JP4494338B2 - 液化天然ガスの再ガス化によるパワーサイクル - Google Patents
液化天然ガスの再ガス化によるパワーサイクル Download PDFInfo
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- JP4494338B2 JP4494338B2 JP2005500635A JP2005500635A JP4494338B2 JP 4494338 B2 JP4494338 B2 JP 4494338B2 JP 2005500635 A JP2005500635 A JP 2005500635A JP 2005500635 A JP2005500635 A JP 2005500635A JP 4494338 B2 JP4494338 B2 JP 4494338B2
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- natural gas
- demethanizer
- plant
- gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
- F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
- F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
- F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
- F17C9/04—Recovery of thermal energy
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J3/0204—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 characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
- F25J3/0214—Liquefied natural gas
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J3/0228—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 characterised by the separated product stream
- F25J3/0233—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 characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J3/0228—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 characterised by the separated product stream
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- F17C2221/035—Propane butane, e.g. LPG, GPL
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- 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
- F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
- F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
- F17C2223/0146—Two-phase
- F17C2223/0153—Liquefied gas, e.g. LPG, GPL
- F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
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- 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
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- F17C2225/01—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the phase
- F17C2225/0107—Single phase
- F17C2225/0123—Single phase gaseous, e.g. CNG, GNC
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- 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
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- F17C2225/01—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the phase
- F17C2225/0146—Two-phase
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- F17C2225/033—Small pressure, e.g. for liquefied gas
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- 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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
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Description
図1は本発明の主題事項による一つの例示のパワーサイクル構成の概略図である。
図2は本発明の主題事項による一つの例示のプラント構成の概略図である。
図3は本発明の主題事項による別の例示のプラント構成の概略図である。
図4は図2による例示の集積化設備の計算された全体バランスを掲げた表である。
本発明者は、LNG中の冷却容量を有効に利用する方法でLNGを加工することができるということを見出した。特に、本発明者は、LNG流を所望の圧力までポンプ圧送し、第1および第2の部分に分割し、ここで第1の部分は作業流体として動作し、および第2の部分は脱メタン装置用の還流物として動作することができるということを見出した。このような構成においては、LNGは、メタンを脱メタン装置中でLNGから生成させる閉鎖型メタンランキン(Rankine)パワーサイクルにおいて凝縮デューティを供給する。
図2に示すプラントの例示の構成において、選択された流れの種々の成分のモル分率を計算し、および結果を下記の表に掲げる。ここで、「LPG」は脱エタン装置のC3+ボトム留分を指し、「パイプラインガス」は脱メタン装置塔頂生成物を指し、および「エタン」は脱エタン装置塔頂生成物を指す。CNGおよびLNGモーター燃料は脱メタン装置塔頂生成物から取り出される。図4中の表1は計算の結果を掲げる。はっきりと判るように、このエタン生成物流れの中にC2成分を特に排除し、C3+成分をLPG流れの中に分離する一方で、このパイプラインガス中のメタン濃度を著しく増加させることができる。
Claims (23)
- 液化天然ガスからプロセス製品を形成する脱メタン装置(114)を含み、前記脱メタン装置は前記液化天然ガスの一部(6)を脱メタン装置還流物として使用し、および膨張タービン(109)が前記プロセス製品を膨張させて、仕事を生み出す、液化天然ガス用の再ガス化プラント(1)。
- 前記プロセス製品が脱メタン装置塔頂蒸気(9)を含んでなる、請求項1に記載の再ガス化プラント。
- 前記プロセス製品が脱メタン装置塔頂蒸気(9)と販売ガス流れ(25)からの再循環蒸気(18)から形成される、請求項2に記載の再ガス化プラント。
- 前記脱メタン装置塔頂蒸気(9)と前記再循環蒸気(18)が、前記液化天然ガス(3)を冷媒として用いて、前記膨張タービン(109)の上流にある熱交換器(104)中で液化される、請求項3に記載の再ガス化プラント。
- 前記液化蒸気が、加熱・気化されて、前記膨張タービン(109)中で膨張される超臨界プロセス製品(29)が形成される、請求項4に記載の再ガス化プラント。
- 前記再循環蒸気(18)が、前記プロセス製品を前記膨張タービン(109)中で膨張させた後の前記プロセス製品を含んでなる、請求項3に記載の再ガス化プラント。
- 前記液化天然ガスの少なくとも一部(4)を膨張させる第2のエキスパンダー(112)を更に含んでなり、前記液化天然ガスが、前記第2のエキスパンダー(112)中での膨張の前に圧縮され、および熱源中で加熱される、請求項1に記載の再ガス化プラント。
- 前記熱源が、脱メタン装置塔頂熱交換器、脱エタン装置還流凝縮器(115)、タービン燃焼空気取り入れ冷却器、ガスタービンからの煙道ガス、熱回収ユニット、空気分離プラント、海水熱交換器、および加熱炉の少なくとも1つである、請求項7に記載の再ガス化プラント。
- 前記プロセス製品の一部が、前記プラントから圧縮天然ガス(26)として取り出され、および前記液化蒸気の一部が前記プラントから液化燃料ガス(21)として取り出される、請求項4に記載の再ガス化プラント。
- 天然ガスの第1の部分(3)を受け入れ、塔頂製品ガスを生産する脱メタン装置(114)と前記製品ガスを冷却して、製品液体(20)を生産する第1の熱交換器(104);
前記製品液体(20)の少なくとも一部(22)の圧力を上昇させて、加圧製品液体(23)を形成するポンプ(103);
前記加圧製品液体を気化させて、超臨界圧縮製品ガス(29)を形成する第2の熱交換器(108);および
前記超臨界圧縮製品ガス(29)の少なくとも一部を膨張させて、仕事を生み出すエキスパンダー(109)
を含んでなる液化天然ガス再ガス化プラント。 - 前記天然ガスが前記脱メタン装置に入る前に、加圧され加熱されている天然ガスの第2の部分(4)から仕事を取り出す第2のエキスパンダー(112)を更に含んでなる、請求項10に記載のプラント。
- 前記塔頂製品ガスの一部(15)が、前記第2のエキスパンダー(112)に運転可能であるように結合されている圧縮器(113)を用いて、パイプライン圧力まで圧縮される、請求項11に記載のプラント。
- 前記膨張された圧縮製品ガス(18)が、前記塔頂製品ガス(16)と合体される、請求項10に記載のプラント。
- 前記脱メタン装置(114)が、加熱液化天然ガス(6)を脱メタン装置還流物として受け入れる、請求項10に記載のプラント。
- 前記第1の熱交換器(104)が、液化天然ガスを加熱して、前記加熱液化天然ガス(6)を形成する、請求項14に記載のプラント。
- 前記圧縮製品ガスの他の一部が前記プラントから圧縮天然ガス(26)として取り出され、および前記製品液体の他の一部が前記プラントから液化天然ガス燃料(21)として取り出される、請求項10に記載のプラント。
- 加熱された超臨界の液化天然ガス(14)を第1の圧力にまで膨張させる第1のエキスパンダー(112);
加熱・圧縮された脱メタン装置塔頂物を第2の圧力まで膨張させる第2のエキスパンダー(109);
を含んでなり、第1および第2のエキスパンダーは相互に流体的に連結され、前記液化天然ガスの少なくとも1つの成分から仕事を生み出す液化天然ガスを再ガス化するためのプラント。 - 第1のポンプ(102)が前記液化天然ガス(4)の少なくとも一部の圧力を上昇させ、および前記液化天然ガスの一部を熱源により加熱して、加熱・気化された液化天然ガスを形成する、請求項17に記載のプラント。
- 前記熱源が、脱メタン装置塔頂熱交換器、脱エタン装置還流凝縮器(115)、タービン燃焼空気取り入れ冷却器、ガスタービンからの煙道ガス、熱回収ユニット、海水熱交換器および加熱炉の少なくとも1つである、請求項18に記載のプラント。
- 第1の熱交換器(104)が脱メタン装置塔頂物を液化し、第2のポンプ(103)は前記液化された脱メタン装置塔頂物の圧力を上昇させ、および第2の熱交換器(106)は前記加圧された液化脱メタン装置塔頂物を加熱・気化して、加熱・圧縮された脱メタン装置塔頂物を形成する、請求項17に記載のプラント。
- 前記第1の熱交換器(104)が、液化天然ガスフィードを冷媒として用いて、前記脱メタン装置塔頂物を冷却する、請求項20に記載のプラント。
- 前記第2の熱交換器(106)が、膨張された脱メタン装置塔頂物を用いて、前記加圧・液化された脱メタン装置塔頂物を加熱する、請求項21に記載のプラント。
- 前記第2の圧力が約4.826MPa(700psi)と10.342MPa(1500psi)の間のパイプライン圧力であり、および前記第1の圧力が約2.068MPa(300psi)と5.171MPa(750psi)の間の脱メタン装置運転圧力である、請求項17に記載のプラント。
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US47677003P | 2003-06-05 | 2003-06-05 | |
PCT/US2003/026805 WO2004109180A1 (en) | 2003-06-05 | 2003-08-26 | Power cycle with liquefied natural gas regasification |
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