US20180115002A1 - Reformer With Bypass For Internal Fuel Cell Reforming - Google Patents
Reformer With Bypass For Internal Fuel Cell Reforming Download PDFInfo
- Publication number
- US20180115002A1 US20180115002A1 US15/389,617 US201615389617A US2018115002A1 US 20180115002 A1 US20180115002 A1 US 20180115002A1 US 201615389617 A US201615389617 A US 201615389617A US 2018115002 A1 US2018115002 A1 US 2018115002A1
- Authority
- US
- United States
- Prior art keywords
- fuel
- bypass
- reformate
- fuel cell
- cathode
- 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.)
- Abandoned
Links
Images
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
- H01M8/06—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
- H01M8/0618—Reforming processes, e.g. autothermal, partial oxidation or steam reforming
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
- B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/248—Reactors comprising multiple separated flow channels
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J7/00—Apparatus for generating gases
-
- 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
- C01B3/384—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 the catalyst being continuously externally heated
-
- 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
-
- 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
- H01M8/04—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
- H01M8/04201—Reactant storage and supply, e.g. means for feeding, pipes
-
- 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
- H01M8/04298—Processes for controlling fuel cells or fuel cell systems
- H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
- H01M8/04746—Pressure; Flow
- H01M8/04753—Pressure; Flow of fuel cell 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
- H01M8/0662—Treatment of gaseous reactants or gaseous residues, e.g. cleaning
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
- B01J2219/00103—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor in a heat exchanger separate from the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00117—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with two or more reactions in heat exchange with each other, such as an endothermic reaction in heat exchange with an exothermic reaction
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00164—Controlling or regulating processes controlling the flow
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/24—Stationary reactors without moving elements inside
- B01J2219/2401—Reactors comprising multiple separate flow channels
- B01J2219/245—Plate-type reactors
- B01J2219/2461—Heat exchange aspects
- B01J2219/2462—Heat exchange aspects the reactants being in indirect heat exchange with a non reacting heat exchange medium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/24—Stationary reactors without moving elements inside
- B01J2219/2401—Reactors comprising multiple separate flow channels
- B01J2219/245—Plate-type reactors
- B01J2219/2476—Construction materials
- B01J2219/2477—Construction materials of the catalysts
- B01J2219/2479—Catalysts coated on the surface of plates or inserts
-
- 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
- C01B2203/06—Integration with other chemical processes
- C01B2203/066—Integration with other chemical processes with fuel cells
- C01B2203/067—Integration with other chemical processes with fuel cells the reforming process taking place in the fuel cell
-
- 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
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
-
- 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
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
- C01B2203/1047—Group VIII metal catalysts
-
- 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
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
- C01B2203/1047—Group VIII metal catalysts
- C01B2203/1064—Platinum group metal catalysts
-
- 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
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
- C01B2203/1082—Composition of support materials
-
- 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
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
-
- 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
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1241—Natural gas or methane
-
- 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
- This disclosure generally relates to fuel cells. More specifically, this disclosure is related to systems and methods which may support internally-reforming fuel cells.
- a fuel cell is an electrochemical system in which a fuel (such as hydrogen) is reacted with an oxidant (such as oxygen) at high temperature to generate electricity.
- a fuel such as hydrogen
- an oxidant such as oxygen
- One type of fuel cell is the solid oxide fuel cell (SOFC).
- SOFC solid oxide fuel cell
- the basic components of a SOFC may include an anode, a cathode, a solid electrolyte, and an interconnect.
- the fuel may be supplied to the anode, and the oxidant may be supplied to the cathode of the fuel cell. At the cathode, electrons ionize the oxidant.
- the electrolyte comprises a material that allows the ionized oxidant to pass through to the anode while simultaneously being impervious to the fluid fuel and oxidant.
- the fuel is combined with the ionized oxidant in an electrochemical reaction that releases electrons to be conducted back to the cathode through the interconnect. Additional heat, generated from ohmic losses within the fuel cell components, is removed from the fuel cell by either the anode or cathode flow stream or is radiated to the environment.
- a SOFC may be structured, e.g., as a segment-in-series or in-plane series arrangement of individual cells.
- the oxidant is typically introduced at one end of the series of cells and flows over the remaining cells until reaching the cathode exhaust outlet.
- Each fuel cell transfers a portion of the ohmic heat into the oxidant thereby raising its temperature, and forming a temperature gradient which increases from the oxidant inlet to the exhaust.
- this temperature gradient reduces the differential temperature between the fuel cell components and the oxidant, thereby reducing the heat transferred between the two. Consequently, a temperature gradient may also develop in the fuel cell which increases from the oxidant inlet to the oxidant exhaust. This temperature gradient may reduce fuel cell performance, reduce life, or cause thermal stresses across the cells that may cause material degradation or failure of the fuel cell components.
- the anode of a SOFC may be a mixed cermet comprising nickel and zirconia (such as, e.g., yttria stabilized zirconia (YSZ)) or nickel and ceria (such as, e.g., gadolinia dope ceria (GDC)).
- Nickel, and other materials may function not only to support the chemical reaction between the fuel and the ionized oxidant but may have catalytic properties which allow the anode to reform a hydrocarbon fuel within the fuel cell.
- One method of reforming the hydrocarbon fuel is steam reforming of methane (CH 4 ), an endothermic reaction:
- Carbon formation can cause fouling and degradation of fuel cell components through anode delamination, metal dusting and other failure mechanisms.
- supplying a mixture of a reformate that has been generated external to the fuel cell and unreformed fuel to the anode may provide better a balance for system performance and durability than supplying the stack with either reformate or unreformed fuel alone.
- the ratio of reformed and unreformed fuel must be precisely controlled. If the ratio is too high, the large temperature gradient across the fuel stack will remain. If it is too low, carbon formation becomes more likely leading to reduced life.
- assemblies for controlling the flow rate of a fluid typically include needle valves or other types of valves and orifice plates.
- Some adjustable orifice plates comprise rotating plates wherein each plate defines an opening. The alignment of plate openings determines the effective flow area of the orifice.
- these solutions are not suitable for the high temperature and pressure conditions of an operating fuel cell and are prone to leakage.
- a reformer with a bypass may contain a flow controller that restricts the bypass flow.
- the flow controller may be adjustable to control the flow rate of the fluid through the bypass, thereby enabling precise control of the ratio of reformate and unreformed fuels supplied to the fuel cell stack.
- effective and adjustable means are provided that control the fluid flow rate within a reformer bypass in a high temperature and pressure environment.
- a reformer unit may have a reforming section, a heat exchanging section, and a bypass section.
- the reforming section may reform a hydrocarbon-containing fuel, and have an inlet in fluid communication with a source of hydrocarbon fuel and an outlet in fluid communication with an anode inlet of a fuel cell stack.
- the heat exchanging section may heat a fluid flowing in the reforming section, in the bypass section, or both, and may have an inlet in fluid communication with an exhaust of a cathode of a fuel cell stack, and an outlet adapted for fluid communication with an inlet of a cathode of a fuel cell stack.
- the heat exchanging section is in thermal communication with said reforming section (or said bypass section or both) to effect heat transfer between the fluids flowing in each section.
- the bypass section provides a flow path for the hydrocarbon-containing fuel around the reforming section, and has an inlet in fluid communication with the reforming section inlet, an outlet in fluid communication with the reforming section outlet, and a variable orifice flow controller positioned in the bypassing flow path.
- a variable orifice flow controller for controlling the flow of a high temperature, high pressure, or both fluid.
- the flow controller may comprise an upstream connector, a downstream connector and an interconnector.
- the upstream connector may have cylindrical tubular portion defining a conduit in fluid communication with a flow path of high temperature fluid and a frusto-conical portion defining a plurality of conduits in fluid communication with the conduit.
- the downstream connector may define a frusto-conical cavity for receiving the frusto-conical portion of said upstream connector and a plurality of conduits in fluid communication with said cavity.
- the interconnector may provide a fluid-tight connection when the frusto-conical portion of the upstream connector is received within the cavity defined by said downstream connector.
- the amount of fluid communication between the plurality of conduits defined by the downstream and upstream connectors is selected by the radial alignment between the upstream and downstream connectors when in a gastight connection.
- a variable orifice flow controller for controlling the flow of a high temperature, high pressure, or both gas.
- the flow controller may comprise an upstream connector, a downstream connector, a disc, and an interconnector.
- the upstream connector may have cylindrical tubular portion defining a conduit in fluid communication with a flow path of high temperature fluid and a frusto-conical portion defining a plurality of conduits in fluid communication with the conduit.
- the downstream connector may define a frusto-conical cavity for receiving the frusto-conical portion of said upstream connector and a conduit in fluid communication with the cavity.
- the disc may define a plurality of conduits and may be adjacent to a face of the frusto-conical portion of said upstream connector in a selected radial alignment such that the plurality of conduits defined by the disc are in fluid communication with the plurality of conduits defined by the frusto-conical portion of the upstream connector and the conduit define by the downstream connector.
- the interconnector may provide a fluid-tight connection when the frusto-conical portion of the upstream connector is received within the cavity defined by said downstream connector.
- the amount of fluid communication between the plurality of conduits define by the disc and the plurality of conduits defined by the frusto-conical portion of said upstream connector is selected by the radial alignment of the conduits when in a gastight connection.
- a reformer unit for a fuel cell may comprise a reforming section, a heat exchanging section, and a bypass plenum.
- the reforming section reforms a hydrocarbon-containing fuel and has an inlet in fluid communication with a source of hydrocarbon-containing fuel and an outlet plenum in fluid communication with an anode inlet of a fuel cell stack.
- the heat exchanging section heats a fluid flowing in the reforming section, the bypass plenum, or both.
- the heat exchanging section has an inlet in fluid communication with the exhaust of a cathode and an outlet adapted for fluid communication with an inlet of cathode of the fuel cell stack.
- the heat exchanging section is in thermal communication with the reforming section and the bypass plenum to effect a heat transfer.
- the bypass plenum provides a flow path for the hydrocarbon-containing fuel to bypass the reforming section and has an inlet in fluid communication with the reforming section inlet, an outlet in fluid communication with the reforming section outlet plenum and a flow restrictor in the flowpath between the outlet of the bypass plenum and the outlet plenum of the reforming section.
- a flow restrictor for restricting the flow of a high temperature fluid through an orifice providing fluid communication between two plenums.
- the flow restrictor may comprise a connector mounted to a wall of a first plenum, a fitting, an elongated flow restricting member, and an internally threaded sealing nut.
- the connector comprises a first portion defining a cylindrical cavity having a threaded portion and a second portion which defines a frusto-cylindrical cavity in communication with the cylindrical cavity.
- the fitting comprises a frusto-conical end portion that is positioned within the frusto-conical cavity and defines an axial slot.
- the elongated flow restricting member comprises a cylindrical threaded portion positioned and threadably engaged with the cylindrical cavity, a portion extending from one end of said cylindrical portion into the axial slot and a tapered portion extending from the other end of the cylindrical portion through the orifice.
- the axial alignment of the tapered portion and the orifice is selectable by rotating the flow restricting member relative to the connector.
- the internally threaded sealing nut engages an external threaded portion of the connector and provides a fluid-tight seal between the fitting and the connector.
- a reforming unit for a fuel cell system may comprise a reforming section, a heat exchanging section and a bypass plenum.
- the reforming section reforms a hydrocarbon containing fuel.
- the heat exchanging section effects a heat transfer between a fluid flowing therethrough and the fluid flowing through the reforming section, the bypass plenum, or both.
- the bypass plenum provides a flowpath for the hydrocarbon-containing fuel to bypass the reforming section.
- the bypass plenum may comprise a flow restrictor in the outlet of the bypass plenum to control the amount of fluid communication between the outlet of the bypass plenum and the outlet of the reforming section.
- a method of controlling the volumetric ratio of a reformate and a hydrocarbon fuel in a mixture may be applied to a fuel cell system comprising a source of hydrocarbon fuel, a reformer and a fuel cell stack.
- the reformer may be configured for receiving the hydrocarbon fuel and converting the hydrocarbon fuel to a reformate.
- the fuel cell stack may have an anode inlet for receiving a mixture of the reformate and the hydrocarbon fuel.
- the method may comprise providing a flow path for fuel to bypass the reformer, controlling the flow rate of fuel within the flow path, and combining the fuel flowing through the bypass flow path with the reformate.
- a method of operating a fuel cell may be configured for internal reforming of a hydrocarbon fuel in the fuel cell stack.
- the method may comprise supplying a hydrocarbon fuel to a reformer to thereby convert the fuel to reformate, bypassing a second portion of the hydrocarbon fuel around the reformer, combining the bypassed hydrocarbon fuel with the reformate at a selected feed rate, supplying the combined reformate and hydrocarbon fuel to an anode inlet of the fuel cell stack, and controlling the volumetric ratio of the combined reformate and hydrocarbon fuel supplied to the anode inlet of the fuel cell stack by selecting the feed rate of the bypassed hydrocarbon fuel.
- a fuel cell system may comprise a fuel cell stack, a source of hydrocarbon fuel and a reformer unit.
- the fuel cell stack may be configured for internal reforming of a hydrocarbon fuel, and may comprise an anode portion in fluid communication with an anode inlet and an anode exhaust, and a cathode portion in fluid communication with a cathode inlet and a cathode exhaust.
- the reformer unit may convert hydrocarbon fuel to a reformate, and may comprise one or more cold-side channels, a fuel supply conduit, a reformate exhaust conduit, one or more hot-side channels, a cathode exhaust conduit, a cathode inlet conduit, one or more bypass channels, and a flow controller.
- the one or more cold-side channels may provide a reforming passage for fuel through the reformer unit.
- the fuel supply conduit may be in fluid communication with the fuel source and the cold-side channels.
- the one or more hot-side channels may provide a passage for a cathode exhaust gas to pass through the reforming unit and may be in sufficient proximity to the cold-side channels to effect a heat transfer between the fluids flowing through the respective channels.
- the cathode exhaust conduit may be in fluid communication with the cathode exhaust and the hot-side channels.
- the cathode inlet conduit may be in fluid communication with the hot-side channels and the cathode inlet.
- the one or more bypass channels may provide a non-reforming passage for fuel through the reformer unit and may be in fluid communication the fuel supply conduit and the reformate exhaust conduit to thereby combined the non-reformed fuel with the reformate.
- the flow controller may control the flow rate of the fuel flowing through said bypass channels.
- FIG. 1 is a system diagram of a fuel cell system with a reformer having a bypass in accordance with some embodiments of the present disclosure.
- FIGS. 2A and 2B are perspective views of a reformer having a bypass in accordance with some embodiments of the present disclosure.
- FIG. 3 provides two perspective views of a flow controller in accordance with some embodiments of the present disclosure.
- FIG. 4 provides two cross-section views of the flow controller of FIG. 3 in accordance with some embodiments of the present disclosure.
- FIG. 5 illustrates a perspective view of the assembled flow controller of FIG. 3 in accordance with some embodiments of the present disclosure.
- FIG. 6 illustrates a disassembled, perspective view of a flow controller in accordance with some embodiments of the present disclosure.
- FIG. 7 illustrates an assembled, perspective view of the flow controller of FIG. 6 in accordance with some embodiments of the present disclosure.
- FIG. 8 illustrates two perspective views of a reformer unit having a bypass plenum in accordance with some embodiments of the present disclosure.
- FIG. 9 illustrates the inlet plenum of a reformer unit having a bypass plenum in accordance with some embodiments of the present disclosure.
- FIG. 10 illustrates a close-up view of a bypass plenum in accordance with some embodiments of the present disclosure.
- FIG. 11 illustrates exploded and assembled cross-sectional views of a flow restrictor in accordance with some embodiments of the present disclosure.
- FIG. 12 provides a close-up view and a cross-sectional view of the outlet of a bypass plenum in accordance with some embodiments of the present disclosure.
- FIG. 1 A system diagram of a fuel cell system 100 configured for internal reforming of a hydrocarbon fuel having a bypass in accordance with some embodiments of the present disclosure is illustrated in FIG. 1 .
- the system 100 comprises a fuel cell stack 102 , a source of hydrocarbon fuel 116 , a reformer unit 118 , and an oxidant source 150 .
- the fuel cell stack 102 comprises an anode portion 104 in fluid communication with an anode inlet 106 and an anode exhaust 108 , and a cathode portion 110 in fluid communication with a cathode inlet 112 and a cathode exhaust 114 .
- the fuel cell stack 102 may be of any fuel cell design, and is preferably a SOFC.
- the source of hydrocarbon fuel 116 may provide any type of hydrocarbon fuel, such as, e.g., methane or natural gas, to the fuel cell system 100 .
- the source of oxidant 150 may provide air or other oxidant to the fuel cell system 100 .
- the reformer unit 118 converts hydrocarbon fuel from the source of hydrocarbon fuel 116 into a reformate and comprises one or more cold-side channels 120 , a fuel supply conduit 122 , a reformate exhaust conduit 124 , one or more hot-side channels 126 , a cathode exhaust conduit 128 , a cathode inlet conduit 130 , one or more bypass channels 132 , and a flow controller 134 .
- the reformer unit 118 is a steam reformer.
- the cold-side channels 120 provide reforming passages that reform the fuel supplied from the source of hydrocarbon fuel 116 into a reformate.
- the cold-side channels 120 may be referred to as a reforming section.
- the reforming passages may contain a catalyst comprising at least one Group VIII metal, and preferably one Group VIII noble metal, such as, e.g., platinum, palladium, rhodium, iridium or a combination thereof.
- a catalyst comprising rhodium and platinum are preferred.
- the catalyst may contain active metals in any suitable amount that achieves the desired amount of hydrocarbon conversion.
- the active catalyst metals may comprise 0.1 to 40 wt % of the catalyst.
- the active catalyst metals may comprise 0.5 to 25 wt % of the catalyst.
- the active catalyst metals may comprise 0.5 to 15 wt % of the catalyst.
- the catalyst may contain one or more promoter elements to improve the catalyst activity, durability, suppress carbon formation, or any combination of these or other improvements.
- the promoter elements may include, but are not limited to, elements from Groups IIa-VIIa, Groups Ib-Vb, lanthanide and actinide series elements, or any combination thereof. Promoters such as magnesia, ceria, and baria may suppress carbon formation.
- the promoter elements may be present in any amount ranging, from 0.01 to 10 wt % of the catalyst. In some embodiments, the promoter elements may be present in amount ranging from 0.01 to 5 wt % of the catalyst.
- the embodiments of the present disclosure are not so limited and may contain any amount of active metal, promoter elements, or both in ranges outside of those expressly listed.
- the catalyst may be supported on a carrier comprising a refractory oxide such as, e.g., silica, alumina, titania, zirconia, tungsten oxides, and mixtures thereof, although the disclosure is not limited to refractory oxides.
- the carrier may comprise a mixed refractory oxide compound comprising at least two cations.
- the catalyst active and promoter elements may be deposited on the carrier by any of a number of techniques.
- the catalyst may be deposited by impregnation onto the carrier, e.g., by contacting the carrier materials with a solution of the catalyst followed by drying and calcining the structure.
- the catalyst may be coated onto the plates of a heat exchanger or on inserts placed into the cold-side channels 120 .
- Catalyst pellets of a suitable size and shape may also be placed in the cold-side channel 120 .
- the embodiments of the present disclosure are not so limited, and any means of incorporating the catalyst into the cold-side channels 120 may be used, such as, e.g., using a porous support structure.
- the cold-side channels 120 are in fluid communication with the source of hydrocarbon fuel 116 via a fuel supply conduit 122 that functions to transport the hydrocarbon fuel from the source of the hydrocarbon fuel 116 to the cold-side channels 120 of the reformer unit 118 .
- the fuel cell system 100 may further comprise a higher hydrocarbon reduction unit 148 which is in fluid communication with both the source of hydrocarbon fuel 116 and the fuel supply conduit 122 .
- the higher hydrocarbon reduction unit 148 may be used upstream of the reformer unit 118 to reduce the level of higher hydrocarbons fed to the reformer unit 118 cold-side channels 120 and the bypass channel 132 . By reducing the level of higher hydrocarbons fed to the reformer unit 118 , the higher hydrocarbon reduction unit 148 inhibits carbon formation within the fuel cell system 100 .
- reformate exhaust conduit 124 which may also be referred to as an outlet plenum, that is in fluid communication with both the cold-side channels 120 and the anode inlet 106 .
- the reformate in the reformate exhaust conduit 124 may reach a junction at which the reformate may be combined and mixed with the flow of an unreformed hydrocarbon fuel flowing through the bypass channel 132 .
- the unreformed hydrocarbon fuel flowing through the bypass channel 132 may flow through a heat exchanger 142 , which may be referred to a second heat exchanging section.
- the heat exchanger 142 transfers heat from the cathode exhaust into the unreformed fuel.
- the heat exchanger may be located upstream from the hot-side channels 126 rather than downstream as depicted in FIG. 1 .
- the hot fluid flowing through heat exchanger 142 may be some fluid other than the cathode exhaust, such as, e.g., the anode exhaust, gasses from a anode-exhaust recycling combustor (such as combustor 146 ), or other source.
- Reformer Unit 118 also comprises one or more hot-side channels 126 , which may referred to as a heat exchange section.
- the hot-side channels 126 provide a passage for a cathode exhaust gas to flow through the reforming unit 118 .
- These channels 126 may be arranged in a sufficiently close proximity and orientation to the cold-side channels 120 in order to effect the transfer of heat between fluids flowing in the hot-side channels 126 and the cold-side channels 120 .
- the fluid flows in these channels maybe oriented for parallel flow, counter flow, cross flow, or any other heat exchanger configuration. Regardless of the proximity of the heat exchange section to the reforming section, both components are arranged to be in thermal communication with one another.
- the hot-side channels 126 of reformer unit 118 are in fluid communication with the cathode exhaust 114 via the cathode exhaust conduit 128 . Additionally, the hot-side channels 126 may be in fluid communication with the cathode inlet 112 via the cathode inlet conduit 130 .
- the cathode exhaust in the cathode inlet conduit 130 is supplied to the suction side of a cathode ejector 140 .
- the oxidant source 150 may provide the motive energy which operates the cathode ejector 140 .
- the cathode exhaust and oxidant may flow through the cold-side channels of a heat exchanger 144 prior to being supplied to the cathode inlet 112 .
- the hot-side channels of heat exchanger 144 may provide passage ways for a combustor 146 exhaust gas flow or other hot fluid which transfers heat into the combined cathode exhaust-oxidant flow supplied to the cathode inlet 112 .
- the reformer unit 118 comprises one or more bypass channels 132 , which may be referred to as a bypass section for providing a bypassing flow path, that provide a non-reforming passage for hydrocarbon fuel to flow through the reformer unit 118 .
- the bypass channel 132 is in fluid communication with the fuel supply conduit 122 and the reformate exhaust conduit 124 .
- the unreformed hydrocarbon fuel from the bypass channel 132 may be combined and mixed with the reformed fuel flowing through the reformate exhaust conduit 124 .
- the bypass channel 132 may be a line comprising a ceramic coating in order to inhibit metal-catalyzed carbon formation.
- FIG. 2A and FIG. 2B perspective views of a reformer having a bypass are illustrated in FIG. 2A and FIG. 2B .
- a portion the reformer unit 118 is illustrated as having a bypass channel 132 .
- the bypass channel 132 may be a line (such as, e.g., piping, hose, or similar component) connected proximate to and in fluid communication with the fuel supply conduit 122 .
- the bypass channel 132 line may pass through the cathode inlet conduit 130 prior to merging with the reformate exhaust conduit 124 .
- the cathode inlet conduit 130 may also be considered an exhaust duct through which the cathode exhaust is removed from the reforming unit 118 .
- the passage of the bypass channel 132 line through the cathode inlet conduit 130 will effect a heat transfer between the two fluids flowing in their respective sections.
- This arrangement may provide the function of heat exchanger 142 , although the embodiments of the present disclosure are not so limited.
- the amount of heat transferred between the cathode exhaust in the cathode inlet conduit 130 and the unreformed fuel in the bypass channel 132 line may be effected by varying the length of the bypass channel 132 line in the cathode inlet conduit 130 .
- the one or more bypass channels 132 may be integrated with the structure of the cold-side channels 120 and the hot-side channels 126 such that the channels 132 are in sufficient proximity to the hot-side channel 126 effect a heat transfer. In some embodiments, the one or more bypass channels 132 may be the equivalent of un-catalyzed cold-side channels 120 .
- the reformer unit 118 may further comprise a flow controller 134 , which may be referred to as a variable orifice flow controller, in the bypass channel 132 .
- the flow controller 134 may be an interchangeable flow orifice.
- the flow controller restricts the flow of the unreformed hydrocarbon fuel by reducing the effective area of the bypass channel 132 . Controlling the flow rate of the unreformed hydrocarbon fuel flowing in the bypass channel 132 allows the precise control of the ratio of reformate to unreformed fuel mixture supplied to the anode 104 .
- the fuel cell system 100 may further comprise one or more anode exhaust recycle lines.
- a portion of the anode exhaust may be drawn into an anode ejector 138 .
- the motive force for the anode ejector 138 may be the source of hydrocarbon fuel 116 , which may be pressurized by any conventional means.
- the recycled anode exhaust may then be combined with the source of hydrocarbon fuel 116 supplied to the reformer unit 118 .
- Another portion of the anode exhaust may be drawn into an auxiliary ejector 136 .
- the auxiliary ejector 136 may be supplied by the oxidant source 150 .
- the combined oxidant—anode exhaust mixture may then flow to a combustor 146 that supplies a combustion product to the hot-side channels of heat exchanger 144 .
- This combustion product may then be vented to the environment at 152 .
- Other systems may be supplied with these combustion products or other portions of the anode exhaust, e.g., to power a turbine which may pressure various flows in the fuel cell.
- a variable orifice flow controller 300 is provided, which may be flow controller 134 as described above.
- One embodiment of the flow controller 300 is illustrated in FIG. 3 to FIG. 5 .
- FIG. 3 illustrates two perspective views of a disassembled flow controller 300 .
- the flow controller 300 comprises an upstream connector 302 , a downstream connector 310 , and an interconnector 316 .
- the upstream connector 302 may have a cylindrical tubular portion which defines a conduit 304 that is in fluid communication with a bypass flow path designed to receive a fluid flowing through the bypass flow path. Other geometric configurations may be suitable for the conduit 304 .
- the upstream connector 302 may further comprise frusto-conical portion 306 which defines a plurality of conduits 308 . The plurality of conduits are in fluid communication with conduit 304 .
- the downstream connector 310 may define a frusto-conical cavity 312 configure to receive the frusto-conical portion 306 of the upstream connector 302 .
- the downstream connector 310 may further define a plurality of conduits 314 in fluid communication with the cavity 312 . Additionally, the conduits 314 are in fluid communication with the reformate exhaust conduit and the anode inlet.
- the plurality of conduits 308 and 314 may each be opposing, arcuate conduits, although other geometric designs may be used, and each conduit 308 may form an opposing pair with a conduit 314 .
- the interconnector 316 may be a connection fitting designed to provide a fluid-tight connection after the frusto-conical portion 306 is received within the frusto-conical cavity 312 .
- the interconnector 316 may comprise a plurality of internal threads (not shown) which engage a plurality of threads (not shown) on the downstream connector 310 . By tightening the interconnector 316 onto the downstream connector, the fluid-tight connection may be achieved.
- the fluid-tight connection may be gastight, wherein the gas refers to the gas flowing through flow controller 300 or the gas surrounding the flow controller 300 , such as, e.g., the atmosphere, or may refer to liquids.
- the interconnector 316 may be a hose nut.
- the amount of fluid communication between the plurality of conduits 308 and 314 may be selected by the radial alignment between the upstream and downstream connectors 302 and 310 , respectively.
- the conduits 308 and 314 may be aligned to provide the maximum flow rate achievable for a give flow controller 300 design, or the conduits 308 and 314 , respectively, may be intentionally misaligned in order to reduce the effective flow area of the flow controller 300 , thereby reducing the overall flow rate of the fluid in the bypass conduit.
- the flow controller 300 may further comprise an alignment tab 318 affixed to the upstream connector 302 and a plurality of alignment notches 320 on the downstream connector 310 .
- the alignment tab 318 and notches 320 function together to prevent the rotation of the upstream connector 302 around its long axis relative to the downstream connector 310 , thereby maintaining the desired alignment and, therefore, flow rate.
- the alignment of the conduits 308 and 314 is maintained by compression fit rather than, or in addition to, the use of the alignment tab 318 and notches 320 .
- FIG. 5 A perspective view of the assembled flow controller 300 is shown in FIG. 5 .
- the flow controller 300 illustrated in FIGS. 3-5 is designed for applications in which other designs would fail due to the high temperature, high pressure, or both high temperature and pressure of those applications. These high temperatures may be caused by the recycled anode exhaust which may be supplied to the fuel cell system reforming unit. Additional heat may be provided by a cathode exhaust gas (or other high temperature gas) heat exchanger which may be located upstream of the flow controller 300 .
- flow controller 300 may be able to maintain a fluid-tight connection at temperatures of at least 650 degrees Celsius, 700 degrees Celsius, 800 degrees Celsius, 850 degrees Celsius, 900 degrees Celsius, or 950 degrees Celsius.
- FIG. 6 illustrates the exploded, unassembled perspective view of the controller 600 .
- An assembled, perspective view of controller 600 may be seen in FIG. 7 .
- This flow controller may function in a manner similar to the controller 300 as described, and may contain components performing like functions.
- the downstream connector (not shown) may, or may not, define a plurality of conduits.
- the flow controller 600 may comprise a disc 622 that defines a plurality of conduits 624 .
- the alignment of the plurality of conduits 308 and 624 will determine the amount of fluid communication in bypass line.
- An alignment tab 618 may be affixed to the disc 622 and may be aligned with one of a plurality of notches 620 on the upstream connector 302 .
- the alignment tab 618 and open of the plurality of notches 620 operate to prevent rotation of the disc 622 relative to the upstream connector, and, therefore, maintain the amount of fluid communication between the plurality of conduits 308 and 624 .
- the flow controller may further comprise a retaining element 626 , such as, e.g., a screw, which retains the disc 622 adjacent to a face 628 of the frusto-conical portion 306 of the upstream connector 302 .
- the flow controller 600 illustrated in FIGS. 6-7 is designed for applications in which other designs would fail due to the high temperature, high pressure, or both high temperature and pressure of those applications. These high temperatures may be caused by the recycled anode exhaust which may be supplied to the fuel cell system reforming unit. Additional heat may be provided by a cathode exhaust gas (or other high temperature gas) heat exchanger which may be located upstream of the flow controller 300 .
- flow controller 600 may be able to maintain a fluid-tight connection at temperatures of at least 650 degrees Celsius, 700 degrees Celsius, 800 degrees Celsius, 850 degrees Celsius, 900 degrees Celsius, or 950 degrees Celsius.
- FIGS. 8-10 and FIG. 12 a reformer unit 800 having a bypass plenum is illustrated in FIGS. 8-10 and FIG. 12 .
- FIG. 8 illustrates two perspective views of the reformer unit 800 .
- FIG. 9 is a close-up of the reforming section inlet 808 .
- FIG. 10 is a close-up view of the bypass plenum 802 .
- FIG. 11 illustrate a flow restrictor.
- FIG. 12 illustrates two perspective views, one being a cross section of the other, of the reforming section outlet plenum 812 and the bypass plenum 802 outlet 810 .
- the reformer unit 800 may comprise a reforming section 804 and a heat exchanging section 816 which may be the cold-side channels and hot-side channels, respectively, as described above.
- the reformer unit 800 may further comprise a bypass plenum 802 having an inlet 806 , an outlet 810 , and a flow restrictor 814 .
- the inlet 806 may be in fluid communication with the reforming section inlet 808 and be configured to receive a portion of the unreformed hydrocarbon-fuel, anode-exhaust mixture flowing thereto.
- the outlet 810 is in fluid communication with the reforming section outlet plenum 812 such that the bypass plenum 802 and reforming section 804 flow paths may converge prior to being supplied to the anode.
- the flow restrictor 814 may be disposed in a flow path between the outlet 810 of the bypass plenum 802 and the outlet plenum 812 of the reforming section 804 .
- the heat exchanging section 816 of the reformer unit 800 may be configured to be in thermal communication with the bypass plenum 802 .
- the bypass plenum may share or have one or more walls in contact with the heat exchange section 816 . This will effect a heat exchange between the cathode exhaust, or other hot fluid, flowing through the heat exchanging section 816 to provide thermal energy to the bypass flow prior to that flow being merged with the reformed fuel from the reforming section 804 .
- the flow of cathode exhaust or other hot fluid in the heat exchange section 816 may be configured to exchange heat with the fluid in the bypass plenum 802 prior to exchanging heat with fluid in the reforming section 804 .
- the flow of cathode exhaust or other hot fluid in the heat exchange section 816 may be configured to exchange heat with the fluid in the reforming section 804 prior to exchanging heat with fluid in the bypass plenum 802 .
- the first occurring heat transfer may also be referred to as an upstream thermal communication.
- Whether the heat exchange between the fluid in the heat exchange section 816 occurs first with the bypass plenum 802 or the reforming section 804 may be controlled by, e.g., selecting the direction of flow of the cathode exhaust or other hot fluid.
- the outlet 810 of the bypass plenum 802 may define an orifice 818 providing fluid communication between the bypass plenum 802 and the outlet plenum 812 of the reforming section 804 .
- the flow restrictor 814 may comprise an elongated member 822 (also referred to as a flow restricting member or an elongated flow restricting member) which extends into the orifice to reduce its cross-sectional area and restrict the fluid flowing there through.
- the flow restrictor 814 may comprise a connector 820 and the flow restricting member 822 .
- the connector 820 may be mounted to the reformer unit 800 on a wall of the bypass plenum 802 .
- the flow restricting member 822 may be elongated and removably carried by the connector 820 .
- the member 822 extends through the orifice 818 , thereby reducing its effective cross-sectional area.
- the flow rate of the fluid flowing between the bypass plenum 802 and the outlet plenum 812 of the reforming section 804 is selected by sizing the flow restricting member 822 relative to the orifice 818 .
- the flow restricting member 822 may be cylindrical. In some embodiments the flow restricting member 822 may have an oval or rectangular cross-section or may be conical or other suitable shape.
- the elongated member 822 may have a threaded portion (not shown) for engaging the connector 820 .
- the flow restricting member 822 may have a taper cross-section.
- the flow rate between the bypass plenum 802 and the outlet plenum, 812 may be determined by the sizing of the member 822 and the orifice 818 and by the axial alignment between the two. This axial alignment may be set by rotating a threadably engaged member 822 within a threaded (not shown) connector 820 .
- the connector 820 may have a first portion defining a cylindrical cavity having a threaded portion for engaging the elongated member 822 , and may further have a second portion which may define a frusto-cylindrical cavity in communication with the cylindrical cavity. This cavity may accept a fitting 824 having a frusto-cylindrical portion defining an axial slot.
- the elongated member 822 may further comprise a portion which extends into this axial slot, thereby preventing rotation of the elongated member 822 while the fitting is installed. In some embodiments, rotation of the elongated member may be prevented when the nut 826 operably engages connector 820 to provide a fluid-tight seal.
- the flow restrictor 814 may further comprise an internally threaded sealing nut 826 which may engage external threading on the connector 820 , thereby providing a fluid-tight seal between the fitting 826 and the connector 820 when nut 826 is tightened on connector 820 . Additionally, fitting 824 may be engaged by the nut 826 to prevent leakage of system fluid around member 822 .
- the flow restrictor 814 illustrated in FIGS. 8 and 10-12 is designed for applications in which other designs would fail due to the high temperature and pressure of those applications. These high temperatures may be caused by the recycled anode exhaust which may be supplied to the fuel cell system reforming unit. Additional heat may be provided by a cathode exhaust gas (or other high temperature gas) heat exchanging section 816 .
- flow restrictor 814 may be able to maintain a fluid-tight connection at temperatures of at least 650 degrees Celsius, 700 degrees Celsius, 800 degrees Celsius, 850 degrees Celsius, 900 degrees Celsius, or 950 degrees Celsius.
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Sustainable Energy (AREA)
- Sustainable Development (AREA)
- Manufacturing & Machinery (AREA)
- Electrochemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Fuel Cell (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
A fuel cell system having a fuel cell stack, comprising an anode portion and a cathode portion, a source of hydrocarbon fuel, and a reformer unit having one or more cold-side, reforming passages, a fuel supply conduit, a reformate exhaust conduit, one or more hot-side channels, a cathode exhaust conduit, a cathode inlet conduit, one or more bypass channels having non-reforming passages for fuel to bypass the cold-side channels, and a flow controller for controlling the flowrate in the bypass channels, and methods for operating the same, is provided.
Description
- This Application is a continuation of U.S. patent application Ser. No. 15/333,255, titled “Steam Reformer Bypass Line and Flow Controller,” filed Oct. 25, 2016, which is herein incorporated by reference in its entirety for all purposes.
- This disclosure generally relates to fuel cells. More specifically, this disclosure is related to systems and methods which may support internally-reforming fuel cells.
- A fuel cell is an electrochemical system in which a fuel (such as hydrogen) is reacted with an oxidant (such as oxygen) at high temperature to generate electricity. One type of fuel cell is the solid oxide fuel cell (SOFC). The basic components of a SOFC may include an anode, a cathode, a solid electrolyte, and an interconnect. The fuel may be supplied to the anode, and the oxidant may be supplied to the cathode of the fuel cell. At the cathode, electrons ionize the oxidant. The electrolyte comprises a material that allows the ionized oxidant to pass through to the anode while simultaneously being impervious to the fluid fuel and oxidant. At the anode, the fuel is combined with the ionized oxidant in an electrochemical reaction that releases electrons to be conducted back to the cathode through the interconnect. Additional heat, generated from ohmic losses within the fuel cell components, is removed from the fuel cell by either the anode or cathode flow stream or is radiated to the environment.
- A SOFC may be structured, e.g., as a segment-in-series or in-plane series arrangement of individual cells. The oxidant is typically introduced at one end of the series of cells and flows over the remaining cells until reaching the cathode exhaust outlet. Each fuel cell transfers a portion of the ohmic heat into the oxidant thereby raising its temperature, and forming a temperature gradient which increases from the oxidant inlet to the exhaust. In turn, this temperature gradient reduces the differential temperature between the fuel cell components and the oxidant, thereby reducing the heat transferred between the two. Consequently, a temperature gradient may also develop in the fuel cell which increases from the oxidant inlet to the oxidant exhaust. This temperature gradient may reduce fuel cell performance, reduce life, or cause thermal stresses across the cells that may cause material degradation or failure of the fuel cell components.
- The anode of a SOFC may be a mixed cermet comprising nickel and zirconia (such as, e.g., yttria stabilized zirconia (YSZ)) or nickel and ceria (such as, e.g., gadolinia dope ceria (GDC)). Nickel, and other materials, may function not only to support the chemical reaction between the fuel and the ionized oxidant but may have catalytic properties which allow the anode to reform a hydrocarbon fuel within the fuel cell. One method of reforming the hydrocarbon fuel is steam reforming of methane (CH4), an endothermic reaction:
-
CH4+H20→CO+3H2ΔH°=206.2 kJ/mole - The heat necessary for reforming methane could be supplied directly from the ohmic heat generated from the fuel cells, with the reforming reaction either taking place in a separate reformer unit, or directly within the fuel cell stack. This direct heat transfer may help cool the stack and reduce thermal stresses. However, in-stack reforming introduces several technical challenges. Unreformed methane must be supplied in the correct amount to avoid excessively cooling of the fuel cell and in the correct manner to avoid localized cooling. Additionally, hydrocarbon fuels have a propensity to form carbon, particularly when a significant amount of reforming is performed:
-
CxH2x+2→C+(x+1)H2 - Carbon formation can cause fouling and degradation of fuel cell components through anode delamination, metal dusting and other failure mechanisms.
- Consequently, supplying a mixture of a reformate that has been generated external to the fuel cell and unreformed fuel to the anode may provide better a balance for system performance and durability than supplying the stack with either reformate or unreformed fuel alone. However, the ratio of reformed and unreformed fuel must be precisely controlled. If the ratio is too high, the large temperature gradient across the fuel stack will remain. If it is too low, carbon formation becomes more likely leading to reduced life.
- Additionally, assemblies for controlling the flow rate of a fluid typically include needle valves or other types of valves and orifice plates. Some adjustable orifice plates comprise rotating plates wherein each plate defines an opening. The alignment of plate openings determines the effective flow area of the orifice. However, these solutions are not suitable for the high temperature and pressure conditions of an operating fuel cell and are prone to leakage.
- There remains a need for precise control of the ratio of reformed and unreformed fuels delivered to a fuel cell stack to ensure that the proper amount of reforming occurs internally to the fuel cell. Additionally, there remains a need for systems and methods to achieve this precise control.
- In accordance with some embodiments of the present disclosure, a reformer with a bypass is provided. The bypass may contain a flow controller that restricts the bypass flow. The flow controller may be adjustable to control the flow rate of the fluid through the bypass, thereby enabling precise control of the ratio of reformate and unreformed fuels supplied to the fuel cell stack. This design permits some of the disclosed embodiments to accommodate a wide range of in-stack reforming fuel cell designs and minimizes the risk for carbon formation.
- In accordance with some embodiments of the present disclosure, effective and adjustable means are provided that control the fluid flow rate within a reformer bypass in a high temperature and pressure environment.
- In accordance with some embodiments of the present disclosure, a reformer unit is provided. The reformer unit may have a reforming section, a heat exchanging section, and a bypass section. The reforming section may reform a hydrocarbon-containing fuel, and have an inlet in fluid communication with a source of hydrocarbon fuel and an outlet in fluid communication with an anode inlet of a fuel cell stack. The heat exchanging section may heat a fluid flowing in the reforming section, in the bypass section, or both, and may have an inlet in fluid communication with an exhaust of a cathode of a fuel cell stack, and an outlet adapted for fluid communication with an inlet of a cathode of a fuel cell stack. The heat exchanging section is in thermal communication with said reforming section (or said bypass section or both) to effect heat transfer between the fluids flowing in each section. The bypass section provides a flow path for the hydrocarbon-containing fuel around the reforming section, and has an inlet in fluid communication with the reforming section inlet, an outlet in fluid communication with the reforming section outlet, and a variable orifice flow controller positioned in the bypassing flow path.
- In accordance with some embodiments of the present disclosure, a variable orifice flow controller for controlling the flow of a high temperature, high pressure, or both fluid is provided. The flow controller may comprise an upstream connector, a downstream connector and an interconnector. The upstream connector may have cylindrical tubular portion defining a conduit in fluid communication with a flow path of high temperature fluid and a frusto-conical portion defining a plurality of conduits in fluid communication with the conduit. The downstream connector may define a frusto-conical cavity for receiving the frusto-conical portion of said upstream connector and a plurality of conduits in fluid communication with said cavity. The interconnector may provide a fluid-tight connection when the frusto-conical portion of the upstream connector is received within the cavity defined by said downstream connector. The amount of fluid communication between the plurality of conduits defined by the downstream and upstream connectors is selected by the radial alignment between the upstream and downstream connectors when in a gastight connection.
- In accordance with some embodiments of the present disclosure a variable orifice flow controller for controlling the flow of a high temperature, high pressure, or both gas is provided. The flow controller may comprise an upstream connector, a downstream connector, a disc, and an interconnector. The upstream connector may have cylindrical tubular portion defining a conduit in fluid communication with a flow path of high temperature fluid and a frusto-conical portion defining a plurality of conduits in fluid communication with the conduit. The downstream connector may define a frusto-conical cavity for receiving the frusto-conical portion of said upstream connector and a conduit in fluid communication with the cavity. The disc may define a plurality of conduits and may be adjacent to a face of the frusto-conical portion of said upstream connector in a selected radial alignment such that the plurality of conduits defined by the disc are in fluid communication with the plurality of conduits defined by the frusto-conical portion of the upstream connector and the conduit define by the downstream connector. The interconnector may provide a fluid-tight connection when the frusto-conical portion of the upstream connector is received within the cavity defined by said downstream connector. The amount of fluid communication between the plurality of conduits define by the disc and the plurality of conduits defined by the frusto-conical portion of said upstream connector is selected by the radial alignment of the conduits when in a gastight connection.
- In accordance with some embodiments of the present disclosure, a reformer unit for a fuel cell is presented. The reformer unit may comprise a reforming section, a heat exchanging section, and a bypass plenum. The reforming section reforms a hydrocarbon-containing fuel and has an inlet in fluid communication with a source of hydrocarbon-containing fuel and an outlet plenum in fluid communication with an anode inlet of a fuel cell stack. The heat exchanging section heats a fluid flowing in the reforming section, the bypass plenum, or both. The heat exchanging section has an inlet in fluid communication with the exhaust of a cathode and an outlet adapted for fluid communication with an inlet of cathode of the fuel cell stack. The heat exchanging section is in thermal communication with the reforming section and the bypass plenum to effect a heat transfer. The bypass plenum provides a flow path for the hydrocarbon-containing fuel to bypass the reforming section and has an inlet in fluid communication with the reforming section inlet, an outlet in fluid communication with the reforming section outlet plenum and a flow restrictor in the flowpath between the outlet of the bypass plenum and the outlet plenum of the reforming section.
- In accordance with some embodiments of the present disclosure, a flow restrictor for restricting the flow of a high temperature fluid through an orifice providing fluid communication between two plenums is provided. The flow restrictor may comprise a connector mounted to a wall of a first plenum, a fitting, an elongated flow restricting member, and an internally threaded sealing nut. The connector comprises a first portion defining a cylindrical cavity having a threaded portion and a second portion which defines a frusto-cylindrical cavity in communication with the cylindrical cavity. The fitting comprises a frusto-conical end portion that is positioned within the frusto-conical cavity and defines an axial slot. The elongated flow restricting member comprises a cylindrical threaded portion positioned and threadably engaged with the cylindrical cavity, a portion extending from one end of said cylindrical portion into the axial slot and a tapered portion extending from the other end of the cylindrical portion through the orifice. The axial alignment of the tapered portion and the orifice is selectable by rotating the flow restricting member relative to the connector. The internally threaded sealing nut engages an external threaded portion of the connector and provides a fluid-tight seal between the fitting and the connector.
- In accordance with some embodiments of the present disclosure, a reforming unit for a fuel cell system is provided. The reforming unit may comprise a reforming section, a heat exchanging section and a bypass plenum. The reforming section reforms a hydrocarbon containing fuel. The heat exchanging section effects a heat transfer between a fluid flowing therethrough and the fluid flowing through the reforming section, the bypass plenum, or both. The bypass plenum provides a flowpath for the hydrocarbon-containing fuel to bypass the reforming section. The bypass plenum may comprise a flow restrictor in the outlet of the bypass plenum to control the amount of fluid communication between the outlet of the bypass plenum and the outlet of the reforming section.
- In accordance with some embodiments of the present disclosure, a method of controlling the volumetric ratio of a reformate and a hydrocarbon fuel in a mixture is provided. The method may be applied to a fuel cell system comprising a source of hydrocarbon fuel, a reformer and a fuel cell stack. The reformer may be configured for receiving the hydrocarbon fuel and converting the hydrocarbon fuel to a reformate. The fuel cell stack may have an anode inlet for receiving a mixture of the reformate and the hydrocarbon fuel. The method may comprise providing a flow path for fuel to bypass the reformer, controlling the flow rate of fuel within the flow path, and combining the fuel flowing through the bypass flow path with the reformate.
- In accordance with some embodiments of the present disclosure, a method of operating a fuel cell is provided. The fuel cell system may be configured for internal reforming of a hydrocarbon fuel in the fuel cell stack. The method may comprise supplying a hydrocarbon fuel to a reformer to thereby convert the fuel to reformate, bypassing a second portion of the hydrocarbon fuel around the reformer, combining the bypassed hydrocarbon fuel with the reformate at a selected feed rate, supplying the combined reformate and hydrocarbon fuel to an anode inlet of the fuel cell stack, and controlling the volumetric ratio of the combined reformate and hydrocarbon fuel supplied to the anode inlet of the fuel cell stack by selecting the feed rate of the bypassed hydrocarbon fuel.
- In accordance with some embodiments of the present disclosure, a fuel cell system is provided. The fuel cell system may comprise a fuel cell stack, a source of hydrocarbon fuel and a reformer unit. The fuel cell stack may be configured for internal reforming of a hydrocarbon fuel, and may comprise an anode portion in fluid communication with an anode inlet and an anode exhaust, and a cathode portion in fluid communication with a cathode inlet and a cathode exhaust. The reformer unit may convert hydrocarbon fuel to a reformate, and may comprise one or more cold-side channels, a fuel supply conduit, a reformate exhaust conduit, one or more hot-side channels, a cathode exhaust conduit, a cathode inlet conduit, one or more bypass channels, and a flow controller. The one or more cold-side channels may provide a reforming passage for fuel through the reformer unit. The fuel supply conduit may be in fluid communication with the fuel source and the cold-side channels. The one or more hot-side channels may provide a passage for a cathode exhaust gas to pass through the reforming unit and may be in sufficient proximity to the cold-side channels to effect a heat transfer between the fluids flowing through the respective channels. The cathode exhaust conduit may be in fluid communication with the cathode exhaust and the hot-side channels. The cathode inlet conduit may be in fluid communication with the hot-side channels and the cathode inlet. The one or more bypass channels may provide a non-reforming passage for fuel through the reformer unit and may be in fluid communication the fuel supply conduit and the reformate exhaust conduit to thereby combined the non-reformed fuel with the reformate. The flow controller may control the flow rate of the fuel flowing through said bypass channels.
- These and many other advantages of the present subject matter will be readily apparent to one skilled in the art to which the disclosure pertains from a perusal of the claims, the appended drawings, and the following detail description of the embodiments.
-
FIG. 1 is a system diagram of a fuel cell system with a reformer having a bypass in accordance with some embodiments of the present disclosure. -
FIGS. 2A and 2B are perspective views of a reformer having a bypass in accordance with some embodiments of the present disclosure. -
FIG. 3 provides two perspective views of a flow controller in accordance with some embodiments of the present disclosure. -
FIG. 4 provides two cross-section views of the flow controller ofFIG. 3 in accordance with some embodiments of the present disclosure. -
FIG. 5 illustrates a perspective view of the assembled flow controller ofFIG. 3 in accordance with some embodiments of the present disclosure. -
FIG. 6 illustrates a disassembled, perspective view of a flow controller in accordance with some embodiments of the present disclosure. -
FIG. 7 illustrates an assembled, perspective view of the flow controller ofFIG. 6 in accordance with some embodiments of the present disclosure. -
FIG. 8 illustrates two perspective views of a reformer unit having a bypass plenum in accordance with some embodiments of the present disclosure. -
FIG. 9 illustrates the inlet plenum of a reformer unit having a bypass plenum in accordance with some embodiments of the present disclosure. -
FIG. 10 illustrates a close-up view of a bypass plenum in accordance with some embodiments of the present disclosure. -
FIG. 11 illustrates exploded and assembled cross-sectional views of a flow restrictor in accordance with some embodiments of the present disclosure. -
FIG. 12 provides a close-up view and a cross-sectional view of the outlet of a bypass plenum in accordance with some embodiments of the present disclosure. - Referring to the drawings, some aspects of non-limiting examples of a fuel cell system in accordance with an embodiment of the present disclosure are schematically depicted. In the drawings, various features, components and interrelationships between aspects of an embodiment of the present disclosure are depicted. However, the present disclosure is not limited to the particular embodiments presented and the components, features and interrelationships as illustrated in the drawings and described herein.
- The objectives and advantages of the claimed subject matter will become apparent from the following detailed description of the preferred embodiments thereof in connection with the accompanying drawings, in which like reference numerals denote like elements.
- A system diagram of a
fuel cell system 100 configured for internal reforming of a hydrocarbon fuel having a bypass in accordance with some embodiments of the present disclosure is illustrated inFIG. 1 . Thesystem 100 comprises afuel cell stack 102, a source ofhydrocarbon fuel 116, areformer unit 118, and anoxidant source 150. Thefuel cell stack 102 comprises ananode portion 104 in fluid communication with ananode inlet 106 and ananode exhaust 108, and acathode portion 110 in fluid communication with acathode inlet 112 and acathode exhaust 114. Thefuel cell stack 102 may be of any fuel cell design, and is preferably a SOFC. - The source of
hydrocarbon fuel 116 may provide any type of hydrocarbon fuel, such as, e.g., methane or natural gas, to thefuel cell system 100. The source ofoxidant 150 may provide air or other oxidant to thefuel cell system 100. - The
reformer unit 118 converts hydrocarbon fuel from the source ofhydrocarbon fuel 116 into a reformate and comprises one or more cold-side channels 120, afuel supply conduit 122, areformate exhaust conduit 124, one or more hot-side channels 126, a cathode exhaust conduit 128, acathode inlet conduit 130, one ormore bypass channels 132, and aflow controller 134. In a preferred embodiment thereformer unit 118 is a steam reformer. - The cold-
side channels 120 provide reforming passages that reform the fuel supplied from the source ofhydrocarbon fuel 116 into a reformate. The cold-side channels 120 may be referred to as a reforming section. The reforming passages may contain a catalyst comprising at least one Group VIII metal, and preferably one Group VIII noble metal, such as, e.g., platinum, palladium, rhodium, iridium or a combination thereof. A catalyst comprising rhodium and platinum are preferred. The catalyst may contain active metals in any suitable amount that achieves the desired amount of hydrocarbon conversion. For example, the active catalyst metals may comprise 0.1 to 40 wt % of the catalyst. In some embodiments, the active catalyst metals may comprise 0.5 to 25 wt % of the catalyst. In some embodiments, the active catalyst metals may comprise 0.5 to 15 wt % of the catalyst. - In some embodiments, the catalyst may contain one or more promoter elements to improve the catalyst activity, durability, suppress carbon formation, or any combination of these or other improvements. The promoter elements may include, but are not limited to, elements from Groups IIa-VIIa, Groups Ib-Vb, lanthanide and actinide series elements, or any combination thereof. Promoters such as magnesia, ceria, and baria may suppress carbon formation. The promoter elements may be present in any amount ranging, from 0.01 to 10 wt % of the catalyst. In some embodiments, the promoter elements may be present in amount ranging from 0.01 to 5 wt % of the catalyst. The embodiments of the present disclosure are not so limited and may contain any amount of active metal, promoter elements, or both in ranges outside of those expressly listed.
- The catalyst may be supported on a carrier comprising a refractory oxide such as, e.g., silica, alumina, titania, zirconia, tungsten oxides, and mixtures thereof, although the disclosure is not limited to refractory oxides. In some embodiments, the carrier may comprise a mixed refractory oxide compound comprising at least two cations. The catalyst active and promoter elements may be deposited on the carrier by any of a number of techniques. The catalyst may be deposited by impregnation onto the carrier, e.g., by contacting the carrier materials with a solution of the catalyst followed by drying and calcining the structure. The catalyst may be coated onto the plates of a heat exchanger or on inserts placed into the cold-
side channels 120. Catalyst pellets of a suitable size and shape may also be placed in the cold-side channel 120. However, the embodiments of the present disclosure are not so limited, and any means of incorporating the catalyst into the cold-side channels 120 may be used, such as, e.g., using a porous support structure. - The cold-
side channels 120 are in fluid communication with the source ofhydrocarbon fuel 116 via afuel supply conduit 122 that functions to transport the hydrocarbon fuel from the source of thehydrocarbon fuel 116 to the cold-side channels 120 of thereformer unit 118. - In accordance with some embodiments, the
fuel cell system 100 may further comprise a higherhydrocarbon reduction unit 148 which is in fluid communication with both the source ofhydrocarbon fuel 116 and thefuel supply conduit 122. The higherhydrocarbon reduction unit 148 may be used upstream of thereformer unit 118 to reduce the level of higher hydrocarbons fed to thereformer unit 118 cold-side channels 120 and thebypass channel 132. By reducing the level of higher hydrocarbons fed to thereformer unit 118, the higherhydrocarbon reduction unit 148 inhibits carbon formation within thefuel cell system 100. - As the hydrocarbon fuel passes through the reforming passages of the cold-
side channels 120 it is at least partially reformed to reformate or syngas (a mixture containing hydrogen and carbon monoxide). This reformate flows into thereformate exhaust conduit 124, which may also be referred to as an outlet plenum, that is in fluid communication with both the cold-side channels 120 and theanode inlet 106. Prior to reaching theanode inlet 106, the reformate in thereformate exhaust conduit 124 may reach a junction at which the reformate may be combined and mixed with the flow of an unreformed hydrocarbon fuel flowing through thebypass channel 132. The unreformed hydrocarbon fuel flowing through thebypass channel 132 may flow through aheat exchanger 142, which may be referred to a second heat exchanging section. Theheat exchanger 142 transfers heat from the cathode exhaust into the unreformed fuel. In some embodiments, the heat exchanger may be located upstream from the hot-side channels 126 rather than downstream as depicted inFIG. 1 . In some embodiments, the hot fluid flowing throughheat exchanger 142 may be some fluid other than the cathode exhaust, such as, e.g., the anode exhaust, gasses from a anode-exhaust recycling combustor (such as combustor 146), or other source. -
Reformer Unit 118 also comprises one or more hot-side channels 126, which may referred to as a heat exchange section. The hot-side channels 126 provide a passage for a cathode exhaust gas to flow through the reformingunit 118. Thesechannels 126 may be arranged in a sufficiently close proximity and orientation to the cold-side channels 120 in order to effect the transfer of heat between fluids flowing in the hot-side channels 126 and the cold-side channels 120. The fluid flows in these channels maybe oriented for parallel flow, counter flow, cross flow, or any other heat exchanger configuration. Regardless of the proximity of the heat exchange section to the reforming section, both components are arranged to be in thermal communication with one another. - The hot-
side channels 126 ofreformer unit 118 are in fluid communication with thecathode exhaust 114 via the cathode exhaust conduit 128. Additionally, the hot-side channels 126 may be in fluid communication with thecathode inlet 112 via thecathode inlet conduit 130. In accordance with some embodiments, the cathode exhaust in thecathode inlet conduit 130 is supplied to the suction side of acathode ejector 140. Theoxidant source 150 may provide the motive energy which operates thecathode ejector 140. The cathode exhaust and oxidant may flow through the cold-side channels of aheat exchanger 144 prior to being supplied to thecathode inlet 112. The hot-side channels ofheat exchanger 144 may provide passage ways for acombustor 146 exhaust gas flow or other hot fluid which transfers heat into the combined cathode exhaust-oxidant flow supplied to thecathode inlet 112. - The
reformer unit 118 comprises one ormore bypass channels 132, which may be referred to as a bypass section for providing a bypassing flow path, that provide a non-reforming passage for hydrocarbon fuel to flow through thereformer unit 118. Thebypass channel 132 is in fluid communication with thefuel supply conduit 122 and thereformate exhaust conduit 124. The unreformed hydrocarbon fuel from thebypass channel 132 may be combined and mixed with the reformed fuel flowing through thereformate exhaust conduit 124. Thebypass channel 132 may be a line comprising a ceramic coating in order to inhibit metal-catalyzed carbon formation. - In accordance with some embodiments of the present disclosure, perspective views of a reformer having a bypass are illustrated in
FIG. 2A andFIG. 2B . A portion thereformer unit 118 is illustrated as having abypass channel 132. Thebypass channel 132 may be a line (such as, e.g., piping, hose, or similar component) connected proximate to and in fluid communication with thefuel supply conduit 122. As shown inFIG. 2B , thebypass channel 132 line may pass through thecathode inlet conduit 130 prior to merging with thereformate exhaust conduit 124. Thecathode inlet conduit 130 may also be considered an exhaust duct through which the cathode exhaust is removed from the reformingunit 118. In some embodiments, the passage of thebypass channel 132 line through thecathode inlet conduit 130 will effect a heat transfer between the two fluids flowing in their respective sections. This arrangement may provide the function ofheat exchanger 142, although the embodiments of the present disclosure are not so limited. The amount of heat transferred between the cathode exhaust in thecathode inlet conduit 130 and the unreformed fuel in thebypass channel 132 line may be effected by varying the length of thebypass channel 132 line in thecathode inlet conduit 130. - In some embodiments, the one or
more bypass channels 132 may be integrated with the structure of the cold-side channels 120 and the hot-side channels 126 such that thechannels 132 are in sufficient proximity to the hot-side channel 126 effect a heat transfer. In some embodiments, the one ormore bypass channels 132 may be the equivalent of un-catalyzed cold-side channels 120. - The
reformer unit 118 may further comprise aflow controller 134, which may be referred to as a variable orifice flow controller, in thebypass channel 132. Theflow controller 134 may be an interchangeable flow orifice. The flow controller restricts the flow of the unreformed hydrocarbon fuel by reducing the effective area of thebypass channel 132. Controlling the flow rate of the unreformed hydrocarbon fuel flowing in thebypass channel 132 allows the precise control of the ratio of reformate to unreformed fuel mixture supplied to theanode 104. - In accordance with some embodiments of the present disclosure, the
fuel cell system 100 may further comprise one or more anode exhaust recycle lines. For example, a portion of the anode exhaust may be drawn into ananode ejector 138. The motive force for theanode ejector 138 may be the source ofhydrocarbon fuel 116, which may be pressurized by any conventional means. The recycled anode exhaust may then be combined with the source ofhydrocarbon fuel 116 supplied to thereformer unit 118. - Another portion of the anode exhaust may be drawn into an
auxiliary ejector 136. Theauxiliary ejector 136 may be supplied by theoxidant source 150. The combined oxidant—anode exhaust mixture may then flow to acombustor 146 that supplies a combustion product to the hot-side channels ofheat exchanger 144. This combustion product may then be vented to the environment at 152. Other systems may be supplied with these combustion products or other portions of the anode exhaust, e.g., to power a turbine which may pressure various flows in the fuel cell. - In accordance with some embodiments of present disclosure, a variable
orifice flow controller 300 is provided, which may beflow controller 134 as described above. One embodiment of theflow controller 300 is illustrated inFIG. 3 toFIG. 5 .FIG. 3 illustrates two perspective views of a disassembledflow controller 300. Theflow controller 300 comprises anupstream connector 302, adownstream connector 310, and aninterconnector 316. - The
upstream connector 302 may have a cylindrical tubular portion which defines aconduit 304 that is in fluid communication with a bypass flow path designed to receive a fluid flowing through the bypass flow path. Other geometric configurations may be suitable for theconduit 304. Theupstream connector 302 may further comprise frusto-conical portion 306 which defines a plurality ofconduits 308. The plurality of conduits are in fluid communication withconduit 304. - The
downstream connector 310 may define a frusto-conical cavity 312 configure to receive the frusto-conical portion 306 of theupstream connector 302. Thedownstream connector 310 may further define a plurality ofconduits 314 in fluid communication with thecavity 312. Additionally, theconduits 314 are in fluid communication with the reformate exhaust conduit and the anode inlet. - The plurality of
conduits conduit 308 may form an opposing pair with aconduit 314. - The
interconnector 316 may be a connection fitting designed to provide a fluid-tight connection after the frusto-conical portion 306 is received within the frusto-conical cavity 312. Theinterconnector 316 may comprise a plurality of internal threads (not shown) which engage a plurality of threads (not shown) on thedownstream connector 310. By tightening theinterconnector 316 onto the downstream connector, the fluid-tight connection may be achieved. The fluid-tight connection may be gastight, wherein the gas refers to the gas flowing throughflow controller 300 or the gas surrounding theflow controller 300, such as, e.g., the atmosphere, or may refer to liquids. Theinterconnector 316 may be a hose nut. - The amount of fluid communication between the plurality of
conduits downstream connectors FIG. 4 , theconduits give flow controller 300 design, or theconduits flow controller 300, thereby reducing the overall flow rate of the fluid in the bypass conduit. - The
flow controller 300 may further comprise analignment tab 318 affixed to theupstream connector 302 and a plurality ofalignment notches 320 on thedownstream connector 310. Thealignment tab 318 andnotches 320 function together to prevent the rotation of theupstream connector 302 around its long axis relative to thedownstream connector 310, thereby maintaining the desired alignment and, therefore, flow rate. In some embodiments the alignment of theconduits alignment tab 318 andnotches 320. - A perspective view of the assembled
flow controller 300 is shown inFIG. 5 . - The
flow controller 300 illustrated inFIGS. 3-5 is designed for applications in which other designs would fail due to the high temperature, high pressure, or both high temperature and pressure of those applications. These high temperatures may be caused by the recycled anode exhaust which may be supplied to the fuel cell system reforming unit. Additional heat may be provided by a cathode exhaust gas (or other high temperature gas) heat exchanger which may be located upstream of theflow controller 300. For example,flow controller 300 may be able to maintain a fluid-tight connection at temperatures of at least 650 degrees Celsius, 700 degrees Celsius, 800 degrees Celsius, 850 degrees Celsius, 900 degrees Celsius, or 950 degrees Celsius. - A
flow controller 600 in accordance with some embodiments of the present disclosure is illustrated inFIG. 6 andFIG. 7 .FIG. 6 illustrates the exploded, unassembled perspective view of thecontroller 600. An assembled, perspective view ofcontroller 600 may be seen inFIG. 7 . This flow controller may function in a manner similar to thecontroller 300 as described, and may contain components performing like functions. In the embodiment illustrated inFIG. 6 andFIG. 7 , the downstream connector (not shown) may, or may not, define a plurality of conduits. Theflow controller 600 may comprise adisc 622 that defines a plurality ofconduits 624. In accordance with some embodiments, the alignment of the plurality ofconduits alignment tab 618 may be affixed to thedisc 622 and may be aligned with one of a plurality ofnotches 620 on theupstream connector 302. When the upstream and downstream connectors are in a fluid-tight connection, thealignment tab 618 and open of the plurality ofnotches 620 operate to prevent rotation of thedisc 622 relative to the upstream connector, and, therefore, maintain the amount of fluid communication between the plurality ofconduits element 626, such as, e.g., a screw, which retains thedisc 622 adjacent to aface 628 of the frusto-conical portion 306 of theupstream connector 302. - The
flow controller 600 illustrated inFIGS. 6-7 is designed for applications in which other designs would fail due to the high temperature, high pressure, or both high temperature and pressure of those applications. These high temperatures may be caused by the recycled anode exhaust which may be supplied to the fuel cell system reforming unit. Additional heat may be provided by a cathode exhaust gas (or other high temperature gas) heat exchanger which may be located upstream of theflow controller 300. For example,flow controller 600 may be able to maintain a fluid-tight connection at temperatures of at least 650 degrees Celsius, 700 degrees Celsius, 800 degrees Celsius, 850 degrees Celsius, 900 degrees Celsius, or 950 degrees Celsius. - In accordance with some embodiments of the present disclosure, a
reformer unit 800 having a bypass plenum is illustrated inFIGS. 8-10 andFIG. 12 .FIG. 8 illustrates two perspective views of thereformer unit 800.FIG. 9 is a close-up of the reformingsection inlet 808.FIG. 10 is a close-up view of thebypass plenum 802.FIG. 11 illustrate a flow restrictor.FIG. 12 illustrates two perspective views, one being a cross section of the other, of the reformingsection outlet plenum 812 and thebypass plenum 802outlet 810. - The
reformer unit 800 may comprise a reformingsection 804 and aheat exchanging section 816 which may be the cold-side channels and hot-side channels, respectively, as described above. Thereformer unit 800 may further comprise abypass plenum 802 having aninlet 806, anoutlet 810, and aflow restrictor 814. Theinlet 806 may be in fluid communication with the reformingsection inlet 808 and be configured to receive a portion of the unreformed hydrocarbon-fuel, anode-exhaust mixture flowing thereto. Theoutlet 810 is in fluid communication with the reformingsection outlet plenum 812 such that thebypass plenum 802 and reformingsection 804 flow paths may converge prior to being supplied to the anode. The flow restrictor 814 may be disposed in a flow path between theoutlet 810 of thebypass plenum 802 and theoutlet plenum 812 of the reformingsection 804. - The
heat exchanging section 816 of thereformer unit 800 may be configured to be in thermal communication with thebypass plenum 802. For example, the bypass plenum may share or have one or more walls in contact with theheat exchange section 816. This will effect a heat exchange between the cathode exhaust, or other hot fluid, flowing through theheat exchanging section 816 to provide thermal energy to the bypass flow prior to that flow being merged with the reformed fuel from the reformingsection 804. In some embodiments, the flow of cathode exhaust or other hot fluid in theheat exchange section 816 may be configured to exchange heat with the fluid in thebypass plenum 802 prior to exchanging heat with fluid in the reformingsection 804. In other embodiments, the flow of cathode exhaust or other hot fluid in theheat exchange section 816 may be configured to exchange heat with the fluid in the reformingsection 804 prior to exchanging heat with fluid in thebypass plenum 802. The first occurring heat transfer may also be referred to as an upstream thermal communication. Whether the heat exchange between the fluid in theheat exchange section 816 occurs first with thebypass plenum 802 or the reformingsection 804 may be controlled by, e.g., selecting the direction of flow of the cathode exhaust or other hot fluid. - As shown in
FIG. 12 , theoutlet 810 of thebypass plenum 802 may define anorifice 818 providing fluid communication between thebypass plenum 802 and theoutlet plenum 812 of the reformingsection 804. The flow restrictor 814 may comprise an elongated member 822 (also referred to as a flow restricting member or an elongated flow restricting member) which extends into the orifice to reduce its cross-sectional area and restrict the fluid flowing there through. - Alternate views of the
flow restrictor 814 are provided inFIG. 11 . The flow restrictor 814 may comprise aconnector 820 and theflow restricting member 822. Theconnector 820 may be mounted to thereformer unit 800 on a wall of thebypass plenum 802. - The
flow restricting member 822 may be elongated and removably carried by theconnector 820. Themember 822 extends through theorifice 818, thereby reducing its effective cross-sectional area. The flow rate of the fluid flowing between thebypass plenum 802 and theoutlet plenum 812 of the reformingsection 804 is selected by sizing theflow restricting member 822 relative to theorifice 818. Theflow restricting member 822 may be cylindrical. In some embodiments theflow restricting member 822 may have an oval or rectangular cross-section or may be conical or other suitable shape. Theelongated member 822 may have a threaded portion (not shown) for engaging theconnector 820. - In some embodiments, the
flow restricting member 822 may have a taper cross-section. The flow rate between thebypass plenum 802 and the outlet plenum, 812 may be determined by the sizing of themember 822 and theorifice 818 and by the axial alignment between the two. This axial alignment may be set by rotating a threadably engagedmember 822 within a threaded (not shown)connector 820. - The
connector 820 may have a first portion defining a cylindrical cavity having a threaded portion for engaging theelongated member 822, and may further have a second portion which may define a frusto-cylindrical cavity in communication with the cylindrical cavity. This cavity may accept a fitting 824 having a frusto-cylindrical portion defining an axial slot. Theelongated member 822 may further comprise a portion which extends into this axial slot, thereby preventing rotation of theelongated member 822 while the fitting is installed. In some embodiments, rotation of the elongated member may be prevented when thenut 826 operably engagesconnector 820 to provide a fluid-tight seal. - The flow restrictor 814 may further comprise an internally threaded sealing
nut 826 which may engage external threading on theconnector 820, thereby providing a fluid-tight seal between the fitting 826 and theconnector 820 whennut 826 is tightened onconnector 820. Additionally, fitting 824 may be engaged by thenut 826 to prevent leakage of system fluid aroundmember 822. - The flow restrictor 814 illustrated in
FIGS. 8 and 10-12 is designed for applications in which other designs would fail due to the high temperature and pressure of those applications. These high temperatures may be caused by the recycled anode exhaust which may be supplied to the fuel cell system reforming unit. Additional heat may be provided by a cathode exhaust gas (or other high temperature gas)heat exchanging section 816. For example, flowrestrictor 814 may be able to maintain a fluid-tight connection at temperatures of at least 650 degrees Celsius, 700 degrees Celsius, 800 degrees Celsius, 850 degrees Celsius, 900 degrees Celsius, or 950 degrees Celsius. - While preferred embodiments of the present subject matter have been described, it is to be understood that the embodiments described are illustrative only and that the scope of the subject matter is to be defined solely by the appended claims when accorded a full range of equivalence, many variations and modifications naturally occurring to those of skill in the art from a perusal hereof.
Claims (20)
1. In a fuel cell system comprising:
a source of a hydrocarbon fuel;
a reformer for receiving the hydrocarbon fuel and converting the hydrocarbon fuel to reformate; and
a fuel cell stack having an anode inlet for receiving a mixture of the reformate and the hydrocarbon fuel,
a method of controlling the volumetric ratio of the reformate and hydrocarbon fuel in the mixture comprising:
providing a flow path for fuel to bypass the reformer;
controlling the flow rate of fuel within the flow path; and
combining the fuel flowing through the bypass flow path with the reformate.
2. The method of claim 1 further comprising:
removing higher hydrocarbons from the hydrocarbon fuel
3. The method of claim 1 further comprising:
heating the fuel bypassing the reformer prior to combining the fuel.
4. The method of claim 3 , wherein the heating results from a transfer of heat from a cathode exhaust gas.
5. The method of claim 1 , wherein at least a portion of the fuel comprises an anode exhaust gas.
6. In a fuel cell system configured for internal reforming of a hydrocarbon fuel in the fuel cell stack, a method of operation comprising:
supplying a hydrocarbon fuel to the system;
feeding a portion of the hydrocarbon fuel to a reformer to thereby convert the fuel to reformate;
bypassing a second portion of the hydrocarbon fuel around the reformer;
combining the bypassed hydrocarbon fuel with the reformate at a selected feed rate;
supplying the combined reformate and hydrocarbon fuel to an anode inlet of the fuel cell stack; and
controlling the volumetric ratio of the combined reformate and hydrocarbon fuel supplied to the anode inlet of the fuel cell stack by selecting the feed rate of the bypassed hydrocarbon fuel.
7. The method of claim 6 further comprising heating the reformate and the bypassed fuel by transferring heat from a gas supplied from a cathode exhaust of the fuel cell stack.
8. The method of claim 7 further comprising coating at least a portion of the surfaces exposed to the bypassed fuel with a ceramic material to thereby inhibit carbon formation on the coated surfaces.
9. A fuel cell system comprising:
a fuel cell stack configured for internal reforming of a hydrocarbon fuel, said fuel cell stack comprising:
an anode portion in fluid communication with an anode inlet and an anode exhaust;
a cathode portion in fluid communication with a cathode inlet and a cathode exhaust;
a source of hydrocarbon fuel;
a reformer unit for converting hydrocarbon fuel to reformate, said reformer unit comprising:
one or more cold-side channels for providing a reforming passage for fuel through said reformer unit;
a fuel supply conduit in fluid communication with said fuel source and said cold-side channels;
a reformate exhaust conduit in fluid communication with said cold-side channels and said anode inlet;
one or more hot-side channels for providing a passage for a cathode exhaust gas through said reforming unit, said hot-side channels being in sufficient proximity to said cold-side channels to effect heat transfer between the fluids flowing through the respective channels;
a cathode exhaust conduit in fluid communication with said cathode exhaust and said hot-side channels;
a cathode inlet conduit in fluid communication with said hot-side channels and said cathode inlet;
one or more bypass channels for providing a non-reforming passage for fuel through said reformer unit, said bypass channels being in fluid communication with said fuel supply conduit and said reformate exhaust conduit to thereby combine the non-reformed fuel with the reformate; and
a flow controller for controlling the flow rate of fuel flowing through said bypass channels.
10. The system of claim 9 , wherein said bypass channels is in sufficient proximity to said hot-side channels to effect heat transfer between the fluids flowing through the respective channel.
11. The system of claim 9 , wherein said bypass channels is in sufficient proximity to said cathode inlet conduit to effect heat transfer between the fluids flowing through the respective channel.
12. The system of claim 11 , wherein said bypass channel is a line which passes through said cathode inlet conduit, wherein said amount of heat transferred from the fluid in the cathode inlet conduit to the non-reformed fuel in the bypass channel is determined at least in part by the length of the bypass channel line disposed in the cathode inlet conduit.
13. The system of claim 9 , wherein said bypass channel is lined with a ceramic coating to inhibit carbon formation.
14. The system of claim 9 , further comprising a higher hydrocarbon reduction unit.
15. The system of claim 9 , further comprising a combustor.
16. The system of claim 9 , wherein the reformer unit is a steam reformer.
17. The system of claim 16 , wherein said reformer unit comprises a catalyst containing at least one Group VIII metal.
18. The system of claim 17 , wherein the at least one Group VIII metal comprises 0.1 to 40 wt % of said catalyst.
19. The system of claim 17 , wherein said catalyst further comprises one or more promoter elements selected from a group containing elements from Groups IIa-VIIa, elements Groups Ib-Vb, lanthanide series, and actinide series.
20. The system of claim 17 , wherein said promoter element comprises 0.01 to 10 wt % of the catalyst.
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US15/389,617 US20180115002A1 (en) | 2016-10-25 | 2016-12-23 | Reformer With Bypass For Internal Fuel Cell Reforming |
PCT/US2017/056606 WO2018080809A1 (en) | 2016-10-25 | 2017-10-13 | Reformer with bypass for internal fuel cell reforming |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US15/333,255 US10164277B2 (en) | 2016-10-25 | 2016-10-25 | Steam reformer bypass line and flow controller |
US15/389,617 US20180115002A1 (en) | 2016-10-25 | 2016-12-23 | Reformer With Bypass For Internal Fuel Cell Reforming |
Related Parent Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US15/333,255 Continuation US10164277B2 (en) | 2016-10-25 | 2016-10-25 | Steam reformer bypass line and flow controller |
Publications (1)
Publication Number | Publication Date |
---|---|
US20180115002A1 true US20180115002A1 (en) | 2018-04-26 |
Family
ID=61970517
Family Applications (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US15/333,255 Expired - Fee Related US10164277B2 (en) | 2016-10-25 | 2016-10-25 | Steam reformer bypass line and flow controller |
US15/389,617 Abandoned US20180115002A1 (en) | 2016-10-25 | 2016-12-23 | Reformer With Bypass For Internal Fuel Cell Reforming |
Family Applications Before (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US15/333,255 Expired - Fee Related US10164277B2 (en) | 2016-10-25 | 2016-10-25 | Steam reformer bypass line and flow controller |
Country Status (2)
Country | Link |
---|---|
US (2) | US10164277B2 (en) |
WO (2) | WO2018080809A1 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US11637300B2 (en) * | 2019-03-14 | 2023-04-25 | Honeywell International Inc. | Fuel cell based power generator |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP6670480B2 (en) * | 2017-02-23 | 2020-03-25 | トヨタ自動車株式会社 | Fuel cell vehicle |
CN110429301B (en) * | 2019-06-28 | 2021-04-16 | 潍柴动力股份有限公司 | High-temperature air mixer and SOFC air inlet system |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20020182132A1 (en) * | 2000-10-04 | 2002-12-05 | Lesieur Roger R. | Fuel gas reformer assemblage |
US20080102328A1 (en) * | 2005-03-08 | 2008-05-01 | Saunders Gary J | Fuel Processor for a Fuel Cell Arrangement and a Method of Operating a Fuel Processor for a Fuel Cell Arrangement |
US20100047641A1 (en) * | 2008-08-19 | 2010-02-25 | Jahnke Fred C | High-efficiency dual-stack molten carbonate fuel cell system |
Family Cites Families (25)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3462306A (en) | 1964-11-06 | 1969-08-19 | Eindhoven Tech Hogeschool | High temperature fuel cell |
US4374184A (en) | 1981-09-29 | 1983-02-15 | Westinghouse Electric Corp. | Fuel cell generator and method of operating same |
US4516606A (en) | 1983-02-16 | 1985-05-14 | Exxon Research And Engineering Co. | Variable orifice valve assembly |
JPH0831322B2 (en) | 1989-09-20 | 1996-03-27 | 株式会社日立製作所 | Internal reforming fuel cell and power plant using the same |
GB9403198D0 (en) | 1994-02-19 | 1994-04-13 | Rolls Royce Plc | A solid oxide fuel cell stack |
US6126908A (en) | 1996-08-26 | 2000-10-03 | Arthur D. Little, Inc. | Method and apparatus for converting hydrocarbon fuel into hydrogen gas and carbon dioxide |
AUPS087502A0 (en) | 2002-03-04 | 2002-03-28 | Ceramic Fuel Cells Limited | Solid oxide fuel cell |
US6923203B2 (en) | 2003-05-29 | 2005-08-02 | Rickey E. Wark | Variable orifice valve for airstream containing particulate coal |
US7732084B2 (en) | 2004-02-04 | 2010-06-08 | General Electric Company | Solid oxide fuel cell with internal reforming, catalyzed interconnect for use therewith, and methods |
US7638226B2 (en) | 2004-07-13 | 2009-12-29 | Ford Motor Company | Apparatus and method for controlling kinetic rates for internal reforming of fuel in solid oxide fuel cells |
US20060057444A1 (en) | 2004-09-13 | 2006-03-16 | Ebara Ballard Corporation | Fuel processing apparatus and method and fuel cell power generation system |
JP5072200B2 (en) | 2005-07-01 | 2012-11-14 | 独立行政法人科学技術振興機構 | Methane steam reforming catalyst, method for producing the same, and method for producing hydrogen using the same |
US20070154745A1 (en) | 2005-12-29 | 2007-07-05 | Michael Penev | Purging a fuel cell system |
US8067122B2 (en) | 2006-04-19 | 2011-11-29 | Panasonic Corporation | Fuel cell system |
US8216738B2 (en) | 2006-05-25 | 2012-07-10 | Versa Power Systems, Ltd. | Deactivation of SOFC anode substrate for direct internal reforming |
US8435683B2 (en) | 2007-07-19 | 2013-05-07 | Cp Sofc Ip, Llc | Internal reforming solid oxide fuel cells |
US8141524B2 (en) | 2008-12-15 | 2012-03-27 | Caterpillar Inc. | Cooling system having variable orifice plates |
US8617763B2 (en) | 2009-08-12 | 2013-12-31 | Bloom Energy Corporation | Internal reforming anode for solid oxide fuel cells |
DE102009060679A1 (en) | 2009-12-28 | 2011-06-30 | J. Eberspächer GmbH & Co. KG, 73730 | Operating method for a fuel cell system |
KR101237735B1 (en) | 2010-06-14 | 2013-02-26 | 포항공과대학교 산학협력단 | Internal Reforming Tubular Type Solid Oxide Fuel Cell Stacks and their Manufacturing Methods |
JP5833122B2 (en) | 2010-08-17 | 2015-12-16 | ブルーム エナジー コーポレーション | Method for producing solid oxide fuel cell |
KR101222782B1 (en) | 2010-09-02 | 2013-01-15 | 삼성전기주식회사 | Solid oxide fuel cell |
GB2513138B (en) | 2013-04-16 | 2019-09-04 | Intelligent Energy Ltd | Modular fuel cell and fuel source |
GB201312329D0 (en) | 2013-07-09 | 2013-08-21 | Ceres Ip Co Ltd | Improved fuel cell systems and methods |
WO2015069749A2 (en) | 2013-11-06 | 2015-05-14 | Watt Fuel Cell Corp. | Liquid fuel cpox reformers and methods of cpox reforming |
-
2016
- 2016-10-25 US US15/333,255 patent/US10164277B2/en not_active Expired - Fee Related
- 2016-12-23 US US15/389,617 patent/US20180115002A1/en not_active Abandoned
-
2017
- 2017-10-13 WO PCT/US2017/056606 patent/WO2018080809A1/en active Application Filing
- 2017-10-13 WO PCT/US2017/056605 patent/WO2018080808A1/en active Application Filing
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20020182132A1 (en) * | 2000-10-04 | 2002-12-05 | Lesieur Roger R. | Fuel gas reformer assemblage |
US20080102328A1 (en) * | 2005-03-08 | 2008-05-01 | Saunders Gary J | Fuel Processor for a Fuel Cell Arrangement and a Method of Operating a Fuel Processor for a Fuel Cell Arrangement |
US20100047641A1 (en) * | 2008-08-19 | 2010-02-25 | Jahnke Fred C | High-efficiency dual-stack molten carbonate fuel cell system |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US11637300B2 (en) * | 2019-03-14 | 2023-04-25 | Honeywell International Inc. | Fuel cell based power generator |
US20230187670A1 (en) * | 2019-03-14 | 2023-06-15 | Honeywell International Inc. | Fuel cell based power generator |
Also Published As
Publication number | Publication date |
---|---|
US10164277B2 (en) | 2018-12-25 |
WO2018080808A1 (en) | 2018-05-03 |
WO2018080809A1 (en) | 2018-05-03 |
US20180115001A1 (en) | 2018-04-26 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US20090280364A1 (en) | Fuel cell system and method of operating same | |
US8227126B2 (en) | Fuel cell system | |
US10686204B2 (en) | Solid oxide fuel cell system | |
EP2842190B1 (en) | Fuel cell module with heat exchanger | |
US10164277B2 (en) | Steam reformer bypass line and flow controller | |
US10158135B2 (en) | Steam reformer bypass plenum and flow controller | |
WO2021153627A1 (en) | Fuel battery power generating system | |
KR102473472B1 (en) | Multi-reformable fuel delivery systems and methods for fuel cells | |
US8956777B2 (en) | Solid oxide fuel cell power plant having a fixed contact oxidation catalyzed section of a multi-section cathode air heat exchanger | |
JP5150068B2 (en) | Reformer and indirect internal reforming type solid oxide fuel cell | |
WO2021171882A1 (en) | Fuel cell system and control method therefor | |
US10340534B2 (en) | Revised fuel cell cycle for in block reforming fuel cells | |
US20230024739A1 (en) | Fuel cell systems and method | |
KR101395049B1 (en) | Fuel supplying system, air supplying system for a fuel cell stack module and fuel cell system comprising the same | |
US10381669B2 (en) | Steam reformer for in-block fuel cell reforming | |
US11742498B1 (en) | Thermal management of a solid oxide fuel cell system | |
US20220407096A1 (en) | Fuel cell system and method for controlling same | |
TW202335339A (en) | Fuel cell system including fuel exhaust processor and method of operating the same | |
CN116231009A (en) | Solid oxide fuel cell stack system and operation control method and application thereof | |
KR20130022634A (en) | Gaseous fuel supply device of fuel cell system and fuel cell system including the same |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: LG FUEL CELL SYSTEMS INC., OHIO Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:CUNNINGHAM, ROBERT;DEAN, ERIC;JENNINGS, MICHAEL;REEL/FRAME:041369/0964 Effective date: 20170120 |
|
STPP | Information on status: patent application and granting procedure in general |
Free format text: RESPONSE TO NON-FINAL OFFICE ACTION ENTERED AND FORWARDED TO EXAMINER |
|
STPP | Information on status: patent application and granting procedure in general |
Free format text: FINAL REJECTION MAILED |
|
STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |