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JP2002295799A - Method and system for treating liquefied natural gas and nitrogen - Google Patents

Method and system for treating liquefied natural gas and nitrogen

Info

Publication number
JP2002295799A
JP2002295799A JP2001104398A JP2001104398A JP2002295799A JP 2002295799 A JP2002295799 A JP 2002295799A JP 2001104398 A JP2001104398 A JP 2001104398A JP 2001104398 A JP2001104398 A JP 2001104398A JP 2002295799 A JP2002295799 A JP 2002295799A
Authority
JP
Japan
Prior art keywords
nitrogen
gas
liquefied natural
natural gas
heat exchanger
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
JP2001104398A
Other languages
Japanese (ja)
Inventor
Tatsuo Yoshida
龍生 吉田
Junichi Nakagawa
潤一 中川
Yoshimi Takiguchi
好美 滝口
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Kobe Steel Ltd
Original Assignee
Kobe Steel 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
Application filed by Kobe Steel Ltd filed Critical Kobe Steel Ltd
Priority to JP2001104398A priority Critical patent/JP2002295799A/en
Publication of JP2002295799A publication Critical patent/JP2002295799A/en
Withdrawn legal-status Critical Current

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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
    • F25J1/0002—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
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0234—Integration with a cryogenic air separation unit
    • 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
    • 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
    • F25J1/0269—Arrangement of liquefaction units or equipments fulfilling the same process step, e.g. multiple "trains" concept
    • F25J1/0271—Inter-connecting multiple cold equipments within or downstream of the cold box
    • F25J1/0272—Multiple identical heat exchangers 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
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • F25J3/0426—The cryogenic component does not participate in the fractionation
    • F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • F25J3/04575—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for a gas expansion plant, e.g. dilution of the combustion gas in a gas turbine
    • F25J3/04581—Hot gas expansion of indirect heated 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
    • 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
    • F25J2210/42—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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or 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
    • F25J2240/90—Hot gas waste turbine of an indirect heated gas for power generation
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/42—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery
    • F25J2260/44—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery using nitrogen for cooling purposes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

PROBLEM TO BE SOLVED: To efficiently perform the condensation and reduction of BOG, and the vaporization and collection of liquid nitrogen, and control the fluctuation of the quantity of BOG. SOLUTION: An LNG storage tank 14 and a liquid nitrogen tank 32A connected to an air separator 30 are provided. Liquid nitrogen of appropriate quantity is pumped to a heat exchanger 20 for generating gaseous nitrogen from the liquid nitrogen tank 32A to a pump 34A. The vaporization of liquid nitrogen and condensation of BOG are simultaneously performed by performing heat exchange of the liquid nitrogen and BOG by the heat exchanger 20, the obtained BOG is reduced to the LNG storage tank, and the gaseous nitrogen is collected to a gas holder 42 as product nitrogen.

Description

【発明の詳細な説明】DETAILED DESCRIPTION OF THE INVENTION

【０００１】[0001]

【発明の属する技術分野】本発明は、液化天然ガス（以
下、ＬＮＧと称する。）を収容する貯槽内のボイルオフ
ガス（以下、ＢＯＧと称する。）を凝縮して還元すると
同時に、製品窒素ガスを生成し回収する方法及びシステ
ムに関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention condenses and reduces boil-off gas (hereinafter, referred to as BOG) in a storage tank containing liquefied natural gas (hereinafter, referred to as LNG) and simultaneously reduces product nitrogen gas. A method and system for generating and collecting.

【０００２】[0002]

【従来の技術】一般に、ＬＮＧ基地に貯蔵されたＬＮＧ
は、専用のポンプで昇圧された後、ＬＮＧ蒸発器で蒸発
され、天然ガス（以下、ＮＧと称する。）として需要地
へ供給される。2. Description of the Related Art Generally, LNG stored in an LNG base is known.
Is pressurized by a dedicated pump, then evaporated by an LNG evaporator, and supplied to a demand area as natural gas (hereinafter, referred to as NG).

【０００３】このＬＮＧ供給システムにおいて、上記Ｌ
ＮＧ貯槽内でＬＮＧから蒸発したメタンガスを主成分と
するＢＯＧについては、このＢＯＧを上記液化天然ガス
貯槽から抜き出して圧縮機で昇圧し、天然ガス（以下、
ＮＧと称する。）に混合して利用に供することが可能で
ある。しかし、その抜き出しを続けると貯槽内ＬＮＧの
メタン成分が減ってそれ以外の成分の濃度が上昇する
（すなわちＬＮＧが濃縮される）ことになり、その濃縮
が進むとＬＮＧの熱量が大きくなり過ぎて調整が困難に
なるおそれがある。In this LNG supply system, the L
With respect to BOG mainly composed of methane gas evaporated from LNG in the NG storage tank, the BOG is extracted from the liquefied natural gas storage tank, pressurized by a compressor, and compressed with natural gas (hereinafter, referred to as “natural gas”).
NG. ) Can be used as a mixture. However, if the extraction is continued, the methane component of LNG in the storage tank decreases, and the concentration of other components increases (that is, LNG is concentrated). As the concentration progresses, the calorific value of LNG becomes too large. Adjustment may be difficult.

【０００４】そこで、このようなＬＮＧ等の濃縮を防ぐ
べく、ＢＯＧを一旦ＬＮＧ貯槽から抜き出した後、これ
を凝縮してＬＮＧ貯槽に還元する方法及び装置の開発が
進められている。例えば、特開平９−６０７９９号公報
には、ＬＮＧ貯槽内から抜き出したＢＯＧをＢＯＧ圧縮
機で圧縮し、この圧縮により当該ＢＯＧの凝縮温度を高
めた状態で当該ＢＯＧと前記ＬＮＧ貯槽から抜き出した
ＬＮＧとを熱交換させることによりＢＯＧを凝縮させる
技術が開示されている。[0004] In order to prevent such concentration of LNG or the like, a method and apparatus for once extracting BOG from the LNG storage tank, condensing it, and reducing it to the LNG storage tank are being developed. For example, Japanese Patent Application Laid-Open No. 9-60799 discloses that BOG extracted from the LNG storage tank is compressed by a BOG compressor, and the BOG and the LNG extracted from the LNG storage tank in a state where the condensation temperature of the BOG is increased by this compression. A technology is disclosed in which BOG is condensed by exchanging heat with BOG.

【０００５】[0005]

【発明が解決しようとする課題】前記公報に記載の装置
では、ＢＯＧをこれとほぼ同成分のＬＮＧと熱交換させ
ることにより凝縮させようとするものであるため、当該
凝縮を可能にするには、ＢＯＧの圧力を上げてその凝縮
温度を高くしなければならず、そのために高価な低温運
転用のＢＯＧ圧縮機を何台も用意しなければならない不
都合がある。また、当該ＢＯＧの圧縮によりＢＯＧの保
有する冷熱が奪われるため、その分熱効率が下がる欠点
もある。In the apparatus described in the above-mentioned publication, BOG is condensed by exchanging heat with LNG having substantially the same component as BOG. , The condensing temperature must be increased by increasing the pressure of the BOG, and therefore, there is a disadvantage in that many expensive BOG compressors for low-temperature operation must be prepared. In addition, the compression of the BOG deprives the BOG of cold heat, and thus has a disadvantage in that the heat efficiency is reduced accordingly.

【０００６】なお、特開昭５９−２１６７８５号公報に
は、船舶にＬＮＧ貯槽と液体窒素貯槽とを搭載し、前記
ＬＮＧ貯槽内のＢＯＧを前記液体窒素貯槽内に溜められ
ている液体窒素と熱交換させることにより当該ＢＯＧを
凝縮させる装置が開示されているが、ＢＯＧの凝縮のみ
を目的として高価な液体窒素を使用するのはコスト上好
ましくない。また、地上に設置されるＬＮＧ貯槽内にお
いては、ＢＯＧの発生量の変動が著しく、特にＬＮＧタ
ンカーの入船時等においては大量のＢＯＧが発生するこ
とになるが、前記液体窒素貯槽内でＢＯＧと熱交換する
液体窒素量は変わらない（逆に使用が進むにつれて減量
する）ので、前記ＢＯＧの発生量の急増に対応すること
は不可能である。Japanese Unexamined Patent Publication (Kokai) No. 59-216785 discloses that a ship is provided with an LNG storage tank and a liquid nitrogen storage tank, and the BOG in the LNG storage tank is combined with liquid nitrogen stored in the liquid nitrogen storage tank and heat. Although an apparatus for condensing the BOG by exchanging the BOG is disclosed, it is not preferable in terms of cost to use expensive liquid nitrogen only for the purpose of condensing the BOG. Also, in the LNG storage tank installed on the ground, the amount of BOG generated fluctuates remarkably, and a large amount of BOG is generated particularly when the LNG tanker enters the vessel, but BOG is generated in the liquid nitrogen storage tank. Since the amount of liquid nitrogen to be heat-exchanged does not change (conversely, the amount decreases as use progresses), it is impossible to cope with the sudden increase in the amount of BOG generated.

【０００７】[0007]

【課題を解決するための手段】本発明者等は、前記課題
を解決する手段として、ＢＯＧの保有する冷熱を利用す
ることにより、当該ＢＯＧの凝縮、還元と同時に製品窒
素ガスの回収を行うことに想到した。Means for Solving the Problems As a means for solving the above-mentioned problems, the present inventors utilize the cold heat of BOG to collect and reduce the BOG and simultaneously recover the product nitrogen gas. I thought.

【０００８】すなわち、本発明は、空気分離装置で精製
した液体窒素を液体窒素タンクに溜める工程と、液化天
然ガスを収容する液化天然ガス貯槽内で発生したボイル
オフガスを窒素ガス生成用熱交換器へ送出するとともに
これに見合う量の液体窒素を前記液体窒素タンクから前
記窒素ガス生成用熱交換器へポンプによって圧送するこ
とにより当該窒素ガス生成用熱交換器で前記ボイルオフ
ガスを凝縮させると同時に前記液体窒素を蒸発させる工
程と、前記ボイルオフガスの凝縮により得られた液化天
然ガスを前記液化天然ガス貯槽内に還元する工程と、前
記液体窒素の蒸発により得られた窒素ガスを製品窒素と
してガスホルダ内に回収する工程とを含む液化天然ガス
及び窒素の処理方法である。That is, the present invention provides a process for storing liquid nitrogen purified in an air separation device in a liquid nitrogen tank, and a boil-off gas generated in a liquefied natural gas storage tank for storing liquefied natural gas. The boil-off gas is condensed by the nitrogen gas generation heat exchanger by pumping liquid nitrogen in an amount corresponding to this to the liquid nitrogen tank from the liquid nitrogen tank to the nitrogen gas generation heat exchanger by pumping. Evaporating the liquid nitrogen; reducing the liquefied natural gas obtained by condensing the boil-off gas into the liquefied natural gas storage tank; and converting the nitrogen gas obtained by evaporating the liquid nitrogen into product gas into a gas holder. And a process for treating liquefied natural gas and nitrogen.

【０００９】また本発明は、液化天然ガスを収容する液
化天然ガス貯槽と、空気を分離して液体窒素を精製する
空気分離装置と、この空気分離装置に接続され、当該空
気分離装置で精製された液体窒素を収容する液体窒素タ
ンクと、前記液化天然ガス貯槽内で発生したボイルオフ
ガスと前記液体窒素タンクから送出される液体窒素とを
熱交換させるための窒素ガス生成用熱交換器と、液化天
然ガス貯槽内で発生したボイルオフガスを前記窒素ガス
生成用熱交換器に通し、この熱交換器で当該ボイルオフ
ガスの凝縮により得られた液化天然ガスを前記液化天然
ガス貯槽内に還元するボイルオフガス循環装置と、前記
液体窒素タンク内の液体窒素を前記窒素ガス生成用熱交
換器へ圧送するポンプ及び当該窒素ガス生成用熱交換器
で蒸発した窒素ガスを貯留するガスホルダを含む製品窒
素回収装置とを備えた液化天然ガス及び窒素の処理シス
テムである。Further, the present invention provides a liquefied natural gas storage tank for containing liquefied natural gas, an air separation device for separating air to purify liquid nitrogen, and an air separation device connected to the air separation device and purified by the air separation device. A liquid nitrogen tank for storing liquid nitrogen, a heat exchanger for generating nitrogen gas for exchanging heat between boil-off gas generated in the liquefied natural gas storage tank and liquid nitrogen sent from the liquid nitrogen tank, and liquefaction. The boil-off gas generated in the natural gas storage tank is passed through the heat exchanger for generating nitrogen gas, and the liquefied natural gas obtained by condensing the boil-off gas in the heat exchanger is returned to the liquefied natural gas storage tank. A circulation device, a pump for pumping liquid nitrogen in the liquid nitrogen tank to the heat exchanger for nitrogen gas generation, and a nitrogen gas evaporated by the heat exchanger for nitrogen gas generation. A processing system of the liquefied natural gas and nitrogen and a nitrogen product recovery apparatus comprising a gas holder for storing.

【００１０】以上の構成によれば、ＬＮＧ貯槽内のＢＯ
Ｇを凝縮させて還元すると同時に、その凝縮熱を利用し
て液体窒素を蒸発することにより得られた窒素ガスをガ
スホルダに回収することにより、ＢＯＧ処理と窒素ガス
の生成及び回収とを同時に実現することができる。しか
も、液体窒素タンクから圧送した液体窒素と前記ＢＯＧ
とを窒素ガス生成用熱交換器で熱交換させるようにして
いるので、例えば液体窒素貯槽内に溜められた状態の液
体窒素とＢＯＧとを熱交換させる場合に比べ熱効率が高
く、また、ＢＯＧと窒素との間には大きな沸点差がある
ため、ＢＯＧを圧縮しなくてもその凝縮及び液体窒素の
蒸発を十分に行うことが可能である。According to the above configuration, the BO in the LNG storage tank is
By condensing and reducing G, and simultaneously collecting the nitrogen gas obtained by evaporating the liquid nitrogen using the heat of condensation in a gas holder, the BOG treatment and the generation and recovery of the nitrogen gas are simultaneously realized. be able to. In addition, the liquid nitrogen pumped from the liquid nitrogen tank and the BOG
Is exchanged with a nitrogen gas generating heat exchanger, so that the heat efficiency is higher than when, for example, liquid nitrogen stored in a liquid nitrogen storage tank and BOG are heat-exchanged, and BOG and Since there is a large boiling point difference with nitrogen, it is possible to sufficiently condense BOG and evaporate liquid nitrogen without compressing BOG.

【００１１】一方、前記液体窒素タンクは空気分離装置
に接続された状態にあり、同装置から常時液体窒素の供
給を受けることが可能であるので、前記ＢＯＧの量が急
増してもこれに見合った量の液体窒素を窒素ガス生成用
熱交換器に供給することが可能であり、ＢＯＧ量の変動
に難なく対応できる。また、余剰の液体窒素は適宜タン
クローリ等で需要先に供給することが可能である。On the other hand, the liquid nitrogen tank is in a state of being connected to an air separation device, and can always receive liquid nitrogen from the air separation device. Liquid nitrogen can be supplied to the heat exchanger for nitrogen gas generation, and it is possible to cope with fluctuations in the BOG amount without difficulty. Excess liquid nitrogen can be supplied to a demand destination by a tank lorry or the like as appropriate.

【００１２】さらに、前記方法において、前記空気分離
装置内で精製された窒素ガスと前記液化天然ガス貯槽か
ら抜き出した液化天然ガスとを熱交換させることにより
当該液化天然ガスを蒸発させて天然ガスを生成すると同
時に前記窒素ガスを凝縮させて液体窒素を生成する工程
を含むようにし、また前記装置において、前記空気分離
装置内で発生する窒素ガスと前記液化天然ガス貯槽から
抜き出される液化天然ガスとを熱交換させることにより
前記窒素ガスを凝縮させて液体窒素を生成すると同時に
前記液化天然ガスを蒸発させて天然ガスを生成する天然
ガス生成用熱交換器を備えるようにすることにより、空
気分離装置での窒素の凝縮、還元を行うと同時にＮＧの
生成を行うことが可能である。Furthermore, in the above method, the natural gas is evaporated by heat-exchanging the nitrogen gas purified in the air separation device with the liquefied natural gas extracted from the liquefied natural gas storage tank to evaporate the liquefied natural gas. The method further comprises the step of condensing the nitrogen gas at the same time as the gas is produced to produce liquid nitrogen, and in the device, the nitrogen gas generated in the air separation device and the liquefied natural gas extracted from the liquefied natural gas storage tank are provided. By condensing the nitrogen gas by heat exchange to generate liquid nitrogen and simultaneously evaporating the liquefied natural gas to provide a natural gas generating heat exchanger for generating natural gas, the air separation device NG can be generated at the same time as the condensation and reduction of nitrogen at the same time.

【００１３】すなわち、この方法及び装置によれば、Ｌ
ＮＧ貯槽、空気分離装置、及び各熱交換器を含む閉じた
系内で、ＬＮＧ貯槽でのＢＯＧの凝縮・還元、窒素ガス
の生成・回収、空気分離装置における窒素ガスの凝縮
（液体窒素の生成）、及びＮＧの生成・回収を同時に実
行することが可能であり、装置台数の少ない簡素な設備
でありながら稼働率の極めて高い総合的な処理システム
を構築することができる。That is, according to this method and apparatus, L
In a closed system including the NG storage tank, the air separation device, and each heat exchanger, BOG condensation and reduction in the LNG storage tank, generation and recovery of nitrogen gas, and nitrogen gas condensation in the air separation device (liquid nitrogen generation) ) And generation and recovery of NG can be executed simultaneously, and a comprehensive processing system with extremely high operation rate can be constructed even with simple equipment with a small number of devices.

【００１４】前記処理システムにおいては、前記ＢＯＧ
循環装置の途中に複数の窒素ガス生成用熱交換器が並列
に設けられるとともに、これらの窒素ガス生成用熱交換
器の使用台数を切換える切換手段が設けられている構成
とするのが、より好ましい。この構成によれば、ＢＯＧ
循環量に応じて窒素ガス生成用熱交換器の使用台数を切
換えることにより、ＢＯＧ循環量に適応した熱交換処理
を効率良く行うことができる。In the processing system, the BOG
More preferably, a plurality of heat exchangers for nitrogen gas generation are provided in parallel in the circulation device, and a switching means for switching the number of these heat exchangers for nitrogen gas generation is provided. . According to this configuration, BOG
By switching the number of heat exchangers used for generating nitrogen gas in accordance with the circulation amount, heat exchange processing adapted to the BOG circulation amount can be efficiently performed.

【００１５】また、前記窒素ガス生成用熱交換器とガス
ホルダとの間に、当該窒素ガス生成用熱交換器から導出
される窒素ガスの冷熱を回収する冷熱回収手段や同窒素
ガスの圧力を利用して電気エネルギーを生成する発電手
段を設けるようにすれば、窒素ガス保有の冷熱や圧力エ
ネルギーを有効に活用してＬＮＧ基地等における冷熱や
電源の需要に応えることが可能になる。Further, between the heat exchanger for generating nitrogen gas and the gas holder, cold heat recovery means for recovering the cold heat of the nitrogen gas derived from the heat exchanger for generating nitrogen gas and the pressure of the nitrogen gas are used. If the power generation means for generating electric energy is provided, it is possible to respond to the demand for cold heat and power at an LNG terminal or the like by effectively utilizing the cold energy or pressure energy possessed by the nitrogen gas.

【００１６】[0016]

【発明の実施の形態】本発明の好ましい実施の形態を図
面に基づいて説明する。DESCRIPTION OF THE PREFERRED EMBODIMENTS Preferred embodiments of the present invention will be described with reference to the drawings.

【００１７】図１は、本発明にかかる処理システムの全
体構成を示したフローシートである。FIG. 1 is a flow sheet showing an overall configuration of a processing system according to the present invention.

【００１８】同図において、ＬＮＧタンカー１０により
岸まで運び込まれたＬＮＧは、アンローディングアーム
１２を通じて地上のＬＮＧ基地に設置されたＬＮＧ貯槽
１４内に導入される。In FIG. 1, LNG carried to the shore by an LNG tanker 10 is introduced through an unloading arm 12 into an LNG storage tank 14 installed at an LNG base on the ground.

【００１９】このＬＮＧ貯槽１４内で発生したＢＯＧ
は、ＢＯＧ循環装置１８により凝縮されてＬＮＧ貯槽１
４内に還元される。具体的に、前記ＢＯＧは熱交換装置
２０において後述の液体窒素と熱交換することにより凝
縮した後、バッファタンク２２で気液分離され、その液
相分がポンプ２４を通じてＬＮＧ貯槽１４内に戻され
る。BOG generated in the LNG storage tank 14
Is condensed by the BOG circulating device 18 and the LNG storage tank 1
It is reduced in 4. Specifically, the BOG is condensed by exchanging heat with liquid nitrogen, which will be described later, in the heat exchange device 20, then gas-liquid separated in the buffer tank 22, and the liquid phase is returned into the LNG storage tank 14 through the pump 24. .

【００２０】ＬＮＧ貯槽１４内のＬＮＧは、ポンプ２６
によって貯槽外へ送出され、気化器２８内で蒸発し、Ｎ
Ｇとして需要先に供給される。さらに、送出されたＬＮ
Ｇの一部は、空気分離装置３０内で精製された窒素ガス
と熱交換し、その熱交換によって蒸発してＮＧとして送
出される。一方、このＬＮＧの蒸発潜熱により凝縮した
窒素は前記空気分離装置３０内へ液体窒素として還元さ
れる。The LNG in the LNG storage tank 14 is
Is discharged out of the storage tank, evaporates in the vaporizer 28,
G is supplied to the demand destination. Further, the transmitted LN
A part of the G exchanges heat with the purified nitrogen gas in the air separation device 30, evaporates by the heat exchange, and is sent out as NG. On the other hand, the nitrogen condensed by the latent heat of vaporization of LNG is reduced as liquid nitrogen into the air separation device 30.

【００２１】空気分離装置３０には液体窒素タンク３２
Ａ及び液体酸素タンク３２Ｂが接続され、空気分離装置
３０で精製された液体窒素及び液体酸素が前記各タンク
３２Ａ，３２Ｂにそれぞれ随時補給される。The air separation device 30 includes a liquid nitrogen tank 32
A and the liquid oxygen tank 32B are connected, and the liquid nitrogen and liquid oxygen purified by the air separation device 30 are supplied to the tanks 32A and 32B as needed.

【００２２】液体窒素タンク３２Ａ内の液体窒素は、ポ
ンプ３４Ａを含む窒素ガス回収装置３５によって製品窒
素ガスとして回収される。The liquid nitrogen in the liquid nitrogen tank 32A is recovered as product nitrogen gas by a nitrogen gas recovery device 35 including a pump 34A.

【００２３】具体的には、前記ＢＯＧ循環装置１８にお
けるＢＯＧ循環量に見合った量の液体窒素が液体窒素タ
ンク３２Ａからポンプ３４Ａによって前記熱交換装置２
０に圧送され、同熱交換装置２０で低温のＢＯＧと熱交
換することにより蒸発して窒素ガスとなる。この窒素ガ
スは、窒素ガス加温器３８で加温され、膨張タービン
（発電手段）４０で仕事をして減圧した後、ガスホルダ
４２内に製品窒素ガスとして回収され、需要先に適宜配
給される。前記膨張タービン４０では、前記窒素ガスの
圧力によって電気エネルギーが生成され、ＬＮＧ基地内
の必要箇所に適宜配電される。Specifically, an amount of liquid nitrogen corresponding to the BOG circulation amount in the BOG circulation device 18 is supplied from the liquid nitrogen tank 32A to the heat exchange device 2 by a pump 34A.
0, and heat-exchanges with the low-temperature BOG in the heat exchange device 20 to evaporate to nitrogen gas. This nitrogen gas is heated by a nitrogen gas heater 38 and worked by an expansion turbine (power generation means) 40 to reduce the pressure. Then, the nitrogen gas is recovered as a product nitrogen gas in a gas holder 42 and is appropriately distributed to a demand destination. . In the expansion turbine 40, electric energy is generated by the pressure of the nitrogen gas, and the electric energy is appropriately distributed to a necessary portion in the LNG terminal.

【００２４】このように、空気分離装置３０に接続され
た液体窒素タンク３２Ａからポンプ３４Ａによって液体
窒素を熱交換装置２０に圧送するという構成をとること
により、実際のＢＯＧ循環量に見合った量の液体窒素を
当該ＢＯＧと熱交換させることができ、ＢＯＧ循環量の
変動に的確に対応することが可能となる。As described above, by adopting a configuration in which liquid nitrogen is pumped from the liquid nitrogen tank 32A connected to the air separation device 30 to the heat exchange device 20 by the pump 34A, an amount of liquid nitrogen corresponding to the actual BOG circulation amount is obtained. Liquid nitrogen can be heat-exchanged with the BOG, and it is possible to appropriately cope with fluctuations in the BOG circulation amount.

【００２５】なお、前記窒素ガス加温器３８では、例え
ば窒素ガスと温水とを熱交換させることにより窒素ガス
の加温のみを行うようにしてもよいが、前記窒素ガスと
適当な熱媒体とを熱交換させて窒素ガスの冷熱を回収
し、その冷熱を例えば図３に示すような空気調和機器４
１に用いるといったことも可能である。In the nitrogen gas heater 38, for example, only the heating of the nitrogen gas may be performed by exchanging heat between the nitrogen gas and hot water. Is exchanged to recover the cold heat of the nitrogen gas, and the cold heat is used, for example, in the air conditioner 4 shown in FIG.
1 can be used.

【００２６】前記ポンプ３４Ａから吐出される液体窒素
のうちの余剰分（窒素ガス回収装置３５側へ供給されな
かった分）は、適宜タンクローリ３６Ａに詰め込まれ、
需要先へ配給される。同様に、液体酸素タンク３２Ｂ内
の液体酸素もポンプ３４Ｂによって適宜タンクローリ３
６Ｂ内に詰め込まれ、需要先へ配給される。The surplus of the liquid nitrogen discharged from the pump 34A (the amount not supplied to the nitrogen gas recovery unit 35) is appropriately packed in a tank lorry 36A.
Distributed to the customer. Similarly, the liquid oxygen in the liquid oxygen tank 32B is also appropriately adjusted by the pump 34B.
6B and distributed to the customer.

【００２７】前記熱交換装置２０の構成を図２に示す。
この熱交換装置２０は、互いに並列に配された複数台
（図例では３台）の窒素ガス生成用熱交換器２０ａ，２
０ｂ，２０ｃと、切換手段である複数の開閉弁とを備え
ている。具体的に、各熱交換器２０ａ，２０ｂ，２０ｃ
におけるＢＯＧ通路の入口部分には開閉弁４４Ａ，４４
Ｂ，４４Ｃが設けられ、同様に前記各ＢＯＧ通路の出口
部分には開閉弁４５Ａ，４５Ｂ，４５Ｃが、熱交換器２
０ａ，２０ｂ，２０ｃにおける各窒素通路の入口部分に
は開閉弁４７Ａ，４７Ｂ，４７Ｃが、前記各窒素通路の
出口部分には開閉弁４８Ａ，４８Ｂ，４８Ｃが、それぞ
れ設けられている。FIG. 2 shows the configuration of the heat exchange device 20.
The heat exchanger 20 includes a plurality (three in the example) of nitrogen gas generating heat exchangers 20a, 20 arranged in parallel with each other.
0b, 20c, and a plurality of on-off valves as switching means. Specifically, each of the heat exchangers 20a, 20b, 20c
The opening and closing valves 44A, 44
B, 44C are provided. Similarly, at the outlet of each of the BOG passages, on-off valves 45A, 45B, 45C are provided.
Opening valves 47A, 47B and 47C are provided at the inlet portions of the respective nitrogen passages at 0a, 20b and 20c, and opening / closing valves 48A, 48B and 48C are provided at the outlet portions of the respective nitrogen passages.

【００２８】この熱交換装置２０において、全ての弁を
開けば、全ての窒素ガス生成用熱交換器２０ａ〜２０ｃ
をフルに使用する状態となり、大量のＢＯＧ及び液体窒
素を処理することが可能となる。一方、例えば弁４４
Ａ，４５Ａ，４７Ａ，４８Ａのみを開いて他の弁を閉じ
るようにすれば、１台の熱交換器２０ａのみを使用する
状態となり、少量のＢＯＧと液体窒素とを効率良く熱交
換させることが可能となる。In this heat exchange apparatus 20, if all the valves are opened, all the nitrogen gas generating heat exchangers 20a to 20c
Is fully used, and a large amount of BOG and liquid nitrogen can be processed. On the other hand, for example, the valve 44
If only the valves A, 45A, 47A, and 48A are opened and the other valves are closed, only one heat exchanger 20a is used, and a small amount of BOG and liquid nitrogen can be efficiently exchanged. It becomes possible.

【００２９】すなわち、この熱交換装置２０において
は、各弁の開閉によって熱交換器２０ａ〜２０ｃの使用
台数を切換えることが可能であり、その切換によってＢ
ＯＧの循環量に見合った液体窒素の取り込み及び効率の
高い熱交換処理を行うことが可能となっている。That is, in the heat exchanger 20, the number of heat exchangers 20a to 20c to be used can be switched by opening and closing the respective valves.
This makes it possible to take in liquid nitrogen corresponding to the circulating amount of OG and to perform highly efficient heat exchange processing.

【００３０】なお、ＢＯＧ発生量が非常に多い場合に
は、例えば図４に示すようにＢＯＧの一部を抜き出して
圧縮機７０により圧縮し、ＮＧとともに需要先へ送出す
るようにしてもよい。すなわち、本発明では必ずしもＢ
ＯＧ全量を循環させなくてもよいのであり、前記のよう
にＢＯＧ循環量を調節することによって、熱交換装置２
０や窒素ガス回収装置３５の小型化を図ることも可能に
なる。When the amount of BOG generation is very large, for example, as shown in FIG. 4, a part of the BOG may be extracted, compressed by the compressor 70, and sent to the demand destination together with NG. That is, in the present invention, B
It is not necessary to circulate the entire amount of OG, and by adjusting the BOG circulation amount as described above, the heat exchange device 2
It is also possible to reduce the size of the zero or nitrogen gas recovery device 35.

【００３１】空気分離装置３０の具体的構成を図５に示
す。同図において、図略の吸着塔等により前処理された
原料ガスは、主熱交換器５０を通じて精留塔高圧塔５２
Ｈ内に導入され、同塔５２Ｈ内の底部から精留塔低圧塔
５２Ｌの中腹部に富酸素液体空気が送られるとともに、
精留塔高圧塔５２Ｈの上段から精留塔低圧塔５２Ｌの塔
頂に窒素ガスが送られる。FIG. 5 shows a specific configuration of the air separation device 30. In the figure, a raw material gas pretreated by an unillustrated adsorption tower or the like is passed through a main heat exchanger 50 to a rectification column
H, oxygen-rich liquid air is sent from the bottom of the tower 52H to the middle part of the rectification column low pressure column 52L,
Nitrogen gas is sent from the upper stage of the high-pressure column 52H to the top of the low-pressure column 52L.

【００３２】精留塔低圧塔５２Ｌの塔底液は、弁５３を
通じて製品酸素として液体酸素タンク３２Ｂ内に補給さ
れる。一方、精留塔低圧塔５２Ｌの塔頂ガス（窒素ガ
ス）は、前記主熱交換器５０で前記前処理済原料ガスと
熱交換した後、窒素予冷器５４、窒素冷却器５６、複数
段の循環圧縮機５８、及び窒素凝縮器６０を順に通って
凝縮し、液窒分離器６２で気液分離される。その気相成
分は前記窒素凝縮器６０及び窒素冷却器５６を通じて循
環圧縮機５８に戻される一方、液相部分は空気分離装置
３０に液体窒素として還元される。具体的に、当該液体
窒素の一部は前記精留塔高圧塔５２Ｈ内に還元され、残
りは弁６４を通じて前記製品窒素タンク３２Ａ内に補給
される。The bottom liquid of the rectification column 52L is supplied to the liquid oxygen tank 32B as product oxygen through a valve 53. On the other hand, the overhead gas (nitrogen gas) of the rectification column low-pressure column 52L is heat-exchanged with the pretreated raw material gas in the main heat exchanger 50, and then the nitrogen precooler 54, the nitrogen cooler 56, The condensate passes through the circulation compressor 58 and the nitrogen condenser 60 in order, and is separated into gas and liquid by the liquid nitrogen separator 62. The gas phase component is returned to the circulating compressor 58 through the nitrogen condenser 60 and the nitrogen cooler 56, while the liquid phase portion is reduced to the air separation device 30 as liquid nitrogen. Specifically, a part of the liquid nitrogen is reduced into the rectification column high pressure column 52H, and the rest is supplied into the product nitrogen tank 32A through a valve 64.

【００３３】前記窒素予冷器５４、窒素冷却器５６、及
び窒素凝縮器６０は熱交換器であり、これらの熱交換器
を通じて、前記ＬＮＧ貯槽１４から抽出されるＬＮＧと
窒素ガスとが熱交換され、この熱交換によりＬＮＧの蒸
発と窒素ガスの凝縮とが同時に行われる。すなわち、窒
素予冷器５４、窒素冷却器５６、及び窒素凝縮器６０は
ＮＧ生成用熱交換器としても機能している。The nitrogen precooler 54, the nitrogen cooler 56, and the nitrogen condenser 60 are heat exchangers, and heat is exchanged between the LNG extracted from the LNG storage tank 14 and nitrogen gas through these heat exchangers. By this heat exchange, evaporation of LNG and condensation of nitrogen gas are simultaneously performed. That is, the nitrogen precooler 54, the nitrogen cooler 56, and the nitrogen condenser 60 also function as a heat exchanger for generating NG.

【００３４】ただし、このＮＧ生成用熱交換器は必ずし
も多段で構成されている必要はなく、単段によるもので
あつてもよい。However, the heat exchanger for generating NG need not necessarily be composed of multiple stages, but may be a single stage.

【００３５】以上示したように、この実施の形態に示す
処理システムによれば、ＬＮＧ貯槽１４、空気分離装置
３０、及び熱交換装置２０を含む閉じた系内で、外部か
らの補助冷熱をほとんど受けることなく、ＢＯＧ循環装
置１８によるＢＯＧの凝縮・還元と、窒素ガス回収装置
３５による製品窒素ガスの生成・回収と、空気分離装置
３０における液体窒素の生成と、ＬＮＧ貯槽１４内のＬ
ＮＧの気化によるＮＧの生成とを同時に行うことが可能
となっている。また、ＢＯＧを凝縮させるのに特別なＢ
ＯＧ圧縮機は不要であり、かつ、そのＢＯＧ循環量の変
動にも柔軟な対応をすることができる。As described above, according to the processing system shown in this embodiment, almost all of the auxiliary cooling heat from outside is closed in the closed system including the LNG storage tank 14, the air separation unit 30, and the heat exchange unit 20. Without receiving the BOG, the BOG is condensed and reduced by the BOG circulating device 18, the product nitrogen gas is generated and recovered by the nitrogen gas recovery device 35, the liquid nitrogen is generated in the air separation device 30, and the LNG in the LNG storage tank 14 is reduced.
It is possible to simultaneously generate NG by vaporizing NG. Also, special B is used to condense BOG.
An OG compressor is not required, and it is possible to flexibly cope with fluctuations in the BOG circulation amount.

【００３６】[0036]

【発明の効果】以上のように本発明は、空気分離装置に
接続された液体窒素タンクから窒素ガス生成用熱交換器
に適当な量の液体窒素を圧送し、当該熱交換器で液体窒
素とＢＯＧとを熱交換させることにより液体窒素の蒸発
とＢＯＧの凝縮とを同時に行い、これにより得られたＢ
ＯＧをＬＮＧ貯槽に還元するとともに窒素ガスを回収す
るようにしたものであるので、ＢＯＧの還元処理及び液
体窒素の気化及び回収処理を同時にかつ効率良く行うこ
とができ、また、ＢＯＧ発生量の変動にも容易に対応す
ることができる効果がある。As described above, according to the present invention, an appropriate amount of liquid nitrogen is pumped from a liquid nitrogen tank connected to an air separation device to a heat exchanger for generating nitrogen gas, and the heat exchanger exchanges liquid nitrogen with the liquid nitrogen. By exchanging heat with BOG, the evaporation of liquid nitrogen and the condensation of BOG are simultaneously performed, and the B
Since the OG is reduced to the LNG storage tank and the nitrogen gas is recovered, the BOG reduction processing and the liquid nitrogen vaporization and recovery processing can be performed simultaneously and efficiently, and the fluctuation of the BOG generation amount Has an effect that can be easily dealt with.

【図面の簡単な説明】[Brief description of the drawings]

【図１】本発明にかかるＬＮＧ及び窒素の処理システム
の全体構成を示すフローシートである。FIG. 1 is a flow sheet showing an overall configuration of an LNG and nitrogen processing system according to the present invention.

【図２】前記処理システムにおける熱交換装置の具体的
構成を示すフローシートである。FIG. 2 is a flow sheet showing a specific configuration of a heat exchange device in the processing system.

【図３】前記処理システムの窒素ガス加温器において冷
熱を回収する例を示すフローシートである。FIG. 3 is a flow sheet showing an example of recovering cold heat in a nitrogen gas heater of the processing system.

【図４】前記処理システムにおいてＢＯＧの一部を圧縮
してＮＧとして送出する例を示すフローシートである。FIG. 4 is a flow sheet showing an example in which a part of a BOG is compressed and transmitted as NG in the processing system.

【図５】前記処理システムにおける空気分離装置の具体
的構成を示すフローシートである。FIG. 5 is a flow sheet showing a specific configuration of an air separation device in the processing system.

【符号の説明】[Explanation of symbols]

１４ ＬＮＧ貯槽 １８ ＢＯＧ循環装置 ２０ 熱交換装置 ２０ａ，２０ｂ，２０ｃ 窒素ガス生成用熱交換器 ３０ 空気分離装置 ３２Ａ 液体窒素タンク ３４Ａ ポンプ ３５ 窒素ガス回収装置 ３８ 窒素ガス加温器（冷熱回収手段） ４０ 膨張タービン（発電手段） ４２ ガスホルダ ４４Ａ，４４Ｂ，４４Ｃ，４５Ａ，４５Ｂ，４５Ｃ，４
７Ａ，４７Ｂ，４７Ｃ，４８Ａ，４８Ｂ，４８Ｃ 開閉
弁（切換手段） ５４ 窒素予冷器（天然ガス生成用熱交換器） ５６ 窒素冷却器（天然ガス生成用熱交換器） ６０ 窒素凝縮器（天然ガス生成用熱交換器）14 LNG storage tank 18 BOG circulation device 20 Heat exchange device 20a, 20b, 20c Heat exchanger for nitrogen gas generation 30 Air separation device 32A Liquid nitrogen tank 34A Pump 35 Nitrogen gas recovery device 38 Nitrogen gas heater (cooling / heat recovery means) 40 Expansion turbine (power generation means) 42 Gas holder 44A, 44B, 44C, 45A, 45B, 45C, 4
7A, 47B, 47C, 48A, 48B, 48C On-off valve (switching means) 54 Nitrogen precooler (heat exchanger for natural gas generation) 56 Nitrogen cooler (heat exchanger for natural gas generation) 60 Nitrogen condenser (natural gas) Heat exchanger)

───────────────────────────────────────────────────── フロントページの続き (72)発明者 滝口 好美 大阪市西区江戸堀１丁目６番14号 株式会 社神戸製鋼所大阪支社内 Ｆターム(参考） 3E073 DD03 4D047 AA08 AA10 AB01 AB02 BA03 BA07 BA08 BA09 BB03 CA07 CA09 CA11 DA03 DA17 EA05 ────────────────────────────────────────────────── ─── Continuing on the front page (72) Inventor Yoshimi Takiguchi 1-6-14 Edobori, Nishi-ku, Osaka-shi Kobe Steel, Ltd. Kobe Steel Osaka Branch Office F-term (reference) 3E073 DD03 4D047 AA08 AA10 AB01 AB02 BA03 BA07 BA08 BA09 BB03 CA07 CA09 CA11 DA03 DA17 EA05

Claims (7)

【特許請求の範囲】[Claims] 【請求項１】 空気分離装置で精製した液体窒素を液体
窒素タンクに溜める工程と、液化天然ガスを収容する液
化天然ガス貯槽内で発生したボイルオフガスを窒素ガス
生成用熱交換器へ送出するとともにこれに見合う量の液
体窒素を前記液体窒素タンクから前記窒素ガス生成用熱
交換器へポンプによって圧送することにより当該窒素ガ
ス生成用熱交換器で前記ボイルオフガスを凝縮させると
同時に前記液体窒素を蒸発させる工程と、前記ボイルオ
フガスの凝縮により得られた液化天然ガスを前記液化天
然ガス貯槽内に還元する工程と、前記液体窒素の蒸発に
より得られた窒素ガスを製品窒素としてガスホルダ内に
回収する工程とを含むことを特徴とする液化天然ガス及
び窒素の処理方法。1. A step of storing liquid nitrogen purified by an air separation device in a liquid nitrogen tank, and sending boil-off gas generated in a liquefied natural gas storage tank containing liquefied natural gas to a heat exchanger for generating nitrogen gas. A corresponding amount of liquid nitrogen is pumped from the liquid nitrogen tank to the nitrogen gas generating heat exchanger by a pump to condense the boil-off gas in the nitrogen gas generating heat exchanger while evaporating the liquid nitrogen. Performing, reducing the liquefied natural gas obtained by condensing the boil-off gas into the liquefied natural gas storage tank, and recovering the nitrogen gas obtained by evaporating the liquid nitrogen as product nitrogen in a gas holder. And a method for treating liquefied natural gas and nitrogen. 【請求項２】 請求項１記載の液化天然ガス及び窒素の
処理方法において、前記空気分離装置内で精製された窒
素ガスと前記液化天然ガス貯槽から抜き出した液化天然
ガスとを熱交換させることにより当該液化天然ガスを蒸
発させて天然ガスを生成すると同時に前記窒素ガスを凝
縮させて液体窒素を生成する工程を含むことを特徴とす
る液化天然ガス及び窒素の処理方法。2. The method for treating liquefied natural gas and nitrogen according to claim 1, wherein heat is exchanged between the nitrogen gas purified in the air separation device and the liquefied natural gas extracted from the liquefied natural gas storage tank. A method for treating liquefied natural gas and nitrogen, comprising: evaporating the liquefied natural gas to generate natural gas and condensing the nitrogen gas to generate liquid nitrogen. 【請求項３】 液化天然ガスを収容する液化天然ガス貯
槽と、空気を分離して液体窒素を精製する空気分離装置
と、この空気分離装置に接続され、当該空気分離装置で
精製された液体窒素を収容する液体窒素タンクと、前記
液化天然ガス貯槽内で発生したボイルオフガスと前記液
体窒素タンクから送出される液体窒素とを熱交換させる
ための窒素ガス生成用熱交換器と、液化天然ガス貯槽内
で発生したボイルオフガスを前記窒素ガス生成用熱交換
器に通し、この熱交換器で当該ボイルオフガスの凝縮に
より得られた液化天然ガスを前記液化天然ガス貯槽内に
還元するボイルオフガス循環装置と、前記液体窒素タン
ク内の液体窒素を前記窒素ガス生成用熱交換器へ圧送す
るポンプ及び当該窒素ガス生成用熱交換器で蒸発した窒
素ガスを貯留するガスホルダを含む製品窒素回収装置と
を備えたことを特徴とする液化天然ガス及び窒素の処理
システム。3. A liquefied natural gas storage tank containing liquefied natural gas, an air separation device for separating air to purify liquid nitrogen, and a liquid nitrogen connected to the air separation device and purified by the air separation device A liquid nitrogen tank, a nitrogen gas generating heat exchanger for exchanging heat between boil-off gas generated in the liquefied natural gas storage tank and liquid nitrogen sent from the liquid nitrogen tank, and a liquefied natural gas storage tank A boil-off gas circulating device for passing the boil-off gas generated in the heat exchanger for nitrogen gas generation through the heat exchanger and reducing the liquefied natural gas obtained by condensation of the boil-off gas with the heat exchanger into the liquefied natural gas storage tank; A pump for pumping liquid nitrogen in the liquid nitrogen tank to the heat exchanger for nitrogen gas generation and a gas for storing the nitrogen gas evaporated by the heat exchanger for nitrogen gas generation. A system for treating liquefied natural gas and nitrogen, comprising a product nitrogen recovery device including a sholder. 【請求項４】 請求項３記載の液化天然ガス及び窒素の
処理システムにおいて、前記ボイルオフガス循環装置の
途中に複数の窒素ガス生成用熱交換器が並列に設けられ
るとともに、これらの窒素ガス生成用熱交換器の使用台
数を切換える切換手段が設けられていることを特徴とす
る液化天然ガス及び窒素の処理システム。4. The liquefied natural gas and nitrogen treatment system according to claim 3, wherein a plurality of heat exchangers for generating nitrogen gas are provided in parallel in the boil-off gas circulating apparatus, and a plurality of heat exchangers for generating nitrogen gas are provided. A system for treating liquefied natural gas and nitrogen, comprising switching means for switching the number of heat exchangers used. 【請求項５】 請求項３または４記載の液化天然ガス及
び窒素の処理システムにおいて、前記窒素ガス生成用熱
交換器とガスホルダとの間に、当該窒素ガス生成用熱交
換器から導出される窒素ガスの冷熱を回収する冷熱回収
手段が設けられていることを特徴とする液化天然ガス及
び窒素の処理システム。5. The liquefied natural gas and nitrogen treatment system according to claim 3, wherein the nitrogen gas is discharged from the nitrogen gas generation heat exchanger between the nitrogen gas generation heat exchanger and a gas holder. A system for treating liquefied natural gas and nitrogen, comprising a cold energy recovery means for recovering the cold energy of gas. 【請求項６】 請求項３〜５のいずれかに記載の液化天
然ガス及び窒素の処理システムにおいて、前記窒素ガス
生成用熱交換器とガスホルダとの間に、当該窒素ガス生
成用熱交換器から導出される窒素ガスの圧力を利用して
電気エネルギーを生成する発電手段が設けられているこ
とを特徴とする液化天然ガス及び窒素の処理システム。6. The liquefied natural gas and nitrogen processing system according to claim 3, wherein the nitrogen gas generating heat exchanger is disposed between the nitrogen gas generating heat exchanger and a gas holder. A system for treating liquefied natural gas and nitrogen, comprising a power generation means for generating electric energy by utilizing the pressure of the derived nitrogen gas. 【請求項７】 請求項３〜６のいずれかに記載の液化天
然ガス及び窒素の処理システムにおいて、前記空気分離
装置内で発生する窒素ガスと前記液化天然ガス貯槽から
抜き出される液化天然ガスとを熱交換させることにより
前記窒素ガスを凝縮させて液体窒素を生成すると同時に
前記液化天然ガスを蒸発させて天然ガスを生成する天然
ガス生成用熱交換器を備えたことを特徴とする液化天然
ガス及び窒素の処理システム。7. The liquefied natural gas and nitrogen processing system according to claim 3, wherein the nitrogen gas generated in the air separation device and the liquefied natural gas extracted from the liquefied natural gas storage tank are combined. Liquefied natural gas characterized by comprising a natural gas generating heat exchanger for condensing the nitrogen gas by heat exchange to generate liquid nitrogen and simultaneously evaporating the liquefied natural gas to generate natural gas. And nitrogen treatment system.
JP2001104398A 2001-04-03 2001-04-03 Method and system for treating liquefied natural gas and nitrogen Withdrawn JP2002295799A (en)

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US11097220B2 (en) 2015-09-16 2021-08-24 1304338 Alberta Ltd. Method of preparing natural gas to produce liquid natural gas (LNG)
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JP2023084327A (en) * 2021-12-07 2023-06-19 エア・ウォーター株式会社 Boil-off gas reliquefaction method and apparatus for liquefied natural gas storage facility
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