US20080006053A1 - Natural Gas Liquefaction Process - Google Patents

Natural Gas Liquefaction Process Download PDF

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Publication number
US20080006053A1
US20080006053A1 US10/573,213 US57321304A US2008006053A1 US 20080006053 A1 US20080006053 A1 US 20080006053A1 US 57321304 A US57321304 A US 57321304A US 2008006053 A1 US2008006053 A1 US 2008006053A1
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United States
Prior art keywords
cooling
hydrocarbon
circuit
liquefaction
refrigeration
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Abandoned
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US10/573,213
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English (en)
Inventor
Heinz Bauer
Hubert Franke
Rainer Sapper
Marc Schier
Manfred Bolt
Jostein Pettersen
Arne Olav Fredheim
Pentti Paurola
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Linde GmbH
Equinor ASA
Original Assignee
Linde GmbH
Statoil ASA
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Priority claimed from DE2003144030 external-priority patent/DE10344030A1/de
Application filed by Linde GmbH, Statoil ASA filed Critical Linde GmbH
Assigned to STATOIL ASA reassignment STATOIL ASA ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: FREDHEIM, ARNE OLAV, PETTERSEN, JOSTEIN, PAUROLA, PENTTI
Assigned to LINDE AG reassignment LINDE AG ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BAUER, HEINZ, BOLT, MANFRED, FRANKE, HUBERT, SAPPER, RAINER, SCHIER, MARC
Assigned to LINDE AKTIENGESELLSCHAFT reassignment LINDE AKTIENGESELLSCHAFT CHANGE OF ASSIGNEE ADDRESS Assignors: BAUER, HEINZ, BOLT, MANFRED, FRANKE, HUBERT, SAPPER, RAINER, SCHIER, MARC
Publication of US20080006053A1 publication Critical patent/US20080006053A1/en
Abandoned legal-status Critical Current

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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
    • 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
    • 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
    • F25J1/0095—Oxides of carbon, e.g. CO2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0217—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 at least a three level refrigeration cascade with at least one MCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
    • F25J1/0217—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 at least a three level refrigeration cascade with at least one MCR cycle
    • F25J1/0218—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 at least a three level refrigeration cascade with at least one MCR cycle with one or more SCR cycles, e.g. with a C3 pre-cooling cycle
    • 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
    • F25J1/0278—Unit being stationary, e.g. on floating barge or fixed platform
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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
    • F25J1/02—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.
    • 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.
    • F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
    • F25J1/0283—Gas turbine as the prime mechanical driver
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
    • 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.
    • F25J1/0295—Shifting of the compression load between different cooling stages within a refrigerant cycle or within a cascade refrigeration system
    • 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
    • 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
    • F25J1/0297—Removal of the heat of compression, e.g. within an inter- or afterstage-cooler against an ambient heat sink using an externally chilled fluid, e.g. chilled water
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B1/00—Compression machines, plants or systems with non-reversible cycle
    • F25B1/10—Compression machines, plants or systems with non-reversible cycle with multi-stage compression
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2309/00—Gas cycle refrigeration machines
    • F25B2309/06—Compression machines, plants or systems characterised by the refrigerant being carbon dioxide
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2400/00—General features or devices for refrigeration machines, plants or systems, combined heating and refrigeration systems or heat-pump systems, i.e. not limited to a particular subgroup of F25B
    • F25B2400/13—Economisers
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B5/00—Compression machines, plants or systems, with several evaporator circuits, e.g. for varying refrigerating capacity
    • F25B5/02—Compression machines, plants or systems, with several evaporator circuits, e.g. for varying refrigerating capacity arranged in parallel
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
    • F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
    • F25B9/008—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant being carbon dioxide
    • 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

Definitions

  • the present invention relates to a method for the liquefaction of a hydrocarbon-rich flow.
  • Natural gas can be obtained from the earth to form a natural gas feed which must be processed before it can be used commercially. Normally the gas is first pre-treated to remove or reduce the content of impurities such as carbon dioxide, water, hydrogen sulphide, mercury, etc.
  • the gas is often liquefied before being transported to its point of use to provide liquefied natural gas (LNG).
  • LNG liquefied natural gas
  • natural gas Since natural gas is a mixture of gases, it liquefies over a range of temperatures. At atmospheric pressure, the usual temperature range within which complete liquefaction occurs is ⁇ 165° C. to ⁇ 155° C. However, since the critical temperature of natural gas is about ⁇ 80° C. to ⁇ 90° C., the gas cannot be liquefied purely by compressing it. It is therefore necessary to use refrigeration processes.
  • Natural gas liquefaction plants are either designed as what are known as LNG baseload plants, i.e. plants for the liquefaction of natural gas for the supply of natural gas as primary energy, or as what are known as peak-shaving plants, i.e. plants for the liquefaction of natural gas to cover peak demand.
  • LNG baseload plants are operated as a rule with coolant circuits consisting of a mixture of hydrocarbons. These mixed refrigerant circuits are more efficient in terms of energy than expander circuits and make it possible, with the high liquefaction capacities of the baseload plants, for correspondingly relatively low energy consumptions to be achieved.
  • the Mixed Fluid Cascade process is known, e.g. from the U.S. Pat. No. 6,253,574, and uses three independent refrigeration cycles, which shifts the limit of a real single train concept with proven compressor drivers to above 8 mtpa LNG.
  • the first coolant circuit serves to provide pre-cooling
  • the second coolant circuit serves to provide the liquefaction
  • the third coolant circuit serves to provide the sub-cooling for the hydrocarbon-rich flow or natural gas respectively.
  • hydrocarbons with higher boiling points are at least those components of the hydrocarbon-rich flow or natural gas which would freeze out during the following cooling stage, i.e. C 5 + hydrocarbons and aromates.
  • hydrocarbons meaning in this situation in particular propane and butane, which would undesirably increase the calorific value of the liquefied natural gas are also separated out before the liquefaction stage.
  • C 3 + separation Due to the provision of this separation, designated hereinafter as C 3 + separation, at a given pressure of the raw gas the temperature level of the separation of these components is set within comparatively narrow limits.
  • an LNG liquefaction process having first and second refrigeration circuits wherein the second refrigeration circuit is used at least partially for pre-cooling the hydrocarbon-rich stream to be liquefied.
  • Part of the refrigerant of the liquefaction cycle may be vaporized under elevated pressure in the precooling section of the process and fed to the LC compressor as a side stream. In this way a substantial load balancing between all the refrigeration cycles can be achieved.
  • a method for the liquefaction of a hydrocarbon-rich flow in particular of a natural gas flow, whereby the liquefaction of the hydrocarbon-rich flow is effected against a refrigerant circuit cascade consisting of three refrigeration circuits, whereby the first of the three refrigeration circuits serves to provide preliminary cooling, the second refrigeration circuit serves to provide the actual liquefaction, and the third refrigeration circuit serves the sub-cooling of the liquefied hydrocarbon-rich flow, and whereby each refrigeration circuit comprises at least one single-stage or multi-stage compressor, characterised in that at least one part flow of the refrigerant of the second refrigeration circuit is used for the preliminary cooling of the hydrocarbon-rich flow.
  • the invention provides a method of liquefying a hydrocarbon-rich gas, wherein the gas flows through a cascade of three refrigeration stages, each stage comprising a refrigerant circuit and a compressor, wherein at least part of the flow of refrigerant from the second circuit is used for the preliminary cooling of the hydrocarbon rich gas in the first refrigeration stage.
  • the part flow of the refrigerant of the second refrigeration (or cooling) circuit, used for the pre-cooling of the hydrocarbon-rich flow is evaporated at a pressure which is higher than the evaporation pressure of the remaining part flow of the refrigerant of the second cooling circuit, and is conducted to the-compressor of the second cooling circuit at an intermediate pressure level.
  • the separation of heavier components and/or components of the hydrocarbon-rich flow which freeze out during the liquefaction of the hydrocarbon-rich flow takes place before the actual liquefaction of the hydrocarbon-rich flow.
  • the volumes and/or evaporation pressures of the two part flows of the second cooling circuit are changeable.
  • At least one part flow of one of the two part flows of the second cooling circuit is used for the provision of cooling in the heavy hydrocarbon separation unit.
  • the invention therefore provides a load balanced liquefaction process for LNG in which each compressor may have a substantially equal share of the total load, and preferably an equal share.
  • This concept can be applied more widely and hence from another aspect the present invention provides a method of liquefaction comprising a plurality of cooling circuits arranged in a cascade formation, each circuit comprising a compressor, wherein each compressor has a substantially equal share of the total load.
  • the benefits of load balancing the refrigeration circuits are not limited to any particular type of refrigerant used.
  • mixed refrigerant cascades provide an efficient system and therefore in one preferred embodiment the refrigeration circuits are mixed refrigerant circuits.
  • a method for the liquefaction of a hydrocarbon-rich flow in particular of a natural gas flow, whereby the liquefaction of the hydrocarbon-rich flow is effected against a mixed refrigerant circuit cascade consisting of three refrigeration circuits, whereby the first of the three refrigeration circuits serves to provide preliminary cooling, the second refrigeration circuit serves to provide the actual liquefaction, and the third refrigeration circuit serves the sub-cooling of the liquefied hydrocarbon-rich flow, and whereby each refrigeration circuit comprises at least one single-stage or multi-stage compressor, characterised in that at least one part flow of the refrigerant of the second refrigeration circuit is used for the preliminary cooling of the hydrocarbon-rich flow.
  • LNG FPSOs Floating LNG production, storage and offloading facilities
  • carbon dioxide Another non-flammable and inert refrigerant option is carbon dioxide, which may operate in a vapour compression cycle giving reasonable efficiency. Carbon dioxide has a freezing point of ⁇ 56.6° C., which restricts the minimum possible evaporating temperature due to the risk of dry ice formation. Therefore carbon dioxide is an option for the precooling process only. Since most of the hydrocarbon refrigerant inventory is in the precooling cycle, a change over to CO 2 may still improve the safety of the liquefaction process significantly.
  • carbon dioxide is also distinguished from the common hydrocarbon refrigerants for natural gas precooling by its rather low critical temperature (31.1° C.), which is comparable to that of ethane (32.3° C.).
  • WO 01/69149 discloses the possibility of providing a carbon dioxide precooling circuit in a cascade arrangement with a main cooling circuit.
  • the low critical temperature of CO 2 is a disadvantage since the throttling loss and heat rejection loss in the refrigerating cycle will be larger than for C 3 and C 3 /C 2 mixtures. In addition, the heat transfer loss will be larger than with mixed refrigerant due to constant-temperature evaporation.
  • the first refrigeration circuit comprises carbon dioxide.
  • the carbon dioxide circuit can be operated to provide a higher minimum evaporation temperature and thus the risk of dry ice formation is reduced.
  • the load of the carbon dioxide cycle is reduced the impact of the lower thermodynamic efficiency of CO 2 compared with C 2 /C 3 is alleviated.
  • the increase in power consumption caused by using CO 2 can be reduced to only a few percent greater than when using hydrocarbons.
  • the carbon dioxide is cooled after condensation to a temperature of 20° C. or less, more preferably to 15° C. or less. This can be achieved using air cooling although preferably cold cooling water is used.
  • the water is preferably sea water, preferably extracted from a depth suitable to give the required low temperature.
  • the carbon dioxide pre-cooling cycle includes a sub-cooling heat exchanger installed after the condenser.
  • the carbon dioxide cooling circuit comprises three pressure levels in order to improve the thermodynamic efficiency of the process.
  • the higher operating pressure required when using CO 2 means that it my be preferable to use a high pressure casing with the carbon dioxide compressor. More preferably the compressor can be split into two casings and a barrel type casing used for the high pressure stage.
  • a LNG liquefaction process comprising three cascade cycles each driven by a compressor, wherein the compressors are substantially equally loaded and one of the cascade cycles is a carbon dioxide cycle.
  • a carbon dioxide pre-cooling circuit for LNG liquefaction wherein the carbon dioxide has a minimum evaporation temperature of no less then ⁇ 50° C., preferably no less than ⁇ 40° C. and most preferably no less than ⁇ 35° C.
  • FIG. 1 shows a load balanced liquefaction process in accordance with a preferred embodiment of the invention
  • FIG. 2 show an alternative embodiment of a load balanced process
  • FIG. 3 shows a graph of overall power demand as a function of a reference temperature
  • FIG. 4 shows a load balanced liquefaction process containing a carbon dioxide pre-cooling circuit
  • FIG. 5 shows hot/cold composite curves for the processes shown in FIGS. 2 and 4 ;
  • FIG. 6 shows a comparison of refrigerant inventories of the processes shown in FIGS. 2 and 4 .
  • FIG. 1 the cooling and liquefaction of the hydrocarbon-rich flow, which is conducted via line 1 , are effected against a mixed refrigerant circuit cascade, consisting of three mixed refrigerant circuits.
  • a mixed refrigerant circuit cascade consisting of three mixed refrigerant circuits.
  • the hydrocarbon-rich flow which is to be liquefied is cooled in the heat exchanger E 1 against the two evaporating mixed refrigerant flows 4 b and 4 d of the first mixture circuit 4 a to 4 e, then cooled by the evaporating mixed refrigerant flow 3 d, and then conducted via line 1 a to a heavy hydrocarbon separation unit S, represented simply as a box.
  • At least one part flow of one of the two part flows 3 b and 3 d of the second cooling agent mixture circuit 3 a to 3 e is used for the provision of cooling in the separation unit S.
  • the choice of which of the two part flows 3 b and/or 3 d is drawn from for this provision of cooling is determined by the temperature level(s) required in the heavy hydrocarbon separation unit S.
  • the hydrocarbon-rich flow to be liquefied is then conducted via line 1 c to a second heat exchanger E 2 , and is liquefied in this against the evaporating mixed refrigerant flow 3 b of the second cooling circuit 3 a to 3 e.
  • the hydrocarbon-rich flow is conducted via line 1 d to a third heat exchanger E 3 , and is subcooled here against the mixed refrigerant flow 2 b of the third cooling circuit 2 a to 2 c.
  • the subcooled liquid product is then conducted via line le to its further use.
  • each of the three cooling circuits 2 a to 2 c, 3 a to 3 e, and 4 a to 4 e has a compressor, V 2 , V 3 , and V 4 respectively. Not shown in the drawing are the corresponding drives for these compressors V 2 , V 3 , and V 4 .
  • the coolers or heat exchangers which are located downstream of the compressors V 2 , V 3 , and V 4 respectively are not shown in the drawing, in which the refrigerant mixture is cooled against a cooling medium, such as water.
  • the refrigerant mixture of the first refrigerant circuit, compressed in the compressor V 4 , is conducted via line 4 a to the heat exchanger E 1 , and is divided here into two part flows 4 b and 4 d after cooling has taken place.
  • the refrigerant mixture in these part flows 4 b and 4 d, after throttling has been effected in the valves d and e or expansion devices, is evaporated to different pressure levels in the heat exchanger E 1 and then conducted via line 4 c or 4 e to the compressor V 4 before the first stage (part flow 4 c ) or to an intermediate pressure level (part flow 4 e ).
  • a part flow 3 d of the refrigerant mixture of the second refrigerant mixture circuit 3 a to 3 e is drawn off after the heat exchanger E 1 , expanded in valve c, and then evaporated in heat exchanger E 1 against cooling process flows, before being conducted via line 3 e, at an intermediate pressure level, to the circuit compressor V 3 .
  • the refrigerant mixture part flow 3 d makes a contribution to the pre-cooling of the hydrocarbon-rich flow in heat exchanger E 1 .
  • the part flow 3 d of the refrigerant mixture of the second mixed refrigerant circuit 3 a to 3 e, used for the pre-cooling of the hydrocarbon-rich flow must be evaporated at a pressure which is higher than the evaporation pressure of the mixed refrigerant part flow 3 b of the second mixed refrigerant circuit 3 a to 3 e.
  • the distribution of the cooling capacity of the second refrigerant circuit onto the heat exchangers E 1 and E 2 , and therefore to the pre-cooling and liquefaction of the hydrocarbon-rich flow which is to be liquefied, can be adjusted almost at will.
  • one compressor is used in each case with a third of the total drive capacity in the first and third refrigerant mixture circuit, i.e. for the pre-cooling as well as for the subcooling of the hydrocarbon-rich flow which is to be liquefied.
  • the compressor of the second refrigerant mixture circuit is operated according to the invention in such a way that it uses 20% of its capacity, and consequently 6.66% of the total capacity, for pre-cooling, while the remaining 80%, i.e. 26.66% of the total capacity, is used for liquefaction.
  • the method according to the invention accordingly makes possible the economical exploitation of the available compressors and drive units, because the (circuit) compressors of the three refrigerant circuits obtain approximately the same drive capacity, i.e. a third of total capacity in each case.
  • FIG. 2 shows an alternative version of the load balanced process.
  • the pre-cooling cycle C 10 comprises a first circuit driven by a first compressor V 10 and one part 22 of the refrigerant stream 21 from the second cycle C 20 .
  • Three General Electric MS 7121 EA (Frame 7) gas turbines are used to drive the compressors V 10 , V 20 , V 30 . If highest availability is of the essence, the three refrigeration cycles can be designed with two times 50% gas turbine/compressor trains. In this case six GE MS 6581 B (Frame 6) gas turbines would replace the three Frame 7s.
  • All LNG plants require the extraction of at least of those hydrocarbons, which would freeze in the LNG under storage conditions (e.g. aromatics and C 5 +).
  • precooling is usually considered as first cooling step between ambient temperature and extraction of the mentioned hydrocarbons.
  • the precooling portion of the overall power demand of all refrigeration compressors for the two gases defined in Table 1 is shown in FIG. 3 as a function of a reference temperature. This is the temperature, under which all main process streams (natural gas, refrigerant fluids) enter into the cryogenic heat exchangers.
  • a process with three refrigeration cycles offers a much wider field for even load distribution between the cycles. If part of the refrigerant of the liquefaction cycle C 20 is vaporized under elevated pressure in the precooling section C 10 and is fed to the LC compressor V 20 as side stream 22 , a perfect load balancing between all three refrigeration cycles can be achieved. This feature is a major aspect of a cost effective design for large production capacities. As all three (3) cycles are symmetrically driven this arrangement is referred to as MFC*s3.
  • the final compressor V 30 of FIG. 2 is split into two casings V 31 , V 32 .
  • the second casing V 32 is designed to deal with high pressures at which the multistage compressor operates.
  • the precooling circuit C 10 of FIG. 2 has been replaced with a pre-cooling circuit C 100 which comprises a carbon dioxide stream 101 .
  • a pre-cooling circuit C 100 which comprises a carbon dioxide stream 101 .
  • the stream 101 is split into three separate streams, 102 , 103 , 104 which are then expanded to different pressures. This compensates for the constant temperature evaporation of CO 2 .
  • Unlike hydrocarbon streams 201 , 301 only part of the carbon dioxide stream 101 is sub-cooled by the pre-cooling heat exchanger E 100 prior to expansion, in order to reduce the internal heat load of this exchanger.
  • the CO 2 precooling compressor V 100 is split into two casings, V 110 , V 120 with a barrel type casing V 120 for the high-pressure stage.
  • the carbon dioxide is cooled by a water cooled condenser C 20 and an additional subcooling heat exchanger C 22 , using seawater to subcool the liquid refrigerant after the condenser C 20 , in order to improve process efficiency.
  • a desuperheater can also be provided after the compressor, as in many conventional systems.
  • load balancing is achieved by allowing the liquefaction compressor V 200 to take over some of the precooling cycle load, leading to a “symmetrical” process.
  • Temperature profiles in the form of hot/cold composite curves for the two cases are shown in FIG. 5 .
  • the three CO 2 precooling temperature levels are easily observed in the left diagram.
  • the highest pressure level to the liquefaction compressor is also considered part of precooling. Changes in the subcooling process are minimal between the two cases.
  • the minimization of hydrocarbon refrigerant inventory is very important in terms of safety.
  • the HC refrigerant inventory is reduced by about 70% in the CO 2 -precooled process.
  • the reduced hydrocarbon charge is positive in relation to loss prevention and to the availability of the three main safety functions of the LNG barge, which are (i) main structural strength, (ii) main escape routes, and (iii) means of evacuation.

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US10/573,213 2003-09-23 2004-09-23 Natural Gas Liquefaction Process Abandoned US20080006053A1 (en)

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DE2003144030 DE10344030A1 (de) 2003-09-23 2003-09-23 Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes
DE10344030.5 2003-09-23
GB0409103.9 2004-04-23
GB0409103A GB0409103D0 (en) 2003-09-23 2004-04-23 Natural gas liquefaction process
PCT/GB2004/004047 WO2005028975A2 (en) 2003-09-23 2004-09-23 Natural gas liquefaction process

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WO2009153427A2 (fr) * 2008-06-20 2009-12-23 Ifp Procede de liquefaction d'un gaz naturel avec pre-refroidissement du melange refrigerant
US20100281915A1 (en) * 2009-05-05 2010-11-11 Air Products And Chemicals, Inc. Pre-Cooled Liquefaction Process
US20110185767A1 (en) * 2006-08-17 2011-08-04 Marco Dick Jager Method and apparatus for liquefying a hydrocarbon-containing feed stream
US20130125568A1 (en) * 2011-11-17 2013-05-23 Air Products And Chemicals, Inc. Compressor Assemblies and Methods to Minimize Venting of a Process Gas During Startup Operations
US20140060111A1 (en) * 2012-09-06 2014-03-06 Linde Aktiengesellschaft Process for liquefying a hydrocarbon-rich fraction
US20160061517A1 (en) * 2014-08-29 2016-03-03 Black & Veatch Holding Company Dual mixed refrigerant system
US9562717B2 (en) 2010-03-25 2017-02-07 The University Of Manchester Refrigeration process
US20170217051A1 (en) * 2016-01-28 2017-08-03 Jean-Charles Viancin Method for manufacturing a flexible mold with peripheral stiffener, and mold resulting from said method
WO2019008267A1 (fr) 2017-07-05 2019-01-10 Engie Dispositif et procédé de liquéfaction d'un gaz naturel ou d'un biogaz
US20190195536A1 (en) * 2016-06-22 2019-06-27 Samsung Heavy Ind. Co., Ltd Fluid cooling apparatus
US11359858B2 (en) * 2019-12-31 2022-06-14 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for liquefying ammonia

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DE102004023814A1 (de) * 2004-05-13 2005-12-01 Linde Ag Verfahren und Vorrichtung zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes
DE102004054674A1 (de) * 2004-11-12 2006-05-24 Linde Ag Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes
DE102005000647A1 (de) * 2005-01-03 2006-07-13 Linde Ag Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes
DE102005029275A1 (de) * 2005-06-23 2006-12-28 Linde Ag Verfahren zum Verflüssigen eines Kohlenwasserstoff-reichen Stromes
GB2450666B (en) * 2006-05-19 2011-05-04 Shell Int Research Method and apparatus for treating a hydrocarbon stream
GB2455658B (en) * 2006-09-22 2010-07-21 Shell Int Research Method and apparatus for producing a cooled hydrocarbon stream
WO2015011742A1 (en) * 2013-07-26 2015-01-29 Chiyoda Corporation Refrigeration compression system using two compressors
DE102014005936A1 (de) * 2014-04-24 2015-10-29 Linde Aktiengesellschaft Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion
DE102015002164A1 (de) * 2015-02-19 2016-08-25 Linde Aktiengesellschaft Verfahren zum Verflüssigen von Erdgas
CN110801639B (zh) * 2019-11-11 2021-06-01 杭州快凯高效节能新技术有限公司 一种工业尾气多级液化及分级制冷回收二氧化碳方法

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US20070175240A1 (en) * 2005-11-24 2007-08-02 Jager Marco D Method and apparatus for cooling a stream, in particular a hydrocarbon stream such as natural gas
US8181481B2 (en) * 2005-11-24 2012-05-22 Shell Oil Company Method and apparatus for cooling a stream, in particular a hydrocarbon stream such as natural gas
US20110185767A1 (en) * 2006-08-17 2011-08-04 Marco Dick Jager Method and apparatus for liquefying a hydrocarbon-containing feed stream
WO2009153427A3 (fr) * 2008-06-20 2013-01-03 IFP Energies Nouvelles Procede de liquefaction d'un gaz naturel avec pre-refroidissement du melange refrigerant
WO2009153427A2 (fr) * 2008-06-20 2009-12-23 Ifp Procede de liquefaction d'un gaz naturel avec pre-refroidissement du melange refrigerant
FR2932876A1 (fr) * 2008-06-20 2009-12-25 Inst Francais Du Petrole Procede de liquefaction d'un gaz naturel avec pre-refroidissement du melange refrigerant
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US20100281915A1 (en) * 2009-05-05 2010-11-11 Air Products And Chemicals, Inc. Pre-Cooled Liquefaction Process
US9562717B2 (en) 2010-03-25 2017-02-07 The University Of Manchester Refrigeration process
US9494281B2 (en) * 2011-11-17 2016-11-15 Air Products And Chemicals, Inc. Compressor assemblies and methods to minimize venting of a process gas during startup operations
US20130125568A1 (en) * 2011-11-17 2013-05-23 Air Products And Chemicals, Inc. Compressor Assemblies and Methods to Minimize Venting of a Process Gas During Startup Operations
US20140060111A1 (en) * 2012-09-06 2014-03-06 Linde Aktiengesellschaft Process for liquefying a hydrocarbon-rich fraction
CN107208962A (zh) * 2014-08-29 2017-09-26 博莱克威奇控股公司 双重混合制冷剂系统
US20160061517A1 (en) * 2014-08-29 2016-03-03 Black & Veatch Holding Company Dual mixed refrigerant system
US20170217051A1 (en) * 2016-01-28 2017-08-03 Jean-Charles Viancin Method for manufacturing a flexible mold with peripheral stiffener, and mold resulting from said method
US20190195536A1 (en) * 2016-06-22 2019-06-27 Samsung Heavy Ind. Co., Ltd Fluid cooling apparatus
US11859873B2 (en) * 2016-06-22 2024-01-02 Samsung Heavy Ind. Co., Ltd Fluid cooling apparatus
WO2019008267A1 (fr) 2017-07-05 2019-01-10 Engie Dispositif et procédé de liquéfaction d'un gaz naturel ou d'un biogaz
FR3068772A1 (fr) * 2017-07-05 2019-01-11 Engie Dispositif et procede de liquefaction d’un gaz naturel ou d’un biogaz
US11359858B2 (en) * 2019-12-31 2022-06-14 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for liquefying ammonia

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WO2005028975A3 (en) 2005-05-26
RU2352877C2 (ru) 2009-04-20

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