuel. During such conditions the reliquefaction system will operate at low capacity, while the fuel gas system being at its full capacity.
- the optimizer can only be in operation when the BOG reliquefaction plant is working. If the reliquefaction plant is stopped, the stand alone evaporator will feed the gas engine without extracting any of the cold duty from the LNG passing theretrough. This means that the cold duty extracted by heating up the LNG is sent to the heating source (steam or hot water)
- the gas supply system will typically be installed on a skid to simplify the installation. All components are assembled on a structural steel skid with all required interconnecting piping, valves, instruments and wiring.
- a typical number of components for one skid are:
- control modules valves, structural steel and interconnecting piping, if required, additional equipment is LP-pumps and a suction drum.
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Abstract
A gas supply system for dual-fuel or gas engines is adapted for integration with a boil-off gas reliquefaction plant. The system includes a cryogenic heat exchanger, a boil-off gas compressor having a boil-off gas preheater, and a nitrogen loop with a compander. The gas is in the form of liquefied natural gas from cargo tanks or condensate from the reliquefaction plant. The gas supply system also includes an evaporator (optimizer) that extracts cold duty from the gas, and/or an evaporator that is arranged in a closed loop, which includes at least one pump and a heating source for an intermediate medium used to optimize extraction of the cold duty.
Description
- The present invention relates to a gas supply system for engines such as dual-fuel or gas engines for vessels transporting liquefied gas as liquefied nature gas (LNG).
- LNG-vessels have traditionally used steam-turbine propulsion but are now changing to slow speed-diesel, dual-fuel or gas propulsion machinery.
- In the following a gas supply system being integrated with a boil-off gas (BOG) reliquefaction system is to be discussed. The new concept covers primarily a “stand alone” evaporator (evaporator) provided with an intermediate closed loop and in addition an integration of an evaporator (optimizer) into the BOG reliquefaction plant in order to utilize the cold duty in vaporized LNG to be feed into the engines for propulsion of the vessel. Utilization of the cold duty in the LNG will result in a reduction of the overall power consumption. If the BOG reliquefaction plant is stopped, the stand alone evaporator will feed the gas engines.
- Condensate from the BOG reliquefaction plant or LNG from the cargo tanks being supplied with the cargo pumps is sent to at least one high pressure (HP) pump for feeding the evaporator. The LNG normally above the supercritical pressure is heated to “gas” in a heat exchanger. This heat exchanger is referred to as an evaporator or vaporizer, respectively; see e.g.
FIGS. 1 and 2 . Thereafter, the high pressure gas is delivered to the propulsion engines or gas turbines, not shown in the drawings. - The discharge pressure of the high pressure pump is typically be up to 30 MPa (300 bar) at design case. The LNG temperature is typically from −140 to −150° C. LNG at high pressure is supercritical and it is not possible to distinguish between liquid and gas phase. Nevertheless, the heating of LNG to ambient temperature at high pressure is referred to as evaporation in this document.
- The discharge pressure of the high pressure pump is typically 30 MPa (300 bar) at design case. The LNG temperature is typically from −140 to −150° C.
- The system is based on an evaporation of LNG at high pressure with a heating source. In order not to use jacket water or steam from machine room directly in a heat exchanger with LNG, i.e. the present evaporator, a closed loop with intermediate medium is used to heat the LNG. The intermediate media could be a brine mixture, glycol mixture, hydrocarbon mixture or a refrigerant and is hereinafter referred to as “brine”. As illustrated in
FIG. 2 , the closed loop comprises a LNG-vaporizer, i.e. the evaporator, a brine pump, and a heating source being denoted steam/hot water steamer in the drawings. This prevents the danger of getting LNG to machine room in case of internal leakage in the vaporizer. Another main reason for using an intermediate loop is that this is a more safe system due to the possibility of freezing. - The evaporator and its closed loop including can be installed in the Cargo Compressor Room (CCR) together with the BOG reliquefaction plant, in a separate location or in the engine room.
- LNG at typically −160° C. and approximately 2-5 bar is pressurized in a cryogenic reciprocating pump (HP pump) to typically 300 bar. The LNG is then evaporated and heated to typically +45° C. in a heat exchanger, i.e. the evaporator. If required a pulsation damper will be installed at the outlet of the pump and/or the evaporator, not illustrated in the drawings.
- A typically configurations are two HP pump in parallel, each with 1×100% capacity, one in operation and one stand by, or 3×50%, two in operation and one in stand by.
- In the evaporator LNG is heated with the brine. The brine is heated with hot water from the engine (jacket water), steam, e.g. machinery room, cooling water from process equipment in a steam/hot water heater. Depending on the intermediate media sea water can also be a heating source.
- If the heating agent is steam, the brine enters the evaporator at typically 90° C. and leaves at typically 30° C. If the heating agent is jacket water, the brine enters the heat exchanger at typically 75° C. and leaves at atypically 30° C. If cooling water from the process equipments is used, the temperature level is lower.
- After the evaporator the intermediate flow (brine) is pumped to a heat exchanger for heating to typically 90° C., alternatively 75° C. This heat exchanger where the brine is heated is the heat source referred to as “steam/hot water, heater” in the drawings.
- There will typically be two brine pumps in parallel, each with 1×100% capacity, one in operation and one stand by.
- Steam can be used as heating source for the evaporator and saturated steam is assumed. Steam condition depends on what is available on the LNG vessel. In the closed loop steam is condensing and sub-cooled in the heater for brine before it is returned to the boilers condensate/feed water tank.
- As mentioned above, the main object of the present invention reduced overall power consumption. This object is achieved by a gas supply system for dual-fuel or gas engines adapted for integration with a boil-off gas reliquefaction plant comprising a cryogenic heat exchanger, a boil-off gas compressor having a boil-off gas preheater, and a nitrogen loop with a compander, the gas being in the form of liquefied natural gas from cargo tanks or condensate from the reliquefaction plant. For utilizing in the reliquefation plant cold duty from gas to be combusted by the engines the system is provided with an evaporator (optimizer) extracting the cold duty and/or an evaporator being arranged in a closed loop comprising of at least one pump and a heating source for an intermediate medium used to optimize the cold duty extraction.
- Thus, the evaporator (optimizer) is used to optimize the cold duty extraction. Although specifying a boil-off gas compressor having a preheater, the preheater can be replaced or supplemented by a precooler. The compander is understood to be a unit having compressor/expander unit, for instance.
- If not already indicated above, favourable embodiments according to the present invention are understood from the dependent claims below.
- The present invention is now to be discussed in more detail with reference to preferred embodiments illustrated in the drawings, in which:
-
FIG. 1 shows a process description for a LNG reliquefation plant including a gas supply system for dual-fuel or gas engines, the gas supply system not being connected to the reliquefation plant; -
FIG. 2 illustrates the gas supply system inFIG. 1 ; -
FIGS. 3 to 5 depict embodiments according to the present invention in which cold duty extracted in an evaporator (optimizer) is transferred into the reliquefation plant upstream a cryogenic heat exchanger, in parallel with a BOG preheater, or in parallel with the cryogenic heat exchanger, respectively; and -
FIG. 6 shows an embodiment minimizing the use of an external heating source for the HP LNG. - According to the present invention represented by
FIGS. 3 to 5 cold duty in a LNG evaporator is removed from the LNG during heating and evaporization thereof and is utilized in a BOG reliquefaction plant in order to reduce the overall power consumption. In other words the cold duty is taken out in the LNG evaporator (optimizer) and put into the BOG reliquefaction plant. The most efficient solution would have been to add an extra pass in a cryogenic heat exchanger, i.e. the cold box. Since the maximum design pressure for the state of the art cold boxes is limited, this solution is not cost efficient today. If BOG or nitrogen is precooled with LNG, less production of cooling duty for liquefying the BOG is required. This means that the compressor work will be reduced for operational modes where the optimizer is in operation. - The cold duty can be transferred into the BOG cycle upstream the cold box, in parallel with the cold box or integrated with the cold box or into the nitrogen cycle upstream or down stream the cold box, in parallel with the cold box or integrated with the cold box. The closed intermediate loop illustrated in
FIG. 2 is hereinafter referred to as a “brine loop” and the LNG is evaporating in the “LNG evaporizer”. The heat exchanger integrated with the BOG reliquefaction plant is referred to as an “optimizer”. Typical solutions are shown in process flow diagrams; seeFIGS. 3 to 5 but the energy integrations are not limited to these figures. The LNG vaporizer and optimizer can be installed in parallel as shown inFIG. 3 , or in series. -
FIG. 3 shows a process flow diagram where the BOG is precooled upstream the cold box. The LNG is vaporizing while the BOG is precooled. An alternative solution is to utilize the cold duty in parallel or integrated in the cold box on the BOG side. - The Boil-off gas is compressed in the BOG compressor and cooled in an aftercooler to ambient condition. The boil-off gas is further cooled upstream or in parallel with the cold box by heat exchanging with the compressed LNG. The compressed LNG is at cryogenic condition (typically −140 to 160 C) and is heated up by the boil-off gas. The available cold duty in the LNG will therefore be utilized in the nitrogen loop. Utilizing of the cold duty results in reduced power consumption for the compander. The separator in the figures will operate as a suction drum for the pump. If required, a low pressure pump (LP pump) will be installed upstream the high pressure pump (HP-pump) in order to secure sufficient net positive suction head (NPSH) for the HP pump. The LP pump will function as a booster pump to the HP pump. The fuel gas system can be fed with both liquefied boil-off gas from the reliquefaction system and LNG from the cargo tanks.
-
FIG. 4 illustrates a process flow diagram where the optimizer is installed in parallel to the BOG preheater. This means that nitrogen at ambient condition is precooled while the LNG is evaporizing in the optimizer. Precooled nitrogen is mixed with the nitrogen flow from the BOG preheater, sent into the cold box and mixed with nitrogen cooled in the cold box. The nitrogen is further cooled in the cold box before it is expanded to almost compressor suction pressure in the expander. The precooled nitrogen can also be introduced into the cold box in a separate connection, precooled further in the cold box and expanded in the expander. Precooling of nitrogen by using high-pressure LNG will result in reduced power consumption for the system. -
FIG. 5 discloses a process flow diagram where the optimizer is in parallel with the cold box. This means that part of the nitrogen at ambient condition is cooled in heat exchanging with LNG in the optimizer. The nitrogen stream is cooled to the inlet expander temperature and mixed with the nitrogen from the cold box. The nitrogen is further expanded to almost compressor suction pressure in the expander. - As shown in
FIG. 6 , instead of using an external heating source for warming the high pressure LNG to required temperature after the optimizer, warm nitrogen gas can be taken from one of the compressor stages upstream intercoolers or aftercooler. Then, warm nitrogen from the compressor stages is to be mixed with nitrogen from the after-cooler before entering the optimizer. Alternatively, nitrogen upstream one of the compressor stage coolers can be sent to a separate heat exchanger after the optimizer. The chilled nitrogen is returned downstream the cooler/heat exchanger unit where the Nitrogen is fetched. - The embodiment in
FIG. 6 is minimizing the use of external heat in the steam/hot water heater as to reduce costs. If the heat gained from the nitrogen is insufficiently, more heat could be extracted ahead of the coolers. A typical situation exists when little BOG is available and the ship is using large quantities of fuel. During such conditions the reliquefaction system will operate at low capacity, while the fuel gas system being at its full capacity. - As already mentioned above, the optimizer can only be in operation when the BOG reliquefaction plant is working. If the reliquefaction plant is stopped, the stand alone evaporator will feed the gas engine without extracting any of the cold duty from the LNG passing theretrough. This means that the cold duty extracted by heating up the LNG is sent to the heating source (steam or hot water)
- The gas supply system will typically be installed on a skid to simplify the installation. All components are assembled on a structural steel skid with all required interconnecting piping, valves, instruments and wiring.
- A typical number of components for one skid are:
- 2 HP pumps; one in stand by,
1 LNG/brine heat exchanger (evaporator),
1 steam or jacket water/brine heat exchanger (brine heater),
2 brine circulation pumps; one in standby,
1 LNG heat exchanger integrated with the reliquefaction plant (optimizer). - control modules,
valves,
structural steel and interconnecting piping,
if required, additional equipment is LP-pumps and a suction drum.
Claims (11)
1. A gas supply system for dual-fuel or gas engines adapted for integration with a boil-off gas reliquefaction plant comprising:
a cryogenic heat exchanger,
a boil-off gas compressor having a boil-off gas preheater, and
a nitrogen loop with a compander,
wherein the gas is in the form of liquefied natural gas from cargo tanks or condensate from the reliquefaction plant, and wherein the gas supply system further comprises an evaporator (optimizer) that extracts cold duty from the gas, and/or an evaporator that is arranged in a closed loop comprising at least one pump and a heating source for an intermediate medium used to optimize extraction of the cold duty.
2. A gas supply system according to claim 1 , wherein the cold duty is transferred to the reliquefaction plant upstream of the cryogenic heat exchanger.
3. A gas supply system according to claim 1 , wherein the cold duty is transferred to the reliquefaction plant in parallel with the boil-off gas preheater.
4. A gas supply system according to claim 1 , wherein the cold duty is transferred to the reliquefaction plant in parallel with the cryogenic heat exchanger or integrated into the cryogenic heat exchanger.
5. A gas supply system according to claim 1 , wherein the extracted cold duty is transferred to the reliquefaction plant using a heat exchanger arranged in a circuit connecting the optimizer to the reliquefaction plant.
6. A gas supply system according to claim 5 , wherein the liquid gas is fed by means of a low pressure pump and high pressure pump.
7. A gas supply system according to claim 1 , wherein the heating source is steam, hot water or a steamer.
8. A gas supply system according to claim 1 , wherein the intermediate medium circulated in the closed loop by means of pump(s) is a brine mixture, glycol mixture, hydrocarbon mixture or a refrigerant.
9. A gas supply system according to claim 8 , wherein there is at least one additional pump in parallel to said at least one pump.
10. A gas supply system according to claim 1 , wherein the gas is fed into the evaporator by means of at least one high pressure pump.
11. A gas supply system according to claim 9 , wherein there are:
two pumps in parallel, wherein one pump is in operation and one pump is in stand by, or
three pumps in parallel, wherein two pumps are in operation and one pump is in stand by.
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NO20082158A NO330187B1 (en) | 2008-05-08 | 2008-05-08 | Gas supply system for gas engines |
PCT/NO2009/000169 WO2009136793A1 (en) | 2008-05-08 | 2009-04-30 | Gas supply systems for gas engines |
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US (1) | US20110146341A1 (en) |
EP (1) | EP2307694B1 (en) |
JP (1) | JP5429719B2 (en) |
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Also Published As
Publication number | Publication date |
---|---|
CN102084114A (en) | 2011-06-01 |
JP5429719B2 (en) | 2014-02-26 |
EP2307694A1 (en) | 2011-04-13 |
NO20082158L (en) | 2009-11-09 |
AU2009244973B2 (en) | 2013-03-21 |
NO330187B1 (en) | 2011-03-07 |
EP2307694B1 (en) | 2011-11-30 |
ATE535699T1 (en) | 2011-12-15 |
CN102084114B (en) | 2014-08-27 |
ES2378631T3 (en) | 2012-04-16 |
JP2011520081A (en) | 2011-07-14 |
AU2009244973A1 (en) | 2009-11-12 |
KR20110023856A (en) | 2011-03-08 |
KR101257910B1 (en) | 2013-04-24 |
WO2009136793A1 (en) | 2009-11-12 |
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