the low solubility and high processing temperatures which characterize the fluoropolymers of the art create considerable incentive to find a functionally equivalent substitute without the disadvantages . the disadvantages of the fluoropolymers of the art are thought largely to be related to the high crystallinity thereof . in the present invention , the highly crystalline fluoropolymers of the art are replaced by noncrystalline fluoropolymers . the non - crystalline fluoropolymers suitable for use in the present invention are substantially fluorinated polymers , preferably perfluorinated polymers , characterized in that they do not exhibit an endotherm greater than 1j / g as determined by differential scanning calorimetry , astm d4591 . for the purposes of the present invention , “ substantially fluorinated ” refers to the replacement of at least about 90 % of the hydrogens in the associated non - fluorinated polymer by fluorines . preferred fluoropolymers are copolymers of tetrafluoroethylene ( tfe ) with comonomers from the group of hexafluoropropylene ( hfp ), perfluoroalkyl vinyl ethers , 2 , 2 - bistrifluoromethyl4 , 5 - difluoro - 1 , 3 - dioxole ( pdd ), and mixtures thereof . preferably , the concentration of tfe monomer units is 80 mol -% or less and the concentration of the comonomer is at least 20 mol -%. most preferred are a terpolymer comprising 60 mol -% tfe , 26 mol -% perfluoromethyl vinyl ether , and 14 mol -% perfluoroethylvinyl ether , and a copolymer of tfe and pdd comprising 67 mol -% pdd . the copolymers of tfe with hfp or perfluoro alkyl vinyl ethers preferred for the practice of the invention , and methods for their synthesis , are described in anolick et al u . s . pat . no . 5 , 663 , 255 , while those of tfe and pdd are described in squire , u . s . pat . no . 4 , 754 , 009 , both of which are incorporated herein in their entirety by reference . the non - crystalline fluoropolymers of the present invention are soluble in a variety of perfluorinated solvents , and coalesce at temperatures of less than 200 ° c ., preferably less than 160 ° c . solvents suitable for the practice of the invention include perfluorooctane and derivatives thereof , perfluorodecalins and derivatives , perfluorobenzene , perfluoromethylcyclohexane , perfluorodimethyl - cyclohexane , perfluoro ( n - butyl tetrahydrofuran ), ( c 4 f 9 ) 3 n , ( c 4 f 9 ) 2 s , ( c 2 f 5 ) 2 so 2 , c 8 f 17 so 2 f . preferred solvents include perfluoro ( n - butyl tetrahydrofuran ), ( c 4 f 9 ) 3 n , and perfluorooctane . alternatively , aqueous dispersions of the fluoropolymers suitable for the , practice of the invention may be made and employed to form the compositions of the invention , but they are less effective at wetting the preferred carbon substrates and thus , are less preferred . in a preferred embodiment of the present invention , a copolymer of ltfe and pdd , most preferably having a concentration of pdd of 67 mol -%, ( available as teflon ® af 1600 from the dupont company , wilmington , del . ), in the form of the as - polymerized polymer powder , is dissolved in perfluorooctane , ( available as pf5080 from the 3m company , minneapolis , minn . ), at or above room temperature to form an amorphous fluoropolymer solution of 1 - 30 % solids by weight . an amorphous fluoropolymer solution of 5 to 10 % solids by weight is preferable . in one embodiment of the invention particularly suitable for use in hydrogen fuel cells , a catalyst composition is formed . a metal , metal alloy and / or metal oxide catalyst selected according to the teachings of the art , preferably platinum ( pt ), is combined with carbon particles to form a supported catalyst . the concentration of the catalyst is about 5 - 60 % by weight , preferably 20 %- 40 %, on the weight of the carbon . the carbon is preferably a medium to high surface area powder ( about 100 to about 2000 m 2 / g ). vulcan ® xc72 carbon black available from cabot corp ., billerica , mass . has been found to be highly suitable . the thus - formed supported catalyst is slurried with a 5 - 10 % solids by weight dispersion of a substantially fluorinated , preferably perfluorinated ionomer in water , alcohol , or , preferably a water / alcohol mixture ( commercially available from dupont company as se - 5112 ) to form a catalyst dispersion . preferred ionomers are perfluorinated copolymers of ptfe and a monomer having pendant groups described by the formula where r and r ′ are independently selected from f , cl or a perfluorinated alkyl group having 1 to 10 carbon atoms , a = 0 , 1 or 2 , b = 0 to 6 , and m is h or a univalent metal . preferably , r is trifluoromethyl , r ′ is f , a = 0 or 1 , b = 1 , and m is h or an alkali metal . most preferably , a = 1 and m is h . when m is not h , an additional ion exchange step must be introduced at some convenient stage in the process herein outlined to convert m to h . contacting the ionomer with a mineral acid in any convenient manner will suffice . suitable ionomers have equivalent weights in the range of 700 - 2000ew . the resulting catalyst dispersion is then slurried with the amorphous fluoropolymer solution ( so as to result in about 1 - 20 wt % of the amorphous fluoropolymer in the final dry composition ) as hereinabove described to form a uniform catalyst paste or ink . any additional additives such as are commonly employed in the art may also be incorporated into the slurry . the resulting catalyst paste or ink may then be coated onto an appropriate substrate for incorporation into an mea . the method by which the coating is applied is not critical to the practice of the present invention . numerous methods are practiced in the art . one method is to first combine the catalyst ink of the invention with a gdb , preferably but not necessarily the gdb of the invention , and then , in a subsequent step , with the spe membrane . the thermal consolidation step of he sintering process required for ptfe , shown in fig1 , is now omitted since the high temperature consolidation of the fluoropolymer is no longer required . instead , the consolidation is performed simultaneously with consolidation of the mea at a temperature no greater than 200 ° c ., preferably in the range of 140 - 160 ° c . in a preferred embodiment , a ccm of the present invention comprises a thin catalyst layer containing an amorphous fluoropolymer disposed upon a solid polymer electrolyte ( spe ) membrane . the catalyst layer is preferably less than about 10 μm in thickness with the carbon supported catalyst loading less than about 0 . 35 mgpt / cm 2 . in one method of preparation , the catalyst film is prepared as a decal by spreading the catalyst ink on a flat release substrate such as kapton ® polyimide film ( available from the dupont company ). before the ink dries , the decal is transferred to the surface of the spe membrane by the application of pressure and optional heat , followed by removal of the release substrate to form a ccm with a catalyst layer having a controlled thickness and catalyst distribution . alternatively , the catalyst layer containing an amorphous fluoropolymer is applied directly to the membrane , such as by printing , and then the catalyst film is dried at a temperature not greater than 200 ° c . preferably , the catalyst ink comprises the alkali metal ionomer form of the resin employed to form the spe membrane , and is converted to the protonated form of the ionomer after consolidation with the spe membrane by contacting the catalyst layer with a mineral acid . the ccm , thus formed , is then combined with a gdb , preferably of the invention , to form the mea of the present invention . in the process of the present invention , the mea is formed , by layering the catalyst ink , the spe membrane , and the gdb , wherein at least one , and preferably both , of the catalyst ink and the gdb comprise an unconsolidated amorphous fluoropolymer , followed by consolidating the entire structure in a single step by heating to a temperature no greater than 200 ° c ., preferably in the range of 140 - 160 ° c ., and applying pressure . both sides of the mea can be formed in the same manner and simultaneously . also , the composition of the catalyst layer and gdb could be different on the two sides of the mea . preferred solid polymer electrolyte membranes are ionomers comprising perfluorinated copolymers of ptfe and a monomer having pendant groups described by the formula where r and r ′ are independently selected from f , cl or a perfluorinated alkyl group having 1 to 10 carbon atoms , a = 0 , 1 or 2 , b = 0 to 6 . preferably , r is trifluoromethyl , r ′ is f , a = 0 or 1 , b = 1 ,. most preferably , a = 1 . preferably , and in like manner to the above , a second coating formed in the same way from the same ingredients is applied to the second side of the preferred solid polymer electrolyte membrane . in another embodiment of the present invention , particularly suitable for use in direct methanol fuel cells , a catalyst composition is formed in the manner hereinabove described however , the carbon catalyst support is omitted . the unsupported catalyst composition so formed may be used instead of the carbon - supported catalyst composition in the above described procedures for forming a ccm and an mea . in a preferred embodiment , the gas diffusion backing of the invention is formed by dipping , at room temperature for a period of at least 30 seconds , a porous conductive substrate ( preferably a conventional graphite paper or cloth ( e . g ., tgph - 090 and tgph - 060 available from the toray company , japan ) commonly employed in the art ), into a & lt ; 5 % solids solution in pf5080 of the most preferred terpolymer of we , pmvf , and peve hereinabove . ( one of skill in the art , however , will recognize that gas diffusion backing may be made of numerous other materials including metals and polymers .) preferably , the paper or cloth is soaked until the concentration of the fluoropolymer in the carbon paper is about 3 % by weight , then removed from the solution , and the residual solvent removed by evaporation as hereinabove described . it has been found in the practice of the present invention that the mea performance is degraded when amounts of the amorphous fluoropolymer of the invention exceed about 5 - 6 % by weight . other means known in the art may be employed for applying the fluoropolymer of the invention to the gas diffusion backing including spray - coating . in the practice of the invention , the catalyst layer of the invention is thermally consolidated with a gdb and a spe membrane at a temperature of under 200 ° c ., preferably 140 - 160 ° c ., to form an mea of the invention . the gdb may be made of any type known in the art or , alternatively , in accordance with the present gdb invention . the catalyst layer of the present invention may be deposited onto the surface of the spe membrane prior to consolidation with the gdb , the method of deposition being any known in the art . or , the catalyst layer of the invention may first be deposited on the gdb by methods known in the art prior to consolidation with the spe membrane . similarly , the gdb of the invention , is thermally consolidated with a catalyst layer and an spe membrane at a temperature of under 200 ° c ., preferably 140 - 160 ° c ., to form an electrode of the invention . the catalyst layer may be that of the invention but need not be . the catalyst layer may be deposited onto the surface of the spe membrane prior to consolidation with the gdb , the method of deposition being any which is known in the art . or , the catalyst layer may be first deposited on the gdb of the invention by methods known in the art prior to consolidation with the spe membrane . for the present invention , either the catalyst layer of the present invention or the gdb of the present invention disclosed herein are required . preferably , the catalyst layer and the gdb are both of the invention , with the catalyst layer and spe membrane being first formed into a ccm as described above . in the practice of the present invention , the solvent is removed , the amorphous fluoropolymer coagulated , and the mea is formed in a single step of beating slowly to a temperature between room temperature and 200 ° c ., preferably 140 - 160 ° c . the meas incorporating a gdb backing of the present invention , having only about 3 % by weight of amorphous fluoropolymer , exhibit highly optimized electrochemical performance similar to or better than the meas of the known art which require about 10 - 30 % of a semi - crystalline fluoropolymer . in the present invention , in addition to replacing the semi - crystalline fluoropolymers taught in the art with a relatively new class of amorphous fluoropolymers which exhibit a glass transition temperature only and do not exhibit a crystalline melting point , the amorphous fluoropolymers of the present invention readily form solutions rather than the dispersions of the more highly crystalline polymers of the art . this improves and simplifies the application of the fluoropolymers of the present invention to the catalyst composition and the gas diffusion backing . additionally , the present invention combines the improved uniformity and adhesion of a catalyst coated membrane with proper water management via controlled hydrophobicity . furthermore , in the present invention , optimum performance is achieved at 50 - 80 % lower concentrations of fluoropolymer than taught in the art . the following specific examples are intended to illustrate the practice of the invention and should not be considered to be limiting in any way . examples 1 - 4 and comparative examples 1 - 3 describe the effects of adding an amorphous fluoropolymer to the catalyst layer . in these examples and comparative examples the gdb is prepared according to a method of the art . in examples 1 - 4 and comparative examples 1 - 3 , a catalyst paste was formulated as follows : 15 g of a 20 % by weight pt carbon - supported pt catalyst ( johnson mathey , ward hill , mass . ), was placed in an ice - cooled glass jar . in a nitrogen atmosphere , 60 g of a 5 wt % nafion ® alcohol / water solution ( dupont , se5112 ) and 48 g of 1 - methoxy2 - propanol ( aldrich chemical ) were added and mixed well using a tempset virti shear stirrer with a setting at 1 for 30 - 45 mins . after stirring , the whole mixture was transferred into a ball mill ( stoneware ball mill , east palestine , ohio ) and milled for 18 hrs using burundam cylinders of size ½ ″× ½ ″. the milled mixture was poured through the filter paper to remove the balls and the balls were washed with additional 1 - methoxy 2 - propanol . the particle size was measured with grind gage # 5252 ( precision cage & amp ; tool co ., ohio ) and found to be 3 - 4 μm . the solvent was evaporated slowly at a moderate temperature ( 50 - 60c .) with nitrogen bubbling for 30 mins to form a catalyst paste . the catalyst paste so prepared contained no fluoropolymer except the nafion ® binder . reference is now made to fig2 , which shows schematically a single cell test assembly . fuel cell test measurements were made employing a single cell test assembly obtained from fuel cell technologies inc , n . mex . as shown in fig2 , a nafion ® perfluorinated ion exchange membrane , 1 , was combined with a catalyst layer , 2 , comprising platinum supported on carbon particles , nafion ® binder , and a gas diffusion backing , 3 , comprising carbon paper and a fluoropolymer , to form an membrane electrode assembly ( mea ). the test assembly was provided with an anode gas inlet , 4 , an anode gas outlet , 5 , a cathode gas inlet , 6 , a cathode gas outlet , 7 , aluminum end blocks , 8 , tied together with tie rods ( not shown ), a gasket for sealing , 9 , an electrically insulating layer , 10 , and graphite current collector blocks with flow fields for gas distribution , 11 , and gold plated current collectors , 12 . fuel cell performance was determined under the following conditions : hydrogen ( 500 cc / min ) and oxygen ( 1000 cc / min ) gases at 30 psi were passed into the anode and cathode side of the fuel cell respectively . these gases were purged through the humidifiers just prior to entering the fuel cell in order to keep the membrane wet the current was observed by varying the potential of the cell at a given temperature . the current for the unit area is calculated from the total current obtained and the potential vs current density plots for the cell at various temperatures are shown in fig3 - 5 . according to a method known in the art , a specimen of toray tgph - 090 carbon paper was soaked for 6 - 8 minutes in teflon ® ptfe t - 30 aqueous dispersion diluted with water in a 4 : 1 ratio of water to teflon ® the teflon ® soaked carbon paper was removed , dried , and sintered according to the cycle shown in fig1 . this sintered ptfe - coated carbon paper was further coated with a slurry formed by adding 80 parts of vulcan ® xc - 72 carbon to 20 parts of teflon ® t - 30 and mixing at high shear . the slurry coated paper was further sintered in a second heating cycle , shown in fig1 , to form a gdb of the art . the final loading of the dried carbon slurry was about 2 mg / cm 2 . applied to the gdb formed , was about al 0 ml portion of the catalyst paste , prepared as described herein above , using a screen printer ( mpm corp ., model tf - 100 ). the thus formed electrodes were first air dried for 30 mins and then oven dried at 90 - 1000 ° c . for 1 hr . the electrodes made by the above process were 25 cm 2 size . two dried 25 cm 2 electrodes were taken and painted , each with 150 mg of 5 wt % nafion ® solution ( se5112 , dupont company ). they were air dried for 20 - 30 mins and oven dried at 90 ° c . for another 60 mins . the dried coated electrodes were positioned on either side of a wet nafion ® n115 perfluorosulfonic acid membrane ( dupont company , wilmington , del .) to form an unconsolidated mea . the unconsolidated mea was placed between two layers of kapton ® polyimide film ( dupont company ) and that assembly between two layers of silicone rubber sheeting , and finally between two flat steel plates . the whole assembly was placed into a hydraulic press preheated to 135 ° c ., and allowed to heat for 3 minutes at just contact pressure followed by application of 3000 lbs of ram force for 2 minutes . the press was cooled to room temperature while the mea assembly was held under pressure , and then the mea was removed and stored in water to maintain the wet condition until used . the mba was placed in the single cell assembly and the cell hardware was tightened to 1 . 5 ft - lbs torque using a wrench . this cell assembly was connected to the test station gt120 ( globetech inc , texas ) and polarization data ( current - potential curve ) was generated at 70 ° c . reference is now made to fig3 , which shows the graphical result for the points corresponding to 0 % teflon ® af , the current density at 0 . 2 volt was about 0 . 8 a / cm2 . 1 . 6 g of a 6 wt % solution of teflon ® af 1601 ( dupont company ) was added to a portion of the catalyst paste prepared as hereinabove described containing 0 . 85 g of pt / c and 0 . 1703 g of nafion ®. the resulting mixture was stirred for 2 hrs to form a catalyst composition containing 8 . 6 wt -% teflon ® af . electrodes and an mea were formed in the same manner as described in comparative example 1 . the mea , so formed , was tested at 70 ° c . as in comparative example 1 . reference is again made to fig3 which shows the graphical result for the points labeled 8 . 6 wt -% teflon ® af . the current density of 0 . 89 a / cm2 at 0 . 2 volt was significantly higher than in comparative example 1 . 0 . 096 g ( 1 . 6 g of 6 wt % solution ) of teflon ® af 1601 was added to another portion of the catalyst paste prepared as hereinabove described containing 0 . 43 g of pt / c and 0 . 086 g of nafion ®. the resulting mixture was stirred for 2 hrs to form a catalyst composition containing 15 . 3 % by weight of teflon ® af . electrodes and an mea were formed in the same manner as described in comparative example 1 . the mea , so formed , was tested at 70 ° c . as in comparative example 1 . in fig3 , the graphical result for these points are labeled 15 . 3 % teflon ® af . the current density of about 0 . 92 a / cm 2 was significantly higher than that in comparative example 1 . the mea of comparative example 1 was tested at 85 ° c . in this comparative example . reference is now made to fig4 , which shows the graphical result for the points labeled 0 % teflon ® af . the current density at 0 . 2 volt was about 1 . 091 a / cm 2 . the mea of example 2 was tested in this example at 85 ° c . reference again is made to fig4 , which shows the graphical result for the points labeled 15 . 3 % teflon ® af . the current density of about 1 . 22 a / cm2 at 0 . 2 volt was higher than that in comparative example 2 . the mea of comparative example 1 was tested at 50 ° c . in this comparative example . results are shown in fig5 for the points labeled 0 % teflon ® af . the mea of example 2 was tested at 50 ° c . in this example . reference is now made to fig5 , which shows the graphical result for the points labeled 15 . 3 % teflon ®) af . the current at 0 . 2 volt was in the same as in comparative example 3 . however , at higher voltages there was a clear increase in current associated with the mea of example 2 . comparative example 4 and examples 5 to 7 describe the effects of adding an amorphous fluoropolymer to the gdb composition , the catalyst layer containing no fluoropolymer except a nafion ® binder was applied to the spe membrane as herein described . a 3 . 5 % solids solution of unhydrolyzed 940ew nafion ® perflouro ionomer resin ( dupont company , wilmington , del .) was formed by combining 586 g of the nafion ® with 16 , 455 g of fluorinerte fc - 40 perfluorinated solvent ( 3m company , minneapolis , minn .) in a 12 l round bottom flask equipped with a stirrer and a water - cooled reflux condenser . the mixture was stirred at 500 rpm for 16 hours at room temperature followed by refluxing at 145 ° . for 4 hours . the resulting solution was cooled and filtered into a 5 gallon plastic pail . a 5 gram sample was dried to determine solids content . 85 g of the nafion ® solution was combined with 15 grams of a 40 % platinum supported on carbon ( etek inc ., natick , mass .) to form a catalyst paste . the carbon was vulcan ® xc - 72 carbon black powder ( cabot corp . billerica , mass .). the mixture was milled for 2 hours , at room temperature , in an eiger mini ® 100 bead mill ( eiger machinery co ., mondelein , ill .) containing 1 . 0 - 1 . 25 mm zirconia beads . following milling , the particle size was determined to be less than i micrometer using a fineness of grind gauge , model 5252 ( precision gauge and tool company , dayton , ohio ) and the % solids was in the range 13 . 56 - 13 . 8 . a 10 . 2 cm × 10 . 2 cm piece of 76 μm thick kapton ® polyimide film ( dupont company , wilmington del . ), after recording its weight , was placed on a flat vacuum board . another piece of 76 μm thick kapton ® film with a 7 . 1 cm × 7 . 1 cm window cut out of it was placed on top of the first piece making sure that the open window in the second piece of film was centered on the first piece . the second piece was slightly bigger than the first to have at least part of it in direct contact with the vacuum board . using a disposable pipette , a small amount (˜ 10 cc ) of the catalyst paste was put on the second kapton ® film just above the open window . with a doctor blade the paste was drawn down so as to fill the area of the open window . the top film was then carefully removed and the coating deposited on the first film was allowed to air dry for several hours until all of the solvent had completely evaporated to form a catalyst coated decal . a wet coating thickness of about 76 μm typically resulted in a catalyst loading of 0 . 3 mgpt / cm 2 in the final ccm . a 10 . 2 cm × 10 . 2 cm piece of wet , acid - exchanged nafion ® n112 perfluoro ionomer membrane ( dupont company , wilmington del .) was sandwiched between two catalyst coated decals formed as hereinabove described . care was taken to ensure that the coatings on the two decals were registered with each other and were positioned facing the membrane . the assembly so formed was introduced between the 20 . 3 cm × 20 . 3 cm platens of a hydraulic press preheated to 145 ° c . the press was closed and brought to a ram force of 22000 n . the sandwich assembly was kept under pressure for ˜ 2 mins and then cooled for ˜ 2 mins still under pressure . the assembly was removed from the press and the kapton ® pieces were slowly peeled off revealing that all the catalyst coating had transferred to the membrane . the ccm thus formed was immersed in a tray of room temperature water ( to ensure that the membrane was completely wet ) and carefully transferred to a zipper bag for storage and future use . prior to forming an mea therewith , in order to hydrolyze the nafion ® in the catalyst layer , the ccms formed as hereinabove were placed between two layers of ptfe lab matting ( obtained from cole - parmer instrument company , vernon hills , ill . 60061 , catalog no . e - 09406 - 00 ) and immersed in a 30 wt % naoh solution at 80 ° c . for 30 min . the solution was stirred to assure uniform hydrolyses . after 30 minutes in the bath , the ccm &# 39 ; s were removed and rinsed completely with fresh deionized water to remove all the naoh . the thus hydrolyzed ccms , still in teflon ® mesh , were then immersed in a 15 wt % nitric acid solution at a temperature of 65 ° c . for 45 minutes . the solution was stirred to assure uniform acid exchange . this procedure was repeated in a second bath containing 15 wt % nitric acid solution at 65 ° c . and for 45 minutes . the ccms were then rinsed in flowing deionized water for 15 minutes at room temperature to ensure removal of all the residual acid . they were then packaged wet until ready for use . 31 ml of teflon ® type 30 , a 60 % solids ptfe dispersion ( dupont company , wilmington del .) was diluted in 469 ml of deionized water , in a glass tray . a 7 . 5 cm × 7 . 5 cm piece of type tgp090 carbon paper ( toray corporation , japan ) was immersed into the dispersion for 1 minute and air dried for 2 hours . the dried film was placed into an oven ( fisher scientific , programmable furnace , model 497 ) and sintered in a nitrogen atmosphere according to the sintering cycle shown in fig1 to form a ptfe - coated gdb . two pieces of carbon paper were thus treated , using separate aliquots of diluted ptfe dispersion . the ptfe concentration was found to be in the range of 8 . 6 - 9 . 5 %. one side of each ptfe - treated gdb was roughened by rubbing with 600 grit sandpaper , and a single cell assembly was constructed for testing , wherein the spe membrane , 1 , and catalyst layer , 2 , form the ccm as herein above described ( see fig2 ). the ccm was placed between the roughened surfaces of the ptfe - coated gdbs , 3 , prepared as hereinabove described , to form the mea . the ccm and the gdb pieces were assembled together without heat consolidation . the single cell assembly was connected to a fuel cell test assembly obtained from the gm / doe fuel cell development center at los alamos national laboratory . reference is now made to fig6 , which shows the voltage - current density profile . this figure shows a performance curve for a cell using gas diffusion backing treated with teflon ® ptfe dispersion . the current density at 0 . 5 volt was about 1 . 2 a / cm 2 . the method for forming a ptfe - coated gdb of comparative example 4 was followed except that the ptfe was replaced by an amorphous terpolymer and the sintering cycle of fig1 was replaced by oven heating to 140 ° c . under vacuum and holding at that temperature for 1 hour . the amorphous terpolymer , comprising 60 mol -% tfe , 26 mol -% perfluoromethyl vinyl ether , and 14 mol -% perfluoroethylvinyl ether produced according to the teachings of anolick et al , u . s . pat . no . 5 , 663 , 255 , was dissolved in pf5080 perfluorooctane available from 3m company , minneapolis , minn ., at the concentrations shown in table 1 , and the carbon paper was soaked 30 seconds with the resultant loading of amorphous fluoropolymer after drying shown as well . reference is now made to fig7 , which shows the fuel cell performance results . in fig7 , 1 . 2 / 2 . 5 stoichiometry @ 1 a / cm 2 refers to the flow rates of hydrogen and air during the fuel cell measurements . hydrogen gas was introduced into the anode side of the fuel cell at a flow rate 12 times that required for the cell to operate at 1 a / cm 2 and air was introduced to the cathode side at a flow rate 2 . 5 times that required for the cell to operate at 1 a / cm 2 . these flow rates in the current cell corresponded to 417 cc hydrogen per minute and 2072 cc air per minute . the gases were humidified to 100 % rh and 50 % rh , respectively , by adding 0 . 08 cc / min and 0 . 176 ml / min of water to the hydrogen and air streams respectively . in fig6 and 7 , similar conditions were applied thus indicating that similar fuel cell performance can be obtained using the new fluoropolymers at a much lower loading than that of the conventionally used ptfe . this is true at the lowest loading of the new fluoropolymer (˜ 3 . 2 wt %) as seen in fig7 .