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WO2025184681A1 - Procédé et système de contrôle de la temperature d'un reformeur - Google Patents

Procédé et système de contrôle de la temperature d'un reformeur

Info

Publication number
WO2025184681A1
WO2025184681A1 PCT/AT2025/060095 AT2025060095W WO2025184681A1 WO 2025184681 A1 WO2025184681 A1 WO 2025184681A1 AT 2025060095 W AT2025060095 W AT 2025060095W WO 2025184681 A1 WO2025184681 A1 WO 2025184681A1
Authority
WO
WIPO (PCT)
Prior art keywords
reformer
gas
stream
flow
oxidation catalyst
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/AT2025/060095
Other languages
German (de)
English (en)
Other versions
WO2025184681A8 (fr
Inventor
Christoph SCHLUCKNER
Bhargav Pandya
Klaus HADL
Raphael NEUBAUER
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
AVL List GmbH
Original Assignee
AVL List GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by AVL List GmbH filed Critical AVL List GmbH
Publication of WO2025184681A1 publication Critical patent/WO2025184681A1/fr
Publication of WO2025184681A8 publication Critical patent/WO2025184681A8/fr
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • 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
    • H01M8/04007—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids related to heat exchange
    • H01M8/04014—Heat exchange using gaseous fluids; Heat exchange by combustion of 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
    • H01M8/04082—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
    • 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
    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/066—Integration with other chemical processes with fuel cells
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0833—Heating by indirect heat exchange with hot fluids, other than combustion gases, product gases or non-combustive exothermic reaction product gases
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/16—Controlling the process
    • C01B2203/1614—Controlling the temperature
    • C01B2203/1623—Adjusting the temperature
    • 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

Definitions

  • the present invention relates to a control method for controlling a reformer temperature, an arrangement for controlling a reformer temperature and a fuel cell system having such an arrangement.
  • a reformer can be used to produce a hydrogen-containing reformate or synthesis gas from a fuel.
  • hydrogen is produced from carbon-containing energy sources and water.
  • Catalysts are used for steam reforming. It is also important that the reformer maintains a reforming temperature within a specific temperature range.
  • one object of the present invention is to efficiently and appropriately temper a reformer.
  • control method for controlling a reformer temperature.
  • the control method comprises the following steps:
  • the proportion of reformer gas flowing through the reformer as reformer feed gas and the proportion of reformer gas flowing through the oxidation catalyst as reformer bypass gas are simultaneously controlled.
  • the flow through the high-temperature valve determines the mass flow of the reformer feed gas through the reformer. This allows the reformer temperature to be controlled using the high-temperature valve.
  • the flow path with the oxidation catalyst therefore represents a bypass.
  • a control method is understood in particular to mean a control method; particularly preferably, a control method is used as a synonym for a control method.
  • the high-temperature valve can be designed as a butterfly valve. Furthermore, the high-temperature valve can be continuously adjustable. In particular, it is possible to adjust the high-temperature valve electronically. The flow rate of the high-temperature valve can be adjusted between 0% and 100%. Furthermore, the high-temperature valve is particularly suitable for high temperatures.
  • the reformer can be part of a fuel cell system.
  • the fuel cell system can comprise one or more fuel cell stacks. The multiple fuel cell stacks can, in turn, form part of a fuel cell stack tower.
  • a reformer is a device that can produce hydrogen, a hydrogen-containing reformate, and/or a synthesis gas from a fuel.
  • the chemical reaction is based on steam reforming.
  • Steam reforming is a process for producing hydrogen from carbon-containing energy sources and water.
  • the oxidation catalyst reduces the proportion of, for example, carbon monoxide, hydrocarbons, and/or formaldehyde in the combustion exhaust gases. It converts gaseous pollutants into harmless substances, such as carbon dioxide and/or water, through oxidation.
  • the reformer feed gas stream is passed through a high-temperature valve and a reformer. This can mean that the reformer feed gas stream flows through the high-temperature valve and the reformer. Heat exchange can occur between the reformer feed gas stream and the reformer. Heat energy is exchanged between the reformer feed gas and the reformer. In this way, the reformer temperature or the reformate equilibrium temperature can be controlled using the reformer feed gas stream.
  • the reformer bypass gas stream is passed over an oxidation catalyst. This can mean that the reformer bypass gas stream flows through the oxidation catalyst.
  • This reformer bypass gas is essentially oxygen-depleted air from the fuel cell stack. It is mixed with the anode exhaust gas, particularly in the bypass. This (now combustible) mixture is converted, particularly in the oxidation catalyst. Without the mixture with the anode exhaust gas, the reformer bypass gas cannot be converted or it would not burn.
  • the stream of reformer bypass gas has a higher pressure than the stream of reformer feed gas. This advantageously ensures that the high-temperature valve is functioning.
  • the high-temperature valve can then be used to control the flow of the reformer feed gas through the reformer. This, in turn, allows the reformer temperature to be adjusted.
  • the flow of reformer bypass gas and the flow of reformer feed gas can be essentially balanced in terms of pressure.
  • the reformer feed gas stream first flows through the high-temperature valve and then through the reformer.
  • the high-temperature valve is arranged upstream of the reformer in the flow direction of the reformer feed gas.
  • a pressure loss of the oxidation catalyst cannot be controlled, which is why the high-temperature valve is arranged upstream of the reformer.
  • This arrangement of the high-temperature valve upstream of the reformer makes it possible for no flow to occur on one heating side of the reformer during nominal operation. This is referred to as adiabatic operation.
  • the pressure loss of the reformer bypass gas flow at the oxidation catalyst is greater than the pressure loss of the reformer feed gas flow at the reformer. This ensures that more mass flow flows through the reformer than through the oxidation catalyst.
  • it can be additionally controlled to prevent the reformer from overheating, i.e., the "excess" mass flow is directed through the oxidation catalyst. The mass flow through the oxidation catalyst is therefore solely the result of the control of the mass flow through the reformer.
  • the flow of reformer feed gas after flowing through the reformer and the flow of reformer bypass gas after flowing through the oxidation catalyst are combined by means of an exhaust gas flow connector to form a flow of exhaust gas.
  • the reformer gas stream is formed by a stream of diverted supply air and a stream of cathode exhaust gas.
  • the diverted supply air stream and the stream of cathode exhaust gas can be combined by means of a reformer gas flow connector.
  • the diverted supply air stream and the stream of cathode exhaust gas can be additionally mixed in a reformer gas mixer.
  • the branched supply air stream is branched from a supply air stream.
  • the supply air stream supplied to the cathode feed gas section of the fuel cell stack is referred to as the cathode feed gas stream.
  • the cathode exhaust gas stream is diverted from the cathode exhaust gas section of the fuel cell stack.
  • a stream of oxidation catalyst feed gas which is formed from the reformer bypass gas stream and a stream of anode exhaust gas, is passed through the oxidation catalyst.
  • the reformer bypass gas stream and the anode exhaust gas stream can be combined by means of an oxidation catalyst flow connector.
  • the reformer bypass gas stream and the anode exhaust gas stream can be additionally mixed in an oxidation catalyst gas mixer.
  • the anode exhaust gas stream is diverted from the anode exhaust gas section of the fuel cell stack.
  • an anode exhaust high-temperature valve is inserted into the anode exhaust stream to control which portion of the anode exhaust stream flows through the oxidation catalyst.
  • the anode exhaust high-temperature valve is arranged upstream of the oxidation catalyst flow connector in the flow direction of the anode exhaust stream.
  • the stream of anode exhaust gas is divided into an anode exhaust gas portion which is passed through the oxidation
  • the catalyst is then divided into an anode exhaust gas recycle gas portion, which is fed to a fuel feed gas stream.
  • the fuel feed gas stream is reformed in the reformer.
  • the reformed gas is fed to the anode feed gas section of the fuel cell stack as an anode feed gas stream. Heat exchange between the anode exhaust gas stream and the anode feed gas stream can occur via a fuel heat exchanger.
  • the arrangement comprises a reformer gas flow splitter for dividing a stream of reformer gas into a stream of reformer feed gas and a stream of reformer bypass gas, a reformer for steam reforming, wherein the reformer is arranged in the stream of reformer feed gas, a high-temperature valve for controlling the passage of the reformer feed gas stream through the high-temperature valve and the reformer to thereby control the reformer temperature, wherein the high-temperature valve is arranged in the stream of reformer feed gas, and an oxidation catalyst for purifying exhaust gases, wherein the oxidation catalyst is arranged in the stream of reformer bypass gas.
  • the reformer gas flow divider, the reformer, the high-temperature valve, and the oxidation catalyst are particularly designed for carrying out a method according to the invention for controlling a reformer temperature.
  • the arrangement according to the invention for controlling a reformer temperature has the same advantages as those described for the method according to the invention for controlling a reformer temperature.
  • the high-temperature valve is arranged upstream of the reformer in the flow direction of the reformer feed gas stream.
  • the high-temperature valve is arranged upstream of the reformer, since a pressure loss of the oxidation catalyst cannot be controlled.
  • the arrangement comprises an exhaust gas flow connector that connects the reformer feed gas flow and the reformer bypass gas flow to form an exhaust gas flow.
  • the exhaust gas flow connector is arranged downstream of the reformer in the flow direction of the reformer feed gas flow and downstream of the oxidation catalyst in the flow direction of the reformer bypass gas flow.
  • the reformer in the reformer feed gas flow and the oxidation catalyst in the reformer bypass gas flow are thus arranged parallel to one another.
  • the arrangement comprises a reformer gas flow connector that connects a stream of branched supply air and a stream of cathode exhaust gas to the reformer gas stream.
  • a reformer gas mixer can be arranged downstream of the reformer gas flow connector in the flow direction of the reformer gas stream. The reformer gas mixer can be used to thoroughly mix the reformer gas stream.
  • the arrangement comprises an oxidation catalyst flow connector that connects the reformer bypass gas stream and a stream of anode exhaust gas to form a stream of oxidation catalyst feed gas.
  • the oxidation catalyst flow connector is arranged in the reformer bypass gas stream between the reformer gas flow divider and the oxidation catalyst.
  • the oxidation catalyst feed gas is passed through the oxidation catalyst.
  • the arrangement can comprise an oxidation catalyst gas mixer arranged between the oxidation catalyst flow connector and the oxidation catalyst.
  • the oxidation catalyst gas mixer can mix the oxidation catalyst feed gas stream, i.e., the reformer bypass gas stream, and the anode exhaust gas stream.
  • an anode exhaust gas high-temperature valve is arranged in the anode exhaust gas flow for controlling the flow of the anode exhaust gas flow through the oxidation catalyst.
  • the anode exhaust gas high-temperature valve is arranged in the flow direction of the Stream of anode exhaust gas arranged upstream of the oxidation catalyst flow connector.
  • the arrangement may further comprise an anode exhaust flow divider.
  • the anode exhaust flow divider divides the anode exhaust flow into an anode exhaust gas portion, which flows through the oxidation catalyst, and an anode exhaust gas recycle portion, which is fed to a fuel feed gas stream.
  • the fuel feed gas stream is reformed in the reformer.
  • the reformed gas is fed to the anode feed gas section of the fuel cell stack as an anode feed gas stream.
  • the arrangement may further comprise a fuel heat exchanger. Heat exchange between the anode exhaust gas stream and the anode feed gas stream can occur via the fuel heat exchanger.
  • a fuel cell system is also described.
  • the fuel cell system comprises at least one fuel cell stack for generating electrical power and at least one arrangement according to the invention for controlling a reformer temperature.
  • the fuel cell system may comprise one or more fuel cell stacks.
  • the multiple fuel cell stacks may, in turn, form part of a fuel cell stack tower.
  • Fig. 1 is a schematic view of a fuel cell system according to the invention with a fuel cell stack and an arrangement according to the invention for controlling a reformer temperature.
  • Fig. 1 shows a schematic view of a fuel cell system 100 according to the invention, comprising a fuel cell stack 110 for generating electrical power and an arrangement 10 according to the invention for controlling a reformer temperature.
  • the fuel cell system 100 can have multiple fuel cell stacks 110.
  • the multiple fuel cell stacks 110 can be part of a fuel cell stack tower.
  • multiple arrangements 10 can be provided.
  • the fuel cell stack 110 shown in Fig. 1 has a cathode supply gas section 60 for supplying a stream of cathode supply gas KZG, a cathode exhaust gas section 62 for discharging a stream of cathode exhaust gas KAG, an anode exhaust gas section 64 for discharging a stream of anode exhaust gas AAG and an anode supply gas section 66 for supplying a stream of anode supply gas AZG.
  • the arrangement 10 for controlling a reformer temperature comprises a reformer gas flow divider 28, a reformer 20, a high-temperature valve 30, and an oxidation catalyst 40.
  • the reformer gas flow divider 28 serves to divide a stream of reformer gas 22 into a stream of reformer feed gas 24 and a stream of reformer bypass gas 26.
  • the reformer 20 is used for steam reforming.
  • the reformer 20 is arranged in the stream of reformer feed gas 24.
  • the high-temperature valve 30 serves to control the passage of the stream of reformer feed gas 24 through the high-temperature valve 30 and the reformer 20. By controlling the passage of the stream of reformer feed gas 24, the reformer temperature can also be controlled.
  • the high-temperature valve 30, like the reformer 20, is arranged in the stream of reformer feed gas 24.
  • the oxidation catalyst 40 is used to purify exhaust gases.
  • the oxidation catalyst 40 is arranged in the stream of reformer bypass gas 26.
  • the high-temperature valve 30 is used to control the proportion of the reformer gas 22 that flows through the reformer 20 as reformer feed gas 24. and the proportion of reformer gas 22 that flows through the oxidation catalyst 40 as reformer bypass gas 26.
  • the path through the oxidation catalyst 40 represents a bypass.
  • the passage through the high-temperature valve 30 determines the mass flow of the reformer feed gas 24 through the reformer 20 and thus the reformer temperature.
  • the high-temperature valve 30 is arranged upstream of the reformer 20 in the flow direction of the reformer feed gas stream 24. Accordingly, the reformer feed gas stream 24 flows first through the high-temperature valve 30 and then through the reformer 20.
  • a stream of supply air 72 is conducted as a stream of cathode supply gas KZG to the cathode supply gas section 60.
  • a stream of branched supply air 32 is branched off from the stream of supply air 72.
  • the arrangement 10 can have a reformer gas flow connector 12.
  • the reformer gas flow connector 12 connects the flow of branched supply air 32 and the flow of cathode exhaust gas KAG to the flow of reformer gas 22.
  • a reformer gas mixer 74 can be arranged downstream of the reformer gas flow connector 12 in the flow direction of the reformer gas 22 flow. With the aid of the reformer gas mixer 74, the flow of reformer gas 22, which is formed by the flow of branched supply air 32 and the flow of cathode exhaust gas KAG, can be thoroughly mixed.
  • the arrangement 10 can have an exhaust flow connector 42.
  • the exhaust flow connector 42 connects the stream of reformer feed gas 24 and the stream of reformer bypass gas 26 to form a stream of exhaust gas 44.
  • the stream of exhaust gas 44 is directed to an exhaust device 76.
  • the exhaust flow connector 42 is arranged downstream of the reformer 20 in the flow direction of the reformer feed gas 24 and downstream of the oxidation catalyst 40 in the flow direction of the reformer bypass gas 26. Accordingly, the reformer 20 in the stream of reformer feed gas 24 and the oxidation catalyst 40 in the stream of reformer bypass gas 26 are arranged parallel to one another.
  • the assembly 10 may also include an oxidation catalyst flow connector 48 which connects the flow of reformer bypass gas 26 and the flow of Anode exhaust gas AAG connects to a stream of oxidation catalyst feed gas 46.
  • the oxidation catalyst flow connector 48 is arranged in the stream of reformer bypass gas 26 between the reformer gas flow divider 28 and the oxidation catalyst 40.
  • the arrangement 10 can have an oxidation catalyst gas mixer 78, which is arranged between the oxidation catalyst flow connector 48 and the oxidation catalyst 40.
  • the oxidation catalyst gas mixer 78 serves to mix the stream of oxidation catalyst feed gas 46, which is formed from the stream of reformer bypass gas 26 and the stream of anode exhaust gas AAG.
  • the assembly 10 may include an anode exhaust high-temperature valve 50 for controlling the flow of the anode exhaust AAG stream through the oxidation catalyst 40.
  • the anode exhaust high-temperature valve 50 is disposed in the anode exhaust AAG stream.
  • the arrangement may include an anode exhaust flow splitter 80.
  • the anode exhaust flow splitter 80 divides the anode exhaust flow AAG into an anode exhaust gas portion 52 and an anode exhaust gas recirculation gas portion 54.
  • the anode exhaust gas portion 52 flows through the oxidation catalyst 40.
  • the anode exhaust gas recirculation gas portion 54 is fed to a fuel feed gas stream 34 at a fuel feed gas flow connector 92.
  • the fuel feed gas stream 34 is supplied from a fuel supply vessel 90 to the reformer 20 and reformed in the reformer 20.
  • the reformed gas is supplied to the anode feed gas section 66 of the fuel cell stack 110 as anode feed gas stream AZG.
  • the arrangement 10 can further comprise a fuel heat exchanger 82. Heat exchange between the anode exhaust gas stream AAG and the anode feed gas stream AZG can take place via the fuel heat exchanger 82.
  • a protective gas container 94 may be provided.
  • a flow of protective gas 96 can be directed from the protective gas container 94 into the flow of fuel supply gas 34 via a protective gas flow connector 98.
  • the arrangement 10 is particularly designed to carry out the following control method for controlling a reformer temperature. The control method comprises the steps described below.
  • a stream of reformer gas 22 is divided into a stream of reformer feed gas 24 and a stream of reformer bypass gas 26 by means of the reformer gas flow divider 28.
  • the stream of reformer feed gas 24 is passed through a high-temperature valve 30 and a reformer 20 for steam reforming.
  • the reformer bypass gas stream 26 is passed through an oxidation catalyst 40 to purify exhaust gases.
  • these steps are carried out simultaneously.
  • the high-temperature valve 30 can be used to control the flow of reformer feed gas 24 through the high-temperature valve 30 and the reformer 20. By controlling the flow of reformer feed gas 24, the reformer temperature can in turn be controlled. In particular, the high-temperature valve 30 also indirectly controls the flow of reformer bypass gas 26, i.e., the setting of the high-temperature valve 30 determines how much flows through the bypass.
  • the stream of reformer bypass gas 26 may have a higher pressure than the stream of reformer feed gas 24. Furthermore, a pressure drop of the stream of reformer bypass gas 26 at the oxidation catalyst 40 may be greater than a pressure drop of the stream of reformer feed gas 24 at the reformer 20.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Sustainable Energy (AREA)
  • Sustainable Development (AREA)
  • Manufacturing & Machinery (AREA)
  • Electrochemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Fuel Cell (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

La présente invention concerne un procédé de contrôle permettant de contrôler une température de reformeur, ledit procédé comprenant les étapes suivantes : séparer un flux de gaz de reformeur (22) en un flux de gaz d'alimentation de reformeur (24) et en un flux de gaz de dérivation de reformeur (26) au moyen d'un séparateur de flux de gaz de reformeur (28), guider le flux de gaz d'alimentation de reformeur (24) par l'intermédiaire d'une vanne haute température (30) et d'un reformeur (20) en vue du reformage à la vapeur, guider le flux de gaz de dérivation de reformeur (26) par l'intermédiaire d'un catalyseur d'oxydation (40) en vue de l'épuration des gaz brûlés, le passage du flux de gaz d'alimentation de reformeur (24) par la vanne haute température (30) et le reformeur (20) étant contrôlé au moyen de la vanne haute température (30), de manière à contrôler ainsi la température de reformeur.
PCT/AT2025/060095 2024-03-06 2025-03-05 Procédé et système de contrôle de la temperature d'un reformeur Pending WO2025184681A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ATA50194/2024 2024-03-06
ATA50194/2024A AT528078A1 (de) 2024-03-06 2024-03-06 Kontrollverfahren und Anordnung zum Kontrollieren einer Reformertemperatur

Publications (2)

Publication Number Publication Date
WO2025184681A1 true WO2025184681A1 (fr) 2025-09-12
WO2025184681A8 WO2025184681A8 (fr) 2025-10-02

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Application Number Title Priority Date Filing Date
PCT/AT2025/060095 Pending WO2025184681A1 (fr) 2024-03-06 2025-03-05 Procédé et système de contrôle de la temperature d'un reformeur

Country Status (2)

Country Link
AT (1) AT528078A1 (fr)
WO (1) WO2025184681A1 (fr)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH05326003A (ja) * 1992-05-21 1993-12-10 Ishikawajima Harima Heavy Ind Co Ltd 燃料電池発電設備の改質器温度制御方法
US20020108306A1 (en) * 2001-02-12 2002-08-15 Grieve Malcolm James Reformer controls
EP3316371B1 (fr) * 2016-10-25 2023-12-20 Robert Bosch GmbH Système de piles à combustible comprenant un reformeur chauffé par les effluents cathodiques

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101958250B1 (ko) * 2017-05-23 2019-07-04 주식회사 미코 연료전지 시스템
GB2589592B (en) * 2019-12-03 2022-04-06 Ceres Ip Co Ltd Improved fuel cell systems and methods

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH05326003A (ja) * 1992-05-21 1993-12-10 Ishikawajima Harima Heavy Ind Co Ltd 燃料電池発電設備の改質器温度制御方法
US20020108306A1 (en) * 2001-02-12 2002-08-15 Grieve Malcolm James Reformer controls
EP3316371B1 (fr) * 2016-10-25 2023-12-20 Robert Bosch GmbH Système de piles à combustible comprenant un reformeur chauffé par les effluents cathodiques

Also Published As

Publication number Publication date
WO2025184681A8 (fr) 2025-10-02
AT528078A1 (de) 2025-09-15

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