U.S. patent application number 15/282080 was filed with the patent office on 2018-04-05 for facile control of pore structure in carbon-supported pgm-based catalysts.
The applicant listed for this patent is GM GLOBAL TECHNOLOGY OPERATIONS LLC. Invention is credited to MICHAEL K. CARPENTER, ANUSORN KONGKANAND.
Application Number | 20180097238 15/282080 |
Document ID | / |
Family ID | 61623751 |
Filed Date | 2018-04-05 |
United States Patent
Application |
20180097238 |
Kind Code |
A1 |
KONGKANAND; ANUSORN ; et
al. |
April 5, 2018 |
FACILE CONTROL OF PORE STRUCTURE IN CARBON-SUPPORTED PGM-BASED
CATALYSTS
Abstract
A method for forming a carbon supported catalyst includes a step
of providing a first carbon supported catalyst having a
platinum-group metal supported on a first carbon support.
Characteristically, the first carbon support has a first average
micropore diameter and a first average carbon surface area. The
first carbon supported catalyst is contacted with an
oxygen-containing gas at a temperature less than about 450.degree.
C. for a predetermined period of time to form a second carbon
supported catalyst, wherein the first carbon support or the second
carbon supported catalyst is acid leached.
Inventors: |
KONGKANAND; ANUSORN;
(ROCHESTER HILLS, MI) ; CARPENTER; MICHAEL K.;
(TROY, MI) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
GM GLOBAL TECHNOLOGY OPERATIONS LLC |
Detroit |
MI |
US |
|
|
Family ID: |
61623751 |
Appl. No.: |
15/282080 |
Filed: |
September 30, 2016 |
Current U.S.
Class: |
1/1 |
Current CPC
Class: |
H01M 4/9083 20130101;
H01M 2008/1095 20130101; H01M 4/8878 20130101; Y02E 60/50 20130101;
H01M 4/926 20130101; H01M 4/8882 20130101 |
International
Class: |
H01M 4/88 20060101
H01M004/88; H01M 4/92 20060101 H01M004/92; H01M 4/90 20060101
H01M004/90 |
Claims
1. A method for forming a carbon supported catalyst, the method
comprising: a) providing a first carbon supported catalyst having a
platinum-group metal supported on a first carbon support, the first
carbon support having a first average pore diameter and a first
average surface area; b) contacting the first carbon supported
catalyst with an oxygen-containing gas at a temperature less than
about 450.degree. C. for a predetermined period of time to form a
second carbon supported catalyst, wherein the first carbon support
or the second carbon supported catalyst is acid leached.
2. The method of claim 1 wherein the first carbon support is acid
leached and then contacted with the oxygen-containing gas at a
temperature less than about 300.degree. C. to form the second
carbon supported catalyst.
3. The method of claim 2 wherein the first carbon supported
catalyst is dried prior to being contacted with the
oxygen-containing gas.
4. The method of claim 3 further comprising contacting the second
carbon supported catalyst with molecular hydrogen.
5. The method of claim 1 wherein the first carbon support is
contacted with the oxygen-containing gas and then acid leached to
form the second carbon supported catalyst.
6. The method of claim 5 further comprising contacting the second
carbon supported with molecular hydrogen.
7. The method of claim 1 wherein the second carbon supported
catalyst includes an altered carbon support having a second average
pore diameter and a second average carbon surface area, the second
average micropore diameter being greater than the first average
micropore diameter and the second average carbon surface area being
less than the first average carbon surface area.
8. The method of claim 7 wherein the first average micropore
diameter is less than 40 angstroms.
9. The method of claim 7 wherein the second average micropore
diameter is greater than 40 angstroms.
10. The carbon supported catalyst of claim 7 wherein the second
average carbon surface area is decreased by more than 2% and a
second average carbon amount is decreased by more than 1%.
11. The method of claim 7 wherein the first carbon support has a
first average pore volume and the altered carbon support has a
second average pore volume for pore size in a range of 40-100
angstroms, the second average pore volume being greater than the
first average pore volume.
12. The method of claim 1 wherein the platinum-group metal is
selected from the group consisting of Pt, Pd, Au, Ru, Ir, Rh, and
Os.
13. The method of claim 1 wherein the platinum-group metal is
Pt.
14. The method of claim 1 wherein the first carbon support is a
carbon powder.
15. A method for forming a carbon supported catalyst, the method
comprising: a) providing a first carbon supported catalyst having a
platinum-group metal supported on a first carbon support, the first
carbon support having a first average micropore diameter and a
first average carbon surface area; b) contacting the first carbon
supported catalyst with an oxygen-containing gas at a temperature
less than about 450.degree. C. for a predetermined period of time
to form a second carbon supported catalyst; c) contacting the
second carbon supported with molecular hydrogen to form a third
carbon supported catalyst; and d) acid leaching the third carbon
supported catalyst to form a fourth carbon supported catalyst
having depleted non-noble metal catalyst particles disposed
thereon.
16. The method of claim 15 wherein the carbon supported catalyst is
dried prior to being contacted with the oxygen-containing gas.
17. The method of claim 15 wherein the second carbon supported
catalyst includes an altered carbon support having a second average
micropore diameter and a second average carbon surface area, the
second average micropore diameter being greater than the first
average micropore diameter and the second average carbon surface
area being less than the first average carbon surface area.
18. The method of claim 15 wherein the platinum-group metal is
selected from the group consisting of Pt, Pd, Au, Ru, Ir, Rh, and
Os.
19. The method of claim 15 wherein the platinum-group metal is Pt.
Description
TECHNICAL FIELD
[0001] In at least one aspect, the present invention relates to
catalyst materials for fuel cells with improved performance.
BACKGROUND
[0002] Fuel cells are used as an electrical power source in many
applications. In particular, fuel cells are proposed for use in
automobiles to replace internal combustion engines. A commonly used
fuel cell design uses a solid polymer electrolyte ("SPE") membrane
or proton exchange membrane ("PEM") to provide ion transport
between the anode and cathode.
[0003] In proton exchange membrane type fuel cells, hydrogen is
supplied to the anode as fuel and oxygen is supplied to the cathode
as the oxidant. The oxygen can either be in pure form (O.sub.2) or
air (a mixture of O.sub.2 and N.sub.2). PEM fuel cells typically
have a membrane electrode assembly ("MEA") in which a solid polymer
membrane has an anode catalyst on one face, and a cathode catalyst
on the opposite face. The anode and cathode layers of a typical PEM
fuel cell are formed of porous conductive materials, such as woven
graphite, graphitized sheets, or carbon paper to enable the fuel
and oxidant to disperse over the surface of the membrane facing the
fuel- and oxidant-supply electrodes, respectively. Each electrode
has finely divided catalyst particles (for example, platinum
particles) supported on carbon particles to promote oxidation of
hydrogen at the anode and reduction of oxygen at the cathode.
Protons flow from the anode through the ionically conductive
polymer membrane to the cathode where they combine with oxygen to
form water which is discharged from the cell. The MEA is sandwiched
between a pair of porous gas diffusion layers ("GDL") which, in
turn, are sandwiched between a pair of non-porous, electrically
conductive elements or plates. The plates function as current
collectors for the anode and the cathode, and contain appropriate
channels and openings formed therein for distributing the fuel
cell's gaseous reactants over the surface of respective anode and
cathode catalysts. In order to produce electricity efficiently, the
polymer electrolyte membrane of a PEM fuel cell must be thin,
chemically stable, proton transmissive, non-electrically conductive
and gas impermeable. In typical applications, fuel cells are
provided in arrays of many individual fuel cell stacks in order to
provide high levels of electrical power.
[0004] High surface area carbon black is often used as a support
for fuel cell catalysts. High surface area carbon black often
contains large quantities of internal micropores (<4 nm) in
their constituent particles. Pt nanoparticles deposited in these
micropores can have restricted access to reactants and show poor
activity. Studies have shown that up to 80% of all Pt particles are
deposited inside the micropores. Opening up these micropores to
better expose the Pt particles should improve the high power
performance of the catalyst. As used herein, the terms "micropores"
and "pores" are used interchangeably, not to be mistaken with
mesopores (pores of 5-15 nm) and macropores (pores >15 nm).
[0005] Catalyst durability, particularly as it relates to the
retention of high power performance, is one of the major challenges
facing the development of automotive fuel cell technology. Platinum
or platinum-alloy particles lose electrochemical surface area
during operation due to dissolution and subsequent Ostwald ripening
and to particle migration and coalescence. Electrochemical
oxidation of the carbon support enhances this particle migration
and subsequent performance loss at high power. Oxidation of carbon
support also causes the collapse of the electrode thickness and
electrode porosity, hindering reactant transport and subsequent
performance loss. Therefore, it is a common practice for those
skilled in the art to avoid oxidation of carbon support.
[0006] On the other hand, in electrodes with small amount of Pt or
low Pt surface area, large fuel cell performance loss is observed.
This is due to the need to support larger flux of reactant oxygen
or hydrogen to the Pt surface. This is particularly difficult for
Pt particles that are embedded in carbon particle micropores.
Accordingly, there is a need for improved catalyst layers.
SUMMARY
[0007] The present invention solves one or more problems of the
prior art by providing, in at least one embodiment, a method for
forming a carbon supported catalyst. The method includes a step of
providing a first carbon supported catalyst having a platinum-group
metal supported on a first carbon support. Characteristically, the
first carbon support has a first average micropore diameter and a
first average carbon surface area. The first carbon supported
catalyst is contacted with an oxygen-containing gas at a
temperature less than about 450.degree. C. for a predetermined
period of time to form a second carbon supported catalyst, wherein
the first carbon support or the second carbon supported catalyst is
acid leached.
[0008] A method for forming a carbon supported catalyst is
provided. The method includes a step of providing a first carbon
supported catalyst having a platinum-group metal supported on a
first carbon support. Characteristically, the first carbon support
has a first average micropore diameter and a first average carbon
surface area. The first carbon supported catalyst is contacted with
an oxygen-containing gas at a temperature less than about
450.degree. C. for a predetermined period of time to form a second
carbon supported catalyst. The second carbon supported is
subsequently contacted with molecular hydrogen to form a third
carbon supported catalyst. The third carbon supported catalyst is
acid leached to form a fourth carbon supported catalyst having
depleted non-noble metal catalyst particles disposed on a carbon
support.
BRIEF DESCRIPTION OF THE DRAWINGS
[0009] FIG. 1 is a schematic cross section of a fuel cell that
incorporates carbon supported catalysts into the anode and/or
cathode catalyst layers;
[0010] FIG. 2 is a schematic flow chart illustrating several
variations of a method of forming a carbon supported catalyst;
[0011] FIG. 3A provides plots of fuel cell voltage versus current
density for variously modified carbon supported catalysts (modified
carbon supported catalyst 46, final carbon supported catalyst 48,
and final carbon supported catalyst 52) that have been acid leached
before treatment with oxygen and hydrogen;
[0012] FIG. 3B provides plots of fuel cell voltage versus current
density for variously modified carbon supported catalysts (final
carbon supported catalyst 48 and final carbon supported catalyst
60) that have been acid leached after treatment with oxygen and
hydrogen;
[0013] FIG. 4A provides plots of fuel cell voltage versus the
number of cycles for variously modified carbon supported catalysts
(modified carbon supported catalyst 46, final carbon supported
catalyst 48, and final carbon supported catalyst 52) that have been
acid leached before treatment with oxygen and hydrogen;
[0014] FIG. 4B provides plots of fuel cell voltage for variously
modified carbon supported catalysts (final carbon supported
catalyst 48 and final carbon supported catalyst 60) that have been
acid leached after treatment with oxygen and hydrogen;
[0015] FIG. 5 is a plot of mass activity versus the number of
cycles for modified carbon supported catalyst 46, final carbon
supported catalyst 48, and final carbon supported catalyst 52;
[0016] FIG. 6 is a plot of oxidation temperature and time for
various modified carbon supported catalysts;
[0017] FIG. 7 is a plot of reaction time needed to achieve desired
carbon loss and pore opening effect for a given reaction
temperature;
[0018] FIG. 8A is a plot of the volume per gram of carbon support
of adsorbed gas versus pore size; and
[0019] FIG. 8B is a plot of the volume of adsorbed gas versus
treatment time of the carbon supported catalyst with oxygen.
DETAILED DESCRIPTION
[0020] Reference will now be made in detail to presently preferred
compositions, embodiments and methods of the present invention
which constitute the best modes of practicing the invention
presently known to the inventors. The Figures are not necessarily
to scale. However, it is to be understood that the disclosed
embodiments are merely exemplary of the invention that may be
embodied in various and alternative forms. Therefore, specific
details disclosed herein are not to be interpreted as limiting, but
merely as a representative basis for any aspect of the invention
and/or as a representative basis for teaching one skilled in the
art to variously employ the present invention.
[0021] Except in the examples, or where otherwise expressly
indicated, all numerical quantities in this description indicating
amounts of material or conditions of reaction and/or use are to be
understood as modified by the word "about" in describing the
broadest scope of the invention. Practice within the numerical
limits stated is generally preferred. Also, unless expressly stated
to the contrary: percent, "parts of," and ratio values are by
weight; the description of a group or class of materials as
suitable or preferred for a given purpose in connection with the
invention implies that mixtures of any two or more of the members
of the group or class are equally suitable or preferred;
description of constituents in chemical terms refers to the
constituents at the time of addition to any combination specified
in the description and does not necessarily preclude chemical
interactions among the constituents of a mixture once mixed; the
first definition of an acronym or other abbreviation applies to all
subsequent uses herein of the same abbreviation and applies mutatis
mutandis to normal grammatical variations of the initially defined
abbreviation; and, unless expressly stated to the contrary,
measurement of a property is determined by the same technique as
previously or later referenced for the same property.
[0022] It is also to be understood that this invention is not
limited to the specific embodiments and methods described below, as
specific components and/or conditions may, of course, vary.
Furthermore, the terminology used herein is used only for the
purpose of describing particular embodiments of the present
invention and is not intended to be limiting in any way.
[0023] It must also be noted that, as used in the specification and
the appended claims, the singular form "a," "an," and "the"
comprise plural referents unless the context clearly indicates
otherwise. For example, reference to a component in the singular is
intended to comprise a plurality of components.
[0024] Throughout this application, where publications are
referenced, the disclosures of these publications in their
entireties are hereby incorporated by reference into this
application to more fully describe the state of the art to which
this invention pertains.
Abbreviations
[0025] "BET" means Brunauer-Emmett-Teller (BET) theory;
[0026] "BOL" means beginning of life;
[0027] "PGM" means platinum group metal.
[0028] With reference to FIG. 1, a cross sectional view of a fuel
cell incorporating the platinum group metal-containing carbon
supported catalysts is provided. PEM fuel cell 10 includes
polymeric ion conducting membrane 12 disposed between cathode
electro-catalyst layer 14 and anode electro-catalyst layer 16. Fuel
cell 10 also includes electrically conductive flow field plates 20,
22 which include gas channels 24 and 26. Flow field plates 20, 22
are either bipolar plates (illustrated) or unipolar plates (i.e.,
end plates). In a refinement, flow field plates 20, 22 are formed
from a metal plate (e.g., stainless steel) optionally coated with a
precious metal such as gold or platinum. In another refinement,
flow field plates 20, 22 are formed from conducting polymers which
also are optionally coated with a precious metal. Gas diffusion
layers 32 and 34 are also interposed between flow field plates and
a catalyst layer. Cathode electro-catalyst layer 14 and anode
electro-catalyst layer 16 include carbon supported catalysts made
by the processes set forth below. Advantageously, the carbon
supported catalysts have improved activity and stability anode and
cathode electro-catalyst layers.
[0029] With reference to FIG. 2, a schematic flow chart
illustrating several variations of a method of forming a carbon
supported catalyst is provided. In a first variation, catalyst
precursor 40 (i.e., a first carbon supported catalyst) is subjected
to acid leaching to form an undried de-alloyed catalyst 42 is step
a. In one refinement, in step b) undried de-alloyed catalyst 42 is
dried to form de-alloyed catalyst 44. De-alloyed catalyst 44 is
then contacted with an oxygen-containing gas in step c) to form
modified carbon supported catalyst 46. Finally, in step d) modified
carbon supported catalyst 46 is then contacted with molecular
hydrogen to form final carbon supported catalyst 48.
[0030] Still referring to FIG. 2, undried de-alloyed catalyst 42 is
contacted with an oxygen-containing gas to form modified carbon
supported catalyst 50 in step b'. In step c'), modified carbon
supported catalyst 50 is then contacted with molecular hydrogen to
form final carbon supported catalyst 52.
[0031] Still referring to FIG. 2, catalyst precursor 40 is
contacted with an oxygen-containing gas to form modified carbon
supported catalyst 54 in step a''). Modified carbon supported
catalyst 54 is then contacted in step b'') with molecular hydrogen
to form carbon supported catalyst 56. Finally, in step c'', carbon
supported catalyst 56 is then acid leached to form final carbon
supported catalyst 60.
[0032] In each of the variations of the method set forth above,
catalyst precursor 40 includes a platinum-group metal. In
particular, the platinum-group metal is selected from the group
consisting of Pt, Pd, Au, Ru, Ir, Rh, and Os. In this regard, Pt is
found to be particularly useful. In one variation, the carbon
supported catalyst includes a carbon support and a platinum-group
metal (PGM) disposed over/supported on the carbon support. In a
refinement, the platinum-group metal is supported on carbon at a
loading from about 5 weight percent to about 50 weight percent. The
carbon supported catalyst is characterized by a multiscale pore
diameters: with micropore and mesopore size of less than 100
angstroms and with macropore size of greater than 100 angstroms.
The carbon supported catalyst is also characterized by its average
surface area which is greater than 500 m.sup.2/g. In a refinement,
the average carbon surface area is greater than, in increasing
order of preference, 500 m.sup.2/g, 600 m.sup.2/g, 700 m.sup.2/g,
or 800 m.sup.2/g. In another refinement, the average carbon surface
area is less than, in increasing order of preference, 3000
m.sup.2/g, 2000 m.sup.2/g, or 1000 m.sup.2/g. In a refinement, the
carbon supported catalyst has an average pore volume that is less
than about 0.6 cm.sup.3/g. In another refinement, the average pore
volume is less than, in increasing order of preference, 1.1
cm.sup.3/g, 1.0 cm.sup.3/g, and 0.9 cm.sup.3/g. In still another
refinement, the average pore volume is greater than, in increasing
order of preference, 0.2 cm.sup.3/g, 0.3 cm.sup.3/g, 0.4
cm.sup.3/g, or 0.5 cm.sup.3/g. In a variation, the pore volume,
pore diameter and surface area are determined by a BET method.
[0033] In a refinement, the catalyst precursor 40 includes an alloy
that includes the platinum group metal and one or more additional
metals. In a refinement, the one or more additional metals include
first or second row transition metals. Specific examples of the one
or more additional metals include Co, Ni, Fe, Ti, Sc, Cu, Mn, Cr,
V, Ru, Zr, Y and W. Typically, the carbon support is a carbon
powder having a plurality of carbon particles. The carbon particles
may have any number of shapes without limiting the invention in any
way. Examples of such shapes include, but are not limited to,
nano-rods, nanotubes, nano-rafts, non-electrically conducting
particles, spherical particles, and the like. In one variation, the
carbon particles are a carbon powder and in particular, a high
surface area carbon (HSC) powder typically having an average
spatial dimension (e.g., diameter) from about 5 to 500 nanometers.
In a refinement, the carbon powder has an average spatial dimension
from about 10 to 300 nanometers. In another refinement, carbon
black having an average spatial dimension from about 30 to 300
nanometers is used for the carbon particles. A particularly useful
example of carbon black is Ketjen Black.
[0034] The catalyst precursor 40 has a first average pore volume, a
first average pore diameter, and a first average surface area. In a
refinement, the first average micropore diameter is less than 70
angstroms, and the first average carbon surface area is greater
than 500 m.sup.2/g. In a refinement, the first average pore
diameter is less than, in increasing order of preference 100
angstroms, 80 angstroms, 70 angstroms and 50 angstroms and greater
than in increasing order of preference, 10 angstroms, 20 angstroms,
30 angstroms, and 40 angstroms. In another refinement, the first
average carbon surface area is greater than, in increasing order of
preference, 400 m.sup.2/g, 500 m.sup.2/g, 600 m.sup.2/g, and 700
m.sup.2/g and less than, in increasing order of preference, 1200
m.sup.2/g, 1000 m.sup.2/g, 800 m.sup.2/g, and 600 m.sup.2/g.
Typically, the first average pore volume is greater than 0.6
cm.sup.3/g. In another refinement, the first average pore volume is
greater than, in increasing order of preference, 0.5 cm.sup.3/g,
0.6 cm.sup.3/g, 0.7 cm.sup.3/g, and 0.8 cm.sup.3/g. In still
another refinement, the first average pore volume is less than, in
increasing order of preference, 1.5 cm.sup.3/g, 1.2 cm.sup.3/g, 1.0
cm.sup.3/g, or 0.9 cm.sup.3/g.
[0035] In each of the method variations set forth above, the pore
size of the final carbon supported catalyst that is formed has a
pore size that is greater than that of catalyst precursor 40. In
particular, each of the carbon supported catalysts formed after the
step of contact with an oxygen-containing gas have a larger pore
size than catalyst precursor 40. In each case, this larger pore
size is characterized by a second average pore volume, a second
average pore diameter, and a second average surface area.
Characteristically, the second average pore diameter is greater
than the first average pore diameter and the second average surface
area is less than the first average surface area. In a refinement,
the second average micro and mesopore volume is greater than the
first average pore volume. Details for the second average pore
volume, second average pore diameter, and the second average
surface area are set forth above. The second average micropore
diameter is typically greater than 50 angstroms. In a refinement,
the second average pore diameter is greater than, in increasing
order of preference, 40 angstroms, 50 angstroms, 55 angstroms, 60
angstroms, or 70 angstroms. In another refinement, the second
average pore diameter is less than, in increasing order of
preference, 150 angstroms, 120 angstroms, 100 angstroms, or 90
angstroms. Typically, the second average carbon surface area is
less than 800 m.sup.2/g. In a refinement, the second average carbon
surface area is less than, in increasing order of preference, 1100
m.sup.2/g, 1000 m.sup.2/g, 900 m.sup.2/g, or 750 m.sup.2/g. In
another refinement, the second average carbon surface area is
greater than, in increasing order of preference, 300 m.sup.2/g, 400
m.sup.2/g, 500 m.sup.2/g, or 650 m.sup.2/g.
[0036] As set forth above, the variations of the method for forming
a carbon supported catalyst includes an acid leaching step.
Typically, leaching is accomplished by contacting the carbon
supported catalyst (e.g., catalyst precursor 40 or carbon supported
catalyst 56) with an aqueous acid. For example, the carbon
supported catalyst being acid leach can be contacted with a 1M
nitric acid solution for 24 hours at 70.degree. C.
[0037] Each of the methods set forth above includes a step in which
a carbon supported catalyst is contacted with an oxygen-containing
gas. Examples of oxygen-containing gas include air, pure oxygen, or
gaseous mixtures including 1 to 99 percent oxygen and a carrier gas
(e.g., N.sub.2, Argon, etc.). In a refinement, the
oxygen-containing gas includes from 0.1 to 100 weight percent
molecular oxygen. In another refinement, the oxygen-containing gas
includes from 1 to 30 weight percent molecular oxygen. As set forth
above, various carbon supported catalysts are contacted with the
oxygen-containing gas at a temperature less than about 450.degree.
C. for a predetermined period of time to form a second carbon
supported catalyst. In other refinements, the first carbon
supported catalyst is contacted with an oxygen-containing gas at a
temperature less than about 300.degree. C. for a predetermined
period of time to form a second carbon supported catalyst. In other
refinements, the first carbon supported catalyst is contacted with
an oxygen-containing gas at a temperature less than about from 150
to 350.degree. C. for a predetermined period of time to form a
second carbon supported catalyst. In still other refinements, the
first carbon supported catalyst is contacted with an
oxygen-containing gas at a temperature less than about from 200 to
300.degree. C. for a predetermined period of time to form a second
carbon supported catalyst. In another variation, the first carbon
supported catalyst is contacted with an oxygen-containing gas at a
temperature less than or equal to, in increasing order of
preference, 450.degree. C., 300.degree. C., 250.degree. C.,
200.degree. C., 180.degree. C., or 150.degree. C., and at a
temperature greater than or equal to 50.degree. C., 75.degree. C.,
90.degree. C., 100.degree. C., or 120.degree. C. The oxidation of
the first carbon supported catalyst typically is performed at
around 1 atm. In each case, the predetermined time can be from 1
minutes to 24 hours depending on the pore sizes that are desired,
the type of carbon, and the temperature at which the carbon
supported catalyst is contacted with the oxygen-containing gas. At
high temperatures from about 350 to 450.degree. C., the
predetermined time can be from 1 second to 2 minutes. At
temperatures from about 200 to 300.degree. C., the predetermined
time can be from 1 minute to 24 hours. When a carbon supported PGM
catalyst is heated in an oxidizing environment, the platinum group
metal catalyst particles serve as oxidation catalyst sites that
allow localized corrosion of the micropores in which they reside,
resulting in larger pores and improved transport properties. The
mild oxidation also preferentially removes some of the less stable
amorphous carbon, partially stabilizing the support and thus
improving catalyst durability. In a refinement, the average pore
diameter of the carbon supported catalyst that is contacted with
the oxygen-containing gas is greater than the first average pore
diameter and the average surface area of the carbon supported
catalyst that is contacted with the oxygen-containing gas is less
than the first average surface area.
[0038] In another embodiment, the carbon supported catalysts set
forth above are used in an ink composition to form fuel cell
catalyst layers by methods known to those skilled in fuel cell
technology. In a refinement, the ink composition includes the
carbon supported catalysts in an amount of about 1 weight percent
to 10 weight percent of the total weight of the ink composition. In
a refinement, the ink composition includes ionomers (e.g., a
perfluorosulfonic acid polymer such as NAFION.RTM.) in an amount
from about 5 weight percent to about 40 weight percent of the
catalyst composition. Typically, the balance of the ink composition
is solvent. Useful solvents include, but are not limited to,
alcohols (e.g., propanol, ethanol, and methanol), water, or a
mixture of water and alcohols. Characteristically, the solvents
evaporate at room temperature.
[0039] The following examples illustrate the various embodiments of
the present invention. Those skilled in the art will recognize many
variations that are within the spirit of the present invention and
scope of the claims.
[0040] FIGS. 3A and 3B provide plots of fuel cell voltage versus
current density for variously modified carbon supported catalysts.
FIG. 3A compares the fuel cell polarization curves for modified
carbon supported catalyst 46, final carbon supported catalyst 48,
and final carbon supported catalyst 52 from FIG. 2. FIG. 3B
compares the fuel cell polarization curves between catalysts
treated before and after the acid leaching step for final carbon
supported catalyst 48 compared to final carbon supported catalyst
60 from FIG. 2. Both catalysts final carbon supported catalyst 48
and final carbon supported catalyst 60 gave comparable
performance.
[0041] FIGS. 4A and 4B provide plots of fuel cell voltage versus
the number of cycles for variously modified carbon supported
catalysts. FIG. 4A shows the fuel cell performance at 2 A/cm.sup.2
under HighP-wet protocol for cathodes with 0.06 mg Pt/cm.sup.2
loadings before and after voltage-cycling accelerated stability
tests (AST) (0.6-1.0 V) for modified carbon supported catalyst 46,
final carbon supported catalyst 48, and final carbon supported
catalyst 52 from FIG. 2. FIG. 4B compares shows the fuel cell
performance for final carbon supported catalyst 48 compared to
final carbon supported catalyst 60 from FIG. 2. All oxidized
catalysts showed about 80 mV higher performance compared to the
baseline at the beginning of life (BOL). It was found that Catalyst
48 gave best performance at BOL, and that gap maintains throughout
the AST, indicating the advantages of the drying and H2 reduction
steps.
[0042] FIG. 5 is a plot of mass activity versus the number of
cycles for 46, 48, and 52. The oxygen reduction activity shown in
FIG. 5 confirms the advantages of the drying and H.sub.2 reduction
steps. FIG. 6 is a plot of oxidation time for various modified
carbon supported catalysts. FIG. 6 shows the carbon losses as a
function of oxidation time at three different temperatures. Because
the reaction was done in excess of reactant oxygen, the linearly
proportional of carbon loss to the oxidation time indicates a
kinetic-controlled reaction. At higher temperature, less time is
needed to achieve the target carbon loss, e.g. the target micropore
size. The carbon oxidation kinetic was found to follow the
Arrhenius relationship. An activation energy of 121 kJ/mol was
determined for this HSC carbon. The carbon oxidation kinetic can be
used to estimate the reaction time needed to achieve target carbon
loss at a reaction temperature. FIG. 7 is a plot of reaction time
versus reaction time for the reaction of carbon supports with
oxygen. FIG. 7 also compares the experimental results (circles) to
the model (solid line). This data suggests that the temperature can
be raised to even further to shorten the reaction time and reduce
process cost.
[0043] FIGS. 8A-B presents gas adsorption data. FIG. 8A is a plot
of the volume per gram of carbon support of adsorbed gas versus
pore size while FIG. 8B is a plot of the volume of adsorbed gas
versus treatment time of the carbon supported catalyst with oxygen.
This is a comparison of a control first catalyst 44 with final
catalysts 48 treated for different treatment times with oxygen
(48a, 48b, and 48c). The gas adsorption analysis shows that there
are small amount of carbon mass and surface area losses. Moreover,
increasing micropore size suggests improved local oxygen transport.
Table 1 provides a summary of the results:
TABLE-US-00001 TABLE 1 Adsorption Properties BET surface Carbon
surface Carbon Carbon area area wt. loss area loss Sample
(mm.sup.2/g) (mm.sup.2/g.sub.carbon) (%) (%) untreated 510 710 48a
501 704 0.8 0.9 48b 488 691 1.5 2.7 48c 452 660 4.2 7.1
[0044] While exemplary embodiments are described above, it is not
intended that these embodiments describe all possible forms of the
invention. Rather, the words used in the specification are words of
description rather than limitation, and it is understood that
various changes may be made without departing from the spirit and
scope of the invention. Additionally, the features of various
implementing embodiments may be combined to form further
embodiments of the invention.
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