EP4578053A2 - Support d'écran cathodique pour pile à combustible à carbonate fondu - Google Patents

Support d'écran cathodique pour pile à combustible à carbonate fondu

Info

Publication number
EP4578053A2
EP4578053A2 EP23776136.6A EP23776136A EP4578053A2 EP 4578053 A2 EP4578053 A2 EP 4578053A2 EP 23776136 A EP23776136 A EP 23776136A EP 4578053 A2 EP4578053 A2 EP 4578053A2
Authority
EP
European Patent Office
Prior art keywords
cathode
fuel cell
anode
current collector
mesh layer
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
EP23776136.6A
Other languages
German (de)
English (en)
Inventor
Abdelkader Hilmi
Chao-Yi Yuh
Timothy C. GEARY
Aaron SATTLER
William C. Horn
William A. Lamberti
Gabor Kiss
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.)
ExxonMobil Technology and Engineering Co
Original Assignee
ExxonMobil Technology and Engineering Co
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
Priority claimed from US18/229,805 external-priority patent/US20240072287A1/en
Application filed by ExxonMobil Technology and Engineering Co filed Critical ExxonMobil Technology and Engineering Co
Publication of EP4578053A2 publication Critical patent/EP4578053A2/fr
Pending legal-status Critical Current

Links

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
    • H01M8/14—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
    • 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
    • H01M8/02—Details
    • H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
    • H01M8/023—Porous and characterised by the material
    • H01M8/0232—Metals or alloys
    • 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
    • H01M8/02—Details
    • H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
    • H01M8/023—Porous and characterised by the material
    • H01M8/0241—Composites
    • H01M8/0245—Composites in the form of layered or coated products
    • 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
    • H01M8/02—Details
    • H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
    • H01M8/0247—Collectors; Separators, e.g. bipolar separators; Interconnectors characterised by the form
    • 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
    • H01M2008/147—Fuel cells with molten 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

  • Cathode screen supports for improving the interface between the cathode and the cathode current collector in a molten carbonate fuel cell are provided, along with methods of operating such a fuel cell.
  • Molten carbonate fuel cells utilize hydrogen and/or other fuels to generate electricity.
  • the hydrogen may be provided by reforming methane or other reformable fuels in a steam reformer, such as steam reformer located upstream of the fuel cell or integrated within the fuel cell.
  • Fuel can also be reformed in the anode cell in a molten carbonate fuel cell, which can be operated to create conditions that are suitable for reforming fuels in the anode.
  • Still another option can be to perform some reforming both externally and internally to the fuel cell. Reformable fuels can encompass hydrocarbonaceous materials that can be reacted with steam and/or oxygen at elevated temperature and/or pressure to produce a gaseous product that comprises hydrogen.
  • the basic structure of a molten carbonate fuel cell includes a cathode, an anode, and a matrix between the cathode and anode that includes one or more molten carbonate salts that serve as the electrolyte.
  • the molten carbonate salts partially diffuse into the pores of the cathode. This diffusion of the molten carbonate salts into the pores of the cathode provides an interface region where CO? can be converted into CO3 2 for transport across the electrolyte to the anode.
  • volume adjacent to the anode and cathode are typically included in the fuel cell. This allows an anode gas flow and a cathode gas flow to be delivered to the anode and cathode, respectively.
  • a cathode current collector structure can be used.
  • An anode collector can be used to similarly provide the volume for the anode gas flow.
  • U.S. Patents 6,492,045 and 8,802,332 describe examples of current collectors for molten carbonate fuel cells. The current collectors correspond to corrugated structures.
  • U.S. Patent Application Publication 2020/0176783 describes cathode current collector structures that provide increased open area for a cathode surface adjacent to the cathode current collector. A mesh layer with a large open area that does not provide structural support was also described.
  • a molten carbonate fuel cell includes an anode.
  • the fuel cell further includes a first separator plate.
  • the fuel cell further includes an anode collector in contact with the anode and the first separator plate to define an anode gas collection zone between the anode and the first separator plate.
  • the fuel cell further includes a cathode having a cathode surface.
  • the fuel cell further includes a second separator plate.
  • the fuel cell further includes a cathode current collector in contact with the second separator plate and adjacent to the cathode surface to define a cathode gas collection zone between the cathode and the second separator plate.
  • the cell further includes a structural mesh layer disposed between the cathode surface and the cathode current collector, the structural mesh layer comprising 50 openings / cm 2 or more and having a mesh contact area of 55% to 75%.
  • the fuel cell includes an electrolyte matrix comprising an electrolyte between the anode and the cathode.
  • the contact area of the cathode current collector can he less than 55%.
  • FIG. 2 shows an example of a molten carbonate fuel cell.
  • FIG. 3 shows an example of a cathode current collector structure.
  • FIG. 4 shows an example of a repeating pattern unit that can be used to represent the cathode current collector structure shown in FIG. 3.
  • FIG. 5 shows another example of the repeating pattern unit of FIG. 4.
  • FIG. 6 shows a flow pattern example for a molten carbonate fuel cell with an anode flow direction that is aligned roughly perpendicular to a cathode flow direction.
  • FIG. 10 shows ohmic resistance versus CO2 utilization for fuel cells including various types of mesh layers disposed between the cathode current collector and the cathode surface.
  • FIG. 11 shows operating voltage versus CO2 utilization for fuel cells including various types of mesh layers disposed between the cathode current collector and the cathode surface.
  • FIG. 12 shows ohmic resistance versus CO2 utilization for fuel cells including various types of mesh layers disposed between the cathode current collector and the cathode surface.
  • FIG. 13 shows operating voltage versus CO2 utilization for fuel cells including various types of mesh layers disposed between the cathode current collector and the cathode surface.
  • FIG. 14 shows CO2 capture selectivity for fuel cells operated at various CO2 utilization levels.
  • molten carbonate fuel cell structures include a structural mesh support layer at the interface between the surface of the cathode and the cathode current collector.
  • the structural mesh layer can have a contact area of 55% to 75%, which corresponds to a mesh open area of 25% to 45%.
  • the structural mesh layer can reduce or minimize ohmic resistance at the interface between the cathode and the cathode current collector while also maintaining favorable open area for transport of CO2 from the cathode gas stream to the electrolyte.
  • Molten carbonate fuel cells provide an unusual and advantageous opportunity for performing carbon capture from power generation and industrial flue gases: Because CO2 is used to form the carbonate ions for transport of electrical charge from the cathode to the anode, molten carbonate fuel cells can provide capture and transport of CO2 from lower concentration cathode gas streams to higher concentration anode gas streams while also generating electrical power. Carbon capture processes utilizing molten carbonate fuel cells thus can be net energy exporters as opposed to the conventional carbon capture processes relying on CO2 absorption or adsorption that require energy import.
  • CO2 removed from the cathode stream of molten carbonate fuel cells can be recovered from the CCh-enriched anode effluent for carbon capture or utilization.
  • CO2 depletion may also reduce the life of the fuel cell.
  • a structural mesh layer with a mesh open area that is lower than the open area of the cathode surface (as defined by the cathode current collector), can improve cell operation by reducing or minimizing loss of cell voltage over time.
  • a structural mesh layer with a contact area of 55% to 75% i.e., a mesh open area of 25% to 45%
  • Such a structural mesh layer with a mesh open area of 25% to 45% can also have a high density of openings per unit area.
  • the mesh contact area is higher than the contact area of the cathode current collector, it is believed that the large number of openings per unit area allows the benefits of increased gas transfer from the cathode current collector volume to the cathode to be maintained.
  • the mesh can also provide sufficient structural stability to improve performance of the fuel cell.
  • the presence of the structural mesh layer allows the contact force of the cathode current collector to be distributed over a larger area while keeping a small size for the features that are in contact the cathode surface. This is beneficial in relation to the goal enhancing CO2 transport from the cathode gas chamber into the cathode pores where the electrochemical process takes place.
  • the small features of the structural mesh layer allow for a large amount of contact area while reducing or minimizing the average diffusion path required for gas to travel around the contact features and reach the cathode surface.
  • the larger contact area of the structural mesh layer distributes the weight of the cathode current collector over a larger percentage of the cathode surface.
  • the numerous small contact features of the structural mesh layer create contacts/support while keeping the mean diffusion path under the cathode current collector - cathode surface contacts short, a feature that reduces transport resistance.
  • the structural mesh layer can have one or more (such as up to all) of the following features.
  • the structural mesh layer can have a mesh contact area of 55% to 75%, or 55% to 70%, which corresponds to mesh open area of 25% to 45%, or 30% to 45%.
  • the structural mesh layer can have a cell density or opening density of 50 openings I cm 2 or more, or 75 openings / cm 2 or more, or 100 openings / cm 2 or more, or 125 openings I cm 2 or more, such as up to 1000 openings / cm 2 or possibly still higher.
  • the structural mesh layer can have a thickness or height of at least 0.25 mm, or at least 0.30 mm, such as up to 0.80 mm or possibly still more.
  • the contact area is defined based on interaction of a structural mesh layer I cathode current collector with an idealized flat or level surface, the contact area is a property of the structural mesh layer I cathode current collector, and is well-defined even if the structural mesh layer or cathode current collector is not actually in contact with a level surface.
  • the contact area can be referred to as a mesh contact area.
  • the contact area can be referred to as a cathode current collector contact area.
  • Mesh Open Area or Cathode Collector Open Area This value is the complement of the contact area. When the contact area for a structure is expressed as a percentage, the open area can be calculated as 100% - ⁇ contact area>. Alternatively, if it easier to characterize the areas of a level surface that would not be in contact with a structural mesh layer or a cathode current collector, the open area could be determined first, and then the contact area could be calculated based on 100% - ⁇ open area>.
  • the contact area of a cathode surface corresponds to the remaining portion of the cathode surface that does not correspond to open area of the cathode surface.
  • open area of a cathode surface is defined independently of the presence or absence of a structural mesh layer.
  • the presence of a structural mesh layer does not alter the calculated value for open area of a cathode surface.
  • the mesh open area of the structural mesh layer can be less than the open area of the cathode surface, as defined by the cathode current collector.
  • Average cathode gas lateral diffusion length is defined as the average lateral distance from an open area location on a cathode surface to each point on the cathode surface.
  • the lateral diffusion length for any point corresponding to an open area location is defined as zero.
  • the average cathode gas lateral diffusion length can also be calculated for cathode surfaces having a repeating pattern, such as the repeating pattern shown in FIG. 4.
  • the same normalized distances shown FIG. 4 can be used, with the end result being multiplied by an appropriate scaling factor to represent a given configuration.
  • an upper limit for the average distance can be determined based on the maximum distance, or the distance from the open area to the top comer of the square. Half of that maximum distance is roughly 0.7, which provides a bounding upper limit for the average distances within corner areas 692, 694, 696, and 696.
  • the above average distances can then be used to determine the average cathode gas lateral diffusion length by multiplying the average distances by the percentage of the total area corresponding to each distance.
  • Areas 672, 674, 682, and 684 correspond to 32% of the total area of the repeat pattern unit shown in FIG. 5.
  • the corner areas correspond to 4% of the total area.
  • the remaining 64% of the area corresponds to the open central area 510, which by definition has a distance of zero.
  • the 0.188 value can then be multiplied by a scaling factor that is representative of a real system.
  • a scaling factor of 0.635 m can be used. Multiplying 0.188 by a scaling factor of 0.635 mm results in an average cathode gas lateral diffusion length of 0.12 mm. It is noted that based on the assumptions used when calculating the average distance values for comer areas 692, 694, 696, and 698, the value of 0.12 mm represents an upper bound for the actual average cathode gas lateral diffusion length.
  • Average contact area diffusion length is defined as the average lateral distance from a contact area location on a cathode surface to each point on the cathode surface. For the purposes of this definition, the contact area diffusion length for any point corresponding to a contact area location is defined as zero. An example of this calculation will be further illustrated below.
  • the anodes in a fuel cell array do not have to be connected in the same way as the cathodes in the array.
  • the input to the first anode stage of a fuel cell array may be referred to as the anode input for the array, and the input to the first cathode stage of the fuel cell array may be referred to as the cathode input to the array.
  • the output from the final anode/cathode stage may be referred to as the anode/cathode output from the array.
  • These individual fuel cell elements can typically have similar voltages (as the reactant and product concentrations are similar), and the total power output can result from the summation of all of the electrical currents in all of the cell elements, when the elements are electrically connected in series.
  • Stacks can also be arranged in a series arrangement to produce high voltages. A parallel arrangement can boost the current. If a sufficiently large volume fuel cell stack is available to process a given exhaust flow, the systems and methods described herein can be used with a single molten carbonate fuel cell stack. In other aspects of the invention, a plurality of fuel cell stacks may be desirable or needed for a variety of reasons.
  • fuel cell should be understood to also refer to and/or is defined as including a reference to a fuel cell stack composed of set of one or more individual fuel cell elements for which there is a single input and output, as that is the manner in which fuel cells are typically employed in practice.
  • fuel cells plural
  • fuel cells should be understood to also refer to and/or is defined as including a plurality of separate fuel cell stacks.
  • all references within this document, unless specifically noted, can refer interchangeably to the operation of a fuel cell stack as a “fuel cell”.
  • the volume of exhaust generated by a commercial scale combustion generator may be too large for processing by a fuel cell (i.e., a single stack) of conventional size.
  • a fuel cell i.e., a single stack
  • a plurality of fuel cells i.e., two or more separate fuel cells or fuel cell stacks
  • each fuel cell can process (roughly) an equal portion of the combustion exhaust.
  • each fuel cell can typically be operated in a generally similar manner, given its (roughly) equal portion of the combustion exhaust.
  • a cathode current collector structure such as the structure 110 shown in FIG. 1 would be oriented so that the plate-like surface is in contact with the cathode surface.
  • a cathode current collector (such as the structure shown in FIG. 1) can be oriented so that the bottom edges 122 of the loop structures 120 are in contact with the cathode surface, while the plate-like surface is in contact with the separator plate.
  • Still other potential sources for an anode input can additionally or alternately include streams with increased water content.
  • an ethanol output stream from an ethanol plant (or another type of fermentation process) can include a substantial portion of H2O prior to final distillation.
  • H2O can typically cause only minimal impact on the operation of a fuel cell.
  • a fermentation mixture of alcohol (or other fermentation product) and water can be used as at least a portion of an anode input stream.
  • the CCh-containing stream from a fuel cell can correspond to a cathode output stream from a different fuel cell, an anode output stream from a different fuel cell, a recycle stream from the cathode output to the cathode input of a fuel cell, and/or a recycle stream from an anode output to a cathode input of a fuel cell.
  • an MCFC operated in standalone mode under conventional conditions can generate a cathode exhaust with a CO2 concentration of at least about 5 vol%.
  • Such a CCh-containing cathode exhaust could be used as a cathode input for an MCFC operated according to an aspect of the invention.
  • a cathode input stream can also be composed of inert/non- reactive species such as N2, H2O, and other typical oxidant (air) components.
  • inert/non- reactive species such as N2, H2O, and other typical oxidant (air) components.
  • the exhaust gas can include typical components of air such as N2, H2O, and other compounds in minor amounts that are present in air.
  • additional species present after combustion based on the fuel source may include one or more of H2O, oxides of nitrogen (NOx) and/or sulfur (SOx), and other compounds either present in the fuel and/or that are partial or complete combustion products of compounds present in the fuel, such as CO.
  • These species may be present in amounts that do not poison the cathode catalyst surfaces though they may reduce the overall cathode activity. Such reductions in performance may be acceptable, or species that interact with the cathode catalyst may be reduced to acceptable levels by known pollutant removal technologies.
  • the amount of O2 present in a cathode input stream can advantageously be sufficient to provide the oxygen needed for the cathode reaction in the fuel cell.
  • the volume percentage of O2 can advantageously be at least 0.5 times the amount of CO2 in the exhaust.
  • additional air can be added to the cathode input to provide sufficient oxidant for the cathode reaction.
  • the amount of N2 in the cathode exhaust can be at least about 78 vol%, e.g., at least about 88 vol%, and/or about 95 vol% or less.
  • the cathode input stream can additionally or alternately contain compounds that are generally viewed as contaminants, such as H2S or NH3. In other aspects, the cathode input stream can be cleaned to reduce or minimize the content of such contaminants.
  • a suitable temperature for operation of an MCFC can be between about 450°C and about 750°C, such as at least about 500°C, e.g., with an inlet temperature of about 550°C and an outlet temperature of about 625 °C.
  • heat Prior to entering the cathode, heat can be added to or removed from the cathode input stream, if desired, e.g., to provide heat for other processes, such as reforming the fuel input for the anode.
  • the source for the cathode input stream is a combustion exhaust stream
  • the combustion exhaust stream may have a temperature greater than a desired temperature for the cathode inlet.
  • heat can be removed from the combustion exhaust prior to use as the cathode input stream.
  • the combustion exhaust could he at very low temperature, for example after a wet gas scrubber on a coal-fired boiler, in which case the combustion exhaust can be below about 100°C.
  • the combustion exhaust could be from the exhaust of a gas turbine operated in combined cycle mode, in which the gas can be cooled by raising steam to run a steam turbine for additional power generation. In this case, the gas can be below about 50°C.
  • Heat can be added to a combustion exhaust that is cooler than desired.
  • a series of lab scale individual fuel cells were tested that included various types of configurations at the interface between the cathode surface and the cathode current collector.
  • the lab scale fuel cells each had a 250 cm 2 of active surface area.
  • the cathode current collector in the fuel cells had a structure corresponding to a contact area of 10% / an open area at the cathode surface of 90%.
  • Some fuel cells did not have a mesh layer between the cathode current collector and the cathode surface.
  • Other fuel cells had a structural mesh layer with varying densities of openings in the mesh and that provided varying amounts of mesh open area.
  • the fuel cells were operated at various conditions that ranged from 4.0 vol% to 10 vol% CO2 in the cathode inlet gas; a current density of 140 mA/cm 2 to 180 mA/cm 2 ; and a CO2 utilization between 65% and 98%.
  • FIG. 7 shows the ohmic resistance for the cells over an extended run length. Each line in FIG. 7 corresponds to data from operation of a single fuel cell.
  • the cells without a mesh layer initially had an ohmic resistance that was similar to the ohmic resistance for the cells that included a mesh layer.
  • the ohmic resistance quickly increased with time during operation of the fuel cells that did not have a mesh layer.
  • the cells that included the structural mesh layer unexpectedly maintained the substantially the same ohmic resistance value over the full course of the runs.
  • FIG. 8 and FIG. 9 illustrate the impact of the increased ohmic resistance on fuel cell performance.
  • FIG. 9 corresponds to the same type of plot as FIG. 7, but for fuel cells operated at roughly 70% CO2 utilization.
  • line 890 For clarity only one fuel cell without a mesh layer is shown (line 890), along with only two of fuel cells including the mesh layer are shown (lines 810 and 820).
  • FIG. 8 shows how the changes in ohmic resistance modify the operating voltage of the fuel cell.
  • the increasing ohmic resistance over time for the fuel cell without a mesh screen results in a substantial drop in operating voltage.
  • the fuel cells including the mesh layer unexpectedly maintained substantially the same operating voltage over time at the selected operating conditions.
  • FIGS. 7, 8, and 9 compare operation of fuel cells without a mesh versus fuel cells that include a structural mesh layer having a high density of openings and a low mesh open area. Additional test runs were performed to determine the types of mesh layers that can provide the benefits shown in FIGS. 7, 8, and 9. The additional test runs were performed at two different types of operating conditions. For both types of operating conditions, the CO2 utilization was varied in different runs to determine how operating voltage and ohmic resistance changed as the CO2 utilization changed.
  • error bars are also provided for line 1090, the cell without a mesh layer, to demonstrate that the differences in ohmic resistance shown in FIG. 10 for Mesh 1 and Mesh 2 are not merely due to expected levels of variance in fuel cell behavior.
  • the cell including comparative Mesh 3 (line 1030) had an ohmic resistance comparable to the ohmic resistance for the cell including no mesh layer (line 1090). It is noted that comparative Mesh 3 had a relatively high density of openings. However, the mesh open area for comparative Mesh 3 was too high.
  • Embodiment 1 A molten carbonate fuel cell, comprising: an anode; a first separator plate; an anode collector in contact with the anode and the first separator plate to define an anode gas collection zone between the anode and the first separator plate; a cathode having a cathode surface; a second separator plate; a cathode current collector in contact with the second separator plate and adjacent to the cathode surface to define a cathode gas collection zone between the cathode and the second separator plate, the cathode current collector having a contact area of less than 55%; a structural mesh layer disposed between the cathode surface and the cathode current collector, the structural mesh layer comprising 50 openings / cm 2 or more and having a mesh contact area of 55% to 75%; and an electrolyte matrix comprising an electrolyte between the anode and the cathode.
  • Embodiment 2 The molten carbonate fuel cell of Embodiment 1, wherein the structural mesh layer comprises 75 openings / cm 2 or more.
  • Embodiment 3 The molten carbonate fuel cell of any of the above embodiments, wherein the structural mesh layer comprises 125 openings / cm 2 or more.
  • Embodiment 4 The molten carbonate fuel cell of any of the above embodiments, wherein the contact area of the cathode current collector is 50% or more.
  • Embodiment 6 The molten carbonate fuel cell of any of the above embodiments, wherein an average contact area diffusion length is 1.0 mm or less, or wherein the average cathode gas lateral diffusion length is 0.35 mm or less, or a combination thereof.
  • Embodiment 7 The molten carbonate fuel cell of any of the above embodiments, wherein the structural mesh layer comprises a thickness of 0.25 mm to 0.80 mm.
  • Embodiment 8 The molten carbonate fuel cell of any of the above embodiments, wherein the structural mesh layer is composed of stainless steel.
  • Embodiment 9 A method for producing electricity in a molten carbonate fuel cell according to any of Embodiments 1 - 8, comprising: introducing an anode input stream comprising H2, a reformable fuel, or a combination thereof into the anode gas collection zone; introducing a cathode input stream comprising O2 and CO2 into the cathode gas collection zone; and operating the molten carbonate fuel cell at an average current density of 60 mA/cm 2 or more to generate electricity, an anode exhaust, and a cathode exhaust.
  • Embodiment 10 The method of Embodiment 9, wherein the fuel cell is operated at a CO2 utilization of 80% or more.
  • Embodiment 12 The method of any of Embodiments 9 to 11, wherein the cathode input stream comprises 4.0 vol% to 10 vol% of CO2.

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

Abstract

L'invention concerne des structures de pile à combustible à carbonate fondu qui comprennent une couche support en maille structurale à l'interface entre la surface de la cathode et le collecteur de courant cathodique. La couche en maille structurale peut avoir une aire d'ouverture de maille de 25 % à 45 %. En plus de fournir un support structural, la couche en maille structurale peut réduire ou réduire au minimum la résistance ohmique à l'interface entre la cathode et le collecteur de courant cathodique.
EP23776136.6A 2022-08-25 2023-08-24 Support d'écran cathodique pour pile à combustible à carbonate fondu Pending EP4578053A2 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US202263373496P 2022-08-25 2022-08-25
US18/229,805 US20240072287A1 (en) 2022-08-25 2023-08-03 Cathode screen support for molten carbonate fuel cell
PCT/US2023/031070 WO2024044328A2 (fr) 2022-08-25 2023-08-24 Support d'écran cathodique pour pile à combustible à carbonate fondu

Publications (1)

Publication Number Publication Date
EP4578053A2 true EP4578053A2 (fr) 2025-07-02

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CN (1) CN119744458A (fr)
WO (1) WO2024044328A2 (fr)

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KR20180073394A (ko) * 2016-12-22 2018-07-02 주식회사 포스코 고체산화물 연료전지용 금속 집전체 및 그를 포함하는 고체산화물 연료전지 스택
WO2020112804A1 (fr) 2018-11-30 2020-06-04 Exxonmobil Research And Engineering Company Structures de collecteur de cathode pour pile à combustible à carbonate fondu
CN114930589B (zh) 2019-11-26 2025-05-30 埃克森美孚技术与工程公司 具有用于平行流动的外部歧管的燃料电池组件

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