JP5872486B2 - 二酸化炭素循環作動流体を用いた高効率発電のためのシステムおよび方法 - Google Patents
二酸化炭素循環作動流体を用いた高効率発電のためのシステムおよび方法 Download PDFInfo
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- JP5872486B2 JP5872486B2 JP2012551259A JP2012551259A JP5872486B2 JP 5872486 B2 JP5872486 B2 JP 5872486B2 JP 2012551259 A JP2012551259 A JP 2012551259A JP 2012551259 A JP2012551259 A JP 2012551259A JP 5872486 B2 JP5872486 B2 JP 5872486B2
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- F23M5/00—Casings; Linings; Walls
- F23M5/08—Cooling thereof; Tube walls
- F23M5/085—Cooling thereof; Tube walls using air or other gas as the cooling medium
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
- F25J3/04533—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the direct combustion of fuels in a power plant, so-called "oxyfuel combustion"
-
- 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
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- 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
- F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
- F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
- F25J3/04545—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels for the gasification of solid or heavy liquid fuels, e.g. integrated gasification combined cycle [IGCC]
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J3/04612—Heat exchange integration with process streams, e.g. from the air gas consuming unit
- F25J3/04618—Heat exchange integration with process streams, e.g. from the air gas consuming unit for cooling an air stream fed to the air fractionation unit
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K3/00—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein
- F01K3/18—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters
- F01K3/185—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters using waste heat from outside the plant
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K3/00—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein
- F01K3/18—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters
- F01K3/186—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters using electric heat
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F05—INDEXING SCHEMES RELATING TO ENGINES OR PUMPS IN VARIOUS SUBCLASSES OF CLASSES F01-F04
- F05D—INDEXING SCHEME FOR ASPECTS RELATING TO NON-POSITIVE-DISPLACEMENT MACHINES OR ENGINES, GAS-TURBINES OR JET-PROPULSION PLANTS
- F05D2260/00—Function
- F05D2260/60—Fluid transfer
- F05D2260/61—Removal of CO2
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L2900/00—Special arrangements for supplying or treating air or oxidant for combustion; Injecting inert gas, water or steam into the combustion chamber
- F23L2900/07001—Injecting synthetic air, i.e. a combustion supporting mixture made of pure oxygen and an inert gas, e.g. nitrogen or recycled fumes
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L2900/00—Special arrangements for supplying or treating air or oxidant for combustion; Injecting inert gas, water or steam into the combustion chamber
- F23L2900/07002—Injecting inert gas, other than steam or evaporated water, into the combustion chambers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23M—CASINGS, LININGS, WALLS OR DOORS SPECIALLY ADAPTED FOR COMBUSTION CHAMBERS, e.g. FIREBRIDGES; DEVICES FOR DEFLECTING AIR, FLAMES OR COMBUSTION PRODUCTS IN COMBUSTION CHAMBERS; SAFETY ARRANGEMENTS SPECIALLY ADAPTED FOR COMBUSTION APPARATUS; DETAILS OF COMBUSTION CHAMBERS, NOT OTHERWISE PROVIDED FOR
- F23M2900/00—Special features of, or arrangements for combustion chambers
- F23M2900/05004—Special materials for walls or lining
-
- 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
- F25J2230/06—Adiabatic compressor, i.e. without interstage cooling
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/70—Steam turbine, e.g. used in a Rankine cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/80—Hot exhaust gas turbine combustion engine
- F25J2240/82—Hot exhaust gas turbine combustion engine with waste heat recovery, e.g. in a combined cycle, i.e. for generating steam used in a Rankine cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
- F25J2260/80—Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.
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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
- Y02E20/32—Direct CO2 mitigation
-
- 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
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
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Description
燃料、O2およびCO2循環流体を燃焼器に導入する工程であって、上記CO2を少なくとも約8MPaの圧力および少なくとも約200℃の温度で導入する工程と、
燃料を燃焼させて、少なくとも約800℃の温度を有するCO2含有燃焼生成物流を提供する工程と、
燃焼生成物流をタービン全体に膨張させて発電する工程であって、上記タービンは、燃焼生成物流を受容するための入口とCO2含有タービン排気流を放出するための出口とを有し、出口でのタービン排気流に対する入口での燃焼生成物流の圧力比が約12未満である工程と、
タービン排気流を熱交換装置に通して冷却したタービン排気流を提供することによって、熱をタービン排気流から取り出す工程と、
CO2に加えて冷却したタービン排気流中に存在する1種以上の二次成分を冷却したタービン排気流から除去して、精製および冷却したタービン排気流を提供する工程と、
精製および冷却したタービン排気流を、CO2臨界圧を超える圧力まで第1の圧縮機で圧縮して、超臨界CO2循環流体流を提供する工程と、
その密度が少なくとも約200kg/m3になる温度まで超臨界CO2循環流体流を冷却する工程と、
超臨界高密度CO2循環流体を第2の圧縮機に通して、燃焼器への流入に必要な圧力までCO2循環流体を加圧する工程と、
取り出した熱を使用してCO2循環流体の温度を上昇させるように超臨界高密度高圧CO2循環流体を同じ熱交換装置に通す工程と、
燃焼器への再利用のための熱交換装置から流出するCO2循環流体の温度とタービン排気流の温度との差が約50℃未満になるようにさらなる量の熱を超臨界高密度高圧CO2循環流体に供給する工程と、
加熱した超臨界高密度CO2循環流体を燃焼器に再利用する工程と、
を含むことができる。
タービン排気流をその水露点未満の温度まで冷却する工程、
タービン排気流を周囲温度冷却媒体に接触させてさらに冷却する工程、
1種以上の二次成分と共に水を凝縮して、H2SO4、HNO3、HClおよび水銀のうちの1種以上を含む溶液を形成する工程、
冷却したタービン排気流を約15MPa未満の圧力まで加圧する工程、
熱交換装置に通す前に超臨界高密度高圧CO2循環流体流から生成物CO2流を取り出す工程、
燃料として部分燃焼生成物流を使用する工程、
CO2循環流体の存在下でO2を用いて炭素含有燃料を燃焼させる工程であって、炭素含有燃料、O2およびCO2循環流体を、炭素含有燃料を部分的にのみ酸化して、可燃成分、CO2ならびにH2、CO、CH4、H2SおよびNH3のうちの1種以上を含む部分的に酸化された燃焼生成物流を生成するような比で提供する工程、
部分的に酸化された燃焼生成物流の温度が、上記流中の不可燃成分の全てが固体粒子の形態である程に十分に低くなるような比で、炭素含有燃料、O2およびCO2循環流体を提供する工程、
部分的に酸化された燃焼生成物流を1つ以上のフィルタに通す工程、
フィルタを使用して、不可燃成分の残留量を部分的に酸化された燃焼生成物の約2mg/m3未満まで減少させる工程、
燃料として石炭、亜炭または石油コークスを使用する工程、
CO2を含むスラリーとして微粒燃料を提供する工程、
のうちの1つ以上を特徴としてもよい。
炭素含有燃料、O2およびCO2循環流体をトランスピレーション冷却式燃焼器に導入する工程であって、CO2を少なくとも約8MPaの圧力および少なくとも約200℃の温度で導入する工程と、
燃料を燃焼させて、少なくとも約800℃の温度を有するCO2含有燃焼生成物流を提供する工程と、
燃焼生成物流を、タービン全体に膨張させて発電する工程であって、上記タービンは、燃焼生成物流を受容するための入口とCO2含有タービン排気流を放出するための出口とを有し、出口でのタービン排気流に対する入口での燃焼生成物流の圧力比が約12未満である工程と、
タービン排気流を、タービン排気流から熱を取り出してCO2循環流体流を提供する一連の少なくとも2つの熱交換器に通す工程と、
CO2に加えて循環流体流中に存在する1種以上の二次成分をCO2循環流体流から除去する工程と、
CO2循環流体流を、CO2循環流体の圧力を少なくとも約8MPaまで上昇させ、かつ循環流体中のCO2をガス状から超臨界流体状態に変える一連の少なくとも2つの圧縮機に通す工程と、
超臨界CO2循環流体を、取り出した熱を使用してCO2循環流体の温度を少なくとも約200℃(または場合により、僅か約50℃だけタービン排気流の温度よりも低い温度)まで上昇させる同じ一連の少なくとも2つの熱交換器に通す工程と、
を含む発電方法に関するものとして表現してもよい。これは、具体的には、外部熱源(すなわち、1つ以上の熱交換器にタービン排気流を通すことに直接由来しない熱源)からのさらなる熱の導入を含んでもよい。
炭素含有燃料、O2および再利用CO2循環流体を、規定の化学量論比でトランスピレーション冷却式燃焼器に導入する工程であって、上記CO2を少なくとも約8MPaの圧力および少なくとも約200℃の温度で導入する工程、
燃料を燃焼させて、少なくとも約800℃の温度を有するCO2含有燃焼生成物流を生成する工程、
燃焼生成物流を、タービン全体に膨張させて発電する工程であって、上記タービンは、燃焼生成物流を受容するための入口とCO2含有タービン排気流を放出するための出口とを有し、出口でのタービン排気流に対する入口での燃焼生成物流の圧力比が約12未満である工程、
タービン排気流を、熱をタービン排気流から取り出しかつCO2循環流体流を提供する一連の少なくとも2つの熱交換器に通す工程、
CO2循環流体流を、CO2循環流体の圧力を少なくとも約8MPaまで上昇させ、かつ循環流体中のCO2をガス状から超臨界流体状態に変える一連の少なくとも2つの圧縮機に通す工程、
CO2循環流体流を分離装置に通す工程であって、化学量論的に必要な量のCO2を再利用し、かつ燃焼器まで導き、大気に放出することなくあらゆる過剰なCO2を取り出す工程、および
再利用CO2循環流体を、取り出した熱を使用して、燃焼器内への導入前にCO2循環流体の温度を少なくとも約200℃(または場合により、僅か約50℃だけタービン排気流の温度よりも低い温度)まで上昇させる同じ一連の少なくとも2つの熱交換器に通す工程、
を含むことができ、
ここでは、燃焼効率は50%超であり、前記効率は、生成される正味電力と、発電のために燃焼される炭素含有燃料の総低位発熱量熱エネルギーとの比として計算する。
CO2循環流体流をCO2臨界圧を超える圧力まで圧縮するように構成された第1の圧縮機、
CO2循環流体流を燃焼器への流入に必要とされる圧力まで圧縮するように構成された第2の圧縮機、
CO2循環流体流をその密度が約200kg/m3超となる温度まで冷却するように構成された冷却装置、
熱を外部源から燃焼器の上流であって第2の圧縮機の下流にあるCO2循環流体まで伝達させる1つ以上の伝熱構成要素、
トランスピレーション冷却式燃焼器の上流にそこに流体連通して配置された第2の燃焼器、
第2の燃焼器とトランスピレーション冷却式燃焼器との間に配置された1つ以上のフィルタまたは分離装置、
流動化媒体で微粒燃料材料のスラリーを形成するための混合装置、
固体燃料を微粒子化するための粉砕装置、
のうちの1つ以上を含んでいてもよい。
CO2循環流体をCO2の臨界圧を上回る圧力まで圧縮する工程、
所要の電力タービン入口温度、例えば、約500℃超(または本明細書に記載されているような他の温度範囲)を達成するためにCO2富化超臨界再利用流体を混合するための装置により、固体、液体またはガス状の炭化水素燃料を実質的に純粋なO2中で直接燃焼させる工程、
軸動力の生成と共に、燃焼生成物および再利用CO2富化流体で形成された超臨界流をタービンで膨張させる工程であって、特に約2MPaを超え、かつ流体を周囲温度冷却手段の使用により一貫した温度まで冷却した際にCO2液相が現れる圧力よりも低い圧力(例えば、約7.3〜7.4MPa)まで膨張させる工程、
タービン排気を、タービン排気を冷却し、かつ熱を再利用CO2富化超臨界流体まで伝達させる熱交換器に導入する工程、
熱交換器を離れるCO2含有流を周囲温度冷却手段に接触させて冷却する工程、および少なくとも微濃度のCO2を含有する水液相と少なくとも微濃度の水蒸気を含有するガス状のCO2相とを分離する工程、
SO2、SO3、H2O、NO、NO2、O2および/またはHgに関与する反応が生じ、その結果、流中に存在する98%超の硫黄がH2SO4に変換され、流中に存在する90%超の窒素酸化物がHNO3に変換され、流中の80%超の水銀が可溶性水銀化合物に変換されるように、ガス状CO2と液体水または弱酸相との密接を有する所望の滞留時間(例えば、最大10秒)を可能にするように水分離を行う工程、
気液相分離により主に気相中にN2、ArおよびO2が残った状態でCO2凝固点に近い温度まで冷却することによって、ガス状CO2相から非凝縮性成分(N2、ArおよびO2など)を分離する工程、
精製したガス状CO2流を、周囲温度冷却手段によって冷却することにより高密度のCO2流体(例えば、少なくとも約200kg/m3、好ましくは少なくとも約300kg/m3またはより好ましくは少なくとも約400kg/m3の密度を有する)が得られる圧力までガス圧縮機で圧縮する工程、
周囲温度冷却手段で圧縮したCO2を冷却して、高密度のCO2超臨界流体(例えば、少なくとも約200kg/m3、好ましくは少なくとも約300kg/m3またはより好ましくは少なくとも約400kg/m3の密度を有する)を形成する工程、
高密度CO2流体をCO2の臨界圧を超える圧力まで圧縮機で圧縮する工程、
高圧CO2流を2つの別個の流れ(熱交換器の低温端に流出する1つの流れと約250℃未満の温度で利用可能な外部加熱源を用いて加熱するもう1つの流れ)に分離する工程、
熱交換器の高温端に流出するタービン排気流の温度と、同じ熱交換器の高温端を離れる再利用CO2循環流体の温度との差が約50℃未満(または本明細書に記載されているような他の温度閾値)になるように、効率的な伝熱(任意の外部熱源の使用を含む)を容易にする工程、
CO2循環流体を、約8MPa〜約50MPaの圧力(または本明細書に記載されているような他の圧力範囲)まで圧縮する工程、
O2流を再利用CO2循環流体流の少なくとも一部および炭素含有燃料流と混合して、燃料の自己着火温度よりも低く、かつ約1,200℃〜3,500℃の断熱火炎温度(または本明細書に記載されているような他の温度範囲)が得られるようにその割合が調整されている単一の流体流(または粉末状の固体燃料を使用する場合にはスラリー)を形成する工程、
再利用CO2循環流体の少なくとも一部を燃焼生成物と混合して、約500℃〜1,600℃の範囲の温度(または本明細書に記載されているような他の温度範囲)の混合した流体流を形成する工程、
約2MPa〜約7.3MPaの圧力(または本明細書に記載されているような他の圧力範囲)を有するタービン排気流を生成する工程、
極低温O2装置の1つ以上の空気圧縮機(特に断熱モード)および/またはCO2圧縮機(特に断熱モード)の動作に由来する圧縮熱を用いて高圧CO2循環流体流の一部を外部から加熱する工程であって、上記熱は好適な伝熱流体(CO2流体それ自体を含む)の循環によって伝達される工程、
当量の余分な燃料をバーナで燃焼させながら1つ以上の外部流体流を熱交換器で加熱する工程であって、1つ以上の外部流体流は、熱交換器で過熱することができる蒸気を含んでいてもよい工程、
外部源から提供された蒸気を凝縮することによって供給された熱を使用して、再利用CO2循環流体流の一部を外部から加熱する工程、
熱交換器でCO2含有流(熱交換器の低温端を離れる)を冷却して、外部から提供された流体流を加熱するために熱を提供する工程、
O2のモル濃度が少なくとも約85%(または本明細書に記載されているような他の濃度範囲)であるO2供給流を提供する工程、
燃焼器を離れ(すなわち燃焼生成物流)、かつタービンに流出する総ガス流中のO2濃度が約0.1%モル超になるように燃焼器を動作させる工程、
1つのみの発電タービンを使用するように発電プロセスを行う工程、
1つのみの燃焼器を使用して燃焼器内に投入される炭素含有燃料を実質的に完全に燃焼させるように発電プロセスを行う工程、および
燃焼器に流出するO2流中のO2の量が燃焼器に流出する燃料流の化学量論的燃焼のために必要な量よりも少なく、従って、燃焼生成物流中のH2および一酸化炭素(CO)のうちの一方または両方が生成されるように燃焼器を動作させる工程、および
それぞれが規定の出口圧力を有する2つ以上のタービンを用いてプロセスを行う工程であって、H2およびCOのうちの一方または両方が第1のタービン(および該当する場合、一連のタービンの中の最終タービンを除くその後のタービン)を離れる排気流中に存在し、かつ第2以降のタービンの入口前にO2流を添加して、第2以降のタービンのそれぞれの動作温度を、最後のタービンからの出口流中に過剰なO2(そのような過剰は約0.1%モル超である)が生じるより高い値まで上昇させることによってH2およびCOの一部または全てを燃焼させる工程、
のうちの1つ以上またはそのような工程を行うために有用な装置をさらに特徴としてもよい。
タービン排気流がその水露点未満の温度まで冷却されるように、CO2循環流体を熱交換システムで冷却されるタービン排気流に接触させて加熱する工程、
タービン排気流を周囲温度冷却媒体に接触させて冷却し、かつ燃料およびH2SO4、HNO3、HClを含む燃焼由来の不純物ならびにイオン性化合物溶液の形態のHgや他の金属などの他の不純物と共に水を凝縮する工程、
精製したCO2循環流体を、第1の圧縮機で、その臨界圧を超えるが10MPa未満の圧力まで圧縮する工程、
循環流体を、その密度が600kg/m3を超える時点まで冷却する工程、
高密度CO2循環流体を、本システムにおける圧力降下に打ち勝ち、かつ燃焼室にCO2循環流体を供給するのに必要な圧力まで圧縮機で圧縮する工程、
燃料流中の炭素の燃焼によって生成されたCO2の実質的に全てを含有する生成物CO2流を除去する工程であって、上記CO2流を、第1の圧縮機または第2の圧縮機の排気流のいずれか一方から取り出す工程、
CO2循環流体と熱交換器の高温端におけるタービン排気との温度差が50℃未満になるように、熱交換器に導くか、あるいはCO2循環流体の一部を含む側流を加熱することによって、冷却されるタービン排気流の水露点を超える温度レベルでさらなる量の熱をCO2循環流体に供給する工程、
トランスピレーション冷却式燃焼器内で、O2で部分的に酸化された不燃性残渣を有する炭素含有燃料を含む燃料を使用して、H2、CO、CH4、H2S、NH3および不燃性残渣を含む流を生成する工程であって、上記燃焼器にCO2循環流体の一部を供給して、部分的に酸化された燃焼生成物を、灰が濾過システムによって出口流体流から完全に除去することができる固体粒子として存在する500℃〜900℃の温度まで冷却する工程、
側流を10℃〜50℃の別々に加熱されたCO2循環流体流と再混合する時点で、冷却されるタービン排気と加熱されるCO2循環流体流との間に温度差を与える工程、
水と不純物との分離前に上記流を冷却する際に液体CO2が全く生成されないように、熱交換器の低温端を離れるタービン排気流の圧力を提供する工程、
タービン排気流の少なくも一部を使用して、従来のボイラシステムおよび原子炉に関連する汽力発電システムに由来する複数の蒸気流を過熱する工程、
さらなる低レベルの熱を、発電所などの外部蒸気源から取り出した1つ以上の圧力レベルの蒸気として循環CO2流に提供する工程、
汽力発電所の復水器を離れる凝縮物の少なくとも一部を加熱するために、熱交換器システムの低温端を離れる膨張した排気流を使用する工程、
開放サイクルガスタービンの高温排気から循環CO2流のためにさらなる低レベルの熱を提供する工程、
完全な燃焼のために、燃料としてのCO2を加えた部分的に酸化された石炭由来ガスを第2の燃焼器に通す工程、
燃料の一部をCO2、H2OおよびSO2を含む酸化生成物に酸化し、かつ燃料の残りをH2、COおよびH2Sを含む成分まで酸化するようなO2と燃料との比で、単一の燃焼器を動作させる工程、
第2のタービンによる膨張前に、還元された成分を燃焼させて中間圧流をより高い温度まで再加熱するために第1のタービンの排気流に注入されるO2との所要の総圧力比を超えて2つのタービンを動作させる工程、
のうちの1つ以上を提供してもよい。
Solutions社(カリフォルニア州パコイマ(Pacoima))(耐火性金属被覆)、Orsam Sylvania社(マサチューセッツ州ダンバーズ)(タングステン/銅)およびMarkeTech International社(ワシントン州ポートタウンゼンド)(タングステン)が挙げられる。そのようなトランスピレーション冷却式システムに適した穴あき材料の例としては、上記材料および供給元(例えば、当該製造技術分野で知られている方法を用いて本来非多孔性である構造を穿孔することによって穴あき端部構造が得られる場所)のうちの全てが挙げられる。好適な積層材料の例としては、上記材料および供給元(例えば、当該製造技術分野で知られている方法を用いて所望の端部多孔率を達成するような方法で非多孔性もしくは部分多孔性構造体を積層することによって積層端部構造が得られる場所)のうちの全てが挙げられる。
本発明に係るシステムおよび方法の具体的な一例を図11に示す。以下の記載は、コンピュータモデリングを用いて、具体的な条件下での具体的なサイクルに関して本システムを説明するものである。
本発明に係るシステムおよび方法の別の具体的な例を図12に示す。以下の記載は、コンピュータモデリングを用いて、具体的な条件下での具体的なサイクルに関して本システムを説明するものである。
蒸気条件 HP蒸気:16.6MPa、565℃、流量:473.14kg/sec
LP蒸気:4.02MPa、565℃、流量:371.62kg/sec
正味電力出力:493.7.Mw
既存の発電所のため石炭:1256.1Mw
正味効率(LHV):39.31%
CO2回収率:0%
既存の発電所に本開示のシステムおよび方法が組み込まれた改造型発電所:
CO2電力システム正味電力出力:371.7Mw
既存の発電所の正味電力:639.1Mw
総正味電力:1010.8Mw
CO2電力システムのための石炭:1053.6Mw
既存の発電所のための石炭:1256.1Mw
全体的正味効率(LHV):43.76%
CO2回収率:45.6%*
*この例では既存の発電所からCO2が全く回収されないことに留意されたい。
Claims (59)
- 燃料、O2およびCO2循環流体を燃焼器に導入する工程であって、CO2を少なくとも12MPaの圧力および少なくとも400℃の温度で導入する工程と、
前記燃料を燃焼させて、少なくとも800℃の温度を有するCO2含有燃焼生成物流を提供する工程と、
前記燃焼生成物流をタービンを通じて膨張させて発電する工程であって、前記タービンは、前記燃焼生成物流を受容するための入口と、CO2含有タービン排気流を放出するための出口とを有し、前記出口での前記タービン排気流の圧力に対する前記入口での前記燃焼生成物流の圧力の比は12未満である工程と、
前記タービン排気流を一次熱交換装置に通して冷却されたタービン排気流を提供することによって、前記タービン排気流から熱を取り出す工程と、
前記冷却されたタービン排気流から、CO2に加えて前記冷却されたタービン排気流中に存在する1種以上の二次成分を除去して、精製および冷却されたタービン排気流を提供する工程と、
前記精製および冷却されたタービン排気流を、第1の圧縮機でCO2臨界圧を超える圧力まで圧縮して、超臨界CO2循環流体流を提供する工程と、
前記超臨界CO2循環流体流を、その密度が少なくとも200kg/m3になる温度まで冷却する工程と、
前記超臨界高密度CO2循環流体を第2の圧縮機に通して、前記CO2循環流体を前記燃焼器に投入するために必要な圧力まで加圧する工程と、
前記取り出した熱を使用して前記CO2循環流体の温度を上昇させるように、前記超臨界高密度高圧CO2循環流体を同じ前記一次熱交換装置に通す工程と、
前記燃焼器への再循環のための前記一次熱交換装置を流出する前記CO2循環流体の温度と前記タービン排気流の温度との差が50℃未満になるように、さらなる量の熱を前記超臨界高密度高圧CO2循環流体に供給して、前記CO2循環流体の温度をさらに上昇させる工程と、
前記加熱した超臨界高密度CO2循環流体を前記燃焼器に再利用する工程と、
を含む発電方法。 - 前記取り出す工程により、前記タービン排気流をその水露点未満の温度に冷却する、請求項1に記載の方法。
- 前記除去する工程は、前記タービン排気流を周囲温度冷却媒体に接触させてさらに冷却する工程を含む、請求項1に記載の方法。
- 前記さらに冷却する工程により、前記1種以上の二次成分と共に水を凝縮させて、H2SO4、HNO3、HClおよび水銀のうちの1種以上を含む溶液を形成する、請求項3に記載の方法。
- 前記一次熱交換装置に通す前に、生成物CO2流を前記超臨界高密度高圧CO2循環流体流から取り出す、請求項1に記載の方法。
- 前記生成物CO2流は、前記燃料中の炭素の燃焼によって形成されたCO2の実質的に全てを含む、請求項5に記載の方法。
- 前記燃焼させる工程を1,200℃〜5,000℃の温度で行う、請求項1に記載の方法。
- 前記燃料は部分燃焼生成物流を含む、請求項1に記載の方法。
- 炭素含有燃料をCO2循環流体の存在下でO2で燃焼させる工程を含み、前記炭素含有燃料、O2およびCO2循環流体を、前記炭素含有燃料を部分的にのみ酸化して前記部分燃焼生成物流を生成するような比で提供し、前記流は、不可燃成分、CO2ならびにH2、CO、CH4、H2SおよびNH3のうちの1種以上を含み、
任意に、前記部分燃焼生成物流の温度が前記流中の前記不可燃成分の全てが固体粒子の形態にある程に十分に低くなるような比で、前記炭素含有燃料、O2およびCO2循環流体を提供する、請求項8に記載の方法。 - 前記部分燃焼生成物流を1つ以上のフィルタに通す工程をさらに含む、請求項9に記載の方法。
- 前記炭素含有燃料は、石炭、亜炭または石油コークスを含む、請求項9に記載の方法。
- 前記炭素含有燃料は微粒子形態であり、CO2を含むスラリーとして提供される、請求項11に記載の方法。
- 微粒燃料は、前記粒子の90%超が500μm未満の平均的大きさを有するような燃料である、請求項12に記載の方法。
- 前記CO2循環流体を少なくとも15MPaの圧力で導入する、請求項1に記載の方法。
- 前記CO2循環流体を少なくとも600℃の温度で導入する、請求項1に記載の方法。
- 前記燃焼生成物流は少なくとも1,000℃の温度を有する、請求項1に記載の方法。
- 前記燃焼生成物流は前記燃焼器に導入されるCO2の圧力の少なくとも90%の圧力を有する、請求項1に記載の方法。
- 前記出口での前記タービン排気流の圧力に対する前記入口での前記燃焼生成物流の圧力の比は1.5〜10であり、または
前記出口での前記タービン排気流の圧力に対する前記入口での前記燃焼生成物流の圧力の比は2〜8である、請求項1に記載の方法。 - 前記燃料は炭素含有燃料であり、前記燃焼器に導入される前記燃料中の炭素に対する前記CO2循環流体中のCO2のモル比は10〜50である、請求項1に記載の方法。
- 前記タービン排気流中のCO2はガス状である、請求項1に記載の方法。
- 前記タービン排気流は7MPa以下の圧力を有する、請求項20に記載の方法。
- 前記一次熱交換装置は一連の少なくとも3つの熱交換器を含む、請求項1に記載の方法。
- 前記第2の圧縮機を通った後の前記超臨界高密度CO2循環流体流は、少なくとも15MPaの圧力を有し、または
前記第2の圧縮機を通った後の前記超臨界高密度CO2循環流体流は、少なくとも25MPaの圧力を有する、請求項1に記載の方法。 - 前記超臨界CO2循環流体流をその密度が少なくとも400kg/m3になる温度まで冷却する、請求項1に記載の方法。
- 前記さらなる量の熱は、O2分離装置から取り出した熱を含む、請求項1に記載の方法。
- 前記膨張が、一連の第1のタービンおよび最後のタービンを通じて前記燃焼生成物流を膨張させることを含む、請求項1に記載の方法。
- 前記燃料の一部をCO2、H2OおよびSO2のうちの1種以上を含む酸化生成物に酸化し、前記燃料の残りの部分をH2、CO、CH4、H2S、NH3およびそれらの組み合わせからなる群から選択される1種以上の可燃成分に酸化するような量で、前記O2を提供する、請求項26に記載の方法。
- 前記第1のタービンおよび前記最後のタービンの間の前記燃焼生成物流を加熱する工程と、
任意に第1のタービンの前記出口において、ある量のO2を前記流体流に添加する工程と
を含む、請求項27に記載の方法。 - 前記タービン排気流は過剰量のO2を含む酸化性流体である、請求項1に記載の方法。
- 前記CO2循環流体を、前記O2および前記燃料のうちの一方または両方との混合物として前記燃焼器に導入する、請求項1に記載の方法。
- 前記燃焼器はトランスピレーション冷却式燃焼器を含む、請求項1に記載の方法。
- 前記CO2循環流体を、前記トランスピレーション冷却式燃焼器内に形成された1つ以上のトランスピレーション流体供給路を通して導かれるトランスピレーション冷却流体の全てまたは一部としてトランスピレーション冷却式燃焼器に導入する、請求項31に記載の方法。
- 前記O2を前記O2のモル濃度が少なくとも85%である流として提供する、請求項1に記載の方法。
- 前記O2のモル濃度は85%〜99.8%である、請求項33に記載の方法。
- 前記タービン排気流を、さらなる燃焼器を通さずに前記一次熱交換装置に直接通す、請求項1に記載の方法。
- 前記工程のうちの前記燃焼により、50%を超える燃焼効率が得られ、前記効率は、燃焼して発電する前記燃料の総低位発熱量熱エネルギーに対する生成された熱量の比として計算する、請求項1に記載の方法。
- 前記燃焼させる工程と前記膨張させる工程との間に、前記燃焼生成物流を、固体もしくは液体状態の汚染物質を除去するための少なくとも1つの装置に通す工程をさらに含む、請求項1に記載の方法。
- 前記膨張させる工程と前記取り出す工程との間に、前記タービン排気流を二次熱交換装置に通す工程をさらに含む、請求項1に記載の方法。
- 前記二次熱交換装置は、前記タービン排気流からの熱を使用して汽力発電システムから得られた1つ以上の流を加熱する、請求項38に記載の方法。
- 前記汽力発電システムは従来のボイラシステムを含む、請求項39に記載の方法。
- 前記従来のボイラシステムは石炭火力発電所を含む、請求項40に記載の方法。
- 前記汽力発電システムは原子炉を含む、請求項39に記載の方法。
- 前記1つ以上の加熱した蒸気流を1つ以上のタービンに通して発電する、請求項39に記載の方法。
- 前記さらなる加熱を、前記第2の圧縮機を通した後であり、前記一次熱交換装置に通す前にCO2循環流体流に直接提供し、または前記さらなる加熱を前記熱交換装置に直接提供し、または前記一次熱交換装置が、一連の少なくとも3つの熱交換装置を備え、かつ前記さらなる加熱を、前記CO2循環流体流の一部を含む側流を加熱することにより提供し、前記側流が、2つの前記熱交換装置の間に存在する、
請求項1に記載の方法。 - 燃料、O2およびCO2循環流体流を受容し、かつ前記CO2循環流体の存在下で前記燃料を燃焼させて、少なくとも8MPaの圧力および少なくとも800℃の温度のCO2含有燃焼生成物流を提供する少なくとも1つの燃焼段階を有するように構成された燃焼器と、
前記燃焼器に流体連通した一次発電タービンであって、前記一次タービンは、前記燃焼生成物流を受容するための入口と、CO2含有タービン排気流を放出するための出口とを有し、前記一次タービンは、前記出口での前記タービン排気流の圧力に対する前記入口での前記燃焼生成物流の圧力の比が12未満になるように圧力降下を制御するように構成されているタービンと、
前記タービン排気流を受容し、かつ熱をそこから前記CO2循環流体流に伝達させるための前記一次タービンに流体連通した一次熱交換装置と、
前記熱交換装置に流体連通した、前記CO2循環流体流を加圧するための少なくとも1つの圧縮機と、
外部源から前記燃焼器の上流であって前記少なくとも1つの圧縮機の下流にある前記CO2循環流体に熱を伝達させるように構成された1つ以上の伝熱構成要素と、
を備える発電システム。 - 前記CO2に加えて前記CO2循環流体中に存在する1種以上の二次成分の除去のために前記熱交換装置と前記少なくとも1つの圧縮機との間に配置された1つ以上の分離装置をさらに備える、請求項45に記載の発電システム。
- 前記少なくとも1つの圧縮機は、前記CO2循環流体流をCO2臨界圧を超える圧力まで圧縮するように構成された第1の圧縮機を備える、請求項46に記載の発電システム。
- 前記第1の圧縮機から流出する前記CO2循環流体流をその密度が200kg/m3を超える温度まで冷却するように構成された冷却装置を備える、請求項47に記載の発電システム。
- 前記冷却されたCO2循環流体流の前記燃焼器への投入に必要な圧力まで圧縮するように構成された第2の圧縮機を備える、請求項48に記載の発電システム。
- 前記1つ以上の伝熱構成要素はO2分離装置に関連している、請求項45に記載の発電システム。
- 前記燃焼器は第1の燃焼器であり、前記第1の燃焼器の上流にそこに流体連通して配置された第2の燃焼器をさらに備える、請求項45に記載の発電システム。
- 前記第2の燃焼器と前記第1の燃焼器との間に配置された1つ以上のフィルタまたは分離装置をさらに備える、請求項51に記載の発電システム。
- 流動化媒体で微粒燃料材料のスラリーを形成するための混合装置をさらに備える、請求項51に記載の発電システム。
- 固体燃料を微粒子化するための粉砕装置をさらに備える、請求項51に記載の発電システム。
- 前記熱交換装置は少なくとも2つの熱交換器を含み、または
前記熱交換装置は一連の少なくとも3つの熱交換器を含む、
請求項45に記載の発電システム。 - 前記一次発電タービンは、一連の少なくとも2つのタービンを含む、請求項45に記載の発電システム。
- 前記一次発電タービンと前記一次熱交換装置との間にそれらに流体連通して配置された二次熱交換装置をさらに備える、請求項45に記載の発電システム。
- 少なくとも1つ蒸気流を介して前記二次熱交換装置に流体連通したボイラをさらに備える、請求項57に記載の発電システム。
- 前記二次熱交換装置からの前記少なくとも1つ蒸気流を受容するための入口を有する二次発電タービンをさらに備える、請求項58に記載の発電システム。
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