CA1305212C - Method for operating a fuel cell on carbon monoxide containing fuel gas - Google Patents
Method for operating a fuel cell on carbon monoxide containing fuel gasInfo
- Publication number
- CA1305212C CA1305212C CA000569048A CA569048A CA1305212C CA 1305212 C CA1305212 C CA 1305212C CA 000569048 A CA000569048 A CA 000569048A CA 569048 A CA569048 A CA 569048A CA 1305212 C CA1305212 C CA 1305212C
- Authority
- CA
- Canada
- Prior art keywords
- carbon monoxide
- catalyst
- fuel gas
- gas
- oxygen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Classifications
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
- H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
-
- 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
Abstract
ABSTRACT
The invention disclosed relates to a method for operating a low-temperature fuel cell on a fuel gas mixture containing carbon monoxide. The gas mixture is mixed with an oxygen-containing gas, such as air, in a molar ratio of oxygen to carbon monoxide of about 0.5 to 3:1. The resulting gas mixture is then contacted with a catalyst, such as platinum, at a reaction temperature of about 10 to 160°C and pressure of about atmospheric to 500 psig. Under these conditions selective oxidation of the carbon monoxide occurs. This novel method permits the use of carbon monoxide-containing fuel gases in low temperature fuel cells employing platinum group metal electrodes without poisoning the electrodes.
The invention disclosed relates to a method for operating a low-temperature fuel cell on a fuel gas mixture containing carbon monoxide. The gas mixture is mixed with an oxygen-containing gas, such as air, in a molar ratio of oxygen to carbon monoxide of about 0.5 to 3:1. The resulting gas mixture is then contacted with a catalyst, such as platinum, at a reaction temperature of about 10 to 160°C and pressure of about atmospheric to 500 psig. Under these conditions selective oxidation of the carbon monoxide occurs. This novel method permits the use of carbon monoxide-containing fuel gases in low temperature fuel cells employing platinum group metal electrodes without poisoning the electrodes.
Description
0~;~12 Thi-s ;l~ven~lon relates to fuel cells, and in particular, to the use of càrbon monoxide containing fuel gas in fuel cells.
Fuels for fuel cells include various hydrocarbons such as natural gas,~;and ~ethanol. These fuels are typically made more reactive by subjecting the~ to a process known as "steam reformation" ie. by reacting them with steam they are converted to a gaseous mixture comprising hydrogen, carbon dioxide, carbon monoxide and related impurities.
Unfortunately, carbon monoxide is a poison to the typical catalyst employed in fuel cell electrodes, namely, noble metals, particularly platinum. For example, steam reformed methanol provides a fuel gas mixture comprising about 0.3~ C0, 25%
C02, with the balance H2. This "reformate" gas mixture fed to a fuel cell operating at about 100C and containing platinum as the only active catalyst material in its fuel (anode) electrode, results in a decay of cell power output to zero in a matter of minutes.
Some resistance to this "poisoning" effect has been achieved by using different electrode materials. For example, in United States Patent No. 3,393,100 of 16 July 1968, in the name of Leonard W. Niedrach, an anti-poisoning agent such as tungsten dioxide is included in the electrode material. This approach involves management of the carbon monoxide within the cell. Using this type of construction power outputs decay significantly over time.
Carbon monoxide resistance may also be achieved by operating the fuel cell at higher temperatures of the order of 160C to 200C, as is done in the case of phosphoric acid fuel ., . , . , ., , ,, , --l~QSZ12 cells. However, when the electrolyte is provided in a solid polymer membrane such as Dupont's Nafio ~, maintenance of membrane conductivity (a function of hydration) and chemical and physical stability are compromised at these higher temperatures.
Applicants have now found that the carbon monoxide poisoning problem can be managed externally of the cell by selectively oxidizing the carbon monoxide in the fuel gas mixture externally of the cell, prior to introduction of the fuel gas into the cell. The resulting conditioned fuel gas is substantially carbon monoxide-free, i.e. C0 levels in the conditioned fuel gas are reduced to trace amounts of the order of 2 to 10 ppm. The conditioned fuel gas is then fed to the fuel cell.
According to the invention, in a method for operating a low-temperature fuel cell, said fuel cell including a solid polymer electrolyte and a noble metal material in the anode, on a fùel gas containing carbon monoxide, the improvement comprising the sequential steps of:
(a) reacting the fuel gas with a suitable oxygen-containing gas in an amount providing a molar ratio of oxygen to carbon monoxide of about 0.5 to 3:1;
(b) contacting the resulting fuel gas mixture with a suitable catalyst at a reaction temperature of about 10 to 160C
and pressure of about atmospheric to 500 psig, to selectively convert carbon monoxide to carbon dioxide, whereby carbon monoxide levels in the fuel gas are reduced to trace amounts of about 2 to 10 parts per million; and (c) feeding the resulting sub~tantially carbon monoxide-free fuel gas to the fuel cell.
~3~SZl'~
In the drawing which illustrates the preferred embodiment of the invention, the figure is a flow diagram which illustrates the operation of the method according to the invention.
Referring to the figure, a feed gas mixture, such as that resulting from the reforming of a hydrocarbon fuel such as natural gas or methanol, containing from 0.1 to 3 volume percent CO, from 50 to 90% hydrogen and from 10 to 50~ C02, either dry, partially saturated or saturated with water is mixed with a suitable oxygen-containing gas, such as air or pure oxygen in an amount providing a molar ratio of oxygen to CO of from about 0.5 to 3:1. This fuel gas mixture is then fed through a packed column containing a supported platinum group metal catalyst. The gas mixture is contacted with the catalyst in the column at a pressure of from about atmospheric to 500 psig and at temperatures from about 10 to 160C. Oxidation of the CO to CO2 occurs as shown in equation (1) below. Excess oxygen i8 completely consumed by conver~ion to water.
Selectivity for the CO oxidation is improved by carrying out the oxidation at these lower temperatures. At higher temperature~, from about 200 to 400C, the reaction between hydrogen and CO/C02 (equation~ (2) and (3) below) is favoured to form methane and water (methanation). ~here high proportions of CO and CO2 are present, large quantities of hydrogen are consumed as shown in equations (2) and (3). For this reason, operation at high temperatures which favours methanation is undesirable.
13C~SZl~
~elective Oxidation CO + ~O2t )CO2 (1) Methanation CO + 3H2 ~--~ CH4 + H2O (2) C2 + 4H2~ ~ CH4 + 2H2O (3) Space velocities through the column can be in the order of 1,000 to 50,000 cubic feet of gas per hour per cubic foot of catalyst, with 5,000 to 30,000 being preferred.
The catalyst can be platinum, rhodium or ruthenium on a suitable support such as alumina, silica, silica gel, diatomaceous earth or clay. Platinum on alumina is preferred. The catalyst metal may be present in the range of about 0.01 to 5% by weight, based upon the weight of the catalytic metal and support, preferably from about 0.05 to 2%. The supported catalyst may be prepared by treating the support with a solution of a suitable metal compound and then reducing the metal compound to metal.
As shown in the figure, the conditioned fuel gas mixture from the column contains CO2, H2, water and only trace amounts of CO ie. from 2 to 10 ppm CO. The conditioned gas mixture is then fed directly to an acid fuel cell. Acid fuel cells are unaffected by CO2 which simply acts as a diluent to the fuel gas. Because levels of CO have been significantly reduced, cell performance dramatically improves as will be apparent hereafter.
Hydrogen from the product gas is consumed at the fuel cell anode releasing protons and electrons as shown in equation (4) below: The protons are injected into the fuel cell electrolyte. The electrons travel outside of the cell to the cell l~OSi~i2 terminal through a load bank back to the cathode terminal and into the cell. At the cathode, oxygen, electrons from the load and protons from the electrolyte combine to form water as shown in equation (5) below.
, Anode Reaction H2 -~ 2H+ + 2e (4) Cathode Reaction ~2 + 2H+ + 2e __~ H20 (5) Example 1 A solid polymer fuel cell was constructed similar to that described in United States Patent No. 3,297,484 of 10 January 1967 in the name of ~eonard W. ~iedrach. The active cell area was about 32 cm2. The solid polymer membrane used for the membrane/electrode assembly was DuPont's Nafio ~ 117 (a fluorinated cationic exchange membrane). In the case of the fuel electrode (the anode) a mixture of platinum and tungsten oxide ~81% Pt, 19~ ~2) was used. Platinum loading was 4 mg/cm2.
In the case of the cathode (air) electrode, platinum alone was used at a loading of 4 mg/cm2.
The fuel cell was fed UHP H2 and air at about atmospheric pressure. Performance output was 0.69V @ 220 mA/cm2 at 55C after about 5 hours operation under a constant 100 mOHM
resistance load. The fuel gas was then switched from UHP H2 to simulated reformed methanol (0.275% CO, 25% CO2, balance H2).
Three hours after the switch to reformate, performance output was 0.49V @ 157 mA/cm2 at 55C under a 100 mOHM resistance load.
Performance after 24 hours was 0.31V @ 97 mA/cm2 at 47C. The results are summarized in Table 1 below. Power density on 13Q~lZ
unconditioned reformate/air after 3 hours operation was 51% of that on hydrogen/air. After 24 hours, power density was only 20 of that of hydrogen/air.
TAsLE I
Hydrogen/Air & Unconditioned Reformate/Air Performance Atmospheric Pressure - 100 mOHM Resistive Load Current Power Volts Density Temperature Time Density (V) (mA/cm2) (C) (hrs)(mW/cm2) 0.69 219 55 4.5 151 Switch from ~HP H2 to Reformate 0.49 157 55 7.5 77 0.31 97 47 28.5 30 Example 2 A selective oxidation column was constructed using a jacketed glass tube 0.5" I.D., 8" long with about 20 ml volume.
The column was filled with 1/8", 0.5% platinum on alumina cylinders. A mixing tee was provided on the inlet to the column where fuel gas and air could be mixed and then fed to the column.
Reformate (0.275% CO, 25% CO2, Balance H2) and air were fed to the column such that the 2 to CO molar ratio was in the range of 1:1 to 2:1. The exit gas from the column was fed directly to the fuel cell described in example 1. Table II
~3~SZl;~
summarizes the test results. After 22 hours operation of conditioned reformate/air, power density was 81% of that of hydrogen/air. This represen~s a four fold improvement over unconditioned reformate/air performance described in Example 1.
TABLE II
Conditioned Reformate/Air Performance Atmospheric Pressure - 100 mOHM Resitive Load . _ _ Current Power Volts Density Temperature Time Density (V) (mA/cm2) (C) (hrs)(mW/cm~) .
0.64 203 55 2 130 0.63 201 55 6 127 0.62 197 55 22 122
Fuels for fuel cells include various hydrocarbons such as natural gas,~;and ~ethanol. These fuels are typically made more reactive by subjecting the~ to a process known as "steam reformation" ie. by reacting them with steam they are converted to a gaseous mixture comprising hydrogen, carbon dioxide, carbon monoxide and related impurities.
Unfortunately, carbon monoxide is a poison to the typical catalyst employed in fuel cell electrodes, namely, noble metals, particularly platinum. For example, steam reformed methanol provides a fuel gas mixture comprising about 0.3~ C0, 25%
C02, with the balance H2. This "reformate" gas mixture fed to a fuel cell operating at about 100C and containing platinum as the only active catalyst material in its fuel (anode) electrode, results in a decay of cell power output to zero in a matter of minutes.
Some resistance to this "poisoning" effect has been achieved by using different electrode materials. For example, in United States Patent No. 3,393,100 of 16 July 1968, in the name of Leonard W. Niedrach, an anti-poisoning agent such as tungsten dioxide is included in the electrode material. This approach involves management of the carbon monoxide within the cell. Using this type of construction power outputs decay significantly over time.
Carbon monoxide resistance may also be achieved by operating the fuel cell at higher temperatures of the order of 160C to 200C, as is done in the case of phosphoric acid fuel ., . , . , ., , ,, , --l~QSZ12 cells. However, when the electrolyte is provided in a solid polymer membrane such as Dupont's Nafio ~, maintenance of membrane conductivity (a function of hydration) and chemical and physical stability are compromised at these higher temperatures.
Applicants have now found that the carbon monoxide poisoning problem can be managed externally of the cell by selectively oxidizing the carbon monoxide in the fuel gas mixture externally of the cell, prior to introduction of the fuel gas into the cell. The resulting conditioned fuel gas is substantially carbon monoxide-free, i.e. C0 levels in the conditioned fuel gas are reduced to trace amounts of the order of 2 to 10 ppm. The conditioned fuel gas is then fed to the fuel cell.
According to the invention, in a method for operating a low-temperature fuel cell, said fuel cell including a solid polymer electrolyte and a noble metal material in the anode, on a fùel gas containing carbon monoxide, the improvement comprising the sequential steps of:
(a) reacting the fuel gas with a suitable oxygen-containing gas in an amount providing a molar ratio of oxygen to carbon monoxide of about 0.5 to 3:1;
(b) contacting the resulting fuel gas mixture with a suitable catalyst at a reaction temperature of about 10 to 160C
and pressure of about atmospheric to 500 psig, to selectively convert carbon monoxide to carbon dioxide, whereby carbon monoxide levels in the fuel gas are reduced to trace amounts of about 2 to 10 parts per million; and (c) feeding the resulting sub~tantially carbon monoxide-free fuel gas to the fuel cell.
~3~SZl'~
In the drawing which illustrates the preferred embodiment of the invention, the figure is a flow diagram which illustrates the operation of the method according to the invention.
Referring to the figure, a feed gas mixture, such as that resulting from the reforming of a hydrocarbon fuel such as natural gas or methanol, containing from 0.1 to 3 volume percent CO, from 50 to 90% hydrogen and from 10 to 50~ C02, either dry, partially saturated or saturated with water is mixed with a suitable oxygen-containing gas, such as air or pure oxygen in an amount providing a molar ratio of oxygen to CO of from about 0.5 to 3:1. This fuel gas mixture is then fed through a packed column containing a supported platinum group metal catalyst. The gas mixture is contacted with the catalyst in the column at a pressure of from about atmospheric to 500 psig and at temperatures from about 10 to 160C. Oxidation of the CO to CO2 occurs as shown in equation (1) below. Excess oxygen i8 completely consumed by conver~ion to water.
Selectivity for the CO oxidation is improved by carrying out the oxidation at these lower temperatures. At higher temperature~, from about 200 to 400C, the reaction between hydrogen and CO/C02 (equation~ (2) and (3) below) is favoured to form methane and water (methanation). ~here high proportions of CO and CO2 are present, large quantities of hydrogen are consumed as shown in equations (2) and (3). For this reason, operation at high temperatures which favours methanation is undesirable.
13C~SZl~
~elective Oxidation CO + ~O2t )CO2 (1) Methanation CO + 3H2 ~--~ CH4 + H2O (2) C2 + 4H2~ ~ CH4 + 2H2O (3) Space velocities through the column can be in the order of 1,000 to 50,000 cubic feet of gas per hour per cubic foot of catalyst, with 5,000 to 30,000 being preferred.
The catalyst can be platinum, rhodium or ruthenium on a suitable support such as alumina, silica, silica gel, diatomaceous earth or clay. Platinum on alumina is preferred. The catalyst metal may be present in the range of about 0.01 to 5% by weight, based upon the weight of the catalytic metal and support, preferably from about 0.05 to 2%. The supported catalyst may be prepared by treating the support with a solution of a suitable metal compound and then reducing the metal compound to metal.
As shown in the figure, the conditioned fuel gas mixture from the column contains CO2, H2, water and only trace amounts of CO ie. from 2 to 10 ppm CO. The conditioned gas mixture is then fed directly to an acid fuel cell. Acid fuel cells are unaffected by CO2 which simply acts as a diluent to the fuel gas. Because levels of CO have been significantly reduced, cell performance dramatically improves as will be apparent hereafter.
Hydrogen from the product gas is consumed at the fuel cell anode releasing protons and electrons as shown in equation (4) below: The protons are injected into the fuel cell electrolyte. The electrons travel outside of the cell to the cell l~OSi~i2 terminal through a load bank back to the cathode terminal and into the cell. At the cathode, oxygen, electrons from the load and protons from the electrolyte combine to form water as shown in equation (5) below.
, Anode Reaction H2 -~ 2H+ + 2e (4) Cathode Reaction ~2 + 2H+ + 2e __~ H20 (5) Example 1 A solid polymer fuel cell was constructed similar to that described in United States Patent No. 3,297,484 of 10 January 1967 in the name of ~eonard W. ~iedrach. The active cell area was about 32 cm2. The solid polymer membrane used for the membrane/electrode assembly was DuPont's Nafio ~ 117 (a fluorinated cationic exchange membrane). In the case of the fuel electrode (the anode) a mixture of platinum and tungsten oxide ~81% Pt, 19~ ~2) was used. Platinum loading was 4 mg/cm2.
In the case of the cathode (air) electrode, platinum alone was used at a loading of 4 mg/cm2.
The fuel cell was fed UHP H2 and air at about atmospheric pressure. Performance output was 0.69V @ 220 mA/cm2 at 55C after about 5 hours operation under a constant 100 mOHM
resistance load. The fuel gas was then switched from UHP H2 to simulated reformed methanol (0.275% CO, 25% CO2, balance H2).
Three hours after the switch to reformate, performance output was 0.49V @ 157 mA/cm2 at 55C under a 100 mOHM resistance load.
Performance after 24 hours was 0.31V @ 97 mA/cm2 at 47C. The results are summarized in Table 1 below. Power density on 13Q~lZ
unconditioned reformate/air after 3 hours operation was 51% of that on hydrogen/air. After 24 hours, power density was only 20 of that of hydrogen/air.
TAsLE I
Hydrogen/Air & Unconditioned Reformate/Air Performance Atmospheric Pressure - 100 mOHM Resistive Load Current Power Volts Density Temperature Time Density (V) (mA/cm2) (C) (hrs)(mW/cm2) 0.69 219 55 4.5 151 Switch from ~HP H2 to Reformate 0.49 157 55 7.5 77 0.31 97 47 28.5 30 Example 2 A selective oxidation column was constructed using a jacketed glass tube 0.5" I.D., 8" long with about 20 ml volume.
The column was filled with 1/8", 0.5% platinum on alumina cylinders. A mixing tee was provided on the inlet to the column where fuel gas and air could be mixed and then fed to the column.
Reformate (0.275% CO, 25% CO2, Balance H2) and air were fed to the column such that the 2 to CO molar ratio was in the range of 1:1 to 2:1. The exit gas from the column was fed directly to the fuel cell described in example 1. Table II
~3~SZl;~
summarizes the test results. After 22 hours operation of conditioned reformate/air, power density was 81% of that of hydrogen/air. This represen~s a four fold improvement over unconditioned reformate/air performance described in Example 1.
TABLE II
Conditioned Reformate/Air Performance Atmospheric Pressure - 100 mOHM Resitive Load . _ _ Current Power Volts Density Temperature Time Density (V) (mA/cm2) (C) (hrs)(mW/cm~) .
0.64 203 55 2 130 0.63 201 55 6 127 0.62 197 55 22 122
Claims (13)
OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. In a method for operating a low-temperature fuel cell, said fuel cell including a solid polymer electrolyte and a noble metal material in the anode, on a fuel gas containing carbon monoxide, the improvement comprising the sequential steps of:
(a) reacting the fuel gas with a suitable oxygen-containing gas in an amount providing a molar ratio of oxygen to carbon monoxide of about 0.5 to 3:1;
(b) contacting the resulting fuel gas mixture with a suitable catalyst at a reaction temperature of about 10 to 160°C
and pressure of about atmospheric to 500 psig, to selectively convert carbon monoxide to carbon dioxide, whereby carbon monoxide levels in the fuel gas are reduced to trace amounts of about 2 to 10 parts per million; and (c) feeding the resulting substantially carbon monoxide-free fuel gas to the fuel cell.
(a) reacting the fuel gas with a suitable oxygen-containing gas in an amount providing a molar ratio of oxygen to carbon monoxide of about 0.5 to 3:1;
(b) contacting the resulting fuel gas mixture with a suitable catalyst at a reaction temperature of about 10 to 160°C
and pressure of about atmospheric to 500 psig, to selectively convert carbon monoxide to carbon dioxide, whereby carbon monoxide levels in the fuel gas are reduced to trace amounts of about 2 to 10 parts per million; and (c) feeding the resulting substantially carbon monoxide-free fuel gas to the fuel cell.
2. A method according to Claim 1, wherein the suitable oxygen-containing gas is selected from the group consisting of air and oxygen.
3. A method according to Claim 2, wherein the suitable catalyst comprises a platinum group metal selected from the group consisting of platinum, rhodium and ruthenium.
4. A method according to Claim 3, wherein the catalyst is provided on a suitable support selected from the group consisting of alumina, silica, silica gel, diatomaceous earth and clay, and wherein the catalyst is provided in an amount of about 0.01 to 5 percent by weight, based upon the weight of the catalyst and support.
5. A method according to Claim 4, wherein the catalyst is platinum on an alumina support.
6. A method according to Claim 5, wherein platinum is provided in an amount of 0.05 to 2 percent by weight, based upon the weight of the catalyst and support.
7. A method according to Claim 6, wherein the catalyst is provided in a column and wherein the space velocity through the column is in the range of 1,000 to 50,000 ft3 of gas per hour per ft3 of catalyst.
8. A method according to Claim 7, wherein the fuel cell is an acid fuel cell.
9. A method according to Claim 1, 3 or 8, wherein the fuel gas comprises hydrogen, carbon dioxide and carbon monoxide.
10. A method according to Claim 1, 3 or 8, wherein the fuel gas is a product of the steam reformation of methanol.
11. A method according to Claim 1, 3 or 8, wherein the fuel gas is a product of the steam reformation of natural gas.
12. A method according to Claim 1, 3 or 8, wherein the suitable oxygen-containing gas, the molar ratio of oxygen to carbon monoxide is about 1-2:1.
13. A method according to Claim 1, 3 or 8, wherein the solid polymer membrane is a fluorinated cationic exchange membrane.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US6048387A | 1987-06-11 | 1987-06-11 | |
| US060,483 | 1987-06-11 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1305212C true CA1305212C (en) | 1992-07-14 |
Family
ID=22029769
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000569048A Expired - Lifetime CA1305212C (en) | 1987-06-11 | 1988-06-09 | Method for operating a fuel cell on carbon monoxide containing fuel gas |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1305212C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104969396A (en) * | 2013-02-05 | 2015-10-07 | 庄信万丰燃料电池有限公司 | Use of an anode catalyst layer |
-
1988
- 1988-06-09 CA CA000569048A patent/CA1305212C/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104969396A (en) * | 2013-02-05 | 2015-10-07 | 庄信万丰燃料电池有限公司 | Use of an anode catalyst layer |
| US9947938B2 (en) | 2013-02-05 | 2018-04-17 | Johnson Matthey Fuel Cells Limited | Carbon monoxide-tolerant anode catalyst layer and methods of use thereof in proton exchange membrane fuel cells |
| US9947939B2 (en) | 2013-02-05 | 2018-04-17 | Johnson Matthey Fuel Cells Limited | Use of an anode catalyst layer |
| CN104969396B (en) * | 2013-02-05 | 2018-06-01 | 庄信万丰燃料电池有限公司 | The purposes of anode catalyst layer |
| US10938038B2 (en) | 2013-02-05 | 2021-03-02 | Johnson Matthey Fuel Cells Limited | Use of an anode catalyst layer |
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