WO2007011155A1 - Appareil de reliquéfaction de gaz d’évaporats de gaz naturel liquéfié - Google Patents

Appareil de reliquéfaction de gaz d’évaporats de gaz naturel liquéfié Download PDF

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Publication number
WO2007011155A1
WO2007011155A1 PCT/KR2006/002818 KR2006002818W WO2007011155A1 WO 2007011155 A1 WO2007011155 A1 WO 2007011155A1 KR 2006002818 W KR2006002818 W KR 2006002818W WO 2007011155 A1 WO2007011155 A1 WO 2007011155A1
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WO
WIPO (PCT)
Prior art keywords
bog
nitrogen
temperature
pressure
gas
Prior art date
Application number
PCT/KR2006/002818
Other languages
English (en)
Inventor
Eui Seok Hong
Yoon Pyo Lee
Original Assignee
Shinyoung Heavy Industries Co., Ltd.
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority claimed from KR1020050078588A external-priority patent/KR100740686B1/ko
Priority claimed from KR1020050109931A external-priority patent/KR100699163B1/ko
Priority claimed from KR1020060001271A external-priority patent/KR100681319B1/ko
Application filed by Shinyoung Heavy Industries Co., Ltd. filed Critical Shinyoung Heavy Industries Co., Ltd.
Priority to JP2008522699A priority Critical patent/JP2009501896A/ja
Priority to EP06783336A priority patent/EP1913117A1/fr
Publication of WO2007011155A1 publication Critical patent/WO2007011155A1/fr

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Classifications

    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63C—LAUNCHING, HAULING-OUT, OR DRY-DOCKING OF VESSELS; LIFE-SAVING IN WATER; EQUIPMENT FOR DWELLING OR WORKING UNDER WATER; MEANS FOR SALVAGING OR SEARCHING FOR UNDERWATER OBJECTS
    • B63C11/00—Equipment for dwelling or working underwater; Means for searching for underwater objects
    • B63C11/02—Divers' equipment
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • 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
    • 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
    • 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
    • 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
    • F25J1/0203—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle
    • F25J1/0208—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
    • 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
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • 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
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
    • 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
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0249—Controlling refrigerant inventory, i.e. composition or quantity
    • F25J1/025—Details related to the refrigerant production or treatment, e.g. make-up supply from feed gas itself
    • 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
    • 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
    • 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
    • F25J1/0284—Electrical motor 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with the feed 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/60—Expansion by ejector or injector, e.g. "Gasstrahlpumpe", "venturi mixing", "jet pumps"
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • 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
    • Y02T70/00—Maritime or waterways transport
    • Y02T70/50—Measures to reduce greenhouse gas emissions related to the propulsion system
    • Y02T70/5218—Less carbon-intensive fuels, e.g. natural gas, biofuels

Definitions

  • the present invention relates to an apparatus for reliquefying boil-off gas
  • natural gas is transported in a liquefied state over long distance.
  • an LNG carrier is utilized for transporting LNG from a first location where natural gas is liquefied to a second location where LNG is vaporized and delivered to a gas distribution system.
  • natural gas is liquefied at an extremely low temperature, i.e., a temperature of approximately -163 0 C under normal pressure
  • external heat transferred to a storage tank of the LNG carrier continuously evaporates LNG in the storage tank. If pressure in the storage tank exceeds a preset safety pressure, boil-off gas from LNG is discharged to the outside via a safety valve.
  • the discharged BOG is reliquefied and then returned to the storage tank or utilized as fuel for the ship.
  • a refrigeration cycle is performed by the steps of compressing a working fluid by a plurality of compressors; cooling the compressed working fluid through indirect heat exchange; expanding the working fluid; heating the expanded working fluid through indirect heat exchange between the compressed working fluid and the expanded working fluid; and returning the heated working fluid to one of the compressors.
  • LNG vapor is at least partially condensed through indirect heat exchange with the expanded working fluid.
  • a working fluid is induced from LNG itself, and thus, the apparatus is operated by an open refrigeration cycle.
  • the fluid is expanded by a valve so that partially condensed LNG is obtained.
  • the partially condensed LNG is divided into a liquid phase to be returned into a storage tank and a vapor phase to be mixed with natural gas that is supplied to a combustion burner. Since the working fluid is heated and cooled in an identical heat exchanger, only one heat exchanger is employed.
  • the heat exchanger is placed on a first skid-mounting platform and a compressor for compressing the working fluid is mounted to a second skid- mounting platform.
  • an incombustible gas be used as a working fluid.
  • an expansion turbine is more preferred to a valve for expanding a working fluid.
  • Apparatuses for reliquefying BOG disclosed in these U.S. patents are constructed such that BOG supplied through a compressor passes through two heat exchangers to ultimately condense BOG. BOG is pre-cooled in the first heat exchanger and then ultimately condensed in the second heat exchanger.
  • nitrogen compressed by passing through the compressor is divided into a first stream and a second stream.
  • the first stream passes through an expansion valve and is used for reliquefaction of BOG and then returned to the compressor, whereas the second stream passes through an expansion turbine and is used for pre-cooling of BOG and then returned to the compressor.
  • respective lines for circulating a plurality of nitrogen refrigerant streams should be constructed, and five or six paths should be provided in the heat exchanger. Due to this structure, there are problems in that the entire configuration of the reliquefaction apparatus is complicated and inefficient.
  • Korean Patent Laid-Open Publication Nos. 2001-0088406 and 2001-0089142 relate to an apparatus for use in a board-type ship so as to reliquefy compressed vapor, wherein components of the apparatuses are manufactured into pre-assemblies.
  • a reliquef action process is carried out through a closed cycle.
  • a working fluid is compressed in one or more compressors 22, 24 and 25, cooled in a first heat exchanger 22, expanded in a turbine 28 and heated in a second heat exchanger 13.
  • the compressed vapor is at least partially condensed.
  • This apparatus comprises a first pre-assembly 10 including the second heat exchanger 13, and a second pre-assembly 20 including the first heat exchanger 22, the compressors 23, 24 and 25 and the expansion turbine 28.
  • the pre-assemblies 10 and 20 are located on platforms 11 and 21, respectively.
  • An object of the present invention is to provide an apparatus for reliquefying LNG BOG, which can constantly maintain a temperature difference between BOG and nitrogen gas within a condenser in a preset range by pre-cooling BOG upstream of the condenser even though the quantity or temperature of BOG generated is changed, in a reliquefaction system for reliquefying BOG generated in a storage tank and flowing out through a safety valve and returning the liquefied BOG into the storage tank while an LNG carrier is plying.
  • Another object of the present invention is to provide an apparatus for reliquefying
  • LNG BOG which can stably maintain temperature and pressure in a storage tank and eliminate a loss of LNG under any conditions by freely lowering the temperature of nitrogen to a smaller value using an expansion valve as well as an expansion turbine, in a reliquefaction system for reliquefying BOG generated in the storage tank and flowing out through a safety valve and returning the liquefied BOG while an LNG carrier is plying.
  • a further object of the present invention is to provided an apparatus for reliquefying BOG, which is improved in view of simplification of a structure, easy installation thereof on a ship, reduction of heat loss, and the like.
  • the nitrogen cycle device includes a nitrogen-pressurizing/cooling means for pressurizing and cooling nitrogen, a nitrogen heat exchanger for cooling high-pressure nitrogen gas that has passed through the nitrogen-pressurizing/
  • an apparatus for reliquefying BOG of LNG including a compressor for compressing BOG generated in a storage tank for LNG, a condenser for at least partially condensing BOG compressed by the compressor, and a nitrogen cycle device for supplying cold heat to the compressor, so as to return BOG reliquefied by the condenser to the storage tank, BOG compressed by the compressor is subjected to pre-cooling upstream of the condenser, and thus, there is an advantage in that the temperature of BOG can be constantly maintained in a preset range even though the quantity or temperature of BOG generated is changed.
  • FIG. 1 is a schematic view of a conventional apparatus for reliquefying LNG BOG.
  • FIG. 2 is a schematic view of an apparatus for reliquefying LNG BOG according to a first embodiment of the present invention.
  • Figs. 3 and 4 are flowcharts illustrating a method of reliquefying LNG BOG according to the first embodiment of the present invention.
  • FIG. 5 is a schematic view of an apparatus for reliquefying LNG BOG according to a second embodiment of the present invention.
  • FIGs. 6 and 7 are flowcharts illustrating a method of reliquefying LNG BOG according to the second embodiment of the present invention.
  • FIG. 8 is a schematic view of an apparatus for reliquefying LNG BOG according to a third embodiment of the present invention.
  • FIGs. 9 and 10 are flowcharts illustrating a method of reliquefying LNG BOG according to the third embodiment of the present invention.
  • FIG. 11 is a schematic view of an apparatus for reliquefying LNG BOG according to a fourth embodiment of the present invention.
  • FIGs. 12 and 13 are flowcharts illustrating a method of reliquefying LNG BOG according to the fourth embodiment of the present invention. Best Mode for Carrying Out the Invention
  • FIG. 2 is a view showing a configuration of the apparatus for reliquefying LNG
  • This apparatus comprises a BOG cycle device, a nitrogen cycle device and a cold box device for interfacing these two devices.
  • Natural gas in a gaseous phase is liquefied and stored in a storage tank 110 in a cryogenic state under atmospheric pressure (1.013 bars).
  • BOG is generated due to continuous heat transfer from the outside, thereby increasing pressure in the storage tank 110.
  • a safety valve 111 is opened and BOG is discharged outside of the storage tank 110 if the pressure in the storage tank 110 reaches about 1.03 bars, and the discharged BOG passes through two-stage bog compressor 115 and 116 and is then subjected to a reliquef action process.
  • a temperature sensor 112 be sensed by a temperature sensor 112 and be controlled to a predetermined temperature through a temperature controller 114, and BOG then flow into the two- stage bog compressor 115 and 116. BOG that has passed through the temperature controller 114 is maintained in a superheated vapor state at a pressure of 1.03 bars and a temperature of -12O 0 C.
  • cryogenic BOG LNG
  • the temperature of BOG can be controlled.
  • the amount of BOG re-circulated is controlled by adjusting the degree of opening of a recirculation valve 113.
  • LNG in the storage tank 110 may be supplied to be mixed with BOG compressed by the BOG compressors 115 and 116, thereby lowering or controlling the temperature of BOG to be supplied into a BOG condenser 131.
  • the temperature controller is operated only until the reliquefaction apparatus reaches a normal state, the recirculation valve 113 is then closed and the cryogenic reliquefied LNG is guided to the storage tank 110.
  • BOG discharged from the two-stage bog compressor 115 and 116 passes through the BOG condenser 131, BOG is in a supercooled liquid state at a pressure of 2.3 bars and a temperature of -155°Cand then flows back into the storage tank 110 or is re-circulated to the temperature controller 114.
  • the BOG condenser 131 will be described in detail below in connection with the cold box device.
  • condensed BOG is supplied through spraying to pressurized BOG that has passed through the two-stage bog compressor 115 and 116, thereby controlling the temperature of the pressurized BOG to be supplied to the BOG condenser.
  • Methods of causing BOG to flow back into the storage tank 110 include a method of spaying BOG through a spray head above the storage tank, a method of supplying BOG to the bottom of the storage tank, and the like. If BOG flows back to the bottom of the storage tank, a nitrogen component that is contained in non-condensed gas included in the condensed BOG is dissolved in LNG so that the ratio of nitrogen in the gaseous phase is maintained at a lower value. Since the liquefaction temperature of nitrogen is lower than that of methane that is a main component of LNG, an increase in the content of nitrogen in BOG can reduce a load applied to the two- stage bog compressor 115 and 116 or the BOG condenser 131.
  • BOG is reliquefied in the BOG condenser 131 by means of heat exchange between
  • BOG and cryogenic nitrogen gas that is a working fluid The following description is made in connection with a cycle device for obtaining cryogenic nitrogen gas required for the reliquef action of BOG.
  • the intermediate coolers 125, 126 and 127 are to cool the nitrogen refrigerant, which serves as the working fluid, in a compression step.
  • conventional methods known from the prior arts disclosed in the "Background Art” herein may be used, it is desirable to use a cooling method using seawater as a refrigerant.
  • the low-temperature and high-pressure nitrogen gas that has passed through the nitrogen heat exchanger 133 passes through an expansion turbine 136 to be converted into gas with an extremely low temperature of -167 0 C and a low pressure of 10.5 bars.
  • the converted nitrogen gas is moved to the BOG condenser 131 and performs a BOG reliquef action process so that it is in a gaseous state at a pressure of 10.3 bars and a temperature of -134 0 C. Thereafter, the nitrogen gas is subjected to inner heat exchange with high-temperature nitrogen in the nitrogen heat exchanger 133 and reaches 10 bars and 4O 0 C, thereby completing the cycle.
  • a nitrogen buffer tank 120 performs the function of adjusting a mass flow rate in the nitrogen cycle in response to changes in the reliquefied amount of BOG, i.e., changes in a cooling load of the nitrogen cycle.
  • a source for supplying a sup- plementary working fluid (nitrogen) may be further provided against a case where the amount of nitrogen is reduced.
  • the cold box device 130 comprises the BOG condenser 131 in which the reliq- uef action of BOG is performed, the nitrogen heat exchanger 133 in which inner heat exchange between a high temperature section and a lower temperature section of the nitrogen cycle is carried out, and the expansion turbine 136 in which cryogenic nitrogen gas is obtained.
  • a generator G that is not an essential element of the present invention may be coupled to the expansion turbine 136 to generate electric power that in tune is used as an auxiliary power source for the BOG compressors 115 and 116, the nitrogen compressors 121, 122 and 123, or the like.
  • the aforementioned devices may be incorporated into the cold box 130 as one module, so that pipes for connecting the devices can be shortened.
  • This enables cryogenic nitrogen required for the reliquefaction of BOG to be secured stably. That is, since the length of a connecting pipe between the nitrogen heat exchanger 133 and an inlet of the expansion turbine 136 is shortened, a cryogenic condition of an outlet of the expansion turbine that may be sensitive to the condition or temperature of an inlet of the expansion turbine 136 can be stabilized. Further, since the length of a connecting pipe between the BOG condenser and the outlet of the expansion turbine is shortened, it is possible to expect that an increase in the temperature of the nitrogen gas caused by the transfer of the nitrogen gas is minimized.
  • the BOG condenser 131 which is at low temperature, the nitrogen heat exchanger 133 and the expansion turbine 136 be constructed into one cold box device 130 and these components be insulated as one module.
  • the insulation is achieved by generally known insulating materials. Due to this configuration, a cryogenic range of the nitrogen gas can be stably managed.
  • the cold box device may be manufactured as a pre-assembly to facilitate mounting thereof on a ship.
  • BOG is circulated through a process comprising the steps of passing BOG, which is discharged after a valve is opened at a predetermined pressure, through the temperature controller and constantly maintaining BOG at a pressure of 1.03 bars and a temperature of -12O 0 C at the inlet of the two- stage bog compressor 115 and 116 (ST 111); compressing BOG in the two-stage compressor 115 and 116 to a pressure of 2.5 bars and a temperature of -12O 0 C so that BOG is in a high temperature and pressure state (ST 112); reliquefying BOG discharged from the BOG compressors 115 and 116 into supercooled liquid with a pressure of 2.3 bars and a temperature of -155°Cin the BOG condenser 131 (ST 113); pressurizing the reliquefied BOG by the circulation pump (ST 114); re-circulating a portion of the
  • the circulation of nitrogen gas for supplying cold heat required for the reliquef action of BOG comprises the steps of passing nitrogen gas with a temperature of 4O 0 C and a pressure of 10 bars through the three-stage compressor 121, 122 and 123 and the intermediate coolers 125, 126 and 127 to increase the pressure of the nitrogen gas to a pressure of 59 bars at a temperature of 43 0 C(ST 117); heat-exchanging the high-pressure nitrogen gas with nitrogen gas in the low-temperature section of the nitrogen heat exchanger to convert the high-pressure nitrogen gas into nitrogen gas with a low temperature of -105 0 C and a pressure of 59 bars (ST 118); converting the high-pressure nitrogen gas with a low temperature of - 167 0 C and a low pressure of 10.5 bars by passing the high-pressure nitrogen through the expansion turbine (ST 119); performing reliquefaction of BOG by the low- temperature and low-pressure nitrogen in the BOG condenser 131 so that the low- temperature and low-pressure nitrogen is converted into nitrogen
  • the pressure of a storage tank can be stably maintained without a loss of stored LNG during a voyage of an LNG carrier.
  • the size of the apparatus for reliquefying LNG BOG can be reduced by employing the simple cold box module and the cryogenic range of the nitrogen gas can be stably managed.
  • FIG. 5 is a view showing a configuration of the apparatus for reliquefying LNG
  • This apparatus comprises a BOG cycle device, a nitrogen cycle device and a cold box device interfacing these two devices.
  • Natural gas in a gaseous phase is liquefied and stored in a storage tank 210 in a cryogenic state under atmospheric pressure (1.013 bars). However, during transportation of LNG, BOG is generated due to continuous heat transfer from the outside, thereby increasing pressure in the storage tank 210.
  • a safety valve 211 is opened and BOG is discharged outside of the storage tank 210 if the pressure in the storage tank 210 reaches about 1.03 bars, and the discharged BOG passes through two-stage bog compressor 215 and 216 and is then subjected to a reliquef action process.
  • a temperature controller 214 be sensed by a temperature sensor 212 and be controlled to a predetermined temperature through a temperature controller 214, and BOG then flow into the two- stage bog compressor 215 and 216. BOG that has passed through the temperature controller 214 is maintained in a superheated vapor state at a pressure of 1.03 bars and a temperature of -12O 0 C. [76] The operation of the temperature controller 214 will be described in greater detail.
  • cryogenic BOG LNG
  • the temperature of BOG can be controlled.
  • the amount of BOG re-circulated is controlled by adjusting the degree of opening of a recirculation valve 213.
  • LNG in the storage tank 210 may be supplied to be mixed with BOG compressed by the BOG compressors 215 and 216, thereby lowering or controlling the temperature of BOG to be supplied into a BOG condenser 231.
  • the temperature controller is operated only until the reliquefaction apparatus reaches a normal state, the recirculation valve 213 is then closed and the cryogenic reliquefied LNG is guided to the storage tank 210.
  • BOG discharged from the two-stage bog compressor 215 and 216 be liquefied in the BOG condenser 231 and then mixed again with non-condensed components separated in a BOG non-condensed gas separator 218 so as to lower the temperature of superheated vapor.
  • BOG After BOG passes the BOG condenser 231 and is then converted to be in a supercooled liquid state at a pressure of 2.3 bars and a temperature of -155 0 C, it flows back into the storage tank 210 or is re-circulated to the temperature controller 214.
  • the BOG condenser 231 will be described in detail below in connection with the cold box device.
  • Methods of causing BOG to flow back into the storage tank 210 include a method of spaying BOG through a spray head above the storage tank, a method of supplying BOG to the bottom of the storage tank, and the like. If BOG flows back to the bottom of the storage tank, a nitrogen component that is contained in non-condensed gas included in the condensed BOG is dissolved in LNG so that the ratio of nitrogen in the gaseous phase is maintained at a lower value. Since the liquefaction temperature of nitrogen is lower than that of methane that is a main component of LNG, an increase in the content of nitrogen in BOG can reduce a load applied to the two- stage bog compressor 215 and 216 or the BOG condenser 231.
  • BOG is reliquefied in the BOG condenser 231 by means of heat exchange between
  • BOG and cryogenic nitrogen gas that is a working fluid The following description is made in connection with a cycle device for obtaining cryogenic nitrogen gas required for the reliquef action of BOG.
  • the intermediate coolers 225, 226 and 227 are to cool the nitrogen refrigerant, which serves as the working fluid, in a compression step.
  • conventional methods known from the prior arts disclosed in the "Background Art” herein may be used, it is desirable to use a cooling method using seawater as a refrigerant.
  • the nitrogen gas is primarily cooled to a temperature of -83.5 0 C through inner heat exchange with low-temperature nitrogen, which has passed through a first nitrogen heat exchanger 233 from the BOG condenser 231 and still has cold heat, in a second nitrogen heat exchanger 234.
  • a portion of the high-pressure nitrogen gas that has passed through the second nitrogen heat exchanger 234 has reduced temperature while passing through an expansion turbine 236, and the low-pressure nitrogen gas of which the temperature is lowered by the expansion turbine 236 is subjected to inner heat exchange with the high-pressure nitrogen, which has passed through the second nitrogen heat exchanger 234, in the first heat exchanger 233. This contributes to reduction in the temperature of the high-pressure nitrogen to a preset temperature at an inlet of an expansion valve 237.
  • the high-pressure nitrogen gas of which the temperature is lowered in the first nitrogen heat exchanger 233 passes through the expansion valve 237 and ultimately converted into cryogenic nitrogen gas with a temperature of -163 0 C required for reliq- uefaction of BOG.
  • This cryogenic nitrogen gas is heat-exchanged with BOG in the BOG condenser 231 to reliquefy BOG and accordingly has increased temperature.
  • a nitrogen buffer tank 230 performs the function of adjusting a mass flow rate in the nitrogen cycle in response to changes in the reliquefied amount of BOG, i.e., changes in a cooling load of the nitrogen cycle.
  • a source for supplying a supplementary working fluid (nitrogen) may be further provided against a case where the amount of nitrogen is reduced.
  • the cold box device 230 comprises the BOG condenser 231 in which the reliq- uefaction of BOG is performed, the first and second nitrogen heat exchangers 233 and 234 in which inner heat exchange between a high temperature section and a lower temperature section of the nitrogen cycle is carried out, the expansion valve 237 in which cryogenic nitrogen gas is obtained, and the expansion turbine 236 in which low- temperature nitrogen gas required for inner heat exchange is obtained.
  • a generator G that is not an essential element of the present invention may be coupled to the expansion turbine 236 to generate electric power that in tune is used as an auxiliary power source for the BOG compressors 215 and 216, the nitrogen compressors 221, 222 and 223, or the like.
  • the aforementioned devices may be incorporated into the cold box 230 as one module, so that pipes for connecting the devices can be shortened.
  • This enables cryogenic nitrogen required for the reliquefaction of BOG to be secured stably. That is, since the length of a connecting pipe between the second nitrogen heat exchanger 234 and the inlet of the expansion turbine 236 or the length of a connecting pipe between the first nitrogen heat exchanger 233 and the inlet of the expansion valve 237 is shortened, a cryogenic condition of nitrogen at the outlet of the expansion turbine 236 or expansion valve 237 that may be sensitive to the condition or temperature of nitrogen at the inlet of the expansion turbine 236 or expansion valve 237 can be stabilized.
  • the BOG condenser 231 which is at low temperature, the nitrogen heat exchangers 233 and 234, and the expansion means 236 and 237 be constructed into one cold box device 230 and these components be insulated as one module.
  • the insulation is achieved by generally known insulating materials.
  • the cold box device may be manufactured as a pre-assembly to facilitate mounting thereof on a ship.
  • the process of the reliquefaction apparatus comprises the steps of compressing BOG generated in the storage tank for LNG; pressurizing and cooling nitrogen gas which is a working fluid, so as to provide cold heat used for condensing the compressed BOG and expanding the pressurized and cooled nitrogen gas to generate cryogenic nitrogen gas; at least partially condensing the compressed BOG through heat exchange with the cryogenic nitrogen gas; and returning BOG reliquefied by means of the condensation to the storage tank.
  • all the pressurized and cooled nitrogen gas is not expanded, but a portion of the pressurized and cooled nitrogen gas is extracted and expanded through a different path to generate low-temperature gas.
  • the low-temperature gas is added to nitrogen gas which has been heat-exchanged for condensing the compressed BOG and has slightly increased temperature, and is then heat-exchanged with the pressurized and cooled nitrogen gas prior to expansion thereof so that it can be pre-cooled.
  • BOG is circulated through a process comprising the steps of passing BOG, which is discharged after a valve 211 is opened at a predetermined pressure, through the temperature controller 214 and constantly maintaining BOG at a pressure of 1.03 bars and a temperature of -12O 0 C at the inlet of the two-stage bog compressor 215 and 216 (ST 211); compressing BOG in the two-stage compressor 215 and 216 to a pressure of 2.5 bars and a temperature of -73 0 C so that BOG is in a high temperature and pressure superheated state (ST 212); sucking gas separated in the BOG non-condensed gas separator 218 due to pressure difference in the venturi nozzle 239 so that the temperature of the gas is lowered (ST 213); reliquefying BOG discharged from the BOG compressors 215 and 216 into supercooled liquid
  • the circulation of nitrogen gas for supplying cold heat required for the reliquefaction of BOG comprises the steps of passing nitrogen gas with a pressure of 14 bars and a temperature of 35.4 0 C through the three-stage compressor 221, 222 and 223 and the intermediate coolers 225, 226 and 227 to increase the pressure of the nitrogen gas to a pressure of 58 bars at a temperature of 43 0 C (ST 219); internally heat-exchanging the high-pressure nitrogen gas with nitrogen gas in the low- temperature section of the second nitrogen heat exchanger 234 to convert the high- pressure nitrogen gas into nitrogen gas with a low temperature of -83.5 0 C and a pressure of 57.3 bars (ST 220); converting a portion of the high-pressure nitrogen gas into low temperature and pressure gas with a low temperature of -14O 0 C and a low pressure of 14.5 bars by passing the portion of the high-pressure nitrogen through the expansion turbine 236 (ST 221); converting nitrogen gas, which has not been transferred to the expansion turbine 236, into nitrogen with a pressure of 57.5 bars and
  • the pressure of a storage tank can be stably maintained without a loss of stored LNG during a voyage of an LNG carrier.
  • the size of the apparatus for reliquefying LNG BOG can be reduced by employing the simple cold box module and the cryogenic range of the nitrogen gas can be stably managed.
  • FIG. 8 is a view showing a configuration of the apparatus for reliquefying LNG BOG according to the third embodiment of the present invention.
  • This apparatus comprises a BOG cycle device, a nitrogen cycle device and a cold box device interfacing these two devices.
  • Natural gas in a gaseous phase is cryogenically liquefied and stored in a storage tank 310 under an atmospheric pressure (1.013 bars).
  • BOG is generated due to continuous heat transfer from the outside, thereby increasing pressure in the storage tank 310.
  • a safety valve 311 is opened and BOG is discharged outside of the storage tank 310 if the pressure in the storage tank 310 reaches about 1.03 bars, and the discharged BOG passes through two-stage bog compressor 315 and 316 and is then subjected to a reliquef action process.
  • a temperature sensor 312 sensed by a temperature sensor 312 and be controlled to a predetermined temperature through a temperature controller 314, and BOG then flow into the two- stage bog compressor 315 and 316.
  • BOG that has passed through the temperature controller 314 is maintained in a superheated vapor state at a pressure of 1.03 bars and a temperature of -12O 0 C.
  • cryogenic BOG LNG
  • the temperature of BOG can be controlled.
  • the amount of BOG re-circulated is controlled by adjusting the degree of opening of a recirculation valve 313.
  • LNG in the storage tank 310 may be supplied to be mixed with BOG compressed by the BOG compressors 315 and 316, thereby lowering or controlling the temperature of BOG to be supplied into a BOG condenser 331.
  • the temperature controller is operated only until the reliquefaction apparatus reaches a normal state, the recirculation valve 313 is then closed and the cryogenic reliquefied LNG is guided to the storage tank 310.
  • BOG discharged from the two-stage bog compressor 315 and 316 is pre-cooled while passing through the first nitrogen heat exchanger 333 with three paths formed therein, so that BOG is in a superheated vapor state at a pressure of 3.3 bars and a temperature of -134 0 C.
  • BOG is cooled in the first nitrogen heat exchanger 333 through heat exchange with nitrogen gas that is obtained by mixing low-pressure and low-temperature nitrogen gas discharged from the BOG condenser 331 to be described below with nitrogen gas which is in a cryogenic state by the expansion turbine 336.
  • the pre-cooled BOG passes through the BOG condenser 331 and is then converted to be in a supercooled liquid state at a pressure of 3.0 bars and a temperature of -154.7 0 C, it flows back into the storage tank 310 or is re-circulated to the temperature controller 314.
  • the BOG condenser 331 will be described in detail below in connection with the cold box device.
  • BOG is pre-cooled by the low-temperature working fluid (nitrogen) as above, there is an advantage in that even though the quantity or temperature of BOG generated is changed, a temperature difference between BOG and nitrogen gas in the BOG condenser 331 can be constantly maintained in a pre-set range.
  • Such a mixture of gas and liquid is divided into gas and liquid in a BOG non- condensed gas separator 318, so that the liquid (condensed BOG) flows back into the storage tank 310 or is re-circulated to the temperature controller 314 by a circulation pump 319 and gas is generally discharged to the outside.
  • Methods of causing BOG to flow back into the storage tank 310 include a method of spaying BOG through a spray head above the storage tank, a method of supplying BOG to the bottom of the storage tank, and the like. If BOG flows back to the bottom of the storage tank, a nitrogen component that is contained in non-condensed gas included in the condensed BOG is dissolved in LNG so that the ratio of nitrogen in the gaseous phase is maintained at a lower value. Since the liquefaction temperature of nitrogen is lower than that of methane that is a main component of LNG, an increase in the content of nitrogen in BOG can reduce a load applied to the two- stage bog compressor 315 and 316 or the BOG condenser 331.
  • BOG and cryogenic nitrogen gas The following description is made in connection with a cycle device for obtaining cryogenic nitrogen gas required for the reliquefaction of BOG.
  • a portion of the cooled nitrogen gas that has passed through the second nitrogen heat exchanger 334 has reduced temperature while passing through an expansion turbine 336, and the nitrogen gas of which the temperature is lowered is mixed with nitrogen which is returned while having passed through the BOG condenser 331.
  • the resulting nitrogen gas is introduced into the first nitrogen heat exchanger 333.
  • the high-pressure nitrogen gas be further cooled through inner heat exchange with high-pressure nitrogen gas, which is partially cooled in the second nitrogen heat exchanger 334, in the first nitrogen heat exchanger 333.
  • the high-pressure nitrogen gas of which the temperature is lowered in the first nitrogen heat exchanger 333 passes through the expansion valve 337 and is ultimately converted into cryogenic nitrogen gas with a temperature of 62.6 0 C required for reliquefaction of BOG.
  • This cryogenic nitrogen gas is heat-exchanged with BOG in the BOG condenser 331 to liquefy BOG and accordingly has increased temperature.
  • a nitrogen buffer tank 320 performs the function of adjusting a mass flow rate in the nitrogen cycle in response to changes in the reliquefied amount of BOG, i.e., changes in a cooling load of the nitrogen cycle.
  • a source for supplying a supplementary working fluid (nitrogen) may be further provided against a case where the amount of nitrogen is reduced.
  • the cold box device 330 comprises the BOG condenser 331 in which the reliq- uefaction of BOG is performed, the nitrogen heat exchangers 333 and 334 in which inner heat exchange between a high temperature section and a lower temperature section of the nitrogen cycle is carried out and BOG is pre-cooled, the expansion valve 337 in which cryogenic nitrogen gas is obtained, and the expansion turbine 336 in which low-temperature nitrogen gas required for inner heat exchange is obtained.
  • a generator G that is not an essential element of the present invention may be coupled to the expansion turbine 336 to generate electric power that in tune is used as an auxiliary power source for the BOG compressors 315 and 316, the nitrogen compressors 321, 322 and 323, or the like.
  • the aforementioned devices may be incorporated into the cold box 330 as one module, so that pipes for connecting the devices can be shortened.
  • This enables cryogenic nitrogen required for the reliquefaction of BOG to be secured stably. That is, since the length of a connecting pipe between the second nitrogen heat exchanger 334 and the inlet of the expansion turbine 336 or the length of a connecting pipe between the first nitrogen heat exchanger 333 and the inlet of the expansion valve 337 is shortened, a cryogenic condition of nitrogen at the outlet of the expansion turbine 336 or expansion valve 337 that may be sensitive to the condition or temperature of nitrogen at the inlet of the expansion turbine 336 or expansion valve 337 can be stabilized. Further, since the length of a connecting pipe between the BOG condenser 331 and the outlet of the expansion valve 337 is shortened, it is possible to expect that an increase in the temperature of the nitrogen gas caused by the transfer of the nitrogen gas is minimized.
  • the BOG condenser 331 which is at low temperature, the nitrogen heat exchangers 333 and 334, and the expansion means 336 and 337 be constructed into one cold box device 330 and these components be insulated as one module.
  • the insulation is achieved by generally known insulating materials. Due to this configuration, a cryogenic range of the nitrogen gas can be stably managed.
  • the cold box device 330 may be manufactured as a pre-assembly to facilitate mounting thereof on a ship.
  • the process of the reliquefaction apparatus comprises the steps of compressing BOG generated in the storage tank 310 for LNG; pressurizing and cooling nitrogen gas which is a working fluid, so as to provide cold heat used for condensing the compressed BOG and expanding the pressurized and cooled nitrogen gas to generate cryogenic nitrogen gas; at least partially condensing the compressed BOG through heat exchange with the cryogenic nitrogen gas; and returning BOG reliquefied by means of the condensation to the storage tank.
  • BOG is circulated through a process comprising the steps of passing BOG, which is discharged after a valve 311 is opened at a predetermined pressure, through the temperature controller 314 and constantly maintaining BOG at a pressure of 1.03 bars and a temperature of -12O 0 C at the inlet of the two-stage bog compressor 315 and 316 (ST 311); compressing BOG in the two-stage compressor 315 and 316 to a pressure of 3.6 bars and a temperature of -43 0 C so that BOG is in a high temperature and pressure superheated state (ST 312); passing BOG through the first nitrogen heat exchanger 333, which is a pre-cooling cold heat exchanger with three paths formed therein, to lower (pre-cool) the temperature of BOG to -134 0 C at a pressure of 3.3 bars (ST 313); reliquef
  • the circulation of nitrogen gas for supplying cold heat required for the reliquefaction of BOG comprises the steps of passing nitrogen gas with a pressure of 14.3 bars and a temperature of 36.08 0 C through the three-stage compressor 321, 322 and 323 and the intermediate coolers 325, 326 and 327 to increase the pressure of the nitrogen gas to a pressure of 58 bars at a temperature of 43 0 C (ST 319); internally heat-exchanging the high-pressure nitrogen gas with nitrogen gas in the low-temperature section of the second nitrogen heat exchanger 334 to convert the high-pressure nitrogen gas into nitrogen gas with a low temperature of -7O 0 C and a pressure of 57.7 bars (ST 320); converting a portion of the high-pressure nitrogen gas into low temperature and pressure gas with a low temperature of -129.3 0 C and a low pressure of 15.2 bars by passing the portion of the high-pressure nitrogen through the expansion turbine 336 (ST 321); converting nitrogen gas, which has not been transferred to the expansion turbine 336, into nitrogen with
  • the step of separating non-condensed gas contained in the reliquefied BOG (ST 315) may be further provided.
  • the reliquefied BOG may be transferred to the storage tank 310 in the step of pressurizing the reliquefied BOG by the circulation pump 319 (ST 316).
  • a portion of the reliquefied BOG may be re-circulated while passing through the recirculation valve 313 and the temperature controller 314 (ST 317) and then supplied to a step before or after the step of compressing BOG (ST 312) so as to pre-cool BOG.
  • the third embodiment of the present invention it is possible to solve a problem in a conventional BOG reliquefaction system utilizing a reverse Brayton cycle of nitrogen, in which if the temperature of nitrogen is lowered using an expansion turbine, a portion of nitrogen is liquefied, causing damage to blades of the expansion turbine.
  • a portion of pressurized nitrogen is extracted and expanded through the expansion turbine 336, the temperature of the remainder of nitrogen is lowered and is then further lowered through the expansion valve 337 so that the temperature of nitrogen can be lowered without a risk of generation of liquid droplets.
  • the operation of a nitrogen cycle can be changed variously by changing a flow rate of nitrogen supplied to the expansion valve 337, and thus, it is possible to easily and rapidly cope with dynamic changes of BOG, i.e., changes of load.
  • the pressure of a storage tank can be stably maintained without a loss of stored LNG during a voyage of an LNG carrier.
  • the size of the apparatus for reliquefying LNG BOG can be reduced by employing the simple cold box module and the cryogenic range of the nitrogen gas can be stably managed.
  • FIG. 11 is a view showing a configuration of the apparatus for reliquefying LNG
  • This apparatus comprises a BOG cycle device, a nitrogen cycle device and a cold box device interfacing these two devices.
  • Natural gas in a gaseous phase is cryogenically liquefied and stored in a storage tank 410 under an atmospheric pressure (1.013 bars).
  • BOG is generated due to continuous heat transfer from the outside, thereby increasing pressure in the storage tank 410.
  • a safety valve 411 is opened and BOG is discharged outside of the storage tank 410 if the pressure in the storage tank 410 reaches about 1.03 bars, and the discharged BOG passes through two-stage bog compressor 415 and 416 and is then subjected to a reliquef action process.
  • a temperature sensor 412 senses a temperature sensor 412 and be controlled to a predetermined temperature through a temperature controller 414, and BOG then flow into the two- stage bog compressor 415 and 416.
  • BOG that has passed through the temperature controller 414 is maintained in a superheated vapor state at a pressure of 1.03 bars and a temperature of -12O 0 C.
  • cryogenic BOG LNG
  • the temperature of BOG can be controlled.
  • the amount of BOG re-circulated is controlled by adjusting the degree of opening of a recirculation valve 413.
  • LNG in the storage tank 410 may be supplied to be mixed with BOG compressed by the BOG compressors 415 and 416, thereby lowering or controlling the temperature of BOG to be supplied into a BOG condenser.
  • the temperature controller is operated only until the reliquefaction apparatus reaches a normal state, the recirculation valve 413 is then closed and the cryogenic reliquefied LNG is guided to the storage tank 410.
  • BOG discharged from the two-stage bog compressor 415 and 416 is pre-cooled while passing through a first nitrogen heat exchanger 433 with three paths formed therein, so that BOG is in a superheated vapor state at a pressure of 3.1 bars and a temperature of -13O 0 C.
  • BOG is cooled in the first nitrogen heat exchanger 433 through heat exchange with nitrogen gas that is obtained by mixing low-pressure and low-temperature nitrogen gas discharged from the BOG condenser 431 to be described below with nitrogen gas which is in a cryogenic state by the expansion turbine 436.
  • the pre-cooled BOG passes through the BOG condenser 431 and is then converted to be in a supercooled liquid state at a pressure of 3.0 bars and a temperature of -154.7 0 C, it flows back into the storage tank 410 or is re-circulated to the temperature controller 414.
  • the BOG condenser 431 will be described in detail below in connection with the cold box device. Since BOG is pre-cooled by the low- temperature working fluid (nitrogen) as above, there is an advantage in that even though the quantity or temperature of BOG generated is changed, a temperature difference between BOG and nitrogen gas in the BOG condenser 431 can be constantly maintained in a pre-set range.
  • Such a mixture of gas and liquid is divided into gas and liquid in a BOG non- condensed gas separator 418, so that the liquid (condensed BOG) flows back into the storage tank 410 or is re-circulated to the temperature controller 414 by a circulation pump 419 and gas is generally discharged to the outside.
  • Methods of causing BOG to flow back into the storage tank 410 include a method of spaying BOG through a spray head above the storage tank, a method of supplying BOG to the bottom of the storage tank, and the like. If BOG flows back to the bottom of the storage tank, a nitrogen component that is contained in non-condensed gas included in the condensed BOG is dissolved in LNG so that the ratio of nitrogen in the gaseous phase is maintained at a lower value. Since the liquefaction temperature of nitrogen is lower than that of methane that is a main component of LNG, an increase in the content of nitrogen in BOG can reduce a load applied to the two- stage bog compressor 415 and 416 or the BOG condenser 431.
  • BOG is reliquefied in the BOG condenser 431 by means of heat exchange between
  • BOG and cryogenic nitrogen gas The following description is made in connection with a cycle device for obtaining cryogenic nitrogen gas required for the reliquefaction of BOG.
  • the nitrogen gas is cooled to a temperature of -77 0 C at a pressure 57.9 bars by means of inner heat exchange with low-pressure nitrogen in a low temperature section, which is returned while having passed through the BOG condenser 431 and a third nitrogen heat exchanger 435 and through a first nitrogen heat exchanger 433, in a second nitrogen heat exchanger 434.
  • the nitrogen gas which has passed through the first nitrogen heat exchanger 433, is heat-exchanged with the stream of nitrogen gas, which has passed through the BOG condenser 431, in the third nitrogen heat exchanger 435 and then discharged as gas with a pressure of 57.7 bars and a temperature of -137 0 C.
  • Such a cooling process is advantageous to reduction in the temperature of the high-pressure nitrogen gas to a preset temperature required at an inlet of the expansion valve 437.
  • the high-pressure nitrogen gas of which the temperature is lowered in the third nitrogen heat exchanger 435 passes through the expansion valve 437 and is cooed ultimately to a temperature of -163.3 0 C to be converted into a cryogenic ideal stream required for reliquefaction of BOG.
  • the cryogenic nitrogen gas is heat-exchanged with BOG in the BOG condenser 431 to reliquefy BOG and has increased temperature.
  • the provision of the third nitrogen heat exchanger 435 allows the temperature of nitrogen at the inlet of the expansion valve 437 to be more stably managed and enables great reduction in the size of each of the nitrogen heat exchangers. Consequently, there is an advantage in that the size of the cold box 430 can be reduced.
  • a nitrogen buffer tank 420 performs the function of adjusting a mass flow rate in the nitrogen cycle in response to changes in the reliquefied amount of BOG, i.e., changes in a cooling load of the nitrogen cycle.
  • a source for supplying a supplementary working fluid (nitrogen) may be further provided against a case where the amount of nitrogen is reduced.
  • the cold box device 430 comprises the BOG condenser 431 in which the reliq- uefaction of BOG is performed, the nitrogen heat exchangers 433, 434 and 435 in which inner heat exchange between a high temperature section and a lower temperature section of the nitrogen cycle is carried out and BOG is pre-cooled, the expansion valve 437 in which cryogenic nitrogen gas is obtained, and the expansion turbine 436 in which low-temperature nitrogen gas required for inner heat exchange is obtained.
  • a generator G that is not an essential element of the present invention may be coupled to the expansion turbine 436 to generate electric power that in tune is used as an auxiliary power source for the BOG compressors 415 and 416, the nitrogen compressors 421, 422 and 423, or the like.
  • the aforementioned devices may be incorporated into the cold box 430 as one module, so that pipes for connecting the devices can be shortened.
  • This enables cryogenic nitrogen required for the reliquefaction of BOG to be secured stably. That is, since the length of a connecting pipe between the second nitrogen heat exchanger 434 and the inlet of the expansion turbine 436 and the length of a connecting pipe between an outlet of the third nitrogen heat exchanger 435 and the inlet of the expansion valve 437 are shortened, a cryogenic condition of nitrogen at the outlet of the expansion turbine 436 or expansion valve 437 that may be sensitive to the condition or temperature of nitrogen at the inlet of the expansion turbine 436 or expansion valve 437 can be stabilized. Further, since the length of a connecting pipe between the BOG condenser 431 and the outlet of the expansion valve 437 is shortened, it is possible to expect that an increase in the temperature of the nitrogen gas caused by the transfer of the nitrogen gas is minimized.
  • the BOG condenser 431 which is at low temperature, the nitrogen heat exchangers 433, 434 and 435, and the expansion means 436 and 437 be constructed into one cold box device 430 and these components be insulated as one module.
  • the insulation is achieved by generally known insulating materials. Due to this configuration, a cryogenic range of the nitrogen gas can be stably managed.
  • the cold box device 430 may be manufactured as a pre-assembly to facilitate mounting thereof on a ship.
  • the process of the reliquefaction apparatus comprises the steps of compressing BOG generated in the storage tank 410 for LNG; pressurizing and cooling nitrogen gas which is a working fluid, so as to provide cold heat used for condensing the compressed BOG and expanding the pressurized and cooled nitrogen gas to generate cryogenic nitrogen gas; condensing the compressed BOG through heat exchange with the cryogenic nitrogen gas; and returning BOG reliquefied by means of the condensation to the storage tank 410.
  • BOG is circulated through a process comprising the steps of passing BOG, which is discharged after a valve 411 is opened at a predetermined pressure, through the temperature controller 414 and constantly maintaining BOG at a pressure of 1.03 bars and a temperature of -12O 0 C at the inlet of the two-stage bog compressor 415 and 416 (ST 411); compressing BOG in the two-stage compressor 415 and 416 to a pressure of 3.2 bars and a temperature of -50.83 0 C so that BOG is in a high temperature and pressure superheated state (ST 412); passing BOG through the first nitrogen heat exchanger 433, which is a pre-cooling cold heat exchanger with three paths formed therein, to lower (pre-cool) the temperature of BOG to -13O 0 C at a pressure of 3.1 bars (ST 413);
  • the circulation of nitrogen gas for supplying cold heat required for the reliquef action of BOG comprises the steps of passing nitrogen gas with a pressure of 14.2 bars and a temperature of 35.46 0 C through the three-stage nitrogen compressors 421, 422 and 423 and the intermediate coolers 425, 426 and 427 to increase the pressure of the nitrogen gas to a pressure of 58 bars at a temperature of 43 0 C (ST 419); internally heat- exchanging the high-pressure nitrogen gas with nitrogen gas in the low-temperature section of the second nitrogen heat exchanger 434 to convert the high-pressure nit rogen gas into nitrogen gas with a low temperature of -77 0 C and a pressure of 57.9 bars (ST 420); converting a portion of the high-pressure nitrogen gas into low temperature and pressure gas with a low temperature of -129.3 0 C and a low pressure of 15.2 bars by passing the portion of the high-pressure nitrogen through the expansion turbine 436 (ST 421); converting nitrogen gas, which has not been transferred to the expansion
  • the step of separating non-condensed gas contained in the reliquefied BOG (ST 415) may be further provided.
  • the reliquefied BOG may be transferred to the storage tank 410 in the step of pressurizing the reliquefied BOG by the circulation pump 419 (ST 416).
  • a portion of the reliquefied BOG may be re-circulated while passing through the recirculation valve 413 and the temperature controller 414 (ST 417) and then supplied to a step before or after the step of compressing BOG (ST 412) so as to pre-cool BOG.
  • the fourth embodiment of the present invention it is possible to solve a problem in a conventional BOG reliquefaction system utilizing a reverse Brayton cycle of nitrogen, in which if the temperature of nitrogen is lowered using an expansion turbine, a portion of nitrogen is liquefied, causing damage to blades of the expansion turbine.
  • a portion of pressurized nitrogen is extracted and expanded through the expansion turbine 436, the temperature of the remainder of nitrogen is lowered and is then further lowered through the expansion valve 437 so that the temperature of nitrogen can be lowered without a risk of generation of liquid droplets.
  • the operation of a nitrogen cycle can be changed variously by changing a flow rate of nitrogen supplied to the expansion valve 437, and thus, it is possible to easily and rapidly cope with dynamic changes of BOG, i.e., changes of load.
  • the pressure of a storage tank can be stably maintained without a loss of stored LNG during a voyage of an LNG carrier.
  • the size of the apparatus for reliquefying LNG BOG can be reduced by employing the simple cold box module and the cryogenic range of the nitrogen gas can be stably managed.
  • the cryogenic condition of the outlet of the expansion valve 437 which is sensitive to the condition or temperature of the inlet of the expansion valve 437 can be stabilized.
  • the length of the connecting pipe between the BOG condenser 431 and the outlet of the expansion valve 437 is shortened, it is possible to minimize an increase in temperature produced upon delivery of the cryogenic nitrogen gas, and it is possible to prevent a loss of cold heat by incorporating the unit elements constituting the low temperature section into the cold box device 430 in the apparatus for reliquefying LNG BOG and managing the cold box device.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Ocean & Marine Engineering (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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  • Oil, Petroleum & Natural Gas (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
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Abstract

L’invention concerne un appareil de reliquéfaction de gaz d’évaporats (BOG) générés dans un réservoir de stockage d’un vaisseau destiné au transport de gaz naturel liquéfié (LNG) cryogénique. Selon la présente invention, dans un appareil de reliquéfaction de BOG de LNG, comprenant un compresseur destiné à la compression du BOG généré dans un réservoir de stockage destiné au LNG, un condensateur destiné à la condensation au moins partielle du BOG compressé par le compresseur, et un dispositif de cycle d’azote destiné à fournir de la chaleur froide au compresseur, de manière à retourner dans le réservoir de stockage le BOG reliquéfié par le condensateur, le BOG compressé par le compresseur est soumis à un pré-refroidissement en amont du condensateur, et ainsi, l’on procure un avantage en ce qu’il est possible de constamment maintenir la température du BOG dans une plage prédéfinie même en cas de modification de la quantité ou de la température du BOG généré. En outre, selon la présente invention, il est possible de réduire la taille de l’appareil de reliquéfaction de BOG de LNG et de gérer de manière stable une plage cryogénique de gaz azote sans perte de chaleur froide in incorporant des éléments unitaires constituant une section à basse température dans un dispositif de boîte froide au sein de l’appareil de reliquéfaction de BOG de LNG.
PCT/KR2006/002818 2005-07-19 2006-07-19 Appareil de reliquéfaction de gaz d’évaporats de gaz naturel liquéfié WO2007011155A1 (fr)

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JP2008522699A JP2009501896A (ja) 2005-07-19 2006-07-19 Ｌｎｇｂｏｇ再液化装置
EP06783336A EP1913117A1 (fr) 2005-07-19 2006-07-19 Appareil de reliquéfaction de gaz d évaporats de gaz naturel liquéfié

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KR10-2005-0065501 2005-07-19
KR1020050065501 2005-07-19
KR1020050078588A KR100740686B1 (ko) 2005-08-26 2005-08-26 Ｂｏｇ 재액화 장치
KR10-2005-0078588 2005-08-26
KR1020050109931A KR100699163B1 (ko) 2005-11-17 2005-11-17 Ｌｎｇ ｂｏｇ의 재액화 장치 및 재액화 방법
KR10-2005-0109931 2005-11-17
KR1020060001271A KR100681319B1 (ko) 2006-01-05 2006-01-05 Ｂｏｇ 재액화 장치
KR10-2006-0001271 2006-01-05

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WO2011062505A1 (fr) * 2009-11-17 2011-05-26 Hamworthy Gas Systems As Installation pour récupérer du gaz évaporé (bog) à partir de gaz naturel liquéfié (lng) stocké dans des réservoirs
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JP2012516263A (ja) * 2009-03-03 2012-07-19 エスティーエックス オフショア・アンド・シップビルディング カンパニー リミテッド 再液化機能を有する電気推進ｌｎｇ運搬船の蒸発ガス処理装置及び方法
EP2594839A3 (fr) * 2011-11-17 2013-07-10 Air Products And Chemicals, Inc. Procédés et ensembles de compresseur afin de réduire au minimum l'évacuation d'un gaz de processus pendant des opérations de démarrage
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CN105066582A (zh) * 2015-07-15 2015-11-18 中国石油大学(北京) 一种利用管网压力能制取液化甲烷气的方法
WO2017037400A1 (fr) * 2015-09-03 2017-03-09 Cryostar Sas Système et procédé de traitement de gaz issu de l'évaporation d'un liquide cryogénique
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US9879906B2 (en) 2008-05-20 2018-01-30 Michiel Gijsbert Van Aken Method of cooling and liquefying a hydrocarbon stream, an apparatus therefor, and a floating structure, caisson or off-shore platform comprising such an apparatus
US10132561B2 (en) 2009-08-13 2018-11-20 Air Products And Chemicals, Inc. Refrigerant composition control
US10145514B2 (en) 2013-11-18 2018-12-04 Man Energy Solutions Se Cold-box system and method for power management aboard ships
JP2018538197A (ja) * 2015-12-14 2018-12-27 エクソンモービル アップストリーム リサーチ カンパニー 液体窒素を貯蔵するｌｎｇ運搬船上の天然ガス液化の方法
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JP2009533642A (ja) * 2006-04-07 2009-09-17 ハムワージー・ガス・システムズ・エイ・エス 再液化システムにおいて圧縮より前にボイルオフガスを周囲温度に予熱するための方法及び装置
WO2007144774A3 (fr) * 2006-05-23 2008-10-16 Cryostar Sas Procédé et appareil de reliquéfaction d'une vapeur
WO2007144774A2 (fr) * 2006-05-23 2007-12-21 Cryostar Sas Procédé et appareil de reliquéfaction d'une vapeur
EP1959217A2 (fr) * 2007-02-13 2008-08-20 Daewoo Shipbuilding & Marine Engineering Co., Ltd Appareil et procédé pour reliquéfier un vaporisat capable de fonctionner à une charge de réfrigération variable
EP1959217A3 (fr) * 2007-02-13 2012-08-01 Daewoo Shipbuilding & Marine Engineering Co., Ltd Appareil et procédé pour reliquéfier un vaporisat capable de fonctionner à une charge de réfrigération variable
US9879906B2 (en) 2008-05-20 2018-01-30 Michiel Gijsbert Van Aken Method of cooling and liquefying a hydrocarbon stream, an apparatus therefor, and a floating structure, caisson or off-shore platform comprising such an apparatus
CN101614464B (zh) * 2008-06-23 2011-07-06 杭州福斯达实业集团有限公司 高低温氮气双膨胀天然气液化方法
JP2010025152A (ja) * 2008-07-15 2010-02-04 Mitsubishi Heavy Ind Ltd 天然ガス処理設備および液化天然ガス運搬船
JP2012516263A (ja) * 2009-03-03 2012-07-19 エスティーエックス オフショア・アンド・シップビルディング カンパニー リミテッド 再液化機能を有する電気推進ｌｎｇ運搬船の蒸発ガス処理装置及び方法
WO2010108464A3 (fr) * 2009-03-27 2013-12-12 Marine Service Gmbh Procédé et dispositif pour faire fonctionner un moteur d'entraînement d'un navire destiné au transport de gaz liquide
WO2010108464A2 (fr) * 2009-03-27 2010-09-30 Marine Service Gmbh Procédé et dispositif pour faire fonctionner un moteur d'entraînement d'un navire destiné au transport de gaz liquide
US9851141B2 (en) 2009-07-02 2017-12-26 Bluewater Energy Services B.V. Pressure control of gas liquefaction system after shutdown
US10132561B2 (en) 2009-08-13 2018-11-20 Air Products And Chemicals, Inc. Refrigerant composition control
WO2011062505A1 (fr) * 2009-11-17 2011-05-26 Hamworthy Gas Systems As Installation pour récupérer du gaz évaporé (bog) à partir de gaz naturel liquéfié (lng) stocké dans des réservoirs
CN102230570A (zh) * 2011-06-29 2011-11-02 中国寰球工程公司 一种液化天然气转运站的蒸发气回收系统和方法
EP2775194A4 (fr) * 2011-10-20 2015-10-28 Mitsubishi Heavy Ind Ltd Dispositif de suppression de hausse de pression pour réservoir de stockage, système de suppression de hausse de pression pourvu de celui-ci, procédé de suppression s'y rapportant, récipient de transport de gaz liquéfié pourvu de celui-ci et installation de stockage de gaz liquéfié pourvue de celui-ci
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
EP2594839A3 (fr) * 2011-11-17 2013-07-10 Air Products And Chemicals, Inc. Procédés et ensembles de compresseur afin de réduire au minimum l'évacuation d'un gaz de processus pendant des opérations de démarrage
US10145514B2 (en) 2013-11-18 2018-12-04 Man Energy Solutions Se Cold-box system and method for power management aboard ships
US11118734B2 (en) 2013-11-18 2021-09-14 Man Energy Solutions Se Cold-box system and apparatus for power management aboard ships
CN104456071A (zh) * 2014-12-08 2015-03-25 日照海达尔加气设备有限公司 一种液化天然气槽车卸载装置和方法
AU2015388393B2 (en) * 2015-03-26 2019-10-10 Chiyoda Corporation Natural gas production system and method
US10995910B2 (en) 2015-07-13 2021-05-04 Technip France Process for expansion and storage of a flow of liquefied natural gas from a natural gas liquefaction plant, and associated plant
CN105066582A (zh) * 2015-07-15 2015-11-18 中国石油大学(北京) 一种利用管网压力能制取液化甲烷气的方法
WO2017037400A1 (fr) * 2015-09-03 2017-03-09 Cryostar Sas Système et procédé de traitement de gaz issu de l'évaporation d'un liquide cryogénique
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