Classifications

• • 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
  • H01M4/921—Alloys or mixtures with metallic elements
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B82—NANOTECHNOLOGY
  • B82Y—SPECIFIC USES OR APPLICATIONS OF NANOSTRUCTURES; MEASUREMENT OR ANALYSIS OF NANOSTRUCTURES; MANUFACTURE OR TREATMENT OF NANOSTRUCTURES
  • B82Y30/00—Nanotechnology for materials or surface science, e.g. nanocomposites
• • 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
  • H01M4/925—Metals of platinum group supported on carriers, e.g. powder carriers
• • 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
  • H01M4/925—Metals of platinum group supported on carriers, e.g. powder carriers
  • H01M4/926—Metals of platinum group supported on carriers, e.g. powder carriers on carbon or graphite
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
  • B01J23/8906—Iron and noble metals
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
  • B01J37/0018—Addition of a binding agent or of material, later completely removed among others as result of heat treatment, leaching or washing,(e.g. forming of pores; protective layer, desintegrating by heat)
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/02—Impregnation, coating or precipitation
  • B01J37/0215—Coating
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M8/00—Fuel cells; Manufacture thereof
  • H01M8/02—Details
  • H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
  • H01M8/023—Porous and characterised by the material
  • H01M8/0234—Carbonaceous material
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M8/00—Fuel cells; Manufacture thereof
  • H01M8/02—Details
  • H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
  • H01M8/023—Porous and characterised by the material
  • H01M8/0239—Organic resins; Organic polymers
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M8/00—Fuel cells; Manufacture thereof
  • H01M8/02—Details
  • H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
  • H01M8/023—Porous and characterised by the material
  • H01M8/0241—Composites
  • H01M8/0243—Composites in the form of mixtures
• • H—ELECTRICITY
  • H01—ELECTRIC ELEMENTS
  • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
  • H01M8/00—Fuel cells; Manufacture thereof
  • H01M8/02—Details
  • H01M8/0202—Collectors; Separators, e.g. bipolar separators; Interconnectors
  • H01M8/023—Porous and characterised by the material
  • H01M8/0241—Composites
  • H01M8/0245—Composites in the form of layered or coated products
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
  • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
  • Y02E60/30—Hydrogen technology
  • Y02E60/50—Fuel cells

Definitions

• the present invention relates to catalysts for use in electrochemical devices, such as fuel cells.
• the present invention relates to methods of forming supported nanoparticle catalysts having good catalytic properties.
• Fuel cells are electrochemical devices that produce usable electricity by the catalyzed combination of a fuel such as hydrogen and an oxidant such as oxygen. In contrast to conventional power plants, such as internal combustion generators, fuel cells do not utilize combustion. As such, fuel cells produce little hazardous effluent. Fuel cells convert hydrogen fuel and oxygen directly into electricity, and can be operated at higher efficiencies compared to internal combustion generators.
• a fuel cell such as a proton exchange membrane (PEM) fuel cell typically contains a membrane electrode assembly (MEA), formed by an electrolyte membrane disposed between a pair of catalyst layers, which are correspondingly disposed between a pair of gas diffusion layers.
• MEA membrane electrode assembly
• the respective sides of the electrolyte membrane are referred to as an anode portion and a cathode portion.
• hydrogen fuel is introduced into the anode portion, where the hydrogen reacts and separates into protons and electrons.
• the electrolyte membrane transports the protons to the cathode portion, while allowing a current of electrons to flow through an external circuit to the cathode portion to provide power.
• Oxygen is introduced into the cathode portion and reacts with the protons and electrons to form water and heat.
• Catalyst layers typically include catalyst particles (e.g., platinum particles) and have catalytic properties that are dependent on the surface areas of the catalyst particles. As such, to achieve desirable operation voltages in fuel cells, there is an ongoing need for catalyst particles that have high surface areas, and for methods of forming such catalyst particles.
• catalyst particles e.g., platinum particles
• the present invention relates to a method of forming a supported catalyst that has good catalytic properties.
• the method includes forming a colloidal suspension of platinum-iron catalyst nanoparticles, depositing at least a portion of the catalyst nanoparticles onto support particles, and removing at least a portion of the iron from the deposited catalyst nanoparticles.
• FIG. 1 is a flow diagram of a method for forming a supported catalyst.
• FIG. 2 is a flow diagram of a method for forming a fuel cell containing a supported catalyst.
• FIG. 3 is a graph representing potentiodynamic polarization curves for
• FIG. 1 is a flow diagram of method 10 for forming a supported catalyst that may be used in a variety of industrial catalytic processes.
• Method 10 includes steps 12-20, and initially involves forming a colloidal suspension of unprotected catalyst nanoparticles in a solvent, where the catalyst nanoparticles include platinum (Pt) and iron (Fe) (step 12).
• the colloidal suspension is formed by initially mixing a platinum-containing halogen and an iron-containing halogen in the solvent.
• the pH of the resulting mixture is then increased by introducing a basic compound (e.g., sodium hydroxide) into the mixture at a controlled rate.
• a basic compound e.g., sodium hydroxide
• suitable pH levels for forming the colloidal suspension include pHs of at least about 5, with particularly suitable pHs including at least about 7, and with even more particularly suitable pHs including at least about 10.
• the increased pH causes the platinum and iron to disassociate from the halogens, allowing platinum and iron particles to associate together to form the catalyst nanoparticles.
• the mixture becomes an opaque white color until a pH of about 11-12 is reached. At this point, the mixture becomes a transparent, yellow color.
• the mixture is then heated to disperse the catalyst nanoparticles in the solvent without the use of protecting agents (e.g., surfactants, polymers, and organic ligands).
• protecting agents e.g., surfactants, polymers, and organic ligands.
• suitable heating temperatures include temperatures of at least about 150 0 C, with particularly suitable temperatures including at least about 190 0 C.
• the resulting colloidal suspension becomes a transparent, dark brown color, which shows that the catalyst nanoparticles are homogenously dispersed in the solvent.
• Support particles are then introduced and mixed into the colloidal suspension (step 14). The support particles may be pre-sheared to increase surface areas and break up agglomerates.
• the support particles are mixed in the colloidal suspension, at least a portion of the catalyst nanoparticles are then deposited onto the support particles (step 16).
• This is performed by altering the stability of the catalyst nanoparticles in the solvent.
• the stability is altered by reducing the pH of the colloidal suspension at a controlled rate, which causes a portion of the catalyst nanoparticles to condense and bond to the outer surfaces of the support particles.
• the pH of the colloidal suspension may be reduced by introducing an acidic compound (e.g., nitric acid) into the colloidal suspension at a controlled rate.
• suitable pH levels for depositing the catalyst nanoparticles onto the support particles include pHs of less than about 5.
• At least a portion of the iron is then removed from the deposited catalyst nanoparticles (step 18).
• the iron removal is performed by altering the solubility of the iron in the solvent, which leaches the iron from the deposited catalyst nanoparticles.
• the solubility of the iron is altered by lowering of the pH of the colloidal suspension.
• the pH of the colloidal suspension is lowered for depositing the catalyst nanoparticles onto the support particles, the lowered pH also leaches iron from the catalyst nanoparticles in a substantially simultaneous manner.
• the iron continues to leach from the catalyst nanoparticles, rendering the resulting catalyst nanoparticles at least partially porous.
• the increased exposed surface areas of the platinum portions correspondingly increases the catalytic properties of the resulting supported catalysts.
• the solubility of the iron is altered by applying an electrical potential to the solvent of the colloidal suspension after the catalyst nanoparticles are deposited onto the support particles.
• the electrical potential also causes at least a portion of the iron to leach from the catalyst nanoparticles, thereby increasing the exposed surface areas of the platinum portions of the catalyst nanoparticles.
• an electrical potential may be applied to the solvent of the colloidal suspension in combination with the reducing the pH of the colloidal suspension to leach the iron from the catalyst nanoparticles.
• the amount of iron removed from the catalyst nanoparticles generally depends on the initial iron concentration and on the duration of the exposure to the solubility-altering conditions.
• suitable amounts of iron removed from the catalyst nanoparticles include at least about 50% of the initial iron concentration in the catalyst nanoparticles, with particularly suitable amounts of iron removed including at least about 75% of the initial iron concentration.
• some iron remains in the catalyst nanoparticles during the formation process of method 10, which allows the remaining iron to function as a catalyst promoter.
• the resulting supported catalyst includes catalyst nanoparticles having small average particle sizes with low standard deviations in particle sizes.
• suitable average particle sizes of the catalyst nanoparticles in the supported catalyst, after the iron removal includes particle sizes of about 2.0 nanometers or less, with suitable standard deviations of about 0.5 nanometers or less.
• the supported catalyst formed pursuant to method 10 is suitable for use in a variety of industrial catalytic processes, such as hydrogenation, hydrosilylation, and petroleum refining.
• the supported catalyst is particularly suitable for use in catalyst layers of electrochemical devices, such as PEM fuel cells.
• the increased surface area of the catalyst nanoparticles correspondingly increases the catalytic properties of the supported catalyst, thereby increasing the attainable operation voltages.
• FIG. 2 is a flow diagram of method 22 for forming a fuel cell containing the supported catalyst.
• Method 22 includes steps 24-36, where steps 24-30 are the same as steps 12-18 of method 10 (shown in FIG. 1 and discussed above).
• the resulting supported catalyst is then used to form a catalyst ink (step 32).
• the catalyst ink is formed by combining the supported catalyst with a carrier fluid (e.g., water) and a polymer solution, such as 10% sulfonated tetrafluorethylene copolymer solution commercially available under the trade designation "NAFION 1100" from DuPont Chemicals, Wilmington, DE.
• a carrier fluid e.g., water
• a polymer solution such as 10% sulfonated tetrafluorethylene copolymer solution commercially available under the trade designation "NAFION 1100” from DuPont Chemicals, Wilmington, DE.
• NAFION 1100 10% sulfonated tetrafluorethylene copolymer solution commercially available
• the catalyst ink is then coated onto a layer of a fuel cell or other electrochemical device (step 34).
• the fuel cell layer is a gas diffusion layer.
• the fuel cell layer is a polymer electrolyte membrane.
• the supported catalyst may be coated to function as an anode catalyst layer, a cathode catalyst layer, or a combination of anode and cathode catalyst layers.
• the supported catalyst may be coated on a fuel cell layer in a variety of manners, such as by extrusion coating, knife coating, notch coating, and hand coating.
• the fuel cell layer is a gas diffusion layer (e.g., carbon paper) that is treated for hydrophobic properties, and is pre-coated with a conductive material (e.g., carbon black) to increase the bond between the gas diffusion layer and the catalyst ink.
• a gas diffusion layer e.g., carbon paper
• a conductive material e.g., carbon black
• the catalyst ink is coated on the layer of conductive material to function as a catalyst layer for the fuel cell.
• the catalyst ink and the fuel cell layer are dried (step 36).
• the resulting catalyst-coated layer is then assembled with additional layers to form the fuel cell.
• the coated gas diffusion layer is then secured to a PEM such that coating of catalyst ink is disposed between the gas diffusion layer and the polymer electrolyte membrane.
• the supported catalyst of the catalyst ink provides a first catalytic site where hydrogen or reformate gases react and separate into protons and electrons (i.e., an anode catalyst layer) and/or provides a second catalytic site where oxygen reacts with the electrons and protons to form water and heat (i.e., a cathode catalyst layer).
• a first catalytic site where hydrogen or reformate gases react and separate into protons and electrons
• a second catalytic site where oxygen reacts with the electrons and protons to form water and heat
• the small particle sizes and increased exposed surface areas of the platinum nanoparticles increases the catalytic properties of the supported catalyst, thereby increasing the attainable operation voltages of the fuel cell.
• the colloidal suspension is formed in steps 12 and 24 of methods 10 and 22 by initially mixing a platinum-containing halogen and an iron- containing halogen in the solvent.
• platinum-containing halogens include platinum-based chlorides, such as dihydrogen hexachloroplatinate (H 2 PtCl 6 ), platinum chlorides (e.g., PtCl 2 and Pt 6 CU 2 ), hydrated compounds thereof, and combinations thereof.
• suitable iron-containing halogens include iron-based chlorides, such as iron trichloride (FeCIs) and hydrated compounds thereof.
• suitable molar concentrations of platinum in the catalyst nanoparticles of the colloidal suspension include at least about 50% platinum, with particularly suitable molar concentrations ranging from about 50% to about 75%, where the residual concentrations constitute iron.
• suitable solvents of the colloidal suspension include polyalcohols, such as alkylene glycols, with particularly suitable alkylene glycols including ethylene glycol, propylene glycol, and combinations thereof.
• the solvent may also include water and low-molecular weight alcohols (e.g., isopropanol), where the polyalcohol desirably constitutes at least about 75 weight percent of the solvent, and more desirably constitutes at least about 90 weight percent of the solvent.
• suitable support particles include porous materials, such as carbon particles (e.g., carbon black), silica particles, zirconia particles, metal oxide particles, and combinations thereof.
• suitable carbon support particles include those commercially available under the trade designations "SHAW C-55" from Chevron Texaco Corp., Houston, TX; and "VULCAN XC-72" and “BLACK PEARL 2000", both from Cabot Corp., Waltham, MA.
• Example 1 An MEA of Example 1 , which included a supported catalyst of the present invention as an anode catalyst layer, was prepared pursuant to the following procedure:
• the supported catalyst was prepared by initially combining 0.58 grams (2.2 millimole) of iron chloride hexahydrate (FeCl3*6H 2 O), 1.0 gram (2.2 millimole) of dihydrogen hexachloroplatinate solution (H 2 PtC ⁇ xH 2 O), and 200 grams of ethylene glycol. The combined components were then mixed for 15 minutes in a 250-milliliter flask to form a glycol mixture that contained an initial platinum to iron (Pt-Fe) molar ratio of 1 :1.
• a small jar was filled with 0.95 grams of carbon black support particles (trade designated “VULCAN XC-72" carbon black from Cabot Corp., Waltham, MA) and 25 grams of ethylene glycol.
• the support particle mixture was then sheared for two minutes at 30,000 rpm with a mechanical homogenizer (trade designated "HANDISHEAR” homogenizer from VirTis Company, Gardiner, NY).
• the sheared support particle mixture was then transferred into another jar containing 242.0 grams of the colloidal suspension.
• the combined colloidal suspension was then sheared with the mechanical homogenizer for an additional 20 seconds.
• nitric acid HNO3
• HNO3 nitric acid
• the combined colloidal suspension was then stirred overnight. This caused the catalyst nanoparticles of the colloidal suspension to deposit on the support particles, and also altered the stability of the iron, causing iron to begin leaching from the catalyst nanoparticles.
• 10 milliliters of the nitric acid was then incrementally added while stirring, and the combined colloidal suspension was then stirred for another hour. This further altered the stability of the iron, causing additional portions of the iron to leach from the deposited catalyst nanoparticles.
• the composition of the resulting supported catalyst was estimated to include about 30% by weight platinum based on the amount of iron chloride hexahydrate, dihydrogen hexachloroplatinate solution, and carbon black added.
• the supported catalyst was then used to prepare a catalyst ink pursuant to the following procedure.
• a mixture was prepared by combining 1.0 gram of the supported catalyst, 4.0 grams of water, and 4.0 grams of a 10% PFSA solution (10% perfluorosulfonic acid/polytetrafluoroethylene (PTFE) copolymer in the acid form solution commercially available under the trade designation "NAFION 1100" from
• a gas diffusion layer was initially prepared by dipping a 50-cm2 piece of carbon paper (275- micrometer thick carbon paper commercially available under the trade designation "TORAY 2903" from Toray Industries, Inc., Tokyo, Japan) in a 5% PTFE dispersion (diluted 60% polytetrafluoroethylene aqueous dispersion commercially available under the trade designation "TEFLON", Cat. No. T-30, from DuPont Chemicals, Wilmington DE), and then drying the dipped carbon paper in an air oven at 5O 0 C - 6O 0 C to drive off the water.
• a 50-cm2 piece of carbon paper 275- micrometer thick carbon paper commercially available under the trade designation "TORAY 2903” from Toray Industries, Inc., Tokyo, Japan
• a 5% PTFE dispersion diluted 60% polytetrafluoroethylene aqueous dispersion commercially available under the trade designation "TEFLON", Cat. No. T-30, from DuPont Chemicals, Wilmington DE
• the gas diffusion layer was then pre-coated with a carbon black dispersion pursuant to the following procedure.
• An aqueous dispersion of carbon black particles (trade designated "VULCAN XC-72" carbon black from Cabot Corp., Waltham, MA) was prepared under high-shear stirring using a Roth mixer equipped with a 7.6-centimeter blade at 4,500 rpm.
• an additional batch of the 5% PTFE dispersion was prepared, and the carbon black dispersion was then added to the 5% PTFE dispersion with stirring.
• the resulting mixture was filtered under vacuum to obtain a retentate that was approximately 20% solids mixture of water, PTFE, and carbon black.
• the pasty mixture was then treated with approximately 3.5% by weight of a surfactant (trade designated "TRITON X-100" from Union Carbide Corp., Danbury, CT), followed by the addition of isopropyl alcohol such that the weight proportion of isopropyl alcohol to the pasty mixture was 1.2: 1.
• a surfactant trade designated "TRITON X-100” from Union Carbide Corp., Danbury, CT
• isopropyl alcohol such that the weight proportion of isopropyl alcohol to the pasty mixture was 1.2: 1.
• the diluted mixture was again stirred at high shear using a three- bladed VersaMixer having an anchor blade at 80 rpm, a dispersator at 7000 rpm, and a rotor-stator emulsifier at 5000 rpm, for 50 minutes at 1O 0 C.
• the resulting dispersion thus was then coated onto the dried gas diffusion layer at a wet thickness of approximately 0.050 millimeters using a notch bar coater.
• the dispersion was then dried overnight at 23 0 C to remove the isopropyl alcohol, and then dried in an oven at 38O 0 C for 10 minutes.
• the pre-coated gas diffusion layer was then hand-coated (i.e., brushed) with the catalyst ink containing the supported catalyst in an amount yielding 0.4 milligrams of platinum per square centimeter (plus any iron remaining in the catalyst nanoparticles) after drying.
• the coated gas diffusion layer was then dried in a vacuum oven at HO 0 C for 30 minutes to form the catalyst-coated gas diffusion layer. 4.
• a PEM of the MEA of Example 1 was prepared by notch-coating an aqueous dispersion of the above-discussed 10% PFSA solution onto a backing of polyvinylchloride-primed polyethylene terephthalate (3M Corporation, St. Paul, MN) at a loading such that the final, dried film was approximately 25 micrometers thick.
• the cast film was first passed through a drying oven at 5O 0 C - 6O 0 C (with a residence time of 3 - 4 minutes), and then dried at 13O 0 C for 4 minutes in an air-impingement oven to remove the remainder of the solvent and to anneal the PFSA film. The dried film was then peeled from the backing for subsequent use.
• the PEM was then sandwiched between the above-formed catalyst-coated gas diffusion layer (cathode portion) and a second catalyst-coated gas diffusion layer (anode portion), where the second catalyst-coated gas diffusion layer contained a standard platinum-ruthenium/carbon black catalyst.
• the gas diffusion layers were oriented such that the catalyst coatings faced the PEM.
• a gasket of TEFLON-coated glass fiber was also placed on each side.
• the catalyst-coated gas diffusion layers were smaller in surface area than the PEM, and each fit in the window of the respective gasket.
• the thickness height of the gasket was 70% of the height of the catalyst-coated gas diffusion layers, to allow a 30% compression of the catalyst-coated gas diffusion layers when the entire MEA assembly was pressed.
• the MEA assembly was pressed in a Carver Press (Fred Carver Co., Wabash, IN) for 10 minutes at a pressure of 2.8 megapascals (i.e., 0.20 tons/inch 2 ) and at a temperature of 13O 0 C.
• the polyimide sheets were then peeled away leaving the finished five-layer MEA of Example 1 containing the supported catalyst as an anode catalyst layer.
• Example 2 An MEA of Example 2 was prepared pursuant to the procedure discussed above for Example 1, except that the supported catalyst was prepared by initially combining 0.36 grams (1.3 millimole) of iron chloride hexahydrate, 1.0 gram (2.2 millimole) of dihydrogen hexachloroplatinate solution, and 200 grams of ethylene glycol. The combined components were then mixed for 15 minutes in a 250-milliliter flask to form a glycol mixture that contained an initial platinum to iron (Pt-Fe) molar ratio of about 2:1.
• Pt-Fe platinum to iron
• Example 3 An MEA of Example 3 was prepared pursuant to the procedure discussed above for Example 2, except that the pre-coated gas diffusion layer was hand-coated (i.e., brushed) with the catalyst ink containing the supported catalyst in an amount yielding 0.24 milligrams of platinum per square centimeter (plus any iron remaining in the catalyst nanoparticles). As such, the anode catalyst layer of the MEA of Example 3 contained a lower amount of the supported catalyst compared to the anode catalyst layer of the MEA of Example 2.
• An MEA of Comparative Example A was prepared pursuant to the following procedure, which was similar to the procedure for Example 2, except that the iron was not removed from the catalyst nanoparticles of the supported catalyst.
• the supported catalyst was prepared by initially combining by initially combining 0.36 grams (1.3 millimole) of iron chloride hexahydrate, 1.0 gram (2.2 millimole) of dihydrogen hexachloroplatinate solution, and 200 grams of ethylene glycol. The combined components were then mixed for 15 minutes in a 250-milliliter flask to form a glycol mixture that contained an initial platinum to iron (Pt-Fe) molar ratio of about 2:1.
• Pt-Fe platinum to iron
• a small jar was then filled with 0.95 grams of carbon black support particles (trade designated “VULCAN XC-72" carbon black from Cabot Corp., Waltham, MA) and 25 grams of ethylene glycol.
• the support particle mixture was then sheared for two minutes at 30,000 rpm with a mechanical homogenizer (trade designated "HANDISHEAR” homogenizer from VirTis Company, Gardiner, NY).
• the sheared support particle mixture was then transferred into another jar containing 242.0 grams of the colloidal suspension.
• the combined colloidal suspension was then sheared with the mechanical homogenizer for an additional 20 seconds.
• the combined colloidal suspension was then stirred overnight, allowing the catalyst nanoparticles of the colloidal suspension to deposit on the support particles. However, because the stability of the iron was not altered, the iron did not leach from the catalyst nanoparticles.
• 200 milliliters of deionized water was then added to the combined colloidal suspension, and the combined colloidal suspension was filtered and washed with copious amounts of deionized water.
• the resulting wet catalyst cake was then dried overnight at HO 0 C under a vacuum.
• the composition of the resulting supported catalyst was estimated to include about 30 weight percent platinum based on the amount of iron chloride hexahydrate, dihydrogen hexachloroplatinate solution, and carbon black added.
• the MEAs of Examples 1-3 and Comparative Examples A were each quantitatively measured for potentiodynamic performance pursuant to the following procedure.
• the given MEA was mounted in a test cell station (Fuel Cell Technologies, Inc., Albuquerque, NM), which included a variable electronic load with separate anode and cathode gas handling systems to control gas flow, pressure, and humidity.
• the electronic load and gas flow were computer controlled.
• Fuel cell polarization curves were obtained under the following test parameters: an electrode of area 50 square centimeters, a cell temperature of 7O 0 C, and anode gas pressure (gauge) of 0 psig, and anode hydrogen flow rate, 800 standard cubic centimeters/minute, an anode humidification temperature of 7O 0 C, a cathode gas pressure (gauge) of 0 psig, a cathode air flow rate of 1,800 standard cubic centimeters/minute, and a cathode humidification temperature of 7O 0 C.
• the cathode gas was a reformate fuel containing 45% hydrogen, 33% nitrogen, 22% CO 2 , and 50 parts-per-million CO, with a 2% of total flow air bleed.
• Humidification of the anode and the cathode gas streams was provided by passing the gas through sparge bottles maintained at the stated temperatures.
• the fuel cell was brought to operating conditions at 7O 0 C under gas and air flows. Test protocols were initiated after 12 hours of operation, at which time the test parameters were measured. Table 1 provides the potentiodynamic polarization scans for the MEAs of Examples 1-3 and Comparative Example A.
• the data in table 1 show the superior catalytic properties of the supported catalysts formed pursuant to the method the present invention.
• a comparison of the results between Example 2 and Comparative Example A show that the removal of the iron from the catalyst nanoparticles of Example 2 increases the catalytic properties of the supported catalyst used in the MEA of Example 2. As discussed above, this is believed to be due to the increased surface area of the platinum in the deposited catalyst nanoparticles.
• the results of Examples 1 and 3 show that lower Pt-Fe ratios (1 :1) and lower catalyst loadings (0.24 mg/cm 2 ) also provide good catalytic properties.
• FIG. 3 is a graph representing potentiodynamic polarization curves for the
• Example 3 MEAs of Examples 1-3 and Comparative Example A, in which hydrogen was used in place of the reformate gas. While the distinctions between the results of Example 2 and Comparative Example A are greater with the use of reformate gas, the data shown in FIG. 3 also illustrate the good catalytic properties of the supported catalysts of the present invention.

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• 2006
  • 2006-07-11 US US11/456,724 patent/US20090215615A1/en not_active Abandoned
• 2007
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  • 2007-07-03 EP EP07812587A patent/EP2043782A1/en not_active Withdrawn
  • 2007-07-03 JP JP2009519590A patent/JP2009543681A/ja not_active Withdrawn
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