JP2000503108A - Method and apparatus for storing and transporting liquefied natural gas - Google Patents

Method and apparatus for storing and transporting liquefied natural gas

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Publication number
JP2000503108A
JP2000503108A JP10540955A JP54095598A JP2000503108A JP 2000503108 A JP2000503108 A JP 2000503108A JP 10540955 A JP10540955 A JP 10540955A JP 54095598 A JP54095598 A JP 54095598A JP 2000503108 A JP2000503108 A JP 2000503108A
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JP
Japan
Prior art keywords
methane
tank
cooler
nitrogen
lng
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Granted
Application number
JP10540955A
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Japanese (ja)
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JP3455765B2 (en
Inventor
ルメルホーフ，カール，ヨルゲン
Original Assignee
クファルナー マリタイム エイ．エス．
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Publication of JP2000503108A publication Critical patent/JP2000503108A/en
Application granted granted Critical
Publication of JP3455765B2 publication Critical patent/JP3455765B2/en
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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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
    • F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63J—AUXILIARIES ON VESSELS
    • B63J2/00—Arrangements of ventilation, heating, cooling, or air-conditioning
    • B63J2/12—Heating; Cooling
    • B63J2/14—Heating; Cooling of liquid-freight-carrying tanks
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C13/00—Details of vessels or of the filling or discharging of vessels
    • F17C13/02—Special adaptations of indicating, measuring, or monitoring 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"
    • F25J1/0045—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
    • F25J1/02—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
    • F25J1/0204—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 as a single flow SCR cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
    • F25J1/0262—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
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
    • 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
    • F25J2230/30—Compression of 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
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements
    • 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
    • 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

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

Abstract

(57)【要約】 主に窒素およびメタンからなる液化天然ガス（ＬＮＧ）を、ＬＮＧデコクションをタンク２内に保存し、保存したまま輸送する方法である。デコクションをタンク２から取出し、デコクションの圧力を高くした後、デコクションをメタンおよび窒素の凝縮温度の間にある温度まで冷却器２０において冷却しする。凝縮されたメタンのみをタンク２に戻す。また、この方法の実施装置でもある。 (57) [Summary] This is a method in which liquefied natural gas (LNG) mainly composed of nitrogen and methane is stored in a tank 2 with LNG decoction, and transported as it is. After the decoc- tion is removed from the tank 2 and the decompression pressure is increased, the decoc- tion is cooled in the cooler 20 to a temperature between the methane and nitrogen condensation temperatures. Only the condensed methane is returned to tank 2. It is also an apparatus for implementing this method.

Description

【発明の詳細な説明】 液化天然ガスの保存・輸送方法および装置 本発明は、窒素および主にメタンなどの他のガス（以下単にメタンと呼ぶ）か らなる液化天然ガス（以下ＬＮＧと呼ぶ）を、ＬＮＧが沸騰し、ガス状のＬＮＧ （以下デコクションと呼ぶ）を発生するタンク内に保存し、輸送する方法に関す る。 また、本発明は、この方法の実施装置にも関する。 ほぼ大気圧に相当する圧力でＬＮＧ（液化天然ガス）を保存したり、輸送する と、このＬＮＧの一部が沸騰し、ガスに変わる。 ＬＮＧ輸送船では、推進のための燃料としてデコクションを使用している。と いうのは、この種の輸送に使用できるより経済的な代替燃料がないからである。 ところが、輸送船の航行費が結果として高くなる。なぜなら、蒸気を発生し、輸 送船を推進する例えばジーゼルモーターよりも効率の低い蒸気タービンを運転す るために、ガスを使用しているからである。 一方、共通の解決策として、天然ガスを再液化し、これをタンクに導入するこ とがあるが、これはエネルギーの消費量がきわめて大きい。 本発明の目的は、液化天然ガスの保存コストおよび輸送コストを削減する方法 および装置を提供することである。 本発明方法および装置の特徴については、特許請求の範囲における特徴項に記 載した通りである。 以下、本発明を添付図面について詳しく説明する。なお、図１は本発明装置に よって、ＬＮＧを保存または輸送するシステムまたはプラントの実施態様を示す 概略配管図である。 図１に示すように、システムのタンク２にＬＮＧ４（液面は参照数字６で示す ）を装入する。この液面６上のタンク空間は、パイプライン８を介して、モータ ー１４によって駆動される第１コンプレッサー１２を有する第１コンプレッサー 装置１０の入り口に連絡する。 このコンプレッサー装置１０の出口は、パイプライン１６を介して、第１冷却 器または第１熱交換器２０の第１流路１８の入り口に連絡する。そして、この流 路１８の出口は気液分離器２２の入り口に連絡する。 冷却器２０の第２流路の入り口には、パイプライン３０を介してそれ自体は標 準的な冷却プラント２６から冷却した冷却液を供給する。そして、その出口がパ イプ２８を介して冷却プラント２６に加熱された冷却液を戻す。 分離された液体が流れ出す気液分離器２２の出口は、パイプライン３２を介し て、ポンプ３４の入り口に接続する。一方、分離されたガスは分離器２２からパ イプライン３６を介して周囲雰囲気に流れ出す。 ポンプ３４の出口は、 パイプライン３７を介してパイプライン１６の導入点 ３６に、 パイプライン４０を介してタンク２内のＬＮＧ液面下部のタンク空間に、そし て パイプライン４２を介してタンク２内のＬＮＧ液面上の空間に連絡する。 タンク２内のパイプライン４２の終点にノズル装置４４を設ける。 また、パイプライン４０、４２には、それぞれ逆止めノズル４６、４８を設け てもよい。 導入点３８と冷却器２０における第１流路１８の入り口との間で、パイプライ ン１６に、電気ケーブル５２を介して電気作動式逆止め弁５４に接続することが できる温度センサー５０を接続する。 ここで使用する冷却プラント２６は、公知形式のもので、モーター６０によっ て駆動される第２コンプレッサー５８を有する第２コンプレッサー装置５６を備 えている。第２コンプレッサー５６の下流側には、中間冷却器６２を設け、その 下流側に第３コンプレッサー６４を設ける。 第２コンプレッサー５８の入り口は、パイプライン７０を介して、第２冷却器 または熱交換器６８の第３流路の出口に連絡する。第２コンプレッサー装置６８ の出口は、パイプライン７３を介して第２熱交換器６８の第４流路７２の入り口 に連絡し、そして第４流路７２の出口は膨張用タービン７４の入り口に連絡する 。このタービ ンの出口は、パイプライン３０を介して、第１熱交換器２０の第２流路２４の入 り口に接続する。第３コンプレッサー６４は膨張用タービン７４によって駆動さ れる。 本発明装置は次のように作動する。 タンク２のデコクションがパイプライン８により第１コンプレッサー装置１０ に流れると、圧縮され、これによって大きく過熱する。このコンプレッサー装置 １０から、デコクションが第１熱交換器２０の第１流路１８を流れると、メタン の凝縮温度と窒素の凝縮温度との間にある温度に冷却される。これによって、気 液混合物が分離器２２に流れ、ここで液体メタンが窒素ガスから分離され、窒素 ガスはパイプライン３６を介して大気中に流れ出る。 逆止め弁４６を開くと、液体メタンの第１部分がパイプライン４０を介してタ ンク２内のＬＮＧ液面下部に戻る。また、逆止め弁４８を開くと、液体メタンの 第２部分がパイプライン４２を介してタンク２に戻り、ノズル装置４４を介して デコクション、即ちＬＮＧ液面６上に広がるため、デコクションを冷却する。こ の結果、その一部がタンク内で凝縮するので、少なくともデコクションが減るこ とになる。 ＬＮＧをタンクに満パイにした状態で船舶輸送する場合、通常は、逆止め弁４ ８が閉じ、逆止め弁４６が開いているが、これら逆止め弁４６、４８、５４の位 置に関する組合せは上記に限定されず、任意の組合せが可能で ある。 第１コンプレッサー装置１０と第１熱交換器２０との間にあるパイプ１６中の デコクションの温度がある限界値を越えると、温度センサー５０が逆止め弁５４ に信号を送り、これを開く。特に、タンク内のＬＮＧ量が多くなく、従ってデコ クションの量がかなり少なくなった場合に信号送信が起きる。この場合、第１コ ンプレッサー装置が最適な作動状態にないと、効率が低下し、圧縮されたデコク ションの温度が比較的高くなる。この場合には、導入点３８を介してパイプライ ン１６に液体メタンの第３部分が送られるため、第１熱交換器２０に流入するデ コクションの温度を下げることができ、これによって第１熱交換器２０がデコク ション温度を必要な温度まで下げることができる。 メタンの第３部分を戻す場合も、熱交換器の成分を通常方法でアルミニウムか ら形成できる程度に、第１熱交換器２０に供給されるデコクションの温度を下げ ることができる。 デコクションがすべて完全に凝縮すると、エネルギー回収効率はほぼ２０％に なる。デコクションのごく一部が凝縮すると、即ち本発明に従ってメタンが一部 凝縮し、窒素がガス状態で雰囲気や大気中に放出されると、エネルギー回収効率 はほぼ３８％に達する。 当業者ならば、第１熱交換器と分離器とをタンクより高い位置に設置すると、 重力により液化メタンをタンク に戻すことができることを理解できるはずである。この場合には、一方、ポンプ によって、第１冷却器２０の入り口の前方にある戻り点に液化メタンを戻す必要 がある。 さらに、当業者ならば、本装置におけるコンプレッサー装置の数を多くし、こ れらを直列に相互接続し、これらの間に中間冷却器を設けることができることも 理解できるはずである。同様に、本発明装置には、それ自体が標準的な配管構成 成分、例えば逆止め弁やチェック弁を上記成分間に設置し、これらを上記と同様 にして作動させることも可能であることを理解できるはずである。DETAILED DESCRIPTION OF THE INVENTION           Method and apparatus for storing and transporting liquefied natural gas   The present invention relates to the use of other gases such as nitrogen and mainly methane (hereinafter simply referred to as methane). Liquefied natural gas (hereinafter referred to as LNG) consisting of LNG (Hereinafter referred to as decoction) in a tank that generates and transports You.   The invention also relates to an apparatus for performing the method.   Stores and transports LNG (liquefied natural gas) at pressures approximately equivalent to atmospheric pressure Then, part of this LNG boils and turns into gas.   LNG carriers use decoction as fuel for propulsion. When This is because there are no more economical alternative fuels available for this type of transportation. However, the transportation costs of the transport ship are increased as a result. Because it produces steam and Drive steam turbines that are less efficient than diesel motors, for example, to propel ships This is because a gas is used for this purpose.   On the other hand, a common solution is to reliquefy natural gas and introduce it into tanks. However, this consumes a great deal of energy.   It is an object of the present invention to reduce the storage and transportation costs of liquefied natural gas. And equipment.   The features of the method and apparatus of the present invention are described in the features of the claims. It is as stated.   Hereinafter, the present invention will be described in detail with reference to the accompanying drawings. FIG. 1 shows the apparatus of the present invention. Thus, an embodiment of a system or plant for storing or transporting LNG is shown. It is a schematic piping diagram.   As shown in FIG. 1, LNG 4 (liquid level is indicated by reference numeral 6) in tank 2 of the system. ). The tank space above the liquid level 6 is connected to a motor via a pipeline 8. Compressor having a first compressor 12 driven by a compressor 14 Contact the entrance of the device 10.   The outlet of the compressor device 10 is connected to the first cooling To the inlet of the first channel 18 of the heat exchanger or first heat exchanger 20. And this style The outlet of line 18 communicates with the inlet of gas-liquid separator 22.   The inlet of the second flow path of the cooler 20 is itself marked via a pipeline 30. Cooled coolant is supplied from a quasi-refrigeration plant 26. And the exit is The heated coolant is returned to the cooling plant 26 via the Ip 28.   The outlet of the gas-liquid separator 22 from which the separated liquid flows flows through a pipeline 32 Connected to the inlet of the pump 34. On the other hand, the separated gas is It flows out to the surrounding atmosphere through the pipeline 36.   The outlet of the pump 34   Introduction point of pipeline 16 via pipeline 37 36,   Through the pipeline 40 into the tank space below the LNG level in the tank 2, hand   The space above the LNG level in the tank 2 is communicated via the pipeline 42.   A nozzle device 44 is provided at the end point of the pipeline 42 in the tank 2.   The pipelines 40 and 42 are provided with non-return nozzles 46 and 48, respectively. You may.   A pipe line is provided between the introduction point 38 and the inlet of the first flow path 18 in the cooler 20. Connected to an electrically operated check valve 54 via an electrical cable 52. A temperature sensor 50 is connected.   The cooling plant 26 used here is of a known type and is driven by a motor 60. A second compressor device 56 having a second compressor 58 driven by I have. On the downstream side of the second compressor 56, an intercooler 62 is provided. A third compressor 64 is provided on the downstream side.   The inlet of the second compressor 58 is connected via a pipeline 70 to a second cooler. Alternatively, it communicates with the outlet of the third flow path of the heat exchanger 68. Second compressor device 68 Is the inlet of the fourth flow path 72 of the second heat exchanger 68 via the pipeline 73 And the outlet of the fourth flow path 72 communicates with the inlet of the expansion turbine 74. . This turbi The outlet of the heat exchanger is connected to the second flow path 24 of the first heat exchanger 20 through a pipeline 30. To the outlet. The third compressor 64 is driven by an expansion turbine 74. It is.   The device of the present invention operates as follows.   The decompression of the tank 2 is performed by the first compressor device 10 by the pipeline 8. As it flows, it is compressed, which causes it to overheat. This compressor device From 10, when decoction flows through the first flow path 18 of the first heat exchanger 20, methane Is cooled to a temperature that is between the condensation temperature of nitrogen and the condensation temperature of nitrogen. With this, The liquid mixture flows to separator 22 where liquid methane is separated from nitrogen gas and Gas flows out into the atmosphere via pipeline 36.   When check valve 46 is opened, a first portion of liquid methane is Return to the lower part of the LNG liquid level in link 2. When the check valve 48 is opened, the liquid methane The second part returns to the tank 2 via the pipeline 42 and via the nozzle device 44 The decoc- tion, that is, the decoc- tion is cooled to spread on the LNG liquid level 6. This As a result, some of the condensation will condense in the tank, so at least And   When transporting a ship with LNG filled with tanks, the check valve 4 8 is closed and the check valve 46 is open. The combinations related to the positions are not limited to the above, and any combination is possible. is there.   In the pipe 16 between the first compressor unit 10 and the first heat exchanger 20 When the decompression temperature exceeds a certain limit, the temperature sensor 50 activates the check valve 54. And send it to open. In particular, the amount of LNG in the tank is not large, Signaling occurs when the amount of action is significantly reduced. In this case, the first If the compressor unit is not in optimal operation, efficiency will drop and the compressed deco Relatively high temperature. In this case, the pipeline Since the third portion of the liquid methane is sent to the heat exchanger 16, the The temperature of the commutation can be reduced, and the first heat exchanger 20 Temperature can be reduced to the required temperature.   When returning the third part of the methane, the components of the heat exchanger are also converted to aluminum The temperature of the decoaction supplied to the first heat exchanger 20 to such an extent that Can be   When all decoys are completely condensed, the energy recovery efficiency is almost 20% Become. Only a small part of the decondensation condenses, i.e. some methane according to the invention When condensed and nitrogen is released into the atmosphere or air in a gaseous state, energy recovery efficiency Reaches almost 38%.   One of ordinary skill in the art would place the first heat exchanger and separator higher than the tank, Liquefied methane tank by gravity You can see that you can go back to In this case, on the other hand, the pump Liquefied methane must be returned to the return point in front of the entrance of the first cooler 20 There is.   Further, those skilled in the art will increase the number of compressor devices in the device and They may be interconnected in series with an intercooler between them. You should understand. Similarly, the device of the present invention itself has a standard piping configuration. Components, such as check valves and check valves, are placed between the components and these are the same as above. It should be understood that it is also possible to operate with.

【手続補正書】特許法第１８４条の８第１項 【提出日】１９９９年１月１８日（１９９９．１．１８） 【補正内容】 液化天然ガスの保存・輸送方法および装置 本発明は、窒素および主にメタンなどの他のガス（以下単にメタンと呼ぶ）か らなる液化天然ガス（以下ＬＮＧと呼ぶ）を、ＬＮＧが沸騰し、ガス状のＬＮＧ （以下デコクションと呼ぶ）を発生するタンク内に保存し、保存したまま輸送す るさいに、デコクションをタンクから取出し、デコクションの圧力を高くし、圧 力の高くなったデコクションを冷却器で冷却し、凝縮してから、タンクに戻すこ とからなる液化天然ガスの保存・輸送方法に関する。 また、本発明は、この方法の実施装置にも関する。 ほぼ大気圧に相当する圧力でＬＮＧ（液化天然ガス）を保存したり、輸送する と、このＬＮＧの一部が沸騰し、ガスに変わる。 ＬＮＧ輸送船では、推進のための燃料としてデコクションを使用している。と いうのは、この種の輸送に使用できるより経済的な代替燃料がないからである。 ところが、輸送船の航行費が結果として高くなる。なぜなら、蒸気を発生し、輸 送船を推進する例えばジーゼルモーターよりも効率の低い蒸気タービンを運転す るために、ガスを使用しているからである。 ＵＳ−Ａ−４６７５０３７によって、上記冒頭に記載した工程を含み、タンク からのすべてのデコクションを 凝縮し、タンクに戻す方法は公知である。ところが、この方法はエネルギーの消 費量がきわめて大きい。 本発明の目的は、液化天然ガスの保存コストおよび輸送コストを削減する方法 および装置を提供することである。 本発明方法および装置の特徴については、特許請求の範囲における特徴項に記 載した通りである。 以下、本発明を添付図面について詳しく説明する。なお、図１は本発明装置に よって、ＬＮＧを保存または輸送するシステムまたはプラントの実施態様を示す 概略配管図である。 図１に示すように、システムのタンク２にＬＮＧ４（液面は参照数字６で示す ）を装入する。この液面６上のタンク空間は、パイプライン８を介して、モータ ー１４によって駆動される第１コンプレッサー１２を有する第１コンプレッサー 装置１０の入り口に連絡する。 請求の範囲 １．窒素および主にメタンなどの他のガス（以下単にメタンと呼ぶ）からなる液 化天然ガス（以下ＬＮＧと呼ぶ）を、ＬＮＧが沸騰し、ガス状のＬＮＧ（以下デ コクションと呼ぶ）を発生するタンク２内に保存し、保存したまま輸送するさい に、デコクションをタンク２から取出し、デコクションの圧力を高くし、この圧 力の高くなったデコクションを冷却器２０で冷却し、凝縮し、タンクに戻すこと からなる液化天然ガスの保存・輸送方法において、 上記のデコクションを圧縮メタンおよび圧縮窒素の凝縮温度の間にある温度ま で冷却し、 凝縮されていないガス状窒素から凝縮されたメタンを分離し、 凝縮されたメタンをタンク２に戻し、そして 凝縮されていない窒素を大気中に放出することを特徴とする液化天然ガスの保 存・輸送方法。 ２．冷却器２０において冷却しないで、上記の凝縮されたメタンの一部を上記デ コクションに供給することを特徴とする請求項１の方法。 ３．窒素および主にメタンなどの他のガス（以下単にメタンと呼ぶ）からなる液 化天然ガス（以下ＬＮＧと呼ぶ）を、ＬＮＧが沸騰し、ガス状のＬＮＧ（以下デ コクションと呼ぶ）を発生するタンク２内に保存し、輸送す るさいに、第１コンプレッサー装置１０を使用して、タンク２からのデコクショ ンを圧縮し、そして入り口を第１コンプレッサー装置１０の出口に接続し、そし て圧縮されたデコクションを冷却する冷却器２０を有する凝縮装置を使用する方 法を実施する装置において、 冷却器２０を使用して、上記の圧縮されたデコクションを圧縮メタンと圧縮窒 素の凝縮温度の間にある温度まで冷却し、 さらに、この凝縮されたメタンからガス状の窒素を分離する分離器と、 凝縮されたメタンをタンク２に戻す第１配管構成４０、４２、４４、４６、４ ８と、そして 凝縮されていない窒素を大気中に放出する第２配管構成３６とを有することを 特徴とする装置。 ４．上記の凝縮されたメタンを分離器２２から第１配管構成にポンプ供給するポ ンプ３４をさらに有することを特徴とする請求項３の装置。 ５．上記の凝縮されたメタンを分離器２２から第３配管構成にポンプ供給して、 冷却器２０の入り口の上流側にある導入点３８にこの凝縮されたメタンを供給す るポンプ３４をさらに有することを特徴とする請求項３の装置。 ６．第３配管構成が、導入点３８と冷却器２０の入り口との間に設けられた温度 センサー５０と、上記ポンプを上記導入点に接続するパイプライン３７と、パイ プライン３７に設けられ、温度センサー５０によって制御され る第１逆止め弁５４とをさらに有することを特徴とする請求項５の装置。 ７．第１配管構成が、上記タンク内の終端に、タンク２の上部に設置されたノズ ル装置４４を設けた第１パイプライン４２有する請求項３〜６のいずれか１項の 装置。 ８．第１配管構成が、タンク２内の底部を終端とした第２パイプライン４０を有 することを特徴とする請求項３〜７のいずれか１項の装置。[Procedure of Amendment] Article 184-8, Paragraph 1 of the Patent Act [Submission date] January 18, 1999 (1.1.1.18) [Correction contents]          Method and apparatus for storing and transporting liquefied natural gas   The present invention relates to the use of other gases such as nitrogen and mainly methane (hereinafter simply referred to as methane). Liquefied natural gas (hereinafter referred to as LNG) consisting of LNG (Hereinafter referred to as decoction) in the tank where they are generated and transported with the storage Remove the decoction from the tank and increase the decompression pressure. Cool the intensified decoys with a cooler and condense them before returning them to the tank. And a method for storing and transporting liquefied natural gas.   The invention also relates to an apparatus for performing the method.   Stores and transports LNG (liquefied natural gas) at pressures approximately equivalent to atmospheric pressure Then, part of this LNG boils and turns into gas.   LNG carriers use decoction as fuel for propulsion. When This is because there are no more economical alternative fuels available for this type of transportation. However, the transportation costs of the transport ship are increased as a result. Because it produces steam and Drive steam turbines that are less efficient than diesel motors, for example, to propel ships This is because a gas is used for this purpose.   According to U.S. Pat. No. 4,675,037, comprising the steps described at the outset above, All the decoys from Methods of condensing and returning to the tank are known. However, this method consumes energy. Cost is extremely large.   It is an object of the present invention to reduce the storage and transportation costs of liquefied natural gas. And equipment.   The features of the method and apparatus of the present invention are described in the features of the claims. It is as stated.   Hereinafter, the present invention will be described in detail with reference to the accompanying drawings. FIG. 1 shows the apparatus of the present invention. Thus, an embodiment of a system or plant for storing or transporting LNG is shown. It is a schematic piping diagram.   As shown in FIG. 1, LNG 4 (liquid level is indicated by reference numeral 6) in tank 2 of the system. ). The tank space above the liquid level 6 is connected to a motor via a pipeline 8. Compressor having a first compressor 12 driven by a compressor 14 Contact the entrance of the device 10.                               The scope of the claims 1. Liquid consisting of nitrogen and other gases, mainly methane (hereinafter simply referred to as methane) Natural gas (hereinafter referred to as LNG) is converted into gaseous LNG (hereinafter referred to as (Called "compression") in the tank 2 where it is generated and transported with the storage Next, the decoction is taken out of the tank 2 and the decompression pressure is increased. Cooling the decoys with increased power with the cooler 20, condensing, and returning to the tank In the storage and transportation of liquefied natural gas consisting of   Keep the above decompression at a temperature between the condensation temperatures of compressed methane and compressed nitrogen. And cool   Separating condensed methane from uncondensed gaseous nitrogen,   Return the condensed methane to tank 2 and   A liquefied natural gas reserve characterized by releasing uncondensed nitrogen into the atmosphere. Presence and transportation method. 2. Without cooling in the cooler 20, a part of the condensed methane is 2. The method of claim 1, wherein the supply is to ciction. 3. Liquid consisting of nitrogen and other gases, mainly methane (hereinafter simply referred to as methane) Natural gas (hereinafter referred to as LNG) is converted into gaseous LNG (hereinafter referred to as Is stored in the tank 2 that generates On the contrary, the first compressor device 10 is used to decoup Compressor, and connect the inlet to the outlet of the first compressor unit 10 and Using a condenser having a cooler 20 for cooling the decompression compressed In an apparatus for performing the method,   Using a cooler 20, the above compressed decoy is compressed with compressed methane and compressed nitrogen. Cooled to a temperature between the elemental condensation temperatures,   Further, a separator for separating gaseous nitrogen from the condensed methane,   First piping structure 40, 42, 44, 46, 4 for returning condensed methane to tank 2 8 and   A second piping arrangement 36 for releasing uncondensed nitrogen into the atmosphere. Characteristic device. 4. A port for pumping the condensed methane from the separator 22 to the first piping configuration. The apparatus of claim 3 further comprising a pump (34). 5. Pumping the condensed methane from separator 22 to a third piping configuration, This condensed methane is supplied to an inlet 38 upstream of the inlet of the cooler 20. The apparatus of claim 3 further comprising a pump (34). 6. The third piping configuration is provided with a temperature provided between the introduction point 38 and the inlet of the cooler 20. A sensor 50, a pipeline 37 connecting the pump to the inlet, Provided on the pipeline 37 and controlled by the temperature sensor 50 The apparatus of claim 5, further comprising a first check valve (54). 7. A first piping configuration is provided at a terminal end in the tank, a nozzle installed at an upper part of the tank 2. 7. The apparatus according to claim 3, wherein the first pipeline includes a first pipeline. apparatus. 8. The first piping configuration has a second pipeline 40 terminating at the bottom in the tank 2. Apparatus according to any of claims 3 to 7, characterized in that:

───────────────────────────────────────────────────── フロントページの続き (81)指定国 ＥＰ(ＡＴ，ＢＥ，ＣＨ，ＤＥ， ＤＫ，ＥＳ，ＦＩ，ＦＲ，ＧＢ，ＧＲ，ＩＥ，ＩＴ，Ｌ Ｕ，ＭＣ，ＮＬ，ＰＴ，ＳＥ)，ＯＡ(ＢＦ，ＢＪ，ＣＦ ，ＣＧ，ＣＩ，ＣＭ，ＧＡ，ＧＮ，ＭＬ，ＭＲ，ＮＥ， ＳＮ，ＴＤ，ＴＧ)，ＡＰ(ＧＨ，ＧＭ，ＫＥ，ＬＳ，Ｍ Ｗ，ＳＤ，ＳＺ，ＵＧ，ＺＷ)，ＵＡ(ＡＭ，ＡＺ，ＢＹ ，ＫＧ，ＫＺ，ＭＤ，ＲＵ，ＴＪ，ＴＭ)，ＡＬ，ＡＭ ，ＡＴ，ＡＵ，ＡＺ，ＢＡ，ＢＢ，ＢＧ，ＢＲ，ＢＹ， ＣＡ，ＣＨ，ＣＮ，ＣＵ，ＣＺ，ＤＥ，ＤＫ，ＥＥ，Ｅ Ｓ，ＦＩ，ＧＢ，ＧＥ，ＧＨ，ＧＭ，ＧＷ，ＨＵ，ＩＤ ，ＩＬ，ＩＳ，ＪＰ，ＫＥ，ＫＧ，ＫＰ，ＫＲ，ＫＺ， ＬＣ，ＬＫ，ＬＲ，ＬＳ，ＬＴ，ＬＵ，ＬＶ，ＭＤ，Ｍ Ｇ，ＭＫ，ＭＮ，ＭＷ，ＭＸ，ＮＯ，ＮＺ，ＰＬ，ＰＴ ，ＲＯ，ＲＵ，ＳＤ，ＳＥ，ＳＧ，ＳＩ，ＳＫ，ＳＬ， ＴＪ，ＴＭ，ＴＲ，ＴＴ，ＵＡ，ＵＧ，ＵＳ，ＵＺ，Ｖ Ｎ，ＹＵ，ＺＷ────────────────────────────────────────────────── ─── Continuation of front page    (81) Designated countries EP (AT, BE, CH, DE, DK, ES, FI, FR, GB, GR, IE, IT, L U, MC, NL, PT, SE), OA (BF, BJ, CF) , CG, CI, CM, GA, GN, ML, MR, NE, SN, TD, TG), AP (GH, GM, KE, LS, M W, SD, SZ, UG, ZW), UA (AM, AZ, BY) , KG, KZ, MD, RU, TJ, TM), AL, AM , AT, AU, AZ, BA, BB, BG, BR, BY, CA, CH, CN, CU, CZ, DE, DK, EE, E S, FI, GB, GE, GH, GM, GW, HU, ID , IL, IS, JP, KE, KG, KP, KR, KZ, LC, LK, LR, LS, LT, LU, LV, MD, M G, MK, MN, MW, MX, NO, NZ, PL, PT , RO, RU, SD, SE, SG, SI, SK, SL, TJ, TM, TR, TT, UA, UG, US, UZ, V N, YU, ZW

Claims (1)

【特許請求の範囲】 １．窒素および主にメタンなどの他のガス（以下単にメタンと呼ぶ）からなる液 化天然ガス（以下ＬＮＧと呼ぶ）を、ＬＮＧが沸騰し、ガス状のＬＮＧ（以下デ コクションと呼ぶ）を発生するタンク２内に保存し、保存したまま輸送するさい に、デコクションをタンク２から取出し、デコクションの圧力を高くする液化天 然ガスの保存・輸送方法において、 上記の圧力の高いデコクションを圧縮メタンおよび圧縮窒素の凝縮温度の間に ある温度まで冷却器２０において冷却し、そして 凝縮されたメタンをタンク２に戻すことを特徴とする液化天然ガスの保存・輸 送方法。 ２．冷却器２０において冷却しないで、上記の凝縮されたメタンの一部を圧力の 高いデコクションに供給することを特徴とする請求項１の方法。 ３．冷却器２０で冷却されているが、まだ液化していない窒素を大気中に放出す る請求項１または２の方法。 ４．窒素および主にメタンなどの他のガス（以下単にメタンと呼ぶ）からなる液 化天然ガス（以下ＬＮＧと呼ぶ）を、ＬＮＧが沸騰し、ガス状のＬＮＧ（以下デ コクションと呼ぶ）を発生するタンク２内に保存し、輸送するさいに、第１コン プレッサー装置１０を使用して、タンク２からのデコクションを圧縮する方法を 実施する装 置において、 入り口を第１コンプレッサー装置１０の出口に接続し、そして圧縮されたデコ クションを圧縮メタンと圧縮窒素の凝縮温度の間にある温度まで冷却する冷却器 ２０と、凝縮されたメタンからガス状の窒素を分離する分離器とを有する凝縮装 置と、 凝縮されたメタンをタンク２に戻す第１配管構成４０、４２、４４、４６、４ ８とを有することを特徴とする装置。 ５．上記の凝縮されたメタンを分離器２２から第１配管構成にポンプ供給するポ ンプ３４をさらに有することを特徴とする請求項４の装置。 ６．上記の凝縮されたメタンを分離器２２から第２配管構成にポンプ供給して、 冷却器２０の入り口の上流側にある導入点３８にこの凝縮されたメタンを供給す るポンプ３４をさらに有することを特徴とする請求項４の装置。 ７．第２配管構成が、導入点３８と冷却器２０の入り口との間に設けられた温度 センサー５０と、上記ポンプを上記導入点に接続するパイプライン３７と、パイ プライン３７に設けられ、温度センサー５０によって制御される第１逆止め弁５ ４とをさらに有することを特徴とする請求項６の装置。 ８．第１配管構成が、上記タンク内の終端に、タンク２の上部に設置されたノズ ル装置４４を設けた第１パイプライン４２有する上記請求項のいずれか１項の装 置。 ９．第１配管構成が、タンク２内の底部を終端とした第２パイプライン４０を有 することを特徴とする上記請求項のいずれか１項の装置。[Claims] 1. Liquid consisting of nitrogen and other gases, mainly methane (hereinafter simply referred to as methane) Natural gas (hereinafter referred to as LNG) is converted into gaseous LNG (hereinafter referred to as (Called "compression") in the tank 2 where it is generated and transported with the storage Then, take out the decoction from tank 2 and increase the decompression pressure In the storage and transportation of natural gas,   The above high pressure decompression is performed between the condensation temperature of compressed methane and compressed nitrogen. Cool in cooler 20 to a certain temperature, and   Storage and transportation of liquefied natural gas characterized by returning condensed methane to tank 2 How to send. 2. Without cooling in the cooler 20, a portion of the condensed methane is 2. The method of claim 1 wherein the high decoys are provided. 3. Releases nitrogen that has been cooled by the cooler 20 but has not yet been liquefied into the atmosphere. 3. The method of claim 1 or claim 2. 4. Liquid consisting of nitrogen and other gases, mainly methane (hereinafter simply referred to as methane) Natural gas (hereinafter referred to as LNG) is converted into gaseous LNG (hereinafter referred to as Is stored in the tank 2 that generates the first conc. A method of compressing the decoction from the tank 2 using the presser device 10 is described. Equipment to be implemented In place   The inlet is connected to the outlet of the first compressor unit 10 and the compressed deco A cooler that cools the section to a temperature between the condensation temperature of compressed methane and compressed nitrogen 20 and a separator for separating gaseous nitrogen from condensed methane And   First piping structure 40, 42, 44, 46, 4 for returning condensed methane to tank 2 8. An apparatus comprising: 5. A port for pumping the condensed methane from the separator 22 to the first piping configuration. The apparatus of claim 4 further comprising a pump (34). 6. Pumping the condensed methane from separator 22 to the second piping configuration, This condensed methane is supplied to an inlet 38 upstream of the inlet of the cooler 20. The apparatus of claim 4 further comprising a pump (34). 7. The second piping configuration is provided with a temperature provided between the introduction point 38 and the inlet of the cooler 20. A sensor 50, a pipeline 37 connecting the pump to the inlet, The first check valve 5 provided in the pipeline 37 and controlled by the temperature sensor 50 7. The apparatus of claim 6, further comprising: 8. A first piping configuration is provided at a terminal end in the tank, a nozzle installed at an upper part of the tank 2. Device according to any of the preceding claims, comprising a first pipeline (42) provided with a filtering device (44). Place. 9. The first piping configuration has a second pipeline 40 terminating at the bottom in the tank 2. Apparatus according to any one of the preceding claims, characterized in that:
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2007506064A (en) * 2003-09-17 2007-03-15 エア　プロダクツ　アンド　ケミカルズ　インコーポレイテッド Hybrid gas liquefaction cycle with multiple expanders
WO2011046315A3 (en) * 2009-10-16 2011-09-01 대우조선해양 주식회사 Ship for supplying liquefied fuel gas
JP2014148306A (en) * 2009-06-30 2014-08-21 Wartsila Oil And Gas Systems As Method and system for storing and transporting liquefied petroleum gas

Families Citing this family (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NO990686L (en) * 1999-02-12 2000-08-14 Kvaerner Maritime As Device for processing LNG decoction from vessels
EP1242769B1 (en) 1999-12-23 2010-12-15 Venturie AS Method, apparatus and system for the condensation of vapours and gases
GB0001801D0 (en) 2000-01-26 2000-03-22 Cryostar France Sa Apparatus for reliquiefying compressed vapour
GB0005709D0 (en) 2000-03-09 2000-05-03 Cryostar France Sa Reliquefaction of compressed vapour
NO315293B1 (en) 2001-10-31 2003-08-11 Procyss As Process for absorbing vapors and gases in the control of overpressure storage tanks for liquids and application of the process
KR100441857B1 (en) * 2002-03-14 2004-07-27 대우조선해양 주식회사 Boil off gas rel iquefaction method and system assembly of Liquefied natural gas carrier
NO322620B1 (en) * 2003-10-28 2006-11-06 Moss Maritime As Device for storing and transporting liquefied natural gas
NO20035047D0 (en) * 2003-11-13 2003-11-13 Hamworthy Kse Gas Systems As Apparatus and method for temperature control of gas condensation
FI118681B (en) * 2004-03-17 2008-02-15 Waertsilae Finland Oy Gas supply arrangement for a watercraft and method for producing gas in a watercraft
KR100699163B1 (en) 2005-11-17 2007-03-23 신영중공업주식회사 Reliquefaction apparatus of lng bog and reliquefaction method
KR100681557B1 (en) * 2005-12-01 2007-02-09 대우조선해양 주식회사 Boil off gas reliquefaction treatment system of liquefied natural gas carrier
KR101290032B1 (en) * 2006-04-07 2013-07-30 배르질래 오일 ＆ 가스 시스템즈 아에스 Method and apparatus for pre-heating lng boil-off gas to ambient temperature prior to compression in a reliquefaction system
US7581411B2 (en) 2006-05-08 2009-09-01 Amcs Corporation Equipment and process for liquefaction of LNG boiloff gas
KR100733157B1 (en) * 2006-08-28 2007-06-28 모던산업가스(주) Lng carrier function test mechanism
US8028724B2 (en) 2007-02-12 2011-10-04 Daewoo Shipbuilding & Marine Engineering Co., Ltd. LNG tank and unloading of LNG from the tank
KR100835090B1 (en) * 2007-05-08 2008-06-03 대우조선해양 주식회사 System and method for supplying fuel gas of lng carrier
US7644676B2 (en) 2008-02-11 2010-01-12 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Storage tank containing liquefied natural gas with butane
KR20090107805A (en) 2008-04-10 2009-10-14 대우조선해양 주식회사 Method and system for reducing heating value of natural gas
JP2013087911A (en) * 2011-10-20 2013-05-13 Mitsubishi Heavy Ind Ltd Pressure rise suppression device for storage tank, pressure rise suppression system provided therewith, suppression method therefor, liquefied gas carrying vessel provided therewith, and liquefied gas storage facility provided therewith
US20140174105A1 (en) * 2012-12-24 2014-06-26 General Electric Campany Systems and methods for re-condensation of boil-off gas
FR3044071B1 (en) * 2015-11-24 2018-05-11 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude METHOD AND SYSTEM FOR STORING A LIQUEFIED GASEOUS MIXTURE, IN PARTICULAR LIQUEFIED AIR
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Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2783624A (en) * 1951-09-29 1957-03-05 Constock Liquid Methane Corp Method of liquefying gas
NO133287C (en) * 1972-12-18 1976-04-07 Linde Ag
US4675037A (en) * 1986-02-18 1987-06-23 Air Products And Chemicals, Inc. Apparatus and method for recovering liquefied natural gas vapor boiloff by reliquefying during startup or turndown

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JP2014148306A (en) * 2009-06-30 2014-08-21 Wartsila Oil And Gas Systems As Method and system for storing and transporting liquefied petroleum gas
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US9810376B2 (en) 2009-06-30 2017-11-07 Wartsila Oil & Gas Systems As Method and system for storage and transport of liquefied petroleum gases
US9982844B2 (en) 2009-06-30 2018-05-29 Wärtsilä Oil & Gas Systems As Method and system for storage and transport of liquefied petroleum gases
US10006589B2 (en) 2009-06-30 2018-06-26 Wärtsilä Oil & Gas Systems As Method and system for storage and transport of liquefied petroleum gases
WO2011046315A3 (en) * 2009-10-16 2011-09-01 대우조선해양 주식회사 Ship for supplying liquefied fuel gas
US9604706B2 (en) 2009-10-16 2017-03-28 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Ship for supplying liquified fuel gas

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FI114820B (en) 2004-12-31
AU6752298A (en) 1998-10-20
NO971364L (en) 1998-09-25
FI990552A0 (en) 1999-03-12
FI990552A (en) 1999-05-12
AU715939B2 (en) 2000-02-10
KR19990046828A (en) 1999-07-05
NO971364D0 (en) 1997-03-21
KR100356764B1 (en) 2002-10-18
JP3455765B2 (en) 2003-10-14
WO1998043029A1 (en) 1998-10-01

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