WO2018044236A1 - Cadre d'écoulement destiné à des cellules électrochimiques - Google Patents

Cadre d'écoulement destiné à des cellules électrochimiques Download PDF

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Publication number
WO2018044236A1
WO2018044236A1 PCT/SG2017/050431 SG2017050431W WO2018044236A1 WO 2018044236 A1 WO2018044236 A1 WO 2018044236A1 SG 2017050431 W SG2017050431 W SG 2017050431W WO 2018044236 A1 WO2018044236 A1 WO 2018044236A1
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WO
WIPO (PCT)
Prior art keywords
contact
electrode
flow
support beams
major surface
Prior art date
Application number
PCT/SG2017/050431
Other languages
English (en)
Inventor
Lijun Liu
Ningping CHEN
Chun Yu LING
Ming Han
Mei Lin Chng
Original Assignee
Temasek Polytechnic
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Temasek Polytechnic filed Critical Temasek Polytechnic
Priority to CN201780053237.8A priority Critical patent/CN109643814A/zh
Publication of WO2018044236A1 publication Critical patent/WO2018044236A1/fr

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Classifications

    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/10—Fuel cells with solid electrolytes
    • H01M8/1004—Fuel cells with solid electrolytes characterised by membrane-electrode assemblies [MEA]
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M4/00—Electrodes
    • H01M4/86—Inert electrodes with catalytic activity, e.g. for fuel cells
    • H01M4/8605—Porous electrodes
    • H01M4/8626—Porous electrodes characterised by the form
    • H01M4/8631—Bipolar electrodes
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M4/00—Electrodes
    • H01M4/86—Inert electrodes with catalytic activity, e.g. for fuel cells
    • H01M4/96—Carbon-based electrodes
    • 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
    • H01M8/24—Grouping of fuel cells, e.g. stacking of fuel cells
    • H01M8/241—Grouping of fuel cells, e.g. stacking of fuel cells with solid or matrix-supported electrolytes
    • H01M8/242—Grouping of fuel cells, e.g. stacking of fuel cells with solid or matrix-supported electrolytes comprising framed electrodes or intermediary frame-like gaskets
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells

Definitions

  • the present invention relates broadly, but not exclusively, to a flow frame for electrochemical cells.
  • An example of a grid-level energy storage device is a flow battery, in which energy is stored externally in a charged electrolyte.
  • a flow battery should ideally consume as little energy as possible.
  • the relatively fast kinetics of redox couples allow high columbic and voltage efficiencies to be obtained, but the values of these efficiencies also depend on internal ohmic resistance (IOR) of the flow battery.
  • Electrodes and bipolar plates are the key components of a flow battery. The performance of a flow battery heavily depends on the bulk resistance of the electrode, the bipolar plate and the contact resistance between them (which is the main contributor to the IOR).
  • the conventional electrode-bipolar plate setup includes pressed-contacted carbon felts on impermeable graphite plates (i.e., the carbon felt electrode comes into contact with the impermeable graphite bipolar plate by assembly compression force).
  • the assembly compression force is too high, the carbon felt electrode is overly compressed which results in high electrolyte flow resistance.
  • the assembly compression force is too weak, the contact resistance between the carbon felt electrode and the bipolar plate is large.
  • the electrolyte is directly supplied into the electrode from one lateral side but in-plane concentration distribution is not uniform, leading to mass transport polarization in regions away from the inlet.
  • Another type of electrochemical device, fuel cells are capable of converting energy of a chemical reaction into electrical energy without combustion and virtually without pollution. The efficiency of a fuel cell is generally better than combustion-type devices. Fuel cells can produce non-stop power regardless of weather conditions (unlike some forms of renewable energy) and require less maintenance. As long as there is a supply of fuel, fuel cells can constantly supply power. As such, fuel cells are suitable for a wide range of applications including standby power, off-grid CCTV surveillance and security applications, etc.
  • PEMFCs Proton exchange membrane fuel cells
  • DMFCs direct methanol fuel cell
  • DMFCs do not have the fuel storage problems typically present for other types of fuel cells.
  • methanol is easier to transport and supply to the public using existing infrastructure because of its liquid state.
  • methanol has a high volumetric energy density which allows for extremely compact power systems.
  • DMFCs are a promising battery replacement for portable applications and small-scale devices where long runtimes are desired.
  • a major technical barrier of DMFCs for further performance enhancement is sluggish methanol oxidation at the anode.
  • a flow frame for an electrochemical cell including: a frame body including a plurality of elongate members that are arranged to define a boundary of the flow frame and to allow an electrolyte solution to flow within the boundary of the flow frame; and one or more support beams disposed within the frame body and coupled to at least two of the plurality of elongate members.
  • Each of the one or more support beams may be disposed within the frame body in an orientation that is based on a direction of flow of the electrolyte solution.
  • each of the one or more support beams may be oriented substantially perpendicular to the direction of flow of the electrolyte solution.
  • the plurality of elongate members may be arranged to accommodate an electrode within the boundary of the flow frame such that at least a portion of the electrode is in contact with the one or more support beams.
  • the electrode may include compressible porous carbon felt to allow the electrolyte solution to flow through the electrode, and the one or more support beams may be configured to reduce a porosity of the compressible porous carbon felt adjacent the portion of the electrode that is in contact with the one or more support beams.
  • an electrode-bipolar plate module for an electrochemical cell including: the flow frame as described herein; an electrode that is disposed within the boundary of the flow frame such that at least a portion of the electrode is in contact with the one or more support beams; and a bipolar plate that is in contact with the electrode.
  • a cell module for a flow battery including: an ion conductive membrane including a first major surface and a second major surface opposite the first major surface; a first electrode-bipolar plate module as described herein, wherein the flow frame of the first electrode-bipolar plate module is in contact with the first major surface; and a second electrode-bipolar plate module as described herein, wherein the flow frame of the second electrode-bipolar plate module is in contact with the second major surface.
  • a flow battery stack including: a plurality of the cell modules as described herein, wherein the plurality of the cell modules are stacked together such that each cell module is in contact with an adjacent cell module; a first monopolar plate that is in contact with a first end of the stack of cell modules and a second monopolar plate that is in contact with a second end of the stack of cell modules; a first current collector that is in contact with the first monopolar plate and a second current collector that is in contact with the second monopolar plate; and a first end plate that is in contact with the first current collector and a second end plate that is in contact with the second current collector.
  • a cell module for a fuel cell including: an ion conductive membrane including a first major surface and a second major surface opposite the first major surface; the electrode-bipolar plate module as described herein, wherein the flow frame of the electrode-bipolar plate module is in contact with the first major surface; an air electrode that is in contact with the second major surface; an air diffusion layer that is in contact with the air electrode; and an additional bipolar plate that is in contact with the air diffusion layer.
  • a fuel cell stack including: a plurality of the cell modules as described herein, wherein the plurality of the cell modules are stacked together such that each cell module is in contact with an adjacent cell module; a first monopolar plate that is in contact with a first end of the stack of cell modules and a second monopolar plate that is in contact with a second end of the stack of cell modules; a first current collector that is in contact with the first monopolar plate and a second current collector that is in contact with the second monopolar plate; and a first end plate that is in contact with the first current collector and a second end plate that is in contact with the second current collector.
  • a method of fabricating a flow frame for an electrochemical cell including: providing a frame body including a plurality of elongate members such that the plurality of elongate members define a boundary of the flow frame and allow an electrolyte solution to flow within the boundary of the flow frame; and disposing one or more support beams within the frame body by coupling the one or more support beams to at least two of the plurality of elongate members.
  • the method may further include arranging the plurality of elongate members to accommodate an electrode within the boundary of the flow frame such that at least a portion of the electrode is in contact with the one or more support beams.
  • the electrode may include compressible porous carbon felt to allow the electrolyte solution to flow through the electrode, and the one or more support beams may be configured to reduce a porosity of the compressible porous carbon felt adjacent the portion of the electrode that is in contact with the one or more support beams.
  • a method of fabricating an electrode-bipolar plate module for an electrochemical cell including: providing a flow frame that has been fabricated according to the method described herein; disposing an electrode within the boundary of the flow frame such that at least a portion of the electrode is in contact with the one or more support beams; and disposing a bipolar plate to be in contact with the electrode.
  • a method of fabricating a cell module for a flow battery including: providing an ion conductive membrane including a first major surface and a second major surface opposite the first major surface; providing a first electrode-bipolar plate module that has been fabricated according to the method described herein; disposing the flow frame of the first electrode-bipolar plate module to be in contact with the first major surface; providing a second electrode- bipolar plate module that has been fabricated according to the method described herein; and disposing the flow frame of the second electrode-bipolar plate module to be in contact with the second major surface.
  • a method of fabricating a flow battery stack including: providing a plurality of the cell modules that have been fabricated according to the method described herein; stacking the plurality of the cell modules together such that each cell module is in contact with an adjacent cell module; providing a first monopolar plate that is in contact with a first end of the stack of cell modules and a second monopolar plate that is in contact with a second end of the stack of cell modules; providing a first current collector that is in contact with the first monopolar plate and a second current collector that is in contact with the second monopolar plate; and providing a first end plate that is in contact with the first current collector and a second end plate that is in contact with the second current collector.
  • a method of fabricating a cell module for a fuel cell including: providing an ion conductive membrane including a first major surface and a second major surface opposite the first major surface; providing an electrode-bipolar plate module that has been fabricated according to the method described herein; disposing the flow frame of the electrode-bipolar plate module to be in contact with the first major surface; providing an air electrode that is in contact with the second major surface; providing an air diffusion layer that is in contact with the air electrode; and providing an additional bipolar plate that is in contact with the air diffusion layer.
  • a method of fabricating a fuel cell stack including: providing a plurality of the cell modules that have been fabricated according to the method described herein; stacking the plurality of the cell modules together such that each cell module is in contact with an adjacent cell module; providing a first monopolar plate that is in contact with a first end of the stack of cell modules and a second monopolar plate that is in contact with a second end of the stack of cell modules; providing a first current collector that is in contact with the first monopolar plate and a second current collector that is in contact with the second monopolar plate; and providing a first end plate that is in contact with the first current collector and a second end plate that is in contact with the second current collector.
  • Figure 1 A is a schematic view of a flow frame with two support beams, according to an example embodiment.
  • Figure 1 B is a schematic view of a flow frame with three support beams, according to an example embodiment.
  • Figure 1 C is a cross-sectional view of a flow frame with support beams, according to an example embodiment.
  • Figure 2 is a plan view of a flow route of an electrolyte solution in a flow frame without support beams.
  • Figure 3 is a plan view of a flow route of an electrolyte solution in a flow frame with two support beams, according to an example embodiment.
  • Figure 4 is a plan view of a flow route of an electrolyte solution in a flow frame with three support beams, according to an example embodiment.
  • Figure 5 is a side view of a flow route of an electrolyte solution in a flow frame with two support beams, according to an example embodiment.
  • Figure 6 is a graph showing the effect of support beams on contact resistance between an electrode and a bipolar plate.
  • Figure 7 is a graph showing the effect of support beams on flow rate.
  • Figure 8 is an exploded view of an electrode-bipolar plate module in a flow battery with an external flow manifold, according to an example embodiment.
  • Figure 9 is an exploded view of a single flow cell module with an external flow manifold, according to an example embodiment.
  • Figure 10 is an exploded view of a flow battery stack with an external flow manifold, according to an example embodiment.
  • Figure 1 1 is a schematic side view of a flow battery stack with an external flow manifold, according to an example embodiment, according to an example embodiment.
  • Figure 12 is an exploded view of a single flow cell module with an internal flow manifold, according to an example embodiment.
  • Figure 13 is an exploded view of a single fuel cell module, according to an example embodiment.
  • Figure 14 is an exploded view of a fuel cell stack, according to an example embodiment.
  • Embodiments of the invention generally relate to flow battery and fuel cell technology, in particular, flow frames for electrochemical cells. Embodiments are suitable for flow batteries and fuel cell systems used in large scale energy storage, as well as backup power or independent power systems. [0045] One particular embodiment relates to an electrode-bipolar plate assembly that seeks to reduce bulk resistance with no significant increase of flow resistance, achieve uniform flow field and improve overall system efficiency.
  • DMFCs are currently constructed using a 2 dimensional electrode.
  • a 3 dimensional electrode instead to significantly increase the effective active area and improve the net kinetics in DMFCs.
  • embodiments of the invention seek to provide a novel anodic architecture using flow frames with support beams and carbon felt electrode materials to increase the effective active area, reduce bulk resistance and achieve substantially uniform flow field in each cell. This can advantageously reduce anodic over-potential and increase overall performance for high endurance, safety, and lower cost.
  • a flow frame for use in an electrochemical cell (such as a flow battery or a fuel cell).
  • the flow frame includes a frame body and the flow frame is preferably a symmetric structure.
  • the frame body comprises a plurality of elongate members that are arranged to define a boundary of the flow frame and to allow an electrolyte solution to flow within the boundary of the flow frame.
  • the flow frame also includes one or more support beams disposed within the frame body (i.e. the boundary of the flow frame) and coupled to at least two of the plurality of elongate members.
  • the support beam(s) are coupled to at least two of the plurality of elongate members, the support beam(s) can provide structural support for the frame body (e.g. by preventing deformation of the frame body during cell stack assembly).
  • Each of the one or more support beams are disposed within the frame body in an orientation that is based on a direction of flow of the electrolyte solution.
  • each of the one or more support beams is oriented substantially perpendicular to the flow / circulation direction of the electrolyte solution.
  • each of the one or more support beams is disposed within the frame body at an angle of about 90 degrees to 70 degrees with respect to the flow / circulation direction of the electrolyte.
  • the plurality of elongate members are arranged to accommodate an electrode within the boundary of the flow frame such that at least a portion of the electrode is in contact with the one or more support beams.
  • the electrode may be substantially planar and can be completely disposed within the frame body.
  • An impermeable graphite bipolar plate is disposed over the electrode and a compressive force may be applied on the bipolar plate.
  • the electrode comprises compressible porous carbon felt to allow the electrolyte solution to flow through the electrode.
  • the one or more support beams is configured to reduce a porosity of the compressible porous carbon felt adjacent the portion of the electrode that is in contact with the one or more support beams.
  • the compressible porous carbon felt electrode is compressed to a greater extent at portions that are in contact with the support beam(s). This causes a difference in porosity between regions of the electrode that are in contact with the one or more support beams and regions of the electrode that are not in contact with the one or more support beams.
  • a flow resistance is relatively higher at regions of the electrode that are in contact with the one or more support beams compared to the flow resistance at regions of the electrode that are not in contact with the one or more support beams.
  • the changes in flow resistance due to the one or more support beams cause the electrolyte solution to flow sideways of the one or more support beams before flowing over the one or more support beams and result in a more uniform flow distribution of the electrolyte solution.
  • a width of each of the one or more support beams is around 1 /30 to 1/6 of a length of the electrode.
  • the width of each support beam is around 1 /20 to 1 /10 of the length of the electrode.
  • the thickness of each support beam is around 1 /10 to 3/5 of the thickness of the electrode.
  • a thickness of each of the one or more support beams is around 0.5 to 5 mm, and preferably about 1 to 3 mm.
  • Each of the support beams can be made of conductive or non-conductive materials.
  • the flow frame with support beams can advantageously reduce bulk resistance with no significant increase in flow resistance while providing a more uniform flow distribution of electrolyte, thus improving overall system efficiency. Moreover, the flow frame with support beams can reduce contact resistance between an electrode and a bipolar plate in a cell unit.
  • FIGS 1 A and 1 B are schematic views of a flow frame with a plurality of support beams, according to an example embodiment.
  • flow frame 102a has two support beams 104a / 104b.
  • flow frame 102b has three support beams 104c / 104d / 104e.
  • the flow frame 102a / 102b is preferably a symmetric structure, comprising a square or rectangle frame body 106 / 106' with a plurality of support beams 104a / 104b / 104c / 104d / 104e.
  • Figure 1 C is a cross- sectional view of a flow frame 102b with a frame body 106' and three support beams 104c / 104d / 104e, according to an example embodiment.
  • Figures 1 A and 1 B show two and three support beams respectively, embodiments can comprises one support beam or more than three support beams depending on particular applications and operational requirements.
  • the support beams 104a / 104b / 104c / 104d / 104e are disposed within the flow frame 102a / 102b and can be oriented based on a flow path of an electrolyte solution. As shown in Figures 1 A and 1 B, the support beams 104a / 104b / 104c / 104d / 104e can be oriented horizontally with respect to the base of the frame body 106a / 106c such that the support beams 104a / 104b / 104c / 104d / 104e are substantially parallel with the base of the frame body 106a / 106c.
  • each support beam 104a / 104b / 104c / 104d / 104e can be from 1 mm to 10mm.
  • the thickness of each support beam 104a / 104b / 104c / 104d / 104e can be from 0.5mm to 5mm.
  • the electrolyte solution flows in a direction from the base of the frame body 106a / 106c to the top of the frame body 106b / 106d.
  • Figure 2 is a plan view of a flow route of an electrolyte solution 208 in a flow frame 202 without support beams, as known in the art.
  • Figure 3 is a plan view of a flow route of an electrolyte solution 308 in a flow frame 302 with two support beams 304a / 304b, according to an example embodiment.
  • Figure 4 is a plan view of a flow route of an electrolyte solution 408 in a flow frame 402 with three support beams 404a / 404b / 404c, according to an example embodiment.
  • Figure 5 is a side view of a flow route of an electrolyte solution in a flow frame 502 with two support beams 504a / 504b, according to an example embodiment.
  • the support beams 504a / 504b are configured to reduce a porosity of the compressible porous carbon felt adjacent the portion of the electrode that is in contact with the support beams 504a / 504b (i.e. regions 590a / 590b).
  • the compressible porous carbon felt electrode is compressed to a greater extent at portions that are in contact with the support beams 504a / 504b (i.e. regions 590a / 590b). This causes a difference in porosity between regions of the electrode that are in contact with the support beams (i.e. regions 590a / 590b) and regions of the electrode that are not in contact with the support beams.
  • a flow resistance is relatively higher at regions of the electrode that are in contact with the support beams (i.e. regions 590a / 590b) compared to the flow resistance at regions of the electrode that are not in contact with the support beams.
  • the changes in flow resistance due to the support beams 504a / 504b cause the electrolyte solution to flow sideways of the support beams 504a / 504b before flowing over the support beams 504a / 504b and result in a more uniform flow distribution of the electrolyte solution.
  • a flow frame with support beam(s) may advantageously allow lower compression rates and reduce the bulk resistance at the same time.
  • Figure 6 is a graph showing the effect of support beams on contact resistance between an electrode and a bipolar plate.
  • the contact resistance using a flow frame with two support beams reduces significantly compared to a flow frame without support beams, especially at low compression rates, e.g., 27% drop at 10% compression rate. This illustrates that relatively lower contact resistance at low compression rates can be achieved with a flow frame with support beam(s) according to embodiments of the invention.
  • the flow rates of an electrolyte solution within a flow frame with/without support beams were measured under a specific pump voltage.
  • FIG 8 is an exploded view of an electrode-bipolar plate module 800 in a flow battery with an external flow manifold, according to an example embodiment.
  • the electrode-bipolar plate module 800 comprises: a flow frame 802 with two support beams 804a / 804b that are disposed within a boundary of the flow frame 802; a carbon felt electrode 810; and a bipolar plate 812.
  • a first side of the electrode 810 is connected to the flow frame 802 while a second side of the electrode 810 (opposite the first side) is connected to the bipolar plate 812.
  • the electrode 810 is constrained within the boundary of the flow frame 802 with support beams 804a / 804b to form an active reaction compartment.
  • An electrolyte solution flows through this active reaction compartment.
  • the electrolyte solution can enter the flow frame 802 from inlet port A1 and exit the flow frame 802 from outlet port A2.
  • An electrochemical flow cell module can be formed by stacking a plurality of bipolar plate modules (such as electrode-bipolar plate module 800) and ion exchange membranes.
  • Figure 9 is an exploded view of a single flow cell module 900 with an external flow manifold, according to an example embodiment.
  • an ion conductive membrane 920 is sandwiched between two adjacent electrode-bipolar plate modules 800 / 800'.
  • FIG. 10 is an exploded view of a flow battery stack 1000 with an external flow manifold, according to an example embodiment.
  • the central part 1050 of the flow battery stack 1000 comprises a plurality of electrode-bipolar plate modules (such as electrode-bipolar plate module 800).
  • Each electrode-bipolar plate module 800 has two functions - one side functions as the anode of one single cell while the opposite side functions as the cathode of an adjacent single cell.
  • the functional requirement is different since no electrode function is needed at the outermost sides. Therefore a pair of monopolar plates is used.
  • the structure of a monopolar plate is similar to the structure of a bipolar plate except that one side of the active reaction compartment is omitted.
  • a pair of current collectors 1040a / 1040b is located on both sides of the active region and a pair of end plates 1042a / 1042b is located at the outermost side.
  • the current collectors 1040a / 1040b are made from electrically conductive materials such as copper, gold or alloys thereof.
  • the end plates 1042a / 1042b can be made from metal, plastic or composites in order to provide necessary strength to hold the stack together.
  • a resistance coating or other suitable means can be used to ensure good electrical insulation between the current collectors 1040a / 1040b and end plates 1042a / 1042b.
  • FIG. 1 1 is a schematic side view of a flow battery stack 1 100 with an external flow manifold, according to an example embodiment, according to an example embodiment.
  • the flow battery stack 1000 / 1 100 comprises: a plurality of bipolar plate modules stacked together; a pair of mono-polar plate modules located at both ends of the stacking of the plurality of bipolar plate modules; a pair of current collectors sandwiching the stacking and the mono-polar plates; and a pair of end plates at the outermost sides.
  • FIG. 12 is an exploded view of a single flow cell module 1200 with an internal flow manifold, according to an example embodiment.
  • the structure of the single flow cell module 1200 with an internal flow manifold is substantially the same as the single flow cell module 900 with an external flow manifold as shown in Figure 9.
  • An ion conductive membrane 1220 is sandwiched between two adjacent electrode-bipolar plate modules 1201 a / 1201 b.
  • a first active reaction compartment containing a first electrolyte is attached to the first major surface of the ion conductive membrane 1220, while a second active reaction compartment containing a second electrolyte is attached to the second major surface (opposite the first major surface) of the ion conductive membrane 1220.
  • flow frame 1202a may comprise an inlet manifold B1 for a positive electrolyte to flow, an outlet manifold B2 for the positive electrolyte to flow, an inlet manifold C1 for a negative electrolyte to flow, and an outlet manifold C2 for the negative electrolyte to flow.
  • Flow frame 1202b may comprise a manifold B3 for a positive electrolyte to flow, a manifold B4 for the positive electrolyte to flow, a manifold C3 for a negative electrolyte to flow, and a manifold C4 for the negative electrolyte to flow.
  • four manifold systems are present in the single flow cell module 1200, namely (B1 +B3), (C1 +C3), (B2+B4), and (C2+C4).
  • the positive electrolyte may pass through manifold B3 and flow into the flow frame 1202a via inlet manifold B1 .
  • the positive electrolyte exits the flow frame 1202a via outlet manifold B2 and enters manifold B4.
  • the negative electrolyte flows in a similar manner, i.e. passing through manifold C1 into C3, through flow frame 1202b and exiting via C4 then C2.
  • FIG. 13 is an exploded view of a single fuel cell module 1300, according to an example embodiment.
  • the single fuel cell module 1300 includes an ion conductive membrane 1320 that is sandwiched between an anodic electrode 1301 a and a cathodic electrode 1301 b.
  • the anodic electrode 1301 a comprises a carbon felt electrode 1310, a flow frame 1302 with support beams 1304a / 1304b, and a bipolar plate 1312.
  • connectors D1 and D2 may be added to the inlet port A1 and the outlet port A2 respectively to facilitate the use of tubings if required.
  • the carbon felt electrode 1310 is connected to the support beams 1304a / 1304b and another side is connected to the bipolar plate 1312.
  • the carbon felt electrode 1310 is constrained within the flow frame 1302 with support beams 1304a / 1304b, forming an active reaction compartment.
  • the electrolyte solution flows through this active reaction compartment.
  • the cathodic electrode 1301 b comprises an air electrode 1360, an air diffusion layer 1362 and a bipolar plate 1364.
  • a first major surface of the air electrode 1360 is connected to the ion conductive membrane 1320, and a second major surface (opposite the first major surface) of the air electrode 1360 is connected to a first major surface of the air diffusion layer 1362.
  • the second major surface (opposite the first major surface) of the air diffusion layer 1362 is connected to the bipolar plate 1364.
  • FIG 14 is an exploded view of a fuel cell stack 1400, according to an example embodiment.
  • the fuel cell stack 1400 can be formed by stacking a plurality of single fuel cell modules (e.g. 1300).
  • the central part 1450 of the fuel cell stack 1400 comprises the plurality of single cell modules and a pair of monopolar plates, together forming the active region for an electrochemical reaction.
  • the stack can comprise more or less single cell modules.
  • a pair of current collectors 1440a / 1440b is located on both sides of the active region and a pair of end plates 1442a / 1442b is located at the outermost side.
  • the current collectors 1440a / 1440b are made from electrically conductive materials such as copper, gold or alloys thereof.
  • the end plates 1442a / 1442b can be made from metal, plastic or composites in order to provide necessary strength to hold the stack together.
  • a method of fabricating a flow frame for an electrochemical cell comprising: providing a frame body comprising a plurality of elongate members such that the plurality of elongate members define a boundary of the flow frame and allow an electrolyte solution to flow within the boundary of the flow frame; and disposing one or more support beams within the frame body by coupling the one or more support beams to at least two of the plurality of elongate members.
  • Each of the one or more support beams may be disposed within the frame body in an orientation that is based on a direction of flow of the electrolyte solution.
  • each of the one or more support beams are oriented substantially perpendicular to the direction of flow of the electrolyte solution.
  • the method may further comprise arranging the plurality of elongate members to accommodate an electrode within the boundary of the flow frame such that at least a portion of the electrode is in contact with the one or more support beams.
  • the electrode may comprise compressible porous carbon felt to allow the electrolyte solution to flow through the electrode, and the one or more support beams may be configured to reduce a porosity of the compressible porous carbon felt adjacent the portion of the electrode that is in contact with the one or more support beams.
  • an electrode-bipolar plate module for an electrochemical cell comprising: providing a flow frame that has been fabricated according to the method described above; disposing an electrode within the boundary of the flow frame such that at least a portion of the electrode is in contact with the one or more support beams; and disposing a bipolar plate to be in contact with the electrode.
  • a method of fabricating a cell module for a flow battery comprising: providing an ion conductive membrane comprising a first major surface and a second major surface opposite the first major surface; providing a first electrode-bipolar plate module that has been fabricated according to the method described above; disposing the flow frame of the first electrode-bipolar plate module to be in contact with the first major surface; providing a second electrode-bipolar plate module that has been fabricated according to the method described above; and disposing the flow frame of the second electrode-bipolar plate module to be in contact with the second major surface.
  • a method of fabricating a flow battery stack comprising: providing a plurality of the cell modules that have been fabricated to the method described above; stacking the plurality of the cell modules together such that each cell module is in contact with an adjacent cell module; providing a first monopolar plate that is in contact with a first end of the stack of cell modules and a second monopolar plate that is in contact with a second end of the stack of cell modules; providing a first current collector that is in contact with the first monopolar plate and a second current collector that is in contact with the second monopolar plate; and providing a first end plate that is in contact with the first current collector and a second end plate that is in contact with the second current collector.
  • a method of fabricating a cell module for a fuel cell comprising: providing an ion conductive membrane comprising a first major surface and a second major surface opposite the first major surface; providing an electrode-bipolar plate module that has been fabricated according to the method described above; disposing the flow frame of the electrode-bipolar plate module to be in contact with the first major surface; providing an air electrode that is in contact with the second major surface; providing an air diffusion layer that is in contact with the air electrode; and providing an additional bipolar plate that is in contact with the air diffusion layer.
  • a method of fabricating a fuel cell stack comprising: providing a plurality of the cell modules that have been fabricated according to the method described above; stacking the plurality of the cell modules together such that each cell module is in contact with an adjacent cell module; providing a first monopolar plate that is in contact with a first end of the stack of cell modules and a second monopolar plate that is in contact with a second end of the stack of cell modules; providing a first current collector that is in contact with the first monopolar plate and a second current collector that is in contact with the second monopolar plate; and providing a first end plate that is in contact with the first current collector and a second end plate that is in contact with the second current collector.

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

Abstract

La présente invention concerne un cadre d'écoulement destiné à une cellule électrochimique, comprenant : un corps de cadre comportant une pluralité d'éléments allongés qui sont agencés de manière à définir une limite du cadre d'écoulement et à permettre à une solution d'électrolyte de s'écouler à l'intérieur de la limite du cadre d'écoulement ; et une ou plusieurs poutres de support disposées à l'intérieur du corps de cadre et accouplées à au moins deux éléments de la pluralité d'éléments allongés.
PCT/SG2017/050431 2016-08-31 2017-08-31 Cadre d'écoulement destiné à des cellules électrochimiques WO2018044236A1 (fr)

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WO2021231155A1 (fr) * 2020-05-15 2021-11-18 Ess Tech, Inc. Ensemble électrode pour batterie à flux redox
DE202022100954U1 (de) 2022-02-18 2022-03-31 Rheinisch-Westfälische Technische Hochschule (Rwth) Aachen Flusszelle mit verbessertem Aufbau

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WO1999034467A2 (fr) * 1997-09-10 1999-07-08 Lynntech, Inc. Dispositif de pile a combustible pour exploitation a faible pression
US5945232A (en) * 1998-04-03 1999-08-31 Plug Power, L.L.C. PEM-type fuel cell assembly having multiple parallel fuel cell sub-stacks employing shared fluid plate assemblies and shared membrane electrode assemblies
US20060286436A1 (en) * 2005-06-21 2006-12-21 Amir Faghri Planar fuel cell stack and method of fabrication of the same
WO2012032368A1 (fr) * 2010-09-07 2012-03-15 Krisada Kampanatsanyakorn Empilement de piles à flux redox à plusieurs étages composé de piles monopolaires possédant des interconnexions intercellulaires bipolaires latérales, étendues et juxtaposées sur chaque étage de l'empilement

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WO2012032368A1 (fr) * 2010-09-07 2012-03-15 Krisada Kampanatsanyakorn Empilement de piles à flux redox à plusieurs étages composé de piles monopolaires possédant des interconnexions intercellulaires bipolaires latérales, étendues et juxtaposées sur chaque étage de l'empilement

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2021231155A1 (fr) * 2020-05-15 2021-11-18 Ess Tech, Inc. Ensemble électrode pour batterie à flux redox
US11677093B2 (en) 2020-05-15 2023-06-13 Ess Tech, Inc. Electrode assembly for a redox flow battery
DE202022100954U1 (de) 2022-02-18 2022-03-31 Rheinisch-Westfälische Technische Hochschule (Rwth) Aachen Flusszelle mit verbessertem Aufbau

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