WO2009059571A1 - Système de cellule à combustible à haute température avec circuit partiel du gaz d'anode et évacuation de composants gazeux - Google Patents

Système de cellule à combustible à haute température avec circuit partiel du gaz d'anode et évacuation de composants gazeux Download PDF

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Publication number
WO2009059571A1
WO2009059571A1 PCT/DE2007/002032 DE2007002032W WO2009059571A1 WO 2009059571 A1 WO2009059571 A1 WO 2009059571A1 DE 2007002032 W DE2007002032 W DE 2007002032W WO 2009059571 A1 WO2009059571 A1 WO 2009059571A1
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WIPO (PCT)
Prior art keywords
gas
anode
fuel cell
temperature fuel
cell system
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Ceased
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PCT/DE2007/002032
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German (de)
English (en)
Inventor
Horst-Eckart Vollmar
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Individual
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Priority to PCT/DE2007/002032 priority Critical patent/WO2009059571A1/fr
Priority to DE112007003752T priority patent/DE112007003752A5/de
Publication of WO2009059571A1 publication Critical patent/WO2009059571A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
    • H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
    • H01M8/04097—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with recycling of the reactants
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04291—Arrangements for managing water in solid electrolyte fuel cell systems
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
    • H01M8/0668—Removal of carbon monoxide or carbon dioxide
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
    • H01M8/0687—Reactant purification by the use of membranes or filters
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/10—Fuel cells with solid electrolytes
    • H01M8/12—Fuel cells with solid electrolytes operating at high temperature, e.g. with stabilised ZrO2 electrolyte
    • H01M2008/1293—Fuel cells with solid oxide electrolytes
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
    • H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
    • H01M8/04119—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants with simultaneous supply or evacuation of electrolyte; Humidifying or dehumidifying
    • H01M8/04126—Humidifying
    • H01M8/04141—Humidifying by water containing exhaust gases
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/14—Fuel cells with fused electrolytes
    • H01M8/144—Fuel cells with fused electrolytes characterised by the electrolyte material
    • H01M8/145—Fuel cells with fused electrolytes characterised by the electrolyte material comprising carbonates
    • 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
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells

Definitions

  • the present invention is in the field of high temperature fuel cells; These include the SOFC (Solid Oxide Fuel Cell) and the MCFC (Molten Carbonate Fuel Cell).
  • SOFC Solid Oxide Fuel Cell
  • MCFC Molten Carbonate Fuel Cell
  • Various process schemes according to the prior art and are e.g. in the work of Matthias Finkenrath entitled “Simulation and Analysis of the Dynamic Behavior of Power Plants with Oxide Ceramics Fuel Cell (SOFC)" (ISBN 3-89336-414-5) are discussed as possible ways to increase the efficiency of partial cycle operation of the cathode and / or
  • a further option discussed is the use of waste heat via a turbine
  • the disadvantage of these process schemes is the finite gas utilization of typically 80% and thus combustion
  • a further disadvantage, especially in the case of completely internal reforming of the fuel gas in the fuel cell stack, is the high heat requirement of the steam reforming reaction and associated therewith high temperature gradient seen in the direction of the fuel gas stream. This also leads to strong changes in the current density along the fuel gas
  • the invention relates to a high-temperature fuel cell system with partial cycle of the anode exhaust gas and to a method for operating the high-temperature fuel cell system.
  • Liquid or gaseous fuels for example natural gas, fuel oil, naphtha or biogas, are used to operate the high-temperature fuel cell system.
  • the hydrocarbonaceous fuels are desulfurized, humidified and pre-reformed prior to the electrochemical reaction in the high temperature fuel cell stack.
  • the high-temperature fuel cell system is used for the particularly efficient generation of electrical energy and for the provision of heating or process heat in combined heat and power.
  • the invention is thus based on the object of specifying a method for operating a high-temperature fuel cell system, in which the efficiency of power generation and the provision of heat are optimized.
  • high-temperature fuel cell systems are specified for carrying out the method.
  • the first object is achieved according to the invention by a method for operating a high-temperature fuel cell system in which valuable as fuel gas components of the anode exhaust gas after separation of water vapor, carbon dioxide and nitrogen are supplied to the anode gas space of the high-temperature fuel cell stack again.
  • the anode exhaust gas is fed to a shift reactor in which the carbon monoxide contained reacts with the water vapor contained as quantitatively as possible to form hydrogen and carbon dioxide. Part of the heat still contained is used to evaporate part of the water separated in the subsequent condenser.
  • the residual gas which consists essentially of hydrogen, carbon dioxide, nitrogen and residual constituents of methane and carbon monoxide, is compressed to about 6 to 15 bar and fed to a pressure swing adsorption plant, commonly known as pressure swing adsorption (PSA).
  • PSA pressure swing adsorption
  • the cylindrical containers of the PSA are filled with zeolites or molecular sieves designed for the adsorption of carbon dioxide and nitrogen.
  • the PSA is operated as follows.
  • the molecular sieve Before the molecular sieve is saturated, it is switched over to a second adsorption unit, at the same time carbon dioxide and nitrogen are expelled in the saturated molecular sieve bed by pressure-compensated backwashing. The process is continuously repeated time-controlled.
  • the typically 90 to 99 percent by volume carbon dioxide existing gas stream is discharged as exhaust gas to the environment or compressed in larger plants, CCV-free power plants, for sequestration.
  • the gas stream which is not adsorbed in the PSA and consists essentially of hydrogen with small amounts of methane and carbon monoxide, according to the invention admixed with the fuel supplied to the high-temperature fuel cell system. This is supplied to the anode gas space of the fuel cell stack after heating, humidifying and pre-reforming.
  • part of the anode exhaust gas stream is returned to the anode gas space in two cycles.
  • the exhaust stream is first taken from the subset containing sufficient water vapor to keep the ratio of water vapor to carbon in the subsequent gas flow above a predetermined value, for example 2.
  • This gas stream is fed via an ejector to the preheated fuel gas stream before the pre-reformer.
  • the remainder of the anode exhaust gas stream passes through the heat exchanger, shift reactor, condenser, compressor and PSA as in the previously described embodiment.
  • the PSA preferably carbon dioxide and nitrogen are separated.
  • the remaining residual gas which consists essentially of hydrogen and residues of methane and carbon monoxide, is admixed with the fuel supplied to the high-temperature fuel cell system.
  • part of the compressed anode exhaust gas is removed before the PSA.
  • the second object the optimization of the heat supply, is achieved via a heating circuit, wherein the condenser and heat exchanger the exhaust gas streams for heating purposes or heat-requiring processes at appropriate temperature levels heat is removed.
  • the condensation heat of the water vapor contained is used.
  • the gas separation of the anode exhaust gas is carried out in a 2-stage PSA plant, wherein in the first stage, hydrogen is separated and separated in the second stage carbon dioxide and nitrogen. It is sufficient if the majority, for example, 80% by volume are adsorbed.
  • the hydrogen is removed cyclically from the high temperature fuel cell system. Carbon dioxide and nitrogen are released into the environment as exhaust gas or compressed for sequestration.
  • the withdrawn hydrogen can be used in various industries or used at hydrogen refueling stations for fueling hydrogen powered vehicles.
  • a high-temperature fuel cell system 2 comprises a high-temperature fuel cell stack 10.
  • the high-temperature fuel cell stack comprises individual ceramic cells with a gas-tight electrolyte 12 coated on both sides with an anode and a cathode, which are electrically connected via gas-tight bipolar plates.
  • the bi polar plates further serve to supply the individual cells on the anode side with fuel gas and on the cathode side with oxidant.
  • the high temperature fuel cell system includes an anode path 20 and a cathode path 40.
  • the cathode path to the high temperature fuel cell stack 10 consists of the oxidant inlet 41, which is air or oxygen or oxygen-enriched air a heat exchanger 43 for preheating the oxidant with simultaneous cooling of the cathode exhaust stream 44.
  • the cathode exhaust gas by means of another heat exchanger 45 for heat transfer to a heating or process water circuit 50 on cooled and finally discharged through the gas outlet 46 to the environment.
  • the anode gas stream 20 consists of the path 21 for the fuel, which initially, not shown in FIG 1, is desulfurized. This is heated via a heat exchanger 22 via the steam temperature of the water, humidified via the steam lines 23 (to start the system) or 24 during operation, then partially reformed in a pre-reformer 25 (preferably the higher hydrocarbons) and a further heat exchanger 26 the Anodengasraum 11 of the high-temperature fuel cell stack supplied. After cooling, the anode exhaust gas stream 27 is fed via the heat exchangers 26 and 22 to the shift reactor 28, in which the carbon monoxide CO contained is preferably reacted with the water vapor H 2 O present to form hydrogen H 2 and carbon dioxide CO 2 .
  • the heat still contained in the exhaust gas stream is used in the evaporator 29 in order to evaporate the water supplied via the line 36.
  • the water vapor is supplied via line 24 to the anode gas.
  • the anode exhaust gas is then dehumidified in the condenser 30.
  • the condenser is cooled via the heating or process water circuit 50 and possibly via an additional, not shown in Figure 1 cooling water circuit.
  • the water taken from the anode exhaust gas is split by a regulator into two partial streams in such a way that the partial stream 36 leads to the evaporator in the anode gas stream at a ratio of steam to carbon greater than about 2.
  • the remaining water is discharged via line 37 to the outside.
  • the dehumidified anode exhaust gas is compressed downstream in a compressor 31 to about 6 to 15 bar.
  • the resulting heat of compression is supplied via a heat exchanger 32 to the heating or process water cycle.
  • carbon dioxide CO 2 and nitrogen N 2 are hydrogen H 2 , carbon dioxide CO 2 and nitrogen N 2 , according to the invention in the pressure swing adsorption 33 of the majority of carbon dioxide CO 2 and nitrogen N 2 separated and discharged via the extraction line 35 to the environment or to Sequestration of CO 2 compacted.
  • the most cylindrical gas tank pressure swing adsorption are with Molecular sieves or zeolites filled, which are adapted to the task of the invention, preferably to adsorb carbon dioxide CO 2 and nitrogen N 2 at high pressures and release them again after the expansion.
  • the cyclic operation of the pressure swing adsorption plant follows the state of the art.
  • the necessary valves are omitted in FIG.
  • the gas which is not adsorbed in the pressure swing adsorption system is admixed via line 34 to the fuel supplied via the inlet 21 to the high-temperature fuel cell system.
  • the preferred separation according to the invention from a pressure swing adsorption plant and the supply of the portions of the anode exhaust gas usable in the fuel cell stack 10 via the supply line 38 to the anode gas path 20 are combined with a partially direct supply of the anode exhaust gas to the anode gas.
  • the anode exhaust gas removed from the anode gas chamber 11 of the high-temperature fuel cell stack 10 via the line 26 is split into two partial streams 27 and 28 via a regulator, not shown in FIG.
  • the partial flow 27 is supplied via an ejector 34 and the line 35 to the anode gas path 20 before the pre-reformer 24.
  • the amount of anode exhaust gas in the direct Kreisleuf via the extraction line 27 is such that the molar ratio of water vapor to carbonaceous compounds is equal to or slightly greater than 2. Thus, sufficient steam is supplied to the anode gas space and deposition of carbon is avoided.
  • the anode exhaust gas flowing into the line 28 is fed via the heat exchangers 25, 45 and 22 to the shift reactor 29, dehydrated in the condenser 30 and compressed in the compressor 31.
  • the compressed anode exhaust gas is divided into the partial stream 33, which is supplied to the ejector, and the partial stream 32, which is supplied to the heat extraction in the heat exchanger 36 of the gas separation in the pressure swing adsorption 37.
  • the pressure swing adsorption plant is, as described in FIG 1, operated.
  • the part stream taken from the pressure swing adsorption unit 39 contains the major proportion of carbon dioxide CO 2 and nitrogen N 2, which is discharged to the outside, while the portion of stream 38, which contains predominantly electrochemically usable fuel gas is supplied to the Anodengasweg 20 fed back.
  • the pressure swing adsorption plant 33 is embodied in two stages so that predominantly hydrogen H 2 in the first stage and predominantly carbon dioxide CO 2 in the second stage and nitrogen N 2 adsorbed and released cyclically become.
  • the removal line 60 high-purity gas or high-purity hydrogen H 2 is discharged for applications outside the high-temperature fuel cell system.
  • the pressure swing adsorption plant 37 is configured in two stages with the discharge of gas with a high hydrogen content or hydrogen of high purity H 2 as in FIG Applications outside the high-temperature fuel cell system.

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  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Engineering & Computer Science (AREA)
  • Manufacturing & Machinery (AREA)
  • Sustainable Energy (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Fuel Cell (AREA)

Abstract

L'invention concerne un procédé de production d'énergie électrique et de chaleur utile partir de composés d'hydrocarbures au moyen de cellules à combustible à haute température, à un rendement électrique aussi élevé que possible. Selon l'invention, le gaz dégagé à l'anode est amené à une séparation de gaz dans laquelle de préférence le dioxyde de carbone et l'azote sont séparés et évacués, tandis que le gaz résiduel est renvoyé dans la chambre à gaz d'anode. Dans une variante, une partie du gaz dégagé à l'anode est amenée directement à l'espace prévu pour le gaz d'anode dans la pile de cellules à combustible à haute température et le reste est envoyé à la séparation de gaz. Dans une autre variante, la séparation de gaz est réalisée en deux étapes ; après la première étape, l'hydrogène est séparé et évacué et après la deuxième étape, le dioxyde de carbone et l'azote sont séparés et évacués du circuit de gaz d'anode. La chaleur dégagée est transférée par un échangeur de chaleur et un séparateur d'eau à un circuit de chauffage ou à un circuit d'eau de processus.
PCT/DE2007/002032 2007-11-10 2007-11-10 Système de cellule à combustible à haute température avec circuit partiel du gaz d'anode et évacuation de composants gazeux Ceased WO2009059571A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
PCT/DE2007/002032 WO2009059571A1 (fr) 2007-11-10 2007-11-10 Système de cellule à combustible à haute température avec circuit partiel du gaz d'anode et évacuation de composants gazeux
DE112007003752T DE112007003752A5 (de) 2007-11-10 2007-11-10 Hochtemperaturbrennstoffzellensystem mit teilweisem Kreislauf des Anodenabgases und Ausschleusung von Gaskomponenten

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PCT/DE2007/002032 WO2009059571A1 (fr) 2007-11-10 2007-11-10 Système de cellule à combustible à haute température avec circuit partiel du gaz d'anode et évacuation de composants gazeux

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Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014131553A1 (fr) * 2013-02-27 2014-09-04 Bayerische Motoren Werke Aktiengesellschaft Système de pile à combustible
EP2940773A1 (fr) * 2014-04-29 2015-11-04 Haldor Topsøe A/S Éjecteur pour système d'empilement de cellule d'électrolyse d'oxyde solide
CN110739471A (zh) * 2019-09-11 2020-01-31 张家港氢云新能源研究院有限公司 基于重整制氢装置与燃料电池的热电联供系统
EP3836268A1 (fr) * 2016-04-21 2021-06-16 Fuelcell Energy, Inc. Post-traitement d'échappement d'anode de pile à combustible à carbonate fondu pour la capture de dioxyde de carbone
EP3872910A1 (fr) * 2020-02-25 2021-09-01 Entrepose Group Extraction de co2 dans la boucle de recyclage d'une pile à combustible
US11508981B2 (en) 2016-04-29 2022-11-22 Fuelcell Energy, Inc. Methanation of anode exhaust gas to enhance carbon dioxide capture
WO2022241494A1 (fr) * 2021-05-18 2022-11-24 Avl List Gmbh Dispositif de recirculation pour recirculation de gaz d'échappement d'anode en tant que gaz de recirculation dans un système de pile à combustible
CN115943506A (zh) * 2020-06-23 2023-04-07 罗伯特·博世有限公司 借助产物水的蒸发/冷凝在燃料电池系统的阴极路径中的热传递
WO2023102006A1 (fr) * 2021-12-02 2023-06-08 Versa Power Systems Ltd Système de pile à combustible comportant un éjecteur
US11975969B2 (en) 2020-03-11 2024-05-07 Fuelcell Energy, Inc. Steam methane reforming unit for carbon capture
US12095129B2 (en) 2018-11-30 2024-09-17 ExxonMobil Technology and Engineering Company Reforming catalyst pattern for fuel cell operated with enhanced CO2 utilization
US12334607B2 (en) 2019-11-26 2025-06-17 ExxonMobil Technology and Engineering Company Fuel cell assembly with external manifold for parallel flow
US12347910B2 (en) 2019-11-26 2025-07-01 ExxonMobil Technology and Engineering Company Fuel cell power plant with a racked fuel cell module
US12355085B2 (en) 2018-11-30 2025-07-08 ExxonMobil Technology and Engineering Company Cathode collector structures for molten carbonate fuel cell
US12374703B2 (en) 2018-11-30 2025-07-29 ExxonMobil Technology and Engineering Company Flow field baffle for molten carbonate fuel cell cathode

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DE3913581A1 (de) * 1989-04-25 1990-10-31 Linde Ag Verfahren zum betrieb von brennstoffzellen
WO2001067530A2 (fr) * 2000-03-08 2001-09-13 N.V. Kema Cellule a combustible generant de l'energie electrique avec une meilleure efficacite
WO2004030130A2 (fr) * 2002-09-27 2004-04-08 Questair Technologies Inc. Systèmes améliorés de pile à combustible à oxyde solide
WO2004054029A1 (fr) * 2002-12-10 2004-06-24 Aker Kværner Technology Procede de traitement des gaz residuaires dans une centrale electrique a piles a combustible a base d'oxyde solide
EP1511110A2 (fr) * 2003-08-26 2005-03-02 Forschungszentrum Jülich Gmbh Méthode de production d'énergie avec une pile à combustible à oxyde solide
US20070017367A1 (en) * 2005-07-25 2007-01-25 Ion America Corporation Partial pressure swing adsorption system for providing hydrogen to a vehicle fuel cell

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Publication number Priority date Publication date Assignee Title
DE3913581A1 (de) * 1989-04-25 1990-10-31 Linde Ag Verfahren zum betrieb von brennstoffzellen
WO2001067530A2 (fr) * 2000-03-08 2001-09-13 N.V. Kema Cellule a combustible generant de l'energie electrique avec une meilleure efficacite
WO2004030130A2 (fr) * 2002-09-27 2004-04-08 Questair Technologies Inc. Systèmes améliorés de pile à combustible à oxyde solide
WO2004054029A1 (fr) * 2002-12-10 2004-06-24 Aker Kværner Technology Procede de traitement des gaz residuaires dans une centrale electrique a piles a combustible a base d'oxyde solide
EP1511110A2 (fr) * 2003-08-26 2005-03-02 Forschungszentrum Jülich Gmbh Méthode de production d'énergie avec une pile à combustible à oxyde solide
US20070017367A1 (en) * 2005-07-25 2007-01-25 Ion America Corporation Partial pressure swing adsorption system for providing hydrogen to a vehicle fuel cell

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014131553A1 (fr) * 2013-02-27 2014-09-04 Bayerische Motoren Werke Aktiengesellschaft Système de pile à combustible
EP2940773A1 (fr) * 2014-04-29 2015-11-04 Haldor Topsøe A/S Éjecteur pour système d'empilement de cellule d'électrolyse d'oxyde solide
US11211625B2 (en) 2016-04-21 2021-12-28 Fuelcell Energy, Inc. Molten carbonate fuel cell anode exhaust post-processing for carbon dioxide
EP3836268A1 (fr) * 2016-04-21 2021-06-16 Fuelcell Energy, Inc. Post-traitement d'échappement d'anode de pile à combustible à carbonate fondu pour la capture de dioxyde de carbone
JP2021101427A (ja) * 2016-04-21 2021-07-08 フュエルセル エナジー， インコーポレイテッドＦｕｅｌｃｅｌｌ Ｅｎｅｒｇｙ， Ｉｎｃ． 二酸化炭素回収のための溶融炭酸塩型燃料電池アノード排気の後処理
JP7270916B2 (ja) 2016-04-21 2023-05-11 フュエルセル エナジー， インコーポレイテッド 二酸化炭素回収のための溶融炭酸塩型燃料電池アノード排気の後処理
US11949135B2 (en) 2016-04-21 2024-04-02 Fuelcell Energy, Inc. Molten carbonate fuel cell anode exhaust post-processing for carbon dioxide capture
US11508981B2 (en) 2016-04-29 2022-11-22 Fuelcell Energy, Inc. Methanation of anode exhaust gas to enhance carbon dioxide capture
US12095129B2 (en) 2018-11-30 2024-09-17 ExxonMobil Technology and Engineering Company Reforming catalyst pattern for fuel cell operated with enhanced CO2 utilization
US12374703B2 (en) 2018-11-30 2025-07-29 ExxonMobil Technology and Engineering Company Flow field baffle for molten carbonate fuel cell cathode
US12355085B2 (en) 2018-11-30 2025-07-08 ExxonMobil Technology and Engineering Company Cathode collector structures for molten carbonate fuel cell
CN110739471A (zh) * 2019-09-11 2020-01-31 张家港氢云新能源研究院有限公司 基于重整制氢装置与燃料电池的热电联供系统
CN110739471B (zh) * 2019-09-11 2022-05-10 张家港氢云新能源研究院有限公司 基于重整制氢装置与燃料电池的热电联供系统
US12347910B2 (en) 2019-11-26 2025-07-01 ExxonMobil Technology and Engineering Company Fuel cell power plant with a racked fuel cell module
US12334607B2 (en) 2019-11-26 2025-06-17 ExxonMobil Technology and Engineering Company Fuel cell assembly with external manifold for parallel flow
EP3872910A1 (fr) * 2020-02-25 2021-09-01 Entrepose Group Extraction de co2 dans la boucle de recyclage d'une pile à combustible
US11975969B2 (en) 2020-03-11 2024-05-07 Fuelcell Energy, Inc. Steam methane reforming unit for carbon capture
CN115943506A (zh) * 2020-06-23 2023-04-07 罗伯特·博世有限公司 借助产物水的蒸发/冷凝在燃料电池系统的阴极路径中的热传递
WO2022241494A1 (fr) * 2021-05-18 2022-11-24 Avl List Gmbh Dispositif de recirculation pour recirculation de gaz d'échappement d'anode en tant que gaz de recirculation dans un système de pile à combustible
WO2023102006A1 (fr) * 2021-12-02 2023-06-08 Versa Power Systems Ltd Système de pile à combustible comportant un éjecteur

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