WO2021077148A1 - Système soec et procédé de fonctionnement d'un système soec - Google Patents

Système soec et procédé de fonctionnement d'un système soec Download PDF

Info

Publication number
WO2021077148A1
WO2021077148A1 PCT/AT2020/060379 AT2020060379W WO2021077148A1 WO 2021077148 A1 WO2021077148 A1 WO 2021077148A1 AT 2020060379 W AT2020060379 W AT 2020060379W WO 2021077148 A1 WO2021077148 A1 WO 2021077148A1
Authority
WO
WIPO (PCT)
Prior art keywords
reactor
synthesis
section
electrolysis
cathode
Prior art date
Application number
PCT/AT2020/060379
Other languages
German (de)
English (en)
Inventor
David REICHHOLF
Nielsen Anders MOELLER
Richard Schauperl
Jürgen RECHBERGER
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
Priority to DE112020003324.4T priority Critical patent/DE112020003324A5/de
Publication of WO2021077148A1 publication Critical patent/WO2021077148A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/08—Production of synthetic natural gas
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
    • C07C1/0485—Set-up of reactors or accessories; Multi-step processes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
    • C07C1/0495—Non-catalytic processes; Catalytic processes in which there is also another way of activation, e.g. radiation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/20—Processes
    • C25B3/25—Reduction
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
    • C25B9/23—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms comprising ion-exchange membranes in or on which electrode material is embedded
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/70—Assemblies comprising two or more cells
    • C25B9/73—Assemblies comprising two or more cells of the filter-press type
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/38—Applying an electric field or inclusion of electrodes in the apparatus
    • 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
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
    • 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 relates to an SOEC system for performing electrolysis and synthesis.
  • the invention also relates to a method for operating such a SOEC system.
  • So-called power-to-gas systems and power-to-SynFuel systems are known in the prior art.
  • hydrogen can be generated in the course of electrolysis and another fuel such as methane can be generated through a subsequent synthesis.
  • the synthesis gas is generated via electrolysis processes and, in a further process step, a synthesis process with the synthesis gas follows under special thermodynamic conditions. This means that electrolysis and synthesis take place separately from one another in terms of time and / or location. This requires a correspondingly large and complex system structure.
  • Such a system can be found in US 2016/0053388 A1.
  • the object of the present invention is to at least partially take into account the problems described above.
  • a method for operating a SOEC system which comprises a reactor for performing an electrolysis for synthesis gas generation and a synthesis for product gas generation, is provided.
  • the procedure consists of the following steps:
  • both the electrolysis and the synthesis can be carried out at least temporarily simultaneously without significant, negative interactions. That is to say, an electrolysis process and a synthesis process are carried out at the same time, at least temporarily, in one and the same reactor.
  • a separate synthesis reactor downstream of the reactor can be dispensed with, or such a synthesis reactor can be made significantly smaller than previously.
  • a generic high-temperature reactor which is usually designed in the form of a fuel cell stack, is usually operated in temperature ranges of well over 700 ° C. for the electrolysis.
  • the reactor according to the invention is designed in particular as a fuel cell stack or has a fuel cell stack.
  • the at least partial synthesis reaction taking place directly in the reactor results in a reduction in the volume flow and thus the flow velocities in the reactor compared to conventional SOEC systems. This leads to This means that the entire synthesis does not have to take place in any subsequent synthesis reactor and, moreover, the flow rates are lower, which significantly influences the conversion rates in the reactor.
  • Carrying out the electrolysis and the synthesis at the same time also leads to thermal stability of the reactor, since an exothermic synthesis reaction can supply an endothermic electrolysis reaction with heat. That is to say, the electrochemical reactions of the electrolysis according to the invention can be strongly endothermic, as a result of which output flows of the reactor have a lower temperature level than input flows of the reactor. So far, this has posed a major challenge to the design and operation of electrolysis systems. Through exothermic synthesis reactions directly at the reactor, a corresponding heat input takes place, through which the endothermic can be compensated. A thermoneutral operating point of the SOEC system can thus advantageously be shifted to lower partial load points and / or lower current densities. To increase the desired effect, the reactor can be cooled during the electrolysis and the synthesis with cooling fluids which are colder than the operating temperature in the reactor.
  • water vapor and carbon dioxide can be fed into a fuel side of the reactor and air can be fed into an air side of the reactor.
  • the reactor can be designed as a fuel cell.
  • the reactor can be designed as a fuel cell stack with a plurality of fuel cells, the above-described supply of water vapor and carbon dioxide into the fuel side and of air into the air side being carried out in each fuel cell.
  • water vapor and carbon dioxide on the fuel side can now be converted into hydrogen and carbon monoxide as part of the electrolysis, while at least temporarily the hydrogen and carbon monoxide produced are simultaneously converted into methane gas and water vapor as part of the synthesis.
  • a fluid mixture with water vapor, Carbon dioxide, hydrogen, carbon monoxide and methane gas are generated.
  • a fluid mixture with air and pure oxygen can be generated at the respective outlet on the air side.
  • Carrying out the electrolysis can be understood to mean the creation of the necessary prerequisites for carrying out the desired electrolysis.
  • performing the synthesis can be understood to mean the creation of the necessary prerequisites for performing the desired electrolysis.
  • the prerequisites include the provision of the necessary substances and the necessary environmental conditions in and / or on the reactor and / or in the SOEC system.
  • the SOEC system can in particular be designed as a reversibly operable SOFC / SOEC system, that is to say in the form of an SOFC system that can also be operated as an SOEC system.
  • Carrying out the electrolysis and the synthesis simultaneously at least temporarily is to be understood as meaning that, for example, only the electrolysis can initially be carried out and then the synthesis is carried out while the electrolysis continues to be carried out.
  • water, in particular water vapor, and carbon dioxide can first be converted into hydrogen and carbon monoxide, and then in the context of a synthesis, the hydrogen and carbon monoxide produced can be converted back into water and methane, while in the Hydrogen and carbon monoxide continue to be produced as part of electrolysis.
  • the SOEC system can advantageously have a temperature sensor, by means of which the temperature in the reactor can be determined. On the basis of the determined temperature, the desired temperature can be set and / or regulated accordingly by a controller of the SOEC system.
  • the temperature sensor system includes, for example, a temperature measuring unit at a fluid inlet of the reactor, at which the fuel and / or the air is fed into the reactor, and / or a temperature measuring unit at a fluid outlet of the reactor. Setting the operating temperature can be understood to mean controlling and / or regulating the operating temperature to a desired value. That is, within the framework of the procedure in particular, attempts are made to keep the temperature in the reactor in the range between 400 ° C. and 700 ° C. and / or to bring it into this temperature range.
  • Setting the operating temperature in the reactor is understood to mean, in particular, setting the operating temperature within the reactor, so that a temperature value during operation of the SOEC system within the reactor is in a range between 400 ° C. and 700 ° C. Particularly good reaction results have been obtained at an operating temperature in a range between 500 ° C and 600 ° C. In other words, even at a temperature of only 600 ° C, the electrolysis and the synthesis could be carried out simultaneously in the desired manner.
  • the invention relates to a system concept which enables the operation of a SOEC system, in particular in the form of a stationary SOEC system, in an advantageous manner, as that directly on the reactor, in particular in the form of a fuel cell stack, not only the SOEC system electrochemical conversion of the gases to be electrolyzed takes place, but also partially and / or based on the thermodynamic equilibrium up to completeness, the desired catalytic chemical synthesis process is carried out. Since high conversion rates on the fuel cell stack are generally not given in generic SOEC systems due to the usually high temperatures, it is advantageous to implement a combined system in which a partial conversion to synthesis products takes place on the fuel cell stack and thus the heat management is improved. With special process management and system adaptation, it is also possible to operate the SOEC system with the aid of suitable materials and / or catalysts in such a way that they accelerate not only the electrochemical reactions but also the synthesis process.
  • the electrolysis is carried out to generate synthesis gas, the synthesis gas in particular comprising hydrogen and carbon monoxide. That is, the electrolysis is carried out in particular to generate hydrogen and carbon monoxide.
  • a synthesis can be understood to mean an equilibrium reaction.
  • the synthesis in the reactor enables partial pressures of the electrolysis products to be reduced. This has a direct influence on the necessary electrolysis voltage and results in a reduction in the necessary electrolysis power.
  • the product gas can be another fuel gas that is differs from hydrogen.
  • the generation of product gas can therefore be understood to mean the generation of a further fuel gas that differs from hydrogen.
  • the product gas can be understood as the gas mixture which results from the synthesis carried out.
  • an operating pressure in the reactor is set in a range between 1 bar and 5 bar during the electrolysis and the synthesis by means of a pressure setting unit.
  • the procedure according to the invention in particular the temperature range according to the invention, enables an advantageous conversion rate to be achieved even at relatively low pressures.
  • Expensive functional components for high pressures can be dispensed with.
  • the desired reactions can even be carried out at pressures below 3 bar and even at pressures below 2 bar and / or take place simultaneously in the reactor.
  • the synthesis is carried out in the form of methanation to generate methane.
  • Methanation has proven to be a particularly advantageous synthesis reaction in order to achieve the desired synergy effects.
  • the reactor has a cathode section and an anode section, with water vapor and / or carbon dioxide being controlled to the cathode section via a process fluid supply section and at least one control valve during the electrolysis and synthesis carried out at the same time is conducted and / or cathode exhaust gas is returned from the cathode section via a recirculation section and through a recirculation control valve in a controlled manner back into the cathode section.
  • the total gas mixture at the process fluid feed section of the fuel cell stack can be influenced by a higher or lower recirculation rate and more or less feed stream in the form of water vapor and / or carbon dioxide. By setting this ratio, it can be influenced whether more or fewer synthesis reactions take place in the reactor. After all, this allows for easy and the conversion rates on and / or in the fuel cell stack can be set in a targeted manner in a reliable manner.
  • the reactor can preferably have a cathode section and an anode section, a flow rate of the cathode fluid required for electrolysis and synthesis through the cathode section being set to a predefined value by a flow rate setting unit during the electrolysis and synthesis carried out at the same time becomes.
  • the conversion rates in the reactor can be significantly influenced by different flow rates, and the lower the flow rates and / or flow rates, the smaller the reactor can be built.
  • a SOEC system with a reactor for simultaneously carrying out an electrolysis for the generation of synthesis gas and a synthesis for the generation of product gas within the reactor.
  • the SOEC system also has a temperature setting unit for setting an operating temperature in the reactor for carrying out the electrolysis and the synthesis in a range between 400 ° C. and 700 ° C. at the same time. That is to say, the temperature setting unit is configured to set an operating temperature in the reactor to a value between 400 ° C. and 700 ° C.
  • a SOEC system according to the invention thus has the same advantages as have been described in detail with reference to the method according to the invention.
  • the electrolysis and the synthesis can take place at least temporarily simultaneously on the same reactive surface within the reactor, in particular in the form of a fuel cell stack with planar fuel cells.
  • a pressure setting unit is configured for setting an operating pressure in the reactor during the electrolysis and the synthesis in a range between 1 bar and 5 bar.
  • the reactor is configured to carry out the synthesis in the form of methanation to generate methane.
  • the reactor can advantageously have a cathode section and an anode section, the cathode section having a cathode catalyst for the catalytic conversion of only a predefined part of the synthesis gas.
  • synthesis gas such as hydrogen and / or carbon monoxide produced on the fuel cell stack can be converted catalytically on, for example, a nickel surface of the reactor in the context of a Sabatier reaction as close as possible to chemical equilibrium.
  • the chemical equilibrium prevents all of the synthesis gas from being converted into methane gas, for example.
  • the reactor has a cathode section and an anode section and the SOEC system also has a process fluid feed section for the controlled supply of water vapor and / or carbon dioxide to the cathode section and a recirculation section for the controlled return of cathode exhaust gas having the cathode section back into the cathode section.
  • a SOEC system according to the invention can have a flow rate setting unit for setting a flow rate of the cathode fluid required for electrolysis and synthesis through the cathode section.
  • the reactor can preferably have a fluid inlet area and a fluid outlet area, wherein a first temperature sensor for determining an inlet temperature is arranged at the fluid inlet area and a second temperature sensor for determining an outlet temperature at the fluid outlet area is arranged at the fluid outlet area, and wherein the temperature setting unit is configured for setting the operating temperature in the reactor for the simultaneous implementation of the electrolysis and the synthesis on the basis of the ascertained inlet temperature and / or on the basis of the ascertained outlet temperature.
  • FIG. 1 shows an illustration for explaining a method according to an embodiment of the present invention
  • FIG. 2 is a block diagram for describing a SOEC system according to an embodiment of the present invention.
  • FIG. 1 shows a simplified illustration to explain a method for operating a SOEC system 10 shown in FIG. 2, which has a reactor 11 in the form of a medium-temperature fuel cell stack for performing an electrolysis for synthesis gas generation and a synthesis for product gas generation and a temperature setting unit 14 for setting an operating temperature in the reactor 11 comprises.
  • the operating temperature is maintained in a range between 500 ° C and 600 ° C during electrolysis and synthesis. In this temperature range, an electrolysis for the generation of synthesis gas and a synthesis for the generation of product gas can be carried out simultaneously in the reactor 11.
  • the reactor 11 shown in FIG. 1 has a cathode section 12 and an anode section 13.
  • the cathode section 12 has a cathode inlet 33 and a cathode outlet 34.
  • the anode section 13 has an anode input 35 and an anode output 36.
  • the cathode section 12 can be understood as the fuel side of the reactor 11.
  • the anode section 13 can be understood as the air side of the reactor 11.
  • the illustrated reactor has an electrolyte membrane 25 which is sandwiched between the cathode section 12 and the anode section 13.
  • the cathode section 12 has a cathode busbar 26 and a cathode catalyst 27.
  • the anode section 13 has an anode catalyst 28 and an anode busbar 29.
  • the cathode catalytic converter 27 is configured for the catalytic conversion of only a predefined part of the synthesis gas.
  • the cathode section 12 more precisely, a fluid conduction section which adjoins the cathode catalytic converter 27, is introduced Fuel mixture, which has water vapor and carbon dioxide, initiated. At the same time, air is introduced into the anode section 13, more precisely into a fluid conducting section which adjoins the anode catalytic converter 28.
  • synthesis gas which comprises hydrogen and carbon monoxide, is initially produced from the fuel mixture as part of the electrolysis. Since this reaction takes place endothermically, the temperature in the reactor 11 drops slightly as a result. The synthesis gas and unconverted water vapor and unconverted carbon dioxide are then located in the cathode section 12.
  • the synthesis gas can now be converted into methane gas and water vapor as part of a synthesis, more precisely as part of methanation. Since this reaction takes place endothermically, the temperature in reactor 11 rises again slightly. There are now water vapor, carbon dioxide, hydrogen, carbon monoxide and methane gas in the cathode section 12. Water vapor and carbon dioxide can continue to react to form hydrogen and carbon monoxide. Likewise, hydrogen and carbon monoxide can continue to react simultaneously to form methane gas and water vapor. A fluid mixture which comprises water vapor, carbon dioxide, hydrogen, carbon monoxide and methane gas then flows out of the cathode section 12 of the reactor 11. A fluid mixture comprising air and pure oxygen flows out of the anode section 13. The operating pressure in the reactor 11 during the electrolysis and the synthesis is set and / or maintained at a value, as far as possible, only slightly above ambient pressure by a pressure setting unit 15 shown in FIG. 2.
  • the SOEC system 10 has the temperature setting unit 14 for setting the operating temperature in the reactor 11 and the pressure setting unit 15 for setting the operating pressure in the reactor 11 on.
  • the reactor 11 is configured to carry out the synthesis in the form of methanation to generate methane and has correspondingly coated electrodes.
  • the temperature setting unit 14 and the pressure setting unit 15 are configured according to FIG. 1 as part of a controller 17 which is configured to set the SOEC operation.
  • the controller 17 further has a flow rate setting unit 16 for setting a flow rate of the cathode fluid required for electrolysis and synthesis through the cathode section 12.
  • the reactor 11 has a fluid inlet area 21 and a fluid outlet area 22, a first temperature sensor 23 for determining an inlet temperature at the cathode inlet 33 being arranged at the fluid inlet area 21, more precisely at a cathode inlet 33, and a first temperature sensor 23 at the fluid outlet area 22, more precisely at the cathode outlet 34 second temperature sensor 24 for determining an outlet temperature is arranged on fluid outlet region 22.
  • the temperature setting unit 14 is configured to set the operating temperature in the reactor 11 for the simultaneous implementation of the electrolysis and the synthesis on the basis of the ascertained inlet temperature and on the basis of the ascertained outlet temperature.
  • the temperature sensors 23, 24 can also be arranged at a fluid inlet and / or a fluid outlet of the reactor 11.
  • the SOEC system 10 furthermore has a process fluid supply section 31 for the controlled supply of water vapor and carbon dioxide to the cathode section 12.
  • the process fluid supply section 31 has a water vapor line 37 and a water vapor control valve 18 for the controlled supply of water vapor to the cathode section 12.
  • the process fluid supply section 31 has a carbon dioxide line 38 and a carbon dioxide control valve 19 for the controlled supply of carbon dioxide to the cathode section 12.
  • a recirculation section 32 is also designed with a recirculation control valve 20 for the controlled return of cathode exhaust gas from the cathode section 12 back into the cathode section 12.
  • cathode exhaust gas from the cathode section 12 can be conducted back into the cathode section 12 in a controlled manner during the electrolysis and synthesis which are carried out simultaneously.
  • a heat exchanger 39 is designed to heat the water vapor line 37 and thus the water vapor in the water vapor line 37 by means of cathode exhaust gas that is not returned to the cathode section 12.
  • Flierzu stands Heat exchanger 39 with the steam line 37 in a heat-transferring connection.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • General Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)

Abstract

La présente invention concerne un procédé de fonctionnement d'un système SOEC (10) qui comprend un réacteur (11) destiné à réaliser une électrolyse pour générer du gaz de synthèse et une synthèse pour générer un gaz produit, ledit procédé comprenant les étapes consistant : à régler, au moyen d'une unité de réglage de température (14), une température de fonctionnement dans le réacteur (11) pour effectuer l'électrolyse et la synthèse dans une plage de 400 °C à 700 °C, à effectuer l'électrolyse pour générer le gaz de synthèse dans le réacteur (11), et à effectuer simultanément, au moins de façon temporaire, la synthèse pour générer du gaz produit dans le réacteur (11). L'invention concerne également un système SOEC (10) permettant la mise en œuvre d'un procédé selon l'invention.
PCT/AT2020/060379 2019-10-24 2020-10-23 Système soec et procédé de fonctionnement d'un système soec WO2021077148A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
DE112020003324.4T DE112020003324A5 (de) 2019-10-24 2020-10-23 SOEC-System und Verfahren zum Betreiben eines SOEC-Systems

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ATA50919/2019 2019-10-24
ATA50919/2019A AT523122B1 (de) 2019-10-24 2019-10-24 SOEC-System und Verfahren zum Betreiben eines SOEC-Systems

Publications (1)

Publication Number Publication Date
WO2021077148A1 true WO2021077148A1 (fr) 2021-04-29

Family

ID=73198057

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/AT2020/060379 WO2021077148A1 (fr) 2019-10-24 2020-10-23 Système soec et procédé de fonctionnement d'un système soec

Country Status (3)

Country Link
AT (1) AT523122B1 (fr)
DE (1) DE112020003324A5 (fr)
WO (1) WO2021077148A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP7216866B1 (ja) 2021-11-15 2023-02-01 日本碍子株式会社 電解セル、及びセルスタック装置
CN118223074A (zh) * 2024-05-24 2024-06-21 山东国创燃料电池技术创新中心有限公司 一种电解水制氢系统的电解槽温度控制方法和装置

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3852180A (en) * 1972-02-04 1974-12-03 Skf Ind Trading & Dev Apparatus for co{11 {11 conversion to methane
US20120003552A1 (en) * 2010-06-08 2012-01-05 Barnett Scott A Method for improving the efficiency and durability of electrical energy storage using solid oxide electrolysis cell
US20120282534A1 (en) * 2011-03-28 2012-11-08 Braun Robert J High efficiency, reversible flow battery system for energy storage
JP2013119556A (ja) * 2011-12-06 2013-06-17 Mitsubishi Heavy Ind Ltd 燃料製造方法及び燃料製造装置
US20160053388A1 (en) 2013-04-08 2016-02-25 Commissariat A L'energie Atomique Et Aux Energies Alternatives Methods for producing combustible gas from the electrolysis of water (hte) or co-electrolysis with h2o/co2 in the same chamber, and associated catalytic reactor and system

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3075832A1 (fr) * 2017-12-22 2019-06-28 Commissariat A L'energie Atomique Et Aux Energies Alternatives Procede de fonctionnement en mode de demarrage ou en mode stand-by d'une unite power-to-gas comportant une pluralite de reacteurs d'electrolyse (soec) ou co-electrolyse a haute temperature

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3852180A (en) * 1972-02-04 1974-12-03 Skf Ind Trading & Dev Apparatus for co{11 {11 conversion to methane
US20120003552A1 (en) * 2010-06-08 2012-01-05 Barnett Scott A Method for improving the efficiency and durability of electrical energy storage using solid oxide electrolysis cell
US20120282534A1 (en) * 2011-03-28 2012-11-08 Braun Robert J High efficiency, reversible flow battery system for energy storage
JP2013119556A (ja) * 2011-12-06 2013-06-17 Mitsubishi Heavy Ind Ltd 燃料製造方法及び燃料製造装置
US20160053388A1 (en) 2013-04-08 2016-02-25 Commissariat A L'energie Atomique Et Aux Energies Alternatives Methods for producing combustible gas from the electrolysis of water (hte) or co-electrolysis with h2o/co2 in the same chamber, and associated catalytic reactor and system

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
JOHN B. HANSEN ET AL: "Production of Sustainable Fuels by Means of Solid Oxide Electrolysis", ECS TRANSACTIONS, vol. 35, no. 1, 1 January 2011 (2011-01-01), pages 2941 - 2948, XP055067864, ISSN: 1938-5862, DOI: 10.1149/1.3570293 *

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP7216866B1 (ja) 2021-11-15 2023-02-01 日本碍子株式会社 電解セル、及びセルスタック装置
JP2023073222A (ja) * 2021-11-15 2023-05-25 日本碍子株式会社 電解セル、及びセルスタック装置
CN118223074A (zh) * 2024-05-24 2024-06-21 山东国创燃料电池技术创新中心有限公司 一种电解水制氢系统的电解槽温度控制方法和装置

Also Published As

Publication number Publication date
DE112020003324A5 (de) 2022-04-07
AT523122B1 (de) 2021-08-15
AT523122A1 (de) 2021-05-15

Similar Documents

Publication Publication Date Title
EP0787679B1 (fr) Procédé et dispositif pour la récupération d'un gaz riche en hydrogène et pauvre en monoxyde de carbone
WO2015185039A1 (fr) Procédé d'électrolyse et système d'électrolyse à fluides de balayage remis en circulation
EP2153485B1 (fr) Système de pile à combustible fonctionnant avec du gaz liquide
EP2906666B1 (fr) Procédé et système pour produire substitute du gaz naturel contenant methane
WO2021077148A1 (fr) Système soec et procédé de fonctionnement d'un système soec
EP1571123A1 (fr) Réformeur et procédé pour transformer un combustible et un oxidant en réformat
WO2021214214A1 (fr) Procédé de fonctionnement de système de piles à oxyde solide
DE10393133T5 (de) Brennstoffsteuerung für Brennstoffaufbereitungsdampferzeugung in Niedertemperatur-Brennstoffzellen-Stromerzeugungsanlage
EP2200114B1 (fr) Système de cellules de combustible de réformateur
DE102020208604B4 (de) Energiewandlungssystem
WO2022268391A1 (fr) Procédé de fonctionnement d'une installation d'électrolyse et installation d'électrolyse
DE10143656B4 (de) Verfahren zur Erzeugung von Energie in einem Brennstoffzellen-Gesamtsystem mit Crackreaktor und Brennstoffzelle sowie Vorrichtung zur Durchführung des Verfahrens
EP3556460A1 (fr) Réacteur de mise en uvre de réactions à équilibre réduit
DE102020208605B4 (de) Energiewandlungssystem
DE19958404C2 (de) Vorrichtung zur selektiven katalytischen Oxidation von Kohlenmonoxid
WO2016041654A1 (fr) Dispositif de piles à combustible comprenant un dispositif de traitement de gaz anodique amélioré
WO2021089183A1 (fr) Procédé et installation de production de monoéthylène glycol
DE102020109016B4 (de) Verfahren und Vorrichtung zur Synthese von Ammoniak
DE10136769A1 (de) Reformereinheit zur Erzeugung eines Reformats
BE1029714B1 (de) Ammoniaksynthese mit CO2-neutralem Wasserstoff
EP3883671B1 (fr) Procédé de changement du mode de fonctionnement d'une installation d'électrolyse ainsi qu'installation d'électrolyse
WO2023025759A1 (fr) Synthèse d'ammoniac avec de l'hydrogène neutre de co2
DE102021003912A1 (de) Elektro-Katalytische Reduktion von ungesättigten Sauerstoffhaltigen organischen Verbindungen in einer Rührzelle mit Wasserstoffelektrolyse
EP4283017A1 (fr) Procédé et installation destinés à la mise en uvre d'un procédé de conversion de matière a l'aide d'une cellule à haute température
DE102021209338A1 (de) Ammoniaksynthese mit CO2-neutralem Wasserstoff

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 20803737

Country of ref document: EP

Kind code of ref document: A1

REG Reference to national code

Ref country code: DE

Ref legal event code: R225

Ref document number: 112020003324

Country of ref document: DE

122 Ep: pct application non-entry in european phase

Ref document number: 20803737

Country of ref document: EP

Kind code of ref document: A1