WO2010078423A2 - Cathodes for microbial electrolysis cells and microbial fuel cells - Google Patents
Cathodes for microbial electrolysis cells and microbial fuel cells Download PDFInfo
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- WO2010078423A2 WO2010078423A2 PCT/US2009/069816 US2009069816W WO2010078423A2 WO 2010078423 A2 WO2010078423 A2 WO 2010078423A2 US 2009069816 W US2009069816 W US 2009069816W WO 2010078423 A2 WO2010078423 A2 WO 2010078423A2
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- 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
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- 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
- H01M4/90—Selection of catalytic material
- H01M4/9008—Organic or organo-metallic compounds
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- 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
- H01M8/16—Biochemical fuel cells, i.e. cells in which microorganisms function as catalysts
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- 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
- H01M2004/8678—Inert electrodes with catalytic activity, e.g. for fuel cells characterised by the polarity
- H01M2004/8689—Positive electrodes
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- 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
- H01M4/8647—Inert electrodes with catalytic activity, e.g. for fuel cells consisting of more than one material, e.g. consisting of composites
- H01M4/8657—Inert electrodes with catalytic activity, e.g. for fuel cells consisting of more than one material, e.g. consisting of composites layered
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- 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
- H01M4/88—Processes of manufacture
- H01M4/8825—Methods for deposition of the catalytic active composition
- H01M4/8853—Electrodeposition
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- 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
- H01M4/90—Selection of catalytic material
- H01M4/9016—Oxides, hydroxides or oxygenated metallic salts
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- 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
- H01M4/90—Selection of catalytic material
- H01M4/92—Metals of platinum group
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
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- 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 invention relates to cathodes used in microbial fuel cells (MFCs), which are used for producing electricity; and microbial electrolysis cells (MECs), which are used to produce hydrogen.
- MFCs microbial fuel cells
- MECs microbial electrolysis cells
- An apparatus which includes a reaction chamber having a wall defining an interior of the reaction chamber and an exterior of the reaction chamber; exoelectrogenic bacteria disposed in the interior of the reaction chamber; an aqueous medium having a pH in the range of 3 - 9, inclusive, the aqueous medium including an organic substrate oxidizable by exoelectrogenic bacteria and the medium disposed in the interior of the reaction chamber.
- An inventive apparatus further includes an anode at least partially contained within the interior of the reaction chamber; and a brush or mesh cathode including stainless steel, nickel or titanium, the cathode at least partially contained within the interior of the reaction chamber.
- an inventive apparatus further includes a brush or mesh cathode consisting essentially of stainless steel, nickel or titanium.
- Stainless steels included in a cathode of the present invention can be any stainless steel, such as Austenitic, Ferritic or Martensitic stainless steel.
- Non-limiting examples of included stainless steels are SS 304, SS 316, SS 420 and SS 286.
- Nickel included in a cathode of the present invention can be any nickel.
- Non-limiting examples of included nickels are Ni 201, Ni 400, Ni 625 and Ni HX.
- Titanium included in a cathode of the present invention can be any titanium.
- a cathode included in an inventive apparatus has, in operation, a solution facing portion and a gas facing portion, and PTFE is excluded from the gas facing portion.
- microbes are substantially excluded from contact with the cathode.
- no exogenous noble metal catalyst is present in the cathode.
- a catalyst is present in the cathode.
- a catalyst such as nickel, platinum, activated carbon, or CoTMPP is present in particular embodiments of cathodes of the present invention.
- a nickel oxide catalyst is present in particular embodiments of cathodes of the present invention.
- a nickel oxide catalyst included in a cathode of the present invention is electrodeposited on a stainless steel, nickel or titanium brush or mesh.
- An apparatus includes a cathode which is generally tubular in shape, having a wall defining an interior space, an interior wall surface, an exterior, and an exterior wall surface, wherein the wall comprises a stainless steel, nickel or titanium mesh, the mesh having a first mesh surface disposed towards the interior space and a second mesh surface disposed towards the exterior.
- a generally tubular cathode can have a cross section of various shapes such as circular, oval, oblong, square and rectangular.
- the mesh has a first mesh surface and a second mesh surface and a coating is present on the first mesh surface, the second mesh surface or both the first mesh surface and the second mesh surface.
- an included coating is a diffusion layer or a cathode protection layer.
- the second mesh surface is disposed towards the exterior of the tubular cathode or is exposed to the exterior of the reactor and the coating on the second mesh surface is a water impermeable coating.
- the second mesh surface is disposed towards the exterior of the tubular cathode or the exterior of the reactor and the coating on the second mesh surface is an oxygen impermeable coating.
- the second mesh surface is disposed towards the exterior of the reactor and the coating on the second mesh surface is an oxygen permeable coating.
- the coating on the first mesh surface, second mesh surface or both the first mesh surface and second mesh surface includes an electron conductive binder.
- the coating on the first mesh surface, second mesh surface or both the first mesh surface and second mesh surface includes a catalyst.
- a microbial electrolysis apparatus includes a power source operably connected to add voltage to enhance an electrical potential between the anode and cathode.
- a microbial electrolysis apparatus includes a hydrogen fuel cell power source operably connected to add voltage to enhance an electrical potential between the anode and cathode, wherein the hydrogen fuel cell power source is at least partially fuelled by the microbial electrolysis apparatus.
- Biological processes for producing hydrogen or electric current are provided according to embodiments of the present invention which include providing an apparatus which includes a reaction chamber having a wall defining an interior of the reaction chamber and an exterior of the reaction chamber; exoelectrogenic bacteria disposed in the interior of the reaction chamber; an aqueous medium having a pH in the range of 3 - 9, inclusive, the aqueous medium including an organic substrate oxidizable by exoelectrogenic bacteria and the medium disposed in the interior of the reaction chamber, wherein the apparatus further includes an anode at least partially contained within the interior of the reaction chamber; and a brush or mesh cathode including stainless steel, nickel or titanium, the cathode at least partially contained within the interior of the reaction chamber; and maintaining oxidizing reaction conditions such that electrons are produced by oxidation of the organic substrate by the electrogenic bacteria and the electrons are transferred to an anode.
- Embodiments of a biological process for producing hydrogen further include application of a voltage in the range of 25-1000 millivolt
- Both electricity and hydrogen production result from the degradation of organic matter by microbes, such as exoelectrogenic bacteria.
- Microbes oxidize organic matter, releasing electrons to a circuit and protons into solution.
- the electrons and protons combine with oxygen to form water.
- the MFC is modified by excluding oxygen and adding a small additional voltage.
- Electrons and protons combine on the cathode in the MEC to form hydrogen gas.
- MFCs and MECs can be used in various applications, such as a method of wastewater treatment, or as a method for renewable energy production, for example. Examples of MFCs for making electricity are exemplified in Liu and Logan (2004) and Liu et al. (2004). Examples of MECs are given by Liu et al. (2005), Cheng and Logan (2007c), and Call and Logan (2008).
- Performance of current MECs and MFCs can be limited by the cathode and current cathodes require expensive materials, such as platinum. Thus, improved cathodes for MECs and MFCs are required.
- Figure 1 illustrates an embodiment of an inventive MEC or MFC system
- Figure 2 illustrates a brush cathode having stainless steel, nickel or titanium bristles included in embodiments of an MEC or MFC;
- Figure 3 illustrates a cross sectional view of an embodiment of a stainless steel, nickel or titanium mesh cathode
- Figure 4 illustrates a tubular embodiment of a stainless steel, nickel or titanium mesh cathode
- FIG. 5 illustrates reactor schematics: reactor VB (vertical brush): half brush anode,
- HBA half brush cathode, HBC
- reactor HB horizontal brush
- full brush anode, FBA full brush cathode, FBC
- reactor FC flat cathode
- platinized carbon cloth cathode, Pt stainless steel cathode, SS. power supply, PS. 10 ⁇ resistor, R;
- Figure 11 is a graph showing LSV curves for the platinized cathode (Pt), the 100% loaded SS brush cathode before (pre) and after (post) accelerated use, and the flat SS cathode (SS
- Figure 12 is a graph showing gas production of MECs with different stainless steel and nickel cathodes at an applied voltage or 0.9V;
- Figure 13 is a graph showing gas production of MECs with different stainless steel and nickel cathodes at an applied voltage or 0.6V;
- Figure 14 is a graph showing current densities for MECs with platinum, Ni 625 or SS
- FIG. 15A shows a Tafel plots for an MEC including a stainless steel 286 alloy cathode
- Figure 15B shows a Tafel plot for an MEC including a platinum metal cathode
- Figure 16 is a graph showing gas production of MECs including cathodes with or without electrodeposited nickel oxide layers on SS A286 and Ni 625, operated at an applied voltage of 0.6V;
- Figure 17 A is a graph showing total gas and current production versus time using a Ni
- Figure 17B is a graph showing total gas and current production versus time using a SS
- Figure 18 shows Tafel plots for the indicated MEC cathodes in 2mM phosphate buffer, scan rate 2 mV/s, third scan;
- Figure 19A is a graph showing total gas production for MECs with Ni210
- Ni210+CB, eNiOx or Pt catalyst cathodes as a function of cycle number at an applied voltage of
- Figure 19B is a graph showing maximum current for MECs with Ni210, Ni210+CB, eNiOx or Pt catalyst cathodes, as a function of cycle number at an applied voltage of 0.6 V;
- Figure 2OA is a graph showing hydrogen production rate in an MEC using a Ni210 catalyst cathode at different applied voltages
- Figure 2OB is a graph showing cathodic recovery and Coulombic efficiency in an MEC using a Ni210 catalyst cathode at different applied voltages
- Figure 2OC is a graph showing energy recovery based on electrical input and overall energy recovery in an MEC using a Ni210 catalyst cathode at different applied voltages;
- Figure 22 is a graph showing voltage generation in an MFC using a SS mesh cathode and a Pt catalyst with 2 PDMS/carbon diffusion layers (M2) compared to an MFC using carbon cloth cathodes with 4 diffusion layers (CC4);
- Figure 23A is a graph showing power density in an MFC using a cathode containing SS mesh with Pt catalyst and 1-5 layers of PDMS/carbon DLs (M1-M5) as a function of current density (normalized to cathode surface area) obtained by varying the external circuit resistance (1000-50 ⁇ );
- Figure 23B is a graph showing power density in an MFC using carbon cloth cathodes with Pt and the same DLs (CC1-CC5) as a function of current density (normalized to cathode surface area) obtained by varying the external circuit resistance (1000-50 ⁇ );
- Figure 24A is a graph showing LSV of MFCs including SS mesh cathodes with a Pt catalyst and 1-5 PDMS/carbon DLs (M1-M5);
- Figure 24B is a graph showing LSV of an MFC including cathode Ml compared with MFCs including cathodes having additional PDMS layers (MP2-MP5), each including
- Figure 24C is a graph showing LSV of an MFC including cathode M2 compared with an MFC including a cathode having a solution-facing side coating containing only carbon black (M2, no Pt), and a cathode with no coating on the solution-facing side (M2, no Pt, no CB);
- Figure 25A is a graph showing the CE of an MFC including a SS mesh cathode with Pt catalyst and 1-5 layers of PDMS/carbon DLs (M1-M5) as a function of current density (normalized to cathode surface area) obtained by varying the external circuit resistance (1000- 50 ⁇ );
- Figure 25B is a graph showing the CE of MFCs including carbon cloth cathodes with Pt and 1-5 layers of PDMS/carbon DLs (CC1-CC5) as a function of current density (normalized to cathode surface area) obtained by varying the external circuit resistance (1000-50 ⁇ );
- Figure 26 is a graph showing oxygen permeability of SS mesh cathodes including a Pt catalyst and PDMS/carbon DLs (M) or PDMS (MP) DLs upon PDMS/carbon base layer; and
- Figure 27 is a graph showing voltage generation in an MFC using different SS mesh cathodes.
- Microbial fuel cells according to the present invention are provided which are configured to produce electricity (MFC) and/or hydrogen (MEC) in particular embodiments.
- An MFC or MEC of the present invention includes at least one anode, at least one cathode, a reaction chamber in which an anode and cathode are at least partially disposed, and a conductive conduit for electrons in electrical communication with the anode and the cathode.
- a power source for enhancing an electrical potential between the anode and cathode is further included.
- a reaction chamber may have one or more compartments, such as an anode compartment and a cathode compartment separated, for instance, by a cation or anion exchange membrane or other separator.
- a reaction chamber may be a single compartment configuration with no separator present between the anode and cathode.
- One or more channels may be included in a reaction chamber for addition and removal of various substances such as substrates for bacterial metabolism and products such as hydrogen.
- oxygen is present at the cathode to facilitate the reaction of protons, electrons and oxygen to form water.
- FIG. 1 illustrates an embodiment of an inventive MEC or MFC at 10.
- a reaction chamber is shown having a wall 5 defining an interior and exterior of the reaction chamber, and fluid, such as an aqueous solution containing a biodegradable substrate, in the interior of the reaction chamber, the fluid level shown at 6.
- An anode having bacteria disposed thereon is shown at 12 and a cathode is shown at 16.
- a space 8 between the electrodes is further depicted. Space 8 is minimized to improve system performance and is generally in the range of 0.1 - 100 cm, inclusive.
- An optional separator such as a proton exchange membrane (PEM) or filter separator, is shown at 14 positioned between the anode 12 and cathode 16.
- a conduit for electrons 17 is shown along with a connected power source (MEC) or load (MFC) shown at 18.
- MEC power source
- MFC load
- Channels 20 and 22 are shown which can serve as flow paths for materials entering or leaving the reaction chamber.
- the present invention provides cathodes for MFCs and MECs that provide good performance for these systems.
- cathodes are characterized by high specific surface area.
- an inventive cathode has a specific surface area greater than 10 m 2 /m 3 .
- Specific surface area is here described as the total surface area of the cathode per unit of cathode volume.
- a cathode of the present invention has a specific surface area greater than 1000 m 2 /m 3 .
- a cathode of the present invention has a specific surface area greater than 5,000 m /m .
- a cathode of the present invention has a specific surface area greater than 10,000 m 2 /m 3 .
- Exemplary high surface area cathodes of the present invention include metal brush cathodes and metal mesh cathodes, where the metal is stainless steel, nickel or titanium.
- a nickel brush or mesh cathode can be nickel metal or a nickel alloy.
- nickel is used herein to refer to nickel metal and nickel alloys unless otherwise specified.
- a titanium brush or mesh cathode can be titanium metal or a titanium alloy.
- titanium is used herein to refer to titanium metal and titanium alloys unless otherwise specified.
- a metal brush cathode includes one or more conductive fibers.
- the one or more fibers are attached to a support.
- a plurality of fibers is attached to the support and the fibers extend generally radially from the support in specific embodiments.
- a brush electrode optionally includes a centrally disposed support having a longitudinal axis.
- Brush electrodes include a variety of configurations illustratively including various twisted wire brush configurations and strip brush configurations.
- a particular twisted wire brush configuration includes a support formed from two or more strands of wire and fibers attached between the wires.
- a strip brush configuration includes fibers attached to a conductive backing strip, the strip attached to the support.
- Fibers of a brush cathode are electrically conductive and are in electrical communication with the support and with an anode.
- Metal brush cathodes include stainless steel, nickel or titanium fibers attached to a stainless steel, nickel or titanium support.
- Figure 2 illustrates a high specific surface area stainless steel, nickel or titanium brush cathode included in embodiments of an MEC or MFC of the present invention.
- Figure 2 shows a configuration of a brush cathode 20 in which stainless steel, nickel or titanium bristles 24 are placed substantially perpendicular to and between two or more conductive, corrosion resistant wires which form a support 22 such that the bristles 24 extend substantially radially from the support 22.
- a wire is optionally twisted around the brushes to maintain good electrical contact with the wire.
- a conductive connector is typically attached to the support 22 to electrically connect the cathode to the anode.
- Brush cathode configurations can include multiple discontinuous bristles and/or one or more continuous wires wound about a central axis, forming looped bristles. Where no support is included, a conductive connector is attached to the wire or wires forming the bristles to electrically connect the cathode anode to the anode. Where a support is included, a conductive connector is typically attached to the support to electrically connect the cathode and an anode. Bristles of a brush cathode can be randomly or non-randomly oriented.
- a brush cathode includes bristles that extend substantially radially from a central axis forming a cylindrical brush.
- bristles extend substantially radially from a central axis forming a partial cylindrical shape, such as a half cylinder or quarter cylinder.
- a half cylindrical brush cathode is preferred in particular MEC and MFC embodiments.
- a brush cathode optionally includes one or more coatings.
- Metal mesh cathodes according to embodiments of the present invention include a stainless steel, nickel or titanium mesh.
- U.S. standard mesh sizes having pore sizes of about one centimeter or less, for example U.S. standard 7/16 inch mesh, 1 A inch mesh, and U.S. standard mesh Nos. 4, 5, 6, 7, 8, 10, 12, 14, 16, 18, 20, 25, 30, 35, 40, 42, 44, 50, 54, 60, 70, 90, 120, 140, 165, 200, 325, 400 and 500 mesh, are included in cathodes for use in MECs and MFCs according to particular embodiments.
- Mesh sizes are known in the art and particular mesh dimensions are illustrated below:
- 42 mesh with a wire diameter of 0.0055 inches or 13.97 mm has an open area of 59.1%, and an opening width of 0.018 inches.
- Specific surface area of the mesh is estimated for 42 mesh at about 11,000 m 2 /m 3 based on the volume defined by the thickness of the mesh and the geometric surface area of a wire.
- the pore size of the stainless steel, nickel or titanium mesh is in the range of 0.005 - 0.02 inch, inclusive. In preferred MFC embodiments, the pore size of the stainless steel, nickel or titanium mesh is in the range of 0.005 - 0.4 inch, inclusive.
- Figure 3 illustrates a cross sectional view of an embodiment of a stainless steel, nickel or titanium mesh cathode 30. Wires 32 of the mesh are shown along with an optional first coating 34 on one side of the mesh and an optional second coating 36 on the opposing side of the mesh.
- a stainless steel, nickel or titanium mesh included in a cathode according to embodiments of the present invention can be shaped to increase surface area.
- the mesh may be pleated to achieve an accordion fold.
- the mesh forms a wall defining an interior space.
- the interior space is open to the exterior of the reactor or to a gas space in the reactor at one or both ends.
- cathodes according to embodiments of the present invention can be generally tubular in shape, having a wall defining an interior space, an interior wall surface, an exterior, and an exterior wall surface.
- Such generally tubular cathodes have any of various cross sectional shapes, including, but not limited to, circular, oblong, square or rectangular.
- an inventive tubular cathode is configured so that air is present inside the tube, and water outside the tube.
- an inventive tubular cathode is configured to separate hydrogen produced from liquid in the reactor where the tube may contain only gas, or may contain an aqueous medium similar or different from that in the reactor.
- the interior space defined by the wall of the tubular cathode may contain liquid having a lower or higher pH than the solution containing the bacteria in order to protect the bacteria from the extreme pH environment of the tubular solution.
- the interior of tubular cathodes of MFCs or MECs may be flushed with solutions or gases to clean or maintain them.
- Figure 4 shows a tubular embodiment of a mesh cathode 50. Illustrated is an optional coating 52 on the side of the mesh disposed toward the exterior of the cathode and an optional coating 54 on the side of the mesh disposed toward the interior of the cathode. The mesh is shown at 56.
- a cathode of the present invention may include one or more coatings on one or more cathode surfaces.
- one or more coatings are included on an inner cathode surface, that is, a cathode surface present in the interior volume of the reaction chamber, and/or an outer surface, that is, a cathode surface exterior to the reaction chamber.
- a cathode surface exterior to the reaction chamber is likely to be present where a gas cathode is used, where the exterior cathode surface is in contact with a gas.
- one or more coatings are included on an interior wall surface of a tubular cathode and/or an exterior wall surface of a tubular cathode.
- Exemplary coatings are functionalized to inhibit or allow passage of a selected substance, such as water and/or oxygen, through the wall.
- a coating may include a binder, such as an electron or proton conductive binder.
- a binder such as an electron or proton conductive binder.
- One or more coatings may be added to act as cathode protection layers or diffusion layers, for example.
- a cathode optionally contains one or more cathode shielding materials.
- a shielding material may preferably include a layer of a shielding material disposed on any cathode surface, including an inner cathode surface, that is, a cathode surface present in the interior volume of the reaction chamber, and an outer surface, that is, a cathode surface exterior to the reaction chamber.
- a cathode surface exterior to the reaction chamber is likely to be present where a gas cathode is used, where the exterior cathode surface is in contact with a gas.
- a cathode protective layer may be used to prevent contact of microbes or other materials with the cathode surface in both electrode assemblies for current producing systems and for hydrogen gas generation systems.
- a cathode protection layer for a current producing microbial fuel cell system can be used as a support for microbes such as bacterial colonization wherein bacteria scavenge oxygen in the vicinity of the cathode so it does not leak into the reactor and it may not directly contact the anode.
- an inner cathode surface is protected by a cathode protection layer (CPL).
- a function of the CPL is to protect the cathode from biofouling of the catalyst.
- a CPL reduces diffusion of carbon dioxide to the cathode so as to limit methane formation from both abiotic and biotic sources, or from the action of bacteria, at the cathode.
- a CPL is configured such that it is in contact with an inner surface of a cathode.
- a CPL may be configured to cover the inner surface of the cathode partially or wholly, such as by bonding of the CPL to the cathode.
- the cathode protection layer may contain chemicals or metals that interfere with bacterial adhesion to the cathode, for example silver particles or cationic surfactants.
- a CPL is present in the interior of an MFC or MEC reaction chamber but not in contact with the cathode.
- the inclusion of such a CPL defines two or more regions of such a reactor based on the presence of the CPL.
- the CPL can be proton, liquid, and/or gas permeable barriers, such as a filter.
- a filter for inhibiting introduction of large particulate matter into the reactor may be positioned between the anode and cathode such that material flowing through the reaction chamber between the anode and cathode passes through the filter.
- a filter may be placed onto the cathode, restricting the passage of bacteria- sized particles to the cathode.
- a filter may be positioned between an inlet channel and/or outlet channel and the interior of the reaction chamber or a portion thereof. Suitable filters may be configured to exclude particles larger than 0.01 micron- 1 micron for example.
- a CPL includes a "proton diffusion layer" for selectively allowing passage of material to the vicinity of a cathode.
- a diffusion layer includes an ion exchange material. Any suitable ion conducting material which conducts protons may be included in a proton exchange membrane. For example, a perfluorinated sulfonic acid polymer membrane may be used. In particular, a proton exchange membrane such as NAFION, that conducts protons, may be used for this purpose.
- a further example of an ion conducting material is polyphenyl sulfone, available commercially as RADEL R.
- a diffusion layer includes an anion exchange material.
- the diffusion layer includes an anion exchange material that conducts anions, associated with protons produced by anodophilic bacteria, to the cathode, such as a quaternary amine styrene divinylbenzene copolymer.
- An included diffusion layer further functions to inhibit diffusion of gas to or from a cathode relative to the anode chamber.
- the protons associated with the negatively charged, anionic, ion exchange groups such as phosphate groups, specifically allow passage of negatively charged anions that contain positively charged protons but overall carry a net negative charge, and not allowing passage of positively charged ions and reducing the diffusion of hydrogen into the anode chamber.
- a diffusion layer allows for efficient conduction of protons across the barrier while inhibiting backpassage of hydrogen.
- An example of such a diffusion layer material is the anion exchange membrane AMI-7001, commercially supplied by Membranes International, Glen Rock, NJ.
- the diffusion layer can also include an anion conducting material applied as a paste directly to a cathode.
- an anion exchange material can be used to contain a catalyst applied to a cathode.
- a diffusion layer for an electrode assembly for a current producing microbial fuel cell system can be configured to allow oxygen diffusion to the catalyst from the air-facing side into the conductive electrode matrix, and to reduce oxygen diffusion into the system.
- An exemplary diffusion layer coated on the air-facing side of a gas cathode is a carbon/PTFE layer or one or more additional PTFE diffusion layers.
- the carbon/PTFE base layer can be prepared by applying a mixture of carbon powder (Vulcan XC-72) and 30 wt% PTFE solution (20 ⁇ l/mg of carbon powder) onto one side of the carbon cloth, air-drying at room temperature for 2 h, followed by heating at 370 0 C for 0.5 h.
- the carbon loading in an exemplary diffusion layer is 2.5 mg cm "2 .
- a oxygen permeable cathode diffusion layer is included which contains a viscoelastic polymer.
- the viscoelastic polymer is an organosilicon compound, particularly a siloxane polymer.
- Poly(dimethylsiloxane) is a preferred siloxane polymer included in a diffusion layer of an inventive cathode according to certain embodiments.
- Poly(l-trimethylsilyl-l-propyne) [PTMSP] is a further example of a preferred siloxane polymer included in a diffusion layer of an inventive cathode according to certain embodiments.
- an included viscoelastic polymer is cured at temperatures of 40 0 C or less.
- Oxygen permeable thermoplastics such as crosslinked poly(butadiene) are included in an MFC cathode diffusion layer according to particular embodiments of the present invention.
- PTFE is excluded from the cathode diffusion layer.
- an oxygen permeable cathode diffusion layer includes conductive carbon and a viscoelastic polymer.
- Conductive carbon includes in an oxygen permeable cathode diffusion layer illustratively includes graphite, carbon nanoparticles such as carbon nanotubes and carbon black.
- a cathode diffusion layer includes viscoelestic polymer in amounts of 1 x 10 ⁇ 2 - 1 x 10 ⁇ 4 mg/cm 2 , inclusive, of mesh and conductive carbon in amounts of 0.1 - 10 mg/cm , inclusive, of mesh, although more or less of each component can be used.
- microorganisms are excluded from the cathode or are present only in amounts which produce no detectable effect on MFC or MEC performance.
- an outer surface of a cathode is covered partially or preferably wholly by a cathode diffusion layer (CDL).
- the CDL may be directly exposed to the gas phase and inhibits water leakage through the cathode from the interior of the reaction chamber.
- a CDL is hydrogen permeable, allowing hydrogen to freely diffuse from the catalyst in the cathode into a gas collection chamber, gas conduit or other component of a gas collection system, such as may be present in an MEC.
- a CDL may further provide support for the cathode and may further form a portion of a wall of a reaction chamber.
- a CDL can also help to reduce bacteria from reaching the cathode and fouling the surface.
- a CDL includes a hydrogen permeable hydrophobic polymer material such as polytetrafluoroethylene (PTFE) or like materials. The thickness of this material can be varied or multiple layers can be applied depending on the need to reduce water leakage.
- PTFE polytetrafluoroethylene
- Cathodes according to embodiments of the present invention include a metal mesh and a conductive coating, for example carbon black in a binder of Nafion or PTFE in contact with the metal mesh. Additional layers can be placed onto this structure, for example, a PTFE diffusion layer on the air side to inhibit water permeability and to reduce oxygen diffusion through the cathode and into the water.
- Cathode Catalyst [00112] In some MEC embodiments, stainless steel serves as the sole cathode catalyst. In particular MEC embodiments, the cathode consists essentially of stainless steel, nickel or titanium in brush or mesh form. Combinations of stainless steel, nickel and titanium can be used.
- stainless steel cathode catalysis is enhanced through the use of steels that have a nickel content of at least 5% by weight. In further embodiments, the performance of stainless steel cathode catalysis is enhanced through the use of steels that have a nickel content of at least 8% by weight. In still further embodiments, the performance of stainless steel cathode catalysis is enhanced through the use of steels that have a nickel content of at least 15% by weight. In yet further embodiments, the performance of stainless steel cathode catalysis is enhanced through the use of steels that have a nickel content of at least 20% by weight.
- a cathode described herein includes an added catalyst, such as, but not limited to, a nickel or platinum catalyst.
- a non-precious metal catalyst such as cobalt tetramethoxyphenylporphyrin (CoTMPP) can be included.
- an added nickel catalyst is a nickel oxide catalyst.
- one or more nickel oxides is deposited on a stainless steel and/or nickel cathode by electrochemical deposition in order to increase catalytic efficiency.
- Activated carbon is an included catalyst in preferred embodiments of inventive cathodes.
- An included catalyst can be integrated with a cathode by methods including, but not limited to electrodeposition, a chemical reaction, and chemical precipitation.
- a catalyst can be included in a cathode coating.
- no noble metal catalyst is added to a cathode of the present invention. While small amounts of noble metals may be present as impurities in stainless steel, nickel or titanium used, no noble metal exogenous to the stainless steel, nickel or titanium is present in preferred embodiments of an inventive cathode.
- Noble metals typically included as cathode catalysts are platinum and palladium. Thus, in preferred embodiments, no platinum or palladium is added to a cathode of the present invention.
- substantially no platinum or palladium is present in a cathode of the present invention.
- the term "substantially no platinum or palladium” refers to an undetectable or catalytically negligible amount of platinum or palladium. For example, where platinum or palladium are undetectable by multi-channel atomic emission spectrometry or is present in amounts of 0.01% by weight or less, it is considered that substantially no platinum or palladium is present in a cathode of the present invention.
- An anode in embodiments of MFCs an MECs of the present invention includes a conductive and corrosion-resistant or non-corroding material, for example carbon paper or cloth, carbon foam, graphite rods, blocks or fibers either in random bundles or arranged in brush form (Logan, 2008; Logan, et al, 2007b).
- An anode material can be treated to make bacteria more easily adhere to the surface.
- an anode is optionally treated to increase current densities, for example by using a high-temperature ammonia gas treatment as described herein.
- an anode included in an MFC or MEC is characterized by high specific surface area, for instance as described in U.S.
- an anode included in embodiments of MECs and MFCs of the present invention is a brush having graphite fiber bristles in electrical contact with a conductive core.
- Electrode Assemblies An anode and cathode may have any of various shapes and dimensions and are positioned in various ways in relation to each other. In one embodiment, the anode and the cathode each have a longest dimension, and the anode and the cathode are positioned such that the longest dimension of the anode is parallel to the longest dimension of the cathode.
- the anode and the cathode each have a longest dimension, and the anode and the cathode are positioned such that the longest dimension of the anode is perpendicular to the longest dimension of the cathode.
- the anode and the cathode each have a longest dimension, and the anode and the cathode are positioned such that the longest dimension of the anode is perpendicular to the longest dimension of the cathode.
- the anode and the cathode may be positioned such that the longest dimension of the anode is at an angle in the range between 0 and 180 degrees with respect to the longest dimension of the cathode. [00125] Space between an anode and cathode is minimized to improve system performance and is generally in the range of 0.1 - 100 cm, inclusive.
- an inventive system which includes more than one anode and/or more than one cathode.
- additional anodes and/or cathodes may be provided.
- the number and placement of one or more anodes and/or one or more electrodes may be considered in the context of the particular application.
- a larger area of anodic surface may be provided.
- a larger area of cathode surface may be appropriate.
- an electrode surface area is provided by configuring a reactor to include one or more electrodes that project into the reaction chamber.
- an electrode surface area is provided by configuring the cathode as a wall of the reactor, or a portion of the wall of the reactor.
- the ratio of the total surface area of the one or more anodes to the total volume of the interior of the reaction chamber is in the range of about 10000:1-1:1, inclusive, square meters per cubic meter in particular embodiments. In further embodiments, the ratio is in the range of about 5000:1-100:1.
- an anode has a surface having a surface area present in the reaction chamber and the cathode has a surface having a surface area in the reaction chamber.
- a ratio of the total surface area of anodes to surface area of cathodes in an inventive system is about 1:1.
- the anode surface area in the reaction chamber is greater than the cathode surface area in the reaction chamber.
- a ratio of the anode surface area in the reaction chamber to the cathode surface area in the reaction chamber is in the range of 1.5:1-1000:1 and more preferably 2:1-10:1.
- the ratio of the total surface area of the one or more cathodes to the total volume of the interior of the reaction chamber is in the range of about 10000:1-1:1, inclusive, square meters per cubic meter in particular embodiments. In further embodiments, the ratio is in the range of about 1000:1-10:1.
- the total surface area of the cathodes described here is exclusive of the surface area of any catalyst included in the cathode.
- a power source for enhancing an electrical potential between the anode and cathode is included in MECs of the present invention.
- Power sources used for enhancing an electrical potential between the anode and cathode are not limited and illustratively include grid power, solar power sources, wind power sources. Further examples of a power source suitable for use in an inventive system illustratively include a DC power source and an electrochemical cell such as a battery or capacitor.
- a power supply for an MEC is an MFC.
- a portion of the hydrogen generated in an MEC of the present invention is used to power a hydrogen fuel cell, the hydrogen fuel cell serving as a power source for the MEC.
- An ion exchange membrane is optionally disposed between an anode and a cathode in embodiments of the present invention.
- An MEC or MFC according to the present invention may be configured as a self- contained system in particular embodiments.
- a quantity of a biodegradable substrate is included in the reactor and no additional substrate is added.
- additional substrate is added at intervals or continuously such that the system operates as a batch processor or as a continuous flow system.
- a hydrogen gas collection system is optionally included in an inventive MEC such that the hydrogen gas generated is collected and may be stored for use, or directed to a point of use, such as to a hydrogen fuel powered device.
- a hydrogen gas collection unit may include one or more hydrogen gas conduits for directing a flow of hydrogen gas from the cathode to a storage container or directly to a point of use.
- a hydrogen gas conduit is optionally connected to a source of a sweep gas. For instance, as hydrogen gas is initially produced, a sweep gas may be introduced into a hydrogen gas conduit, flowing in the direction of a storage container or point of hydrogen gas use.
- a hydrogen collection system may include a container for collection of hydrogen from the cathode.
- a collection system may further include a conduit for passage of hydrogen.
- the conduit and/or container may be in gas flow communication with a channel provided for outflow of hydrogen gas from the reaction chamber.
- the conduit and/or container are in gas flow communication with the cathode, particularly where the cathode is a gas cathode.
- a channel is included defining a passage from the exterior of the reaction chamber to the interior in particular embodiments. More than one channel may be included to allow and/or regulate flow of materials into and out of the reaction chamber. For example, a channel may be included to allow for outflow of a gas generated at the cathode. Further, a channel may be included to allow for outflow of a gas generated at the anode.
- a channel may be included to allow flow of a substance into a reaction chamber and a separate channel may be used to allow outflow of a substance from the reaction chamber. More than one channel may be included for use in any inflow or outflow function.
- a regulator device such as a valve, may be included to further regulate flow of materials into and out of the reaction chamber. Further, a cap or seal is optionally used to close a channel. For example, where a fuel cell is operated remotely or as a single use device such that no additional materials are added, a cap or seal is optionally used to close a channel.
- a pump may be provided for enhancing flow of liquid or gas into and/or out of a reaction chamber.
- Exoelectrogenic microbes included in an MFC or MEC preferably include at least one or more species of exoelectrogenic bacteria.
- exoelectrogenic bacteria and “anodophilic bacteria” are used interchangeably herein refer to bacteria that transfer electrons to an electrode, either directly or indirectly.
- exoelectrogenic bacteria are obligate or facultative anaerobes.
- exoelectrogenic bacteria include bacteria selected from the families Aeromonadaceae, Alteromonadaceae, Clostridiaceae, Comamonadaceae, Desulfuromonaceae, Enterobacteriaceae, Geobacteraceae, Pasturellaceae, and Pseudomonadaceae.
- Exoelectrogenic bacteria preferably are in contact with an anode for direct transfer of electrons to the anode.
- the bacteria may be present elsewhere in the reactor and still function to produce electrons useful in an inventive process.
- a mediator of electron transfer is included in a fuel cell.
- mediators are exemplified by ferric oxides, neutral red, anthraquinone-l,6-disulfonic acid (ADQS) and 1,4- napthoquinone (NQ).
- Mediators are optionally chemically bound to the anode, or the anode modified by various treatments, such as coating, to contain one or more mediators.
- Exoelectrogenic bacteria may be provided as a purified culture, enriched in exoelectrogenic bacteria, or even enriched in a specified species of bacteria, if desired. Pure culture tests have reported Coulombic efficiencies as high as 98.6% in Bond, D. R.
- Bacteria can be selected or genetically engineered that can increase Coulombic efficiencies and potentials generated at the anode.
- a mixed population of bacteria may be provided, including exoelectrogenic anaerobes and other bacteria.
- a biodegradable substrate included in a microbial fuel cell according to embodiments of the present invention is oxidizable by exoelectrogenic bacteria or biodegradable to produce a material oxidizable by exoelectrogenic bacteria.
- a biodegradable substrate is an organic material biodegradable to produce an organic substrate oxidizable by exoelectrogenic bacteria in preferred embodiments.
- Any of various types of biodegradable organic matter may be used as "fuel" for bacteria in an MEC or MFC, including carbohydrates, amino acids, fats, lipids and proteins, as well as animal, human, municipal, agricultural and industrial wastewaters.
- Naturally occurring and/or synthetic polymers illustratively including carbohydrates such as chitin and cellulose, and biodegradable plastics such as biodegradable aliphatic polyesters, biodegradable aliphatic-aromatic polyesters, biodegradable polyurethanes and biodegradable polyvinyl alcohols.
- biodegradable plastics include polyhydroxyalkanoates, polyhydroxybutyrate, polyhydroxyhexanoate, polyhydroxy valerate, polyglycolic acid, polylactic acid, polycaprolactone, polybutylene succinate, polybutylene succinate adipate, polyethylene succinate, aliphatic-aromatic copolyesters, polyethylene terephthalate, polybutylene adipate/terephthalate and polymethylene adipate/terephthalate.
- Organic substrates oxidizable by exoelectrogenic bacteria are known in the art.
- an organic substrate oxidizable by exoelectrogenic bacteria include, but are not limited to, monosaccharides, disaccharides, amino acids, straight chain or branched C 1 -C 7 compounds including, but not limited to, alcohols and volatile fatty acids.
- organic substrates oxidizable by exoelectrogenic bacteria include aromatic compounds such as toluene, phenol, cresol, benzoic acid, benzyl alcohol and benzaldehyde. Further organic substrates oxidizable by exoelectrogenic bacteria are described in Jardin, D. R. et al., Applied and Environmental Microbiology 56:1858-1864, 1990.
- a provided substrate may be provided in a form which is oxidizable by exoelectrogenic bacteria or biodegradable to produce an organic substrate oxidizable by exoelectrogenic bacteria.
- organic substrates oxidizable by exoelectrogenic bacteria include glycerol, glucose, acetate, butyrate, ethanol, cysteine and combinations of any of these or other oxidizable organic substances.
- biodegradable refers to an organic material decomposed by biological mechanisms illustratively including microbial action, heat and dissolution. Microbial action includes hydrolysis, for example.
- a biological process for producing hydrogen or electric current includes providing an MEC or MFC, the MEC or MFC including a reactor having an interior; providing exoelectrogenic bacteria disposed within the interior of the reactor; introducing a biodegradable organic material oxidizable by an oxidizing activity of the exoelectrogenic bacteria; incubating the organic material oxidizable by the exoelectrogenic bacteria under oxidizing reaction conditions such that electrons are produced and transferred to an anode.
- the electrons are transferred to the anode, and, through a load such as a device to be powered, to a stainless steel, nickel or titanium-containing cathode. Protons and electrons then react with oxygen at the cathode, producing water.
- the electrons are transferred to the anode and a power source is activated to increase a potential between the anode and a stainless steel, nickel or titanium-containing cathode, such that electrons and protons combine to produce hydrogen gas.
- the activation of the power source includes application of a voltage in the range of 25-1000 millivolts, preferably in the range of 50 - 900 millivolts .
- reaction conditions include variable such as pH, temperature, osmolarity, and ionic strength of the medium in the reactor.
- alkaline reactor conditions in an MEC or MFC reactor are avoided and the pH of the medium in the reactor is in the range of pH 3 - pH 9, inclusive, and preferably between pH 5- pH 8.5 inclusive.
- conditions for use of a cathode according to the present invention in an MEC are significantly different compared to conditions of oxygen reduction in seawater.
- Hydrogen evolution in an MEC takes place in neutral pH solutions, such as pH 5-9, over a large range of salinities.
- metals, such as stainless steel are used in methods of the present invention as catalysts for hydrogen evolution at neutral pH. It is a further aspect of inventive cathodes that nickel oxides work well for hydrogen evolution in neutral pH conditions and in MECs.
- An aqueous medium in a reaction chamber of an MEC or MFC of the present invention is formulated to be non-toxic to exoelectrogenic microbes in contact with the aqueous medium.
- the medium or solvent may be adjusted to a be compatible with exoelectrogenic microbe metabolism, for instance by adjusting pH to be in a desired range, by adding a buffer to the medium or solvent if necessary, and by adjusting the osmolarity of the medium or solvent by dilution or addition of a osmotically active substance.
- Ionic strength may be adjusted by dilution or addition of a salt for instance.
- nutrients, cofactors, vitamins and other such additives may be included to maintain a healthy bacterial population, if desired, see for example examples of such additives described in Lovley and Phillips, Appl. Environ. Microbiol., 54(6): 1472-1480.
- Reaction temperatures are typically in the range of about 10-40 0 C for non- thermophilic bacteria, although the device may be used at any temperature in the range of 0 to 100 0 C by including suitable bacteria for growing at selected temperatures. However, maintaining a reaction temperature above ambient temperature may require energy input and it is preferred to maintain the reactor temperature at about 15-25°C without input of energy.
- Reaction temperatures in the range of 16-25°C, inclusive or more preferably temperatures in the range of 18-24°C, inclusive and further preferably in the range of 19-22°C, inclusive allow hydrogen generation, electrode potentials, Coulombic efficiencies and energy recoveries comparable to reactions run at 32°C which is generally believed to be an optimal temperature for anaerobic growth and metabolism, including oxidation of an organic material.
- an MFC or MEC reactor is operated at temperatures up to about 40 0 C at start-up and the temperature is then allowed to operate at ambient temperatures in the range of 10-40 0 C.
- Ionic strength of a medium in a reactor is preferably in the range of 50-500 millimolar, more preferably in the range of 75-450 millimolar inclusive, and further preferably in the range of 100-400 millimolar, inclusive.
- Methods for Fabricating Cathodes are provided according to embodiments of the present invention which include fabricating a cathode for an MEC or MFC without exposing the cathode to temperatures above 100 0 C and/or pressures above ambient pressure.
- a coating included in a cathode of the present invention is applied to a stainless steel, nickel or titanium mesh without pressure application, such as by painting the mesh with a desired coating so that the coating adheres to the mesh and is present in the pores, forming a continuous coating on one or both sides of the mesh.
- a coating included in a cathode of the present invention is applied to a stainless steel, nickel or titanium mesh and is not exposed to temperatures above 100 0 C.
- ambient pressure refers to air pressure of the surrounding atmosphere, generally about 1 atmosphere. The described preference against exposure to pressures above ambient pressure is intended to exclude “hot-press" application of materials in preferred embodiments.
- a flat piece of grade 304 SS (McMaster-Carr, Cleveland, OH) was used in some tests (surface area of 7 cm ).
- SS cathodes were cleaned before use by sonication in an ultrasonic cleaner (model 1510, Branson, Danbury, CT) for 10 min in 70% ethanol, followed by rinsing with DI water, and sonication again for 5 min in fresh DI water.
- an ultrasonic cleaner model 1510, Branson, Danbury, CT
- FIG. 5 diagramatically shows three different MEC architectures used to determine the effect of cathode brush architecture, with all reactors containing an ammonia treated, graphite fiber brush anode in which ammonia gas treatment of an anode is accomplished using a thermogravimetric analyzer. For this procedure, the furnace temperature was ramped up to 700 0 C at 50 °C/min using nitrogen gas (70 mL/min) before switching the gas feed to 5% NH 3 in helium gas. The anode is held at 700 0 C for 60 min. before being cooled to room temperature under nitrogen gas (70 mL/min) over 120 min.
- An anaerobic gas collection tube was installed above the brush cathode.
- Reactor HB was used to examine SS brush cathodes with different surface areas and the graphite brush cathode, with each cathode brush inserted perpendicular to the core of the anode.
- the brush anodes were first enriched in an MFC using the effluent from an active MFC.
- PBS phosphate buffer medium
- Na 2 HPO 4 4.58 g/L
- nutrient solution NH 4 Cl, 0.31 g/L
- KCl 0.13 g/L
- trace vitamins and minerals having a final solution conductivity of 7.5 mS/cm.
- the specific surface area of the flat SS cathode was more than a hundred fold smaller than the graphite brush cathode, current generation was greater (64 +2 A/m 3 ).
- the current density produced by the flat SS cathode (2.6 cm electrode spacing) was also 2.7 times greater than the SS brush core (24 + 0 A/m 3 ; 3.5cm electrode spacing).
- the higher current density of the flat SS cathode suggests that the orientation and distance of the cathode was more important for increased current density than surface area.
- Reactor VB was producing the highest current density of 194 + 1 A/m 3 , compared to 182 + 2A/m for Reactor FC.
- both reactors generated a similar average current density, with Reactor FC reaching 188 + 10 A/m 3 and Reactor VB obtaining 186 + 2 A/m 3 .
- the higher current density of Reactor VB with the SS brush was a result of a lower cathodic overpotential than that of Reactor FC with the Pt/C cathode ( Figure 10).
- the Pt/C cathode had a higher overpotential than that of the SS brush, likely due to the higher current density.
- both the SS brush and Pt/C cathode exhibited roughly the same overpotential, but several later cycles the Pt/C cathode showed an increase in overpotential (cycles 3 and 4). This trend may have been due to minor Pt catalyst inactivation in combination with an activation of the SS for the hydrogen evolution reaction (HER).
- the SS cathode in Reactor VB produced a cathode potential of -0.910 +0.002 V, whereas the Pt/C cathode exhibited a higher overpotential with a value of -0.924+0.003 V.
- These potentials correspond to cathodic losses of about 0.29 V for the SS brush and 0.30 V for the Pt/C cathode relative to the equilibrium potential of hydrogen formation (-0.62 V vs Ag/AgCl).
- LSV Linear sweep voltammetry
- a potentiostat model PC4/750, Gamry Instruments, Warminster, PA
- 1 mV/s rates on the cathodes (100% loaded SS brush, flat SS, and Pt/C) at 30 0 C in a 28 mL reactor.
- the LSV reactor also included an Ag/AgCl reference electrode (Princeton Applied Research, Oak Ridge, TN) and a 2 cm 2 pure platinum foil counter electrode.
- the reactor was filled with 50 rnM PBS, pH 7.0, without trace nutrients and sparged with UHP nitrogen.
- Chronopotentiometry at 50mA for 24 h in 50 mM PBS was performed to simulate accelerated use of a 100% loaded SS brush. Stripping was performed with cyclic voltammetry in 0.5 MH 2 SO 4 from-0.5 to +1.5 V vs Ag/AgCl at 250 mV/s.
- the SS brush was stripped using cyclic voltammetry until the currents corresponding to hydrogen and oxygen evolution became constant (about five cycles).
- the SS brush Compared to a flat SS cathode, the SS brush exhibited a lower overpotential, particularly at lower currents, thus confirming the effectiveness of the high surface area.
- Cathodes of stainless steel alloys 304, 316, 420 and A286 or nickel alloys 201, 400, 625 and HX were made by cutting sheet metal (McMaster-Carr, IL) into 3.8cm diameter disks. Metal compositions are listed in Table I. A platinum metal disk (99.9% purity) used for comparison to these other metal materials was pre-cut by the manufacturer (Hauser & Miller, MO). Metal cathodes were cleaned with ethanol before placing them in the reactors. Carbon cloth cathodes (projected surface area of 7 cm 2 ) were made using a platinum catalyst (0.5mg cm "2 ) [00186] Table I
- a power source (3645A; Circuit Specialists, Inc., AZ) was used to apply either 0.6 or 0.9V to the reactors. After each cycle, the reactors were drained, refilled with substrate solution, and sparged with ultra high purity nitrogen gas for 5min. The reactors were maintained in a 3O 0 C constant temperature room. Once reactors reached similar current ( ⁇ 0.57mA cm “ ) and gas production volumes (-30 ml) for three consecutive cycles using carbon cloth cathodes, the cathodes were replaced with sheet metal cathodes. All reactors were run in duplicate, and tests with new cathodes were run for at least three consecutive cycles. [00188] Analysis
- the overall hydrogen recovery (rm,co D ) is the ratio of hydrogen recovered compared to the maximum theoretical hydrogen produced based on substrate utilization:
- nH2,C0D rH2,C0D ⁇ w) nH2,C0D
- n H2 is the actual number of hydrogen moles produced.
- the Coulombic efficiency (C ⁇ ) is the ratio of electrons recovered as hydrogen gas relative to the total electrons available from substrate consumption, calculated as: ⁇ _ n H2,cat _ r H2,C0D sr ⁇ n H 2,COD r H2,cat [00195]
- the energy efficiency relative to electrical input ( ⁇ g) is the ratio of energy content of hydrogen produced to the input electrical energy:
- Wm (kJ) is the energy produced by hydrogen
- W E (kJ) the amount of energy added to the circuit by the power source minus the losses across the resistor
- AHm 285.83 kJ/mol the energy content of hydrogen based on the heat of combustion
- E ap (V) the voltage applied by the power source.
- the number of moles of substrate consumed during a batch cycle based on COD removal (n s ) is:
- the molecular weight needs to be multiplied by a conversion factor of 0.78 g COD g "1 sodium acetate.
- the overall energy recovery based on both electric and substrate inputs ( ⁇ E + s) is:
- MEC results for different metal cathodes (stainless steel, nickel and platinum) at an applied voltage of 0.9V Metal r H2 , cat (%) rm,co ⁇ > (%) ⁇ E (%) ⁇ E+s (%) I v (A/m 3 ) Q (m7m J d) H 2 (%)
- Table II is a summary of MEC results for different metal cathodes (stainless steel, nickel and platinum) at an applied voltage of 0.9 V.
- the platinum sheet metal displayed only average performance compared to the other metals, being surpassed by both SS 304 and SS A286 in terms of hydrogen recoveries and energy efficiencies at an applied voltage of 0.9 V.
- Hydrogen concentrations at 0.6V were reduced to 172+13.2% H 2 (vs. 67.5+8.6% H 2 at 0.9 V), and methane concentrations increased (69.0+13.3% at 0.6V vs. 23.9+8.3% at 0.9 V).
- Ni 625 performed better than the other metals in terms of total hydrogen gas production at this lower applied voltage (6.61ml H 2 ), but the product gas was mainly methane (47.3% CH 4 , 40.8% H 2 , 11.9% CO 2 ).
- Platinum sheet metal produced only 11.2ml H 2 , with a gas composition of 49.8% CH 4 , 35.0% H 2 and 15.1% CO 2 .
- the Tafel plots for SS A286 and platinum are shown as typical examples in Figure 15, with two linear regions: one at high current densities (solid line) and one at low current densities (dashed line).
- the larger Tafel slopes and y-intercepts indicate better catalytic performance.
- the Tafel slope is a function of the transfer coefficient ⁇ c and the number of electrons n e transferred during the reaction.
- the y-intercept is controlled by the exchange current density JQ.
- the best cathodes based on Tafel slopes and y-intercepts were SS 286, Ni 625, Ni HX and platinum sheet metal, with slopes ranging from 3.68 to 4.31 decade A cm “2 V "1 and y- intercepts of 5.25-5.45A cm “2 at low current densities.
- V-intersect is the voltage at which the linear regressions intersect.
- the MEC should operate at a higher current density for a given overpotential.
- SS 286 has the lowest V-intersect (0.45 V) of all the metals tested. The ranking of the metal alloys based on electrochemical results thus confirms the same relative performance of the materials observed in MEC tests.
- Ni625 + NiO x 52 ⁇ 9 56 ⁇ 10 137 ⁇ 24 48 ⁇ 9 131+7 0.76 ⁇ 0.15 76 ⁇ 5 [00208] Both nickel oxide modified metals reached similar hydrogen production and recovery values, suggesting the sheet metal was less of a factor than the metal oxide surface for performance. For example, energy recovery based on electrical input (T ⁇ E ) increased from 3.1% (SS A286) and 31% (Ni 625) to 137% for both SS A286 and Ni 625 plus nickel oxide. Volumetric hydrogen production rates (Q) also improved from 0.01 (SS A286) and 0.1 (Ni 625) to 0.76m3 H 2 m ⁇ 3 day "1 for both nickel oxide modified metals.
- Cathodes were made by mixing the metal powder with NafionTM binder (Sigma-Aldrich, MO), and applying the mixture using a brush onto carbon cloth (surface area 7 cm 2 , 30% wet proof, BASF Fuel Cell, NJ).
- Platinum catalyst was used as a control (0.002 ⁇ m) (10 wt% on Vulcan XC-72; BASF Fuel Cell, NJ).
- Carbon cloth cathodes were prepared before electrodeposition by applying a base coat of carbon black (CB, 5 mg/cm ) and NAFION (33 ⁇ L/cm 2 ).
- Anodes were ammonia-treated graphite fiber brushes (25 mm diameter x 25 mm length, 0.22 m 2 surface area) made with a titanium wire twisted core.
- the anodes were first enriched with bacteria in microbial fuel cells (MFCs) containing conventional Pt-catalyst air cathodes that were inoculated using a solution from an acetate-fed MFC reactor that had been running for over two years.
- Duplicate reactors were operated in fed-batch mode using acetate (1 g/L) and a 50 mM phosphate buffer nutrient medium (pH 7) in a 30 0 C temperature room.
- the MFCs were modified to function as MECs by replacing the cathodes and sealing the end of the reactors from air, providing an oxygen-free environment.
- the voltage needed for MECs was supplied via an external power source (3645A; Circuit Specialists, Inc, Arizona).
- the reactors were drained, exposed to air for 15 minutes to minimize growth of methanogens (except as noted), refilled with substrate solution, and sparged with ultra high purity nitrogen gas for five minutes.
- the reactors were drained and refilled inside an anaerobic glove box (N 2 /H 2 volume ratio of 95/5). In this case, it was not necessary to sparge the reactors with nitrogen.
- a p is the surface area of a single particle
- V p the volume of particles calculated using the average particle radius, r
- p b p the bulk density of the particle (provided by the manufacturer)
- m the mass of catalyst added to the cathode.
- Table VI shows overpotentials vs SHE at current density of -3.2 log A/cm 2 for cathodes during third LSV scan at 2 mV/s. The surface area indicated in Table VI was calculated using equation (13).
- Table VII and Figures 19A and 19B show volumetric gas production, gas composition and current production for MECs using nickel cathodes, Ni 210, Ni 210+CB or eNiOx compared with Pt cathodes.
- Table VII Summary of MEC results for Ni210, Ni210+CB, eNiOx and Pt catalyst cathodes at an applied voltage of 0.6V, eighth cycle of operation.
- the cathodes include a current collector (stainless steel mesh, SS), catalyst (Pt), and diffusion layer (poly(dimethylsiloxane), PDMS) in one single cathode structure.
- the SS mesh used in this example (type 304 SS, 90x90, woven wire diameter 0.0055 inches, McMaster-Carr, OH) had 90x90 openings per square inch.
- PDMS was made using a 10:1 mixture of SYLGARD 184 silicone elastomer base and SYLGARD 184 silicone elastomer curing agent (Dow Corning, MI), that was further diluted to 10 wt% with toluene to decrease the solution viscosity.
- the PDMS (6.25xlO ⁇ 3 mg/cm 2 ) was applied with carbon black (1.56 mg/cm 2 ) to the side of the SS that faced the air.
- carbon black (1.56 mg/cm 2 )
- DLs additional diffusion layers
- cathodes were air dried for 2 hours, and then heated at 80 0 C for 30 min to crosslink the PDMS oligomers.
- a Pt catalyst layer (5 mg/cm 2 10 % Pt on Vulcan XC-72 with 33.3 ⁇ L/cm 2 of 5 wt% Nafion as binder) was applied to the SS mesh on the side facing the solution and the coated cathode was dried for at least 1 day at room temperature before being used.
- Cathodes were also prepared with no coating on the solution-facing side of mesh, or with only a carbon black layer (both with 2 PDMS/carbon DLs on the air side).
- Carbon cloth (E-Tek, Type B, 30% wet proofing, BASF Fuel Cell, Inc. NJ) was also tested as a cathode supporting material.
- One or more DLs of PDMS/carbon and the Pt catalyst were applied as described above for the metal mesh cathode.
- MFC Construction and Operation 5 mg/cm 2 10 % Pt on Vulcan XC-72 with 33.3 ⁇ L/cm 2 of 5 wt% Nafion as binder
- MFCs were single-chamber cubic- shaped reactors constructed as described in Example 2 with an anode chamber 4 cm long and 3 cm in diameter.
- the anode was an ammonia gas treated graphite fiber brush (25 mm diameter x 25 mm length; fiber type PANEX 33 160K, ZOLTEK (continuous carbon fiber manufactured from polyacrylonitrile (PAN) precursor having fiber diameter 7.2 ⁇ m (0.283 mil), no twist, 117,472 Denier (g/9000 m), 77 m/kg (114 ft/lb) yield and 0.06493 cm 2 (0.01006 in 2 ) average tow cross sectional area).
- PAN polyacrylonitrile
- All reactors were inoculated using a solution from an MFC operated for over 1 year (initially inoculated from the effluent of the primary clarifier of the local wastewater treatment plant).
- the medium contained acetate as the fuel (0.5 g/L for fixed resistance tests, and 1.0 g/L for polarization tests), and a phosphate buffer nutrient solution (PBS; conductivity of 8.26 mS/cm) containing: Na 2 HPO 4 , 4.58 g/L; NaH 2 PHO 4 -H 2 O 2.45 g/L; NH 4 Cl 0.31 g/L; KCl 0.13 g/L; trace minerals (12.5 mL/L) and vitamins (5 mL/L).
- PBS phosphate buffer nutrient solution
- LSV Linear sweep voltammetry
- Oxygen permeability was measured in terms of oxygen transfer coefficient as described in Cheng, S. et al, Electrochemistry Communications, 2006, 8:489-494.
- the 4-cm cubical reactor used in MFC tests was used for oxygen transport measurements.
- Dissolved oxygen concentrations were measured using a non-consumptive dissolved oxygen probe (FOXY, Ocean Optics, Inc., Dunedin, FL).
- Figure 22 is a graph showing voltage generation in an MFC using a SS mesh cathode and a Pt catalyst with 2 PDMS/carbon diffusion layers (M2) compared to an MFC using carbon cloth cathodes with 4 diffusion layers (CC4); using 5OmM PBS buffer and 0.5g/L sodium acetate.
- Figure 23 A is a graph showing power density in an MFC using a cathode containing SS mesh with Pt catalyst and 1-5 layers of PDMS/carbon DLs (M1-M5) as a function of current density (normalized to cathode surface area) obtained by varying the external circuit resistance (1000-50 ⁇ ).
- Figure 23B is a graph showing power density in an MFC using carbon cloth cathodes with Pt and the same DLs (CC1-CC5) as a function of current density (normalized to cathode surface area) obtained by varying the external circuit resistance (1000-50 ⁇ ).
- Error bars + SD in Figures 23 A and 23B are based on measurement of two duplicate reactors. Large differences in power production were observed based on polarization data.
- FIG. 24A is a graph showing LSV of MFCs including SS mesh cathodes with a Pt catalyst and 1-5 PDMS/carbon DLs (M1-M5).
- Figure 24B is a graph showing LSV of an MFC including cathode Ml compared with MFCs including cathodes having additional PDMS layers (MP2-MP5), each including Pt catalyst.
- Figure 24C is a graph showing LSV of an MFC including cathode M2 compared with an MFC including a cathode having a solution-facing side coating containing only carbon black (M2, no Pt), and a cathode with no coating on the solution-facing side (M2, no Pt, no CB).
- FIG. 25A is a graph showing the CE of an MFC including a SS mesh cathode with Pt catalyst and 1-5 layers of PDMS/carbon DLs (M1-M5) as a function of current density (normalized to cathode surface area) obtained by varying the external circuit resistance (1000-50 ⁇ ).
- Figure 25B is a graph showing the CE of MFCs including carbon cloth cathodes with Pt and 1-5 layers of PDMS/carbon DLs (CC1-CC5) as a function of current density (normalized to cathode surface area) obtained by varying the external circuit resistance (1000-50 ⁇ ). Error bars + SD in Figures 25A and 25B are based on measurement of two duplicate reactors. In each of these cases, the CE increased with current density.
- CEs of the SS mesh cathode ranged from 15% to 64% with single PDMS/carbon base layer, and only slightly increased when adding the second layer. The highest CE of 80% was obtained when 3 DLs were applied to this cathode.
- the carbon cloth cathodes CEs ranged from 13 to 46% with the first DL, with the highest value of 57% with 4 DLs.
- COD removals over a cycle of operation ranged from 90% to 95%, and there was no effect of the number of DLs or the type of material (SS or carbon cloth) on COD removal.
- Oxygen permeability of the cathodes
- FIG. 26 is a graph showing oxygen permeability of SS mesh cathodes including a Pt catalyst and PDMS/carbon DLs (M) or PDMS (MP) DLs upon PDMS/carbon base layer. Error bars + SD in Figure 26 are based on two or more measurements. With one base layer of PDMS/carbon on the SS mesh cathode, the oxygen mass transfer coefficient was 1.2 + 0.1 xlO " cm/s.
- SS mesh cathode with the base PDMS/carbon layer had an initial water evaporation loss of 5% of the water in the anode chamber each day. Water losses decreased with additional DLs, and were not detectable for cathodes with five DLs. For carbon cloth cathodes, the water losses were larger, with 10% to 5% per day with one to five DLs. However, as a biofilm developed on the cathodes after several cycles, water loss gradually decreased for both SS and carbon cloth cathodes by about 20-30%.
- PDMS mixed with carbon black is effective at reducing water losses and allowing oxygen transfer to the cathode catalyst.
- Use of a SS mesh cathode with two PDMS/carbon layers resulted in a maximum power density of 1610 + 56 mW/m (47.0 + 1.6 W/m 3 ).
- the best performance with a carbon cloth cathode was 1635 + 62 mW/m 2 with three PDMS/carbon layers.
- the recovery of the substrate as current was also improved using SS mesh cathodes, with CEs ranging from 15-67% for the SS cathodes, compared to 14- 51% for the carbon cloth cathodes for the above two cases.
- SS mesh cathodes had a CE as high as 80% with 3 PDMS/carbon DLs, over a current density range of 0.8 - 6.6 A/m .
- Carbon cloth cathodes with the same DL had CEs that ranged from 13% to 57% over similar current densities.
- CEs can be compared with those of carbon cloth cathodes with 4 PTFE DLs that had CEs ranging from 20% to 27% at current densities of 0.8-2.5 A/m 2 using a flat carbon cloth anode, and from 40% to 60% at 0.8-11 A/m 2 using a graphite fiber brush anode.
- a comparison of these results suggests that high CEs achieved with the SS mesh cathodes are partly due to high current densities.
- the cycle time is reduced, and thus the amount of oxygen that can diffuse into the reactor is substantially reduced in proportion to the cycle time.
- SS mesh cathode had a higher maximum CE than other materials, likely due to the lower oxygen permeability of the mesh DL.
- DLs diffusion layers
- PTFE polytetrafluoroethylene
- Figure 27 is a graph showing voltage generation in an MFC using cathodes containing SS U.S. standard mesh No. 50 or No. 70.
- compositions and methods described herein are presently representative of preferred embodiments, exemplary, and not intended as limitations on the scope of the invention. Changes therein and other uses will occur to those skilled in the art. Such changes and other uses can be made without departing from the scope of the invention as set forth in the claims.
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MX2011006971A MX2011006971A (en) | 2008-12-30 | 2009-12-30 | Cathodes for microbial electrolysis cells and microbial fuel cells. |
SG2011047800A SG172809A1 (en) | 2008-12-30 | 2009-12-30 | Cathodes for microbial electrolysis cells and microbial fuel cells |
AU2009335012A AU2009335012A1 (en) | 2008-12-30 | 2009-12-30 | Cathodes for microbial electrolysis cells and microbial fuel cells |
EP09837161A EP2382681A2 (en) | 2008-12-30 | 2009-12-30 | Cathodes for microbial electrolysis cells and microbial fuel cells |
CA2748603A CA2748603A1 (en) | 2008-12-30 | 2009-12-30 | Cathodes for microbial electrolysis cells and microbial fuel cells |
CN200980157601.0A CN102334221B (en) | 2008-12-30 | 2009-12-30 | For the negative electrode of microorganism electrolytic cell and microbiological fuel cell |
BRPI0923775A BRPI0923775A2 (en) | 2008-12-30 | 2009-12-30 | apparatus using combustible or electrolysis microbial cell and manufacturing method |
ZA2011/04812A ZA201104812B (en) | 2008-12-30 | 2011-06-29 | Cathodes for microbial electrolysis cells and microbial fuel cells |
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AU2009335012A1 (en) | 2011-08-18 |
WO2010078423A3 (en) | 2010-10-14 |
US20100119920A1 (en) | 2010-05-13 |
SG172809A1 (en) | 2011-08-29 |
CN102334221A (en) | 2012-01-25 |
BRPI0923775A2 (en) | 2019-09-24 |
CN102334221B (en) | 2016-05-04 |
IL213878A0 (en) | 2011-07-31 |
US10978713B2 (en) | 2021-04-13 |
US20190326604A1 (en) | 2019-10-24 |
EP2382681A2 (en) | 2011-11-02 |
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ZA201104812B (en) | 2012-06-27 |
CA2748603A1 (en) | 2010-07-08 |
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