Patent Application
20150064606
The invention relates to assemblies of a porous metallic gas diffusion substrate and a polymeric separator membrane, e.g. for use in alkaline electrolysers and in alkaline fuel cells. The invention further relates to a method for the production of such an assembly.
Electrolysers and fuel cells comprise electrodes (anodes and cathodes) and a separator, impervious to gas at least in operating conditions, separating the anode and the cathode. The separator can be a polymeric separator membrane. Since fuel and reaction products are available in gaseous and liquid state, the electrodes must provide the means to allow the diffusion of these fuel and reaction products to and from the reaction zone. This can be realized by using electrodes with an open channel structure, e.g. mesh, stretch metal or porous metal substrate. A catalyst can be used, wherein the catalyst is provided on the electrode or on the separator (e.g. on a polymeric separator membrane). The porous metal substrate and—present—the catalyst form part of the electrode. It is preferred that the reactive sites of the electrodes are in close contact with the membrane for highest efficiency of the electrolyser or fuel cell.
It is current practice to manufacture a separator membrane and to manufacture porous substrates separately. A catalyst can be provided on the separator membrane or on the porous substrates. The separator membrane and the porous substrate are combined in a separate process into a so-called membrane-electrode assembly (MEA) that is used in the electrolyser or in the fuel cell.
For use in alkaline electrolysers, polymeric separator membranes can be used that are gas tight when filled with wet electrolyte. Examples are membranes that comprise a particulate inorganic hydrophilic material in an organic polymeric binder, see e.g. EP0232923A. The document describes a method for preparing an ion-permeable diaphragm comprising an organic fabric embedded in a film forming mixture of a particulate inorganic hydrophilic material and an organic polymeric binder.
WO 93/15529 describes a method for making a porous membrane for alkaline electrolysers comprising the steps of making a suspension from a solution of an organic binder (preferably polysulphone and use of polyvinyl pyrrolidone as pore-forming agent) and a metal oxide or metal hydroxide (preferably zirconium oxide), applying the suspension on a support by extrusion and removing the solvent by extraction through immersion in an organic non-solvent. Other methods and compositions are described e.g. in WO 2006/15462, WO 2009/147084 and WO 2009/147086. In order to have an adequate polymeric separator membrane, a reinforcing web or reinforcing fabric is required in the polymeric separator membrane. Otherwise, problems arise in the production of the membrane electrode assembly due to limited dimensional stability of the polymeric separator membrane. Double sided coating of a reinforcing web or reinforcing fabric for the production of a separator membrane is disclosed in WO 2006/015462, WO 2009/147084 and WO 2009/9147086. The presence of the reinforcing web or reinforcing fabric has drawbacks for the performance of the electrochemical cell. Another drawback is that two coating processes or a double sided coating process are required to make the polymeric separator membrane reinforced with a web of fabric.
It is a problem that the production of the stack of assemblies of the porous gas diffusion layer with the membrane is complex. An assembly is made today by pressing the gas diffusion layers and the membrane together. Multiple assemblies are further combined together into a stack. The membrane needs to be perfectly flat at this assembly process. If the flatness is not achieved, performance (efficiency) and lifetime of the electrochemical cell are negatively affected. In the prior art, the flatness can be realized by means of the use of a reinforcing carrier web of fabric in the membrane. The presence of a supporting substrate in the membrane also results in a thicker membrane than required functionally and in a reduction of the efficiency of the electrolyser or fuel cell using such a membrane. Furthermore, a thicker membrane leads to increased dimensions of the electrolyser stack which is negative in terms of machine footprint. Moreover, the reinforcing carrier web is usually a polymeric fabric which limits the maximum operational temperature of the electrolyser.
It is a drawback of the prior art that the membrane production and the production of the assembly of the membrane and the gas diffusion layer is in different steps.
A high performance of the system—expressed in performance per unit of area of the membrane surface—is required by users of electrolysers and fuel cells.
A first objective of the invention is to provide an assembly of a porous metallic gas diffusion substrate and a polymeric separator membrane that results in higher efficiency when used in a fuel cell or in an electrolyser.
It is a second objective of the invention to provide an assembly of two porous metallic gas diffusion substrates with in between a polymeric separator membrane that results in higher efficiency when used in a fuel cell or in an electrolyser.
It is another objective of the invention to provide a production method for an assembly of a porous metallic gas diffusion substrate and a polymeric separator membrane in which the polymeric separator membrane is an ion-permeable separator that is gastight when saturated with electrolyte. The result is higher energy efficiency when used in an alkaline fuel cell or in an alkaline electrolyser. The benefits of the production method include one-step roll to roll production of an assembly of a porous metallic gas diffusion substrate and a polymeric separator membrane.
It is another objective of the invention to provide an assembly of a porous metallic gas diffusion substrate and a polymeric separator membrane of reduced thickness that results in reduced machine footprint.
It is another objective of the invention to provide an assembly of porous metallic gas diffusion substrate and a polymeric separator membrane that allow operation of the electrolyser at increased temperature resulting in higher efficiency of the electrolyser.
It is another objective of the invention to provide an inline production method to produce an assembly of two porous metallic gas diffusion substrates with in between a polymeric separator membrane.
According to a first aspect of the invention an assembly is provided of a porous metallic gas diffusion substrate and a polymeric separator membrane for use in an alkaline electrolyser or alkaline fuel cell. The polymeric separator membrane comprises inorganic hydrophilic particulates dispersed in an organic polymeric binder and is gas tight when filled with electrolyte. The polymeric separator membrane is penetrating into at least a top portion of the porous metallic gas diffusion substrate.
Preferably, the polymeric separator membrane is devoid of a reinforcing web that is incorporated in the polymeric separator membrane, or the polymeric separator is devoid of a reinforcing fabric that is incorporated in the polymeric separator membrane.
The assembly according to the first aspect of the invention is providing a higher efficiency when used in an alkaline hydrolyser or fuel cell compared to prior art products. The increased efficiency is thanks to a synergetic combination of a number of elements: increased stability, maintaining high flow rate of the separator membrane, the flatness of the membrane, the membrane can be made thinner and the contact between separator membrane and electrode is more intense (e.g. via a partial penetration of the membrane into the top portion of the porous metallic gas diffusion substrate) and higher maximum operational temperature.
The porous metallic gas diffusion substrate which is a functional element for the electrochemical cell acts at the same time as reinforcement for the ion-permeable separator membrane. In addition, the flatness and increased stability of the separator membrane is ensured by the invention. Absence of a supporting web or supporting fabric incorporated in the polymeric separator membrane has the benefit that the electrolyser can be operated at higher temperature, resulting in increased performance and efficiency.
The porous metallic gas diffusion substrate can be an open cell porous metal substrate. The porous metallic gas diffusion substrate can e.g. comprise sintered metal powder webs or expanded metal plates, more preferably sintered or unsintered metal fiber webs. If the polymeric separator membrane is contacting an unsintered or sintered metal fiber web of the porous metallic gas diffusion substrate, it is penetrating into at least a top portion of the unsintered or sintered metal fiber web.
The porous metallic gas diffusion substrate can be provided with a (precious) metal, metal oxide or organic metallic catalyst on the side onto which the polymeric separator membrane is formed.
The polymeric separator membrane of the invention can be a polymeric membrane layer that has a porous structure, is wettable and swellable with an electrolyte solution, that is sufficiently gastight when saturated with an electrolyte solution such that mixing of gases formed during the electrolysis is prevented, and is capable of transporting ions with low electrical resistance.
The polymeric membrane layer preferably comprises at least a polymer and inorganic particles (preferably zirconium oxide) dispersed in the polymeric membrane layer. Preferred organic binders are polysulphone and preferred use in production is made of polyvinyl pyrrolidone as pore-forming agent. The polymeric membrane layer can be prepared by coating a paste layer onto the substrate, followed by a phase inversion process in the coated layer to form a porous structure in that layer. The structure and ion conductivity of such membrane separators can be improved if dispersed zirconium oxide particles are incorporated. The weight ratio of the zirconium oxide particles with respect to the pore-forming polymer is preferably in the range of 2:1 to 19:1.
The depth of the penetration of the polymeric separator membrane in at least a top portion of the porous metallic gas diffusion substrate is preferably higher than the average diameter of the pore size in the porous metallic gas diffusion substrate and more preferably higher than the average diameter of the pore size in the top portion of the porous metallic diffusion substrate (meaning the portion of the metallic substrate which is in contact with the polymeric separator membrane). The average pore size of a porous metallic gas diffusion substrate can be determined by means of the bubble point method, according to ASTM E128-61, equivalent to ISO 4003.
Preferably, the penetration depth is less than 25% of the thickness of the porous metal diffusion substrate, more preferable less than 10%. Preferably, the penetration depth is higher than 1% of the thickness of the porous metal diffusion substrate.
A level of penetration is beneficial as it creates an intimate contact between electrode (and its reactive sites) and the polymeric separator membrane. The result is increased performance, e.g. in terms of reduced voltage drop at any given current density (leading to improved energy efficiency of the system). An excessive penetration depth is less preferred, as it blocks part of the porous metal diffusion substrate.
The porous metallic gas diffusion substrate can be a multilayer material. The multilayer material can be formed by different materials, e.g. a woven metal screen with a sintered metal fiber web on it; or be formed by same materials, e.g. multiple layers of metal fiber webs, e.g. metal fiber webs of different fiber types (diameters, lengths, chemical type or alloys) or porosity.
In a preferred embodiment, the porous metallic gas diffusion substrate comprises a sintered or an unsintered metal fiber web, e.g. comprising nickel, titanium, stainless steel, zirconium or fibers of alloys thereof, and of any other metal alloy known to be compatible with use in alkaline environments.
For alkaline electrolysers, nickel fibers are most preferred because of the reactivity of nickel in water electrolysis in alkaline environment, which, when using the assembly of the invention, makes it possible to obtain high efficiency, even without using a catalyst. Preferable equivalent metal fiber diameters are 5 to 100 μm, more preferably 20-50 μm. With equivalent diameter is meant the diameter of a circle that has the same surface as the cross section of the metal fibers.
The cross section of the metal fibers can be round or can be polygonal (e.g. rectangular, hexagonal, triangular, square). The metal fibers can be bundle drawn, can be produced via shaving or via machining, as is known in the art.
Average fibre lengths of the metal fibres can be between 1 and 100 mm, preferably between 5 and 50 mm.
A preferred porosity range of the porous metallic gas diffusion substrate is 50 to 95%, more preferably 60 to 80%, resulting in the good combination of properties for best efficiency of the alkaline hydrolyser or alkaline fuel cell.
The porous metallic gas diffusion substrate can comprise several layers, e.g. several layers of sintered on unsintered metal fiber webs, e.g. two layers, e.g. three layers. The layers can have the same or a different structure and/or composition, e.g. layers with different porosity.
The porous metallic gas diffusion substrate can comprise one or more mesh layers (e.g. woven metal meshes). For instance, the meshes (e.g. 1 to 6 meshes, preferably 2 to 4 meshes) can be co-sintered with one or more layers of metal fibers webs.
In a further preferred embodiment, the metallic gas diffusion substrate comprises a number of fiber web layers, e.g. two fiber webs, wherein part of or all the fiber web layers have different physical properties.
Metallic gas diffusion substrates that contain a number of different sintered or unsintered metal fiber web layers can be used. It is preferred that a layer with finer fibers and/or lower porosity is in contact with the polymeric separator membrane in order to provide a good and smooth contact as finer fibers provide more contact points between diffusion substrate and separator membrane. More homogenous contact and equal pressure drop over the separator membrane is a result, increasing the efficiency of the electrolyser or fuel cell. Other layers of the metallic gas diffusions substrates can comprise coarser fibers and/or have higher porosity levels, beneficial for the flow through of liquid and gaseous products. The use of coarser fibers provides stability and integrity of the metallic gas diffusion substrate and hence also of the electrolyser or fuel cell stack.
In a more preferred embodiment in which the metallic gas diffusion substrate comprises a number of fiber web layers, the two sides of the metallic gas diffusion substrate have a different average pore size and the polymeric separator membrane is positioned on the side of the metallic gas diffusion substrate with the smallest average pore size.
According to a second aspect of the invention an assembly is provided of two porous metallic gas diffusion substrates with in between a polymeric separator membrane. The assembly is suited for use in an electrolyser or in a fuel cell. The assembly comprises an assembly of a porous metallic gas diffusion substrate and a polymeric separator membrane as in the first aspect of the invention and a second porous metallic gas diffusion substrate. The polymeric separator membrane is positioned in between both metallic gas diffusion substrates. The second porous metallic gas diffusion substrate can be selected from the same group of candidates as the metallic gas diffusion substrate of the first aspect of the invention. Preferably, both metallic gas diffusion substrates are the same.
Preferably, the polymeric separator membrane of the assembly of two porous metallic gas diffusion substrates with in between a polymeric separator membrane is penetrating at least into a top portion of the second porous metallic gas diffusion substrate. The benefit is a further increased efficiency of the electrolyser or fuel cell using such an assembly.
According to a third aspect of the invention, a method is provided for the production of an assembly of a porous metallic gas diffusion substrate and a polymeric separator membrane as in the first aspect of the invention. The method comprises the steps of
With “coating” is meant the application of a layer of paste on a side of the porous metallic gas diffusion layer. Any known method can be used, e.g. knife or doctor blade coating, extrusion coating, slot coating, roller coating . . . .
An anti-wetting agent can be provided on the porous metallic gas diffusion substrate prior to coating the paste onto it, in order to restrict the extent of penetration of the paste into the metallic substrate.
Preferably for the invention, the full functional surface of the first porous metallic gas diffusion substrate will be coated to form a polymeric separator membrane.
Preferably, the coating is performed in one single coating operation. Alternatively, the coating can be performed in different steps in which each time a layer of paste (the same or a different paste) is applied.
In a preferred embodiment of the third aspect of the invention, the paste comprises a solvent and the method comprises the additional step of evaporating at least part of the solvent of the paste after coating the paste onto the porous metallic gas diffusion substrate. The evaporation of the solvent can be in part or in full.
In a preferred embodiment of the third aspect of the invention, the method comprises the additional step of coagulating the paste after it has been coated onto the porous metallic gas diffusion substrate. The coagulation step allows the formation of the polymeric separator membrane on the porous metallic gas diffusion substrate.
A preferred paste is a composition comprising a solution of a pore-forming polymer in a solvent and a dispersion of zirconium oxide particles in the polymer solution.
Suitable pore-forming polymers include polysulphone (PSU), polyvinyl chloride (PVC), polyacrylonitrile (PAN), polyester, polyethersulphone (PES), polyetherketone (PEK), polyetheretherketone (PEEK), polyvinylidene fluoride (PVDF), polyphenylene sulfide (PPS), polyvinyl acetate (PVAc), polyvinyl alcohol (PVA), polyamide (PA), polyvinylpyrrolidone (PVP), crosslinked PVP, cellulosics such as cellulose acetate (CA) and cellulose triacetate (CTA), polycarbonate block polymers, a rubber selected from the group consisting of silicone rubber, polymethylpentene, Chloroprene, SBR, NBR, Urethane, Hypalon®, Neoprene, Nitrile, Buna, Urethane, Epichlorohydrin, Viton®, EPDM, Butyl, Natural Rubber (Latex), acrylrubber, fluoroelastomers and, perfluoroelastomers, and mixtures/blends thereof. Further suitable membrane polymers include chlorinated polyvinyl chloride (CPVC), copolymers of acrylonitrile e.g. with vinyl chloride or ethyl acrylate, polyethylene succinate (PESU), polyurethanes (PU), polyimides (PI), polyetherimide (PEI) and cellulosics such as hydroxypropyl cellulose (HPC), carboxymethyl cellulose (CMC), and cellulose tricarbanilate (CTC) mixtures/blends thereof and their grafted derivatives (sulphonated, acrylated, aminated . . . ).
The pore-forming polymer preferably includes polysulphone (PSU), polyvinylidene fluoride (PVDF), poly(acrylonitrile) (PAN), polyethyleneoxide (PEO), polymethylmethacrylate or copolymers thereof. Polyvinylidene fluoride (PVDF), copolymers of vinylidene fluoride (VDF) and organic polymers composed of primarily of polyvinylidene fluoride are particularly preferred from the point of view of oxidation/reduction-resistance and film-forming properties. Among these, terpolymers of vinylidene fluoride (VDF), hexafluoropropylene (HFP) and chlorotrifluoroethylene (CTFE) are preferred for their excellent swelling property, heat resistance and adhesion to electrodes.
The paste may further comprise a hydrophilizing and stabilizing agent such as polypropylene glycol, ethylene glycol, tripropylene glycol, polyethylene glycol (PEG) such as PEG 8000 and PEG 20000, glycerol, polyhydric alcohols such as glycerine, dibutyl phthalate (DBP), diethyl phthalate (DEP), diundecyl phtalate (DUP), isononanoic acid, and neo decanoic acid can also be incorporated after the phase-inversion process is completed, but before drying. Other suitable hydrophilic polymers include poly(vinyl pyrrolidone) (PVP), crosslinked polyvinylpyrrolidone (PVPP), poly(vinyl alcohol), poly(vinyl acetate), methyl cellulose and polyethylene oxide.
The solvent of the solution of the pore-forming polymer in the paste is preferably a polar solvent. Suitable polar organic solvents include N-methyl-pyrrolidone (NMP), N-ethyl-pyrrolidone (NEP), N,N-dimethylformamide (DMF), formamide, dimethylsulphoxide (DMSO), N,N-dimethylacetamide (DMAC), acetonitrile and mixtures thereof. Films formed by immersion of a polysulphone-NMP solution in water are porous. However, different membrane structures can be obtained upon immersion of a polysulphone-NMP-THF solution in water. Often a variation in solvent mixture will give rise to different film morphologies and hence in membrane performance.
Inorganic particles such as TiO2, HfO2, Al2O3, ZrO2, Zr3(PO4)4, Y2O3, SiO2, perovskite oxide materials, siliconcarbide (SiC) and C(Pt/Rh/Ru), with metal oxides and hydroxides being preferred e.g. a titanium oxide can be used and/or added to the paste, alone or in combination. Inorganic oxides and hydroxides have the additional advantage of increasing the ionic conductivity of the ion-permeable separator membrane. Highly preferred materials are zirconium oxide particles.
The paste preferably has a ratio of viscosity at a shear of 1 s−1 to the viscosity at a shear of 100 s−1 at the impregnation temperature of at least 2.0, more preferably at least 2.5, most preferably at least 5. The viscosity ratio can be increased by adding an inorganic pigment or a polymer as thickener.
The phase inversion process is preferably a process wherein a wet layer of the paste, coated on a porous metallic gas diffusion substrate, is treated with a solvent, which is a non-solvent for the pore-forming polymer, to induce coalescence of the polymer and forming a porous structure in the polymeric layer. Coalescence of the polymer can be obtained by contacting the wet paste layer with a non-solvent in the vapour phase and/or by immersing the wet paste layer in a non-solvent in liquid phase. In a preferred process, the wet paste layer is transported through a zone, which is saturated by vapour of a non-solvent, immediately after the coating step, usually followed by immersing the paste layer in a non-solvent liquid. Usually, the solvent of the paste composition and the non-solvent for inducing coalescence are miscible. Coalescence of the polymer by immersing the wet paste layer into a non-solvent in liquid phase is known as coagulation.
The non-solvent can be any solvent wherein the pore-forming polymer has a poor solubility such that the polymer precipitates (or coagulates), more preferably wherein the pore-forming polymer is insoluble. Typically, the non-solvent includes water vapour phase (water vapour or cold steam, preferably at a vapour pressure of 0.02 to 5 bar and particularly preferably at a vapour pressure of 0.05 to 0.2 bar), water, alcohols such as methanol, ethanol, propanol, isopropanol, buthanol, ethylene glycol, tripropylene glycol, polypropylene glycol, 1,3-butanediol, 1,4-butanediol, polyethylene glycol monoethyl ether, and polyhydric alcohols such as glycerol, and a mixture of two or more of them. If a water bath is used as a source of water vapour for the phase inversion, the vapour can be realized by forced convection across the surface of the water bath or by allowing the atmosphere in a closed region above a heated water bath to come into equilibrium with the heated water bath below e.g. overnight. When phase inversion occurs in a water bath, the water should preferably be replaced when the concentration of the solvent removed from the paste in the water reaches 20% by weight. Hence, preferably the phase inversion is a coagulation.
In the coagulation step following immediately after the coating step, the pore formation is induced from both sides of the paste coated porous metallic gas diffusion layer. The pore formation can be split up into two phases: the skin pore formation (outer pores) and bulk pore formation (internal pores). The skin pores are formed by the contact with the non-solvent vapour, followed by coagulation of the pore-forming polymer. The bulk pores are formed by diffusion from the non-solvent into the polymer layer, followed by extraction of the solvent in the paste composition. This gives a wide variety of parameter tools for developing the desired composite or complex pore structures. The use of vapour or liquid during the phase inversion process determines the pore size attainable with pore sizes below 10 μm being obtained with vapour-induced phase separation (VIPS) and pore sizes below 50 nm being obtained with liquid-induced phase separation (LIPS). The choice of separator membrane polymer and pigment also has an influence upon the pore size. It is known that the structure of such separator membranes depends on the speed at which the solvent is removed. This speed is clearly different depending on the choice of non-solvent.
Separator membranes prepared by coating onto the porous metallic gas diffusion layer have the advantage of obtaining a smooth surface and a fine symmetrical pore structure which are sufficiently gastight when saturated with electrolyte to prevent mixing of gases and to avoid the occurrence of gas leakage through the separator membrane.
In an alternative method, separator membrane formation can be performed by evaporation of the solvent (dry phase inversion). The paste may comprise two solvents in which case the solvent having the lower boiling point is evaporated first and a membrane composition is formed. The solvent with the higher boiling point is trapped in the pores of the membrane composition and is evaporated afterwards.
According to a forth aspect of the invention a method is provided to produce an assembly comprising two porous metallic gas diffusion substrates with in between a polymeric separator membrane as in the second aspect of the invention, comprising the steps of
It is a benefit of this aspect of the invention that the polymeric separator membrane is in close contact (e.g. via partial penetration of the membrane into a top portion of both porous metallic gas diffusion layers) of the membrane with both porous metallic gas diffusion substrates, leading to increased efficiency of the electrolyser or fuel cell using this assembly. It is another benefit of this aspect of the invention that an assembly of two porous metallic gas diffusion substrates with a polymeric separator membrane in between can be produced in one single continuous process. A catalyst can previously have been applied on the side of the second porous metallic gas diffusion substrate that will be contacted with the polymeric separator.
In a specific embodiment of the forth aspect of the invention, the polymeric separator membrane of the assembly of two porous metallic gas diffusion substrates with in between a polymeric separator membrane is obtained via laminating to each other two assemblies made as in the third aspect of the invention, with the two polymeric separator membrane surfaces facing each other to form one single polymeric separator membrane. The lamination can be performed via thermal lamination (e.g. hot pressing, in a continuous or in a discontinuous way) or by means of the application of an appropriate adhesive.
A fifth aspect of the invention is an alkaline electrolyser or an alkaline fuel cell comprising an assembly of a porous metallic gas diffusion substrate and a polymeric separator membrane as in the first aspect of the invention.
Another aspect of the invention is an alkaline electrolyser or an alkaline fuel cell comprising an assembly of two porous metallic gas diffusion substrates with in between a polymeric separator membrane as in the second aspect of the invention.
An example of a paste that can be used according to the invention to coat a membrane layer onto the porous metallic gas diffusion layer contains 49.07 percent by weight of Zirconia (e.g. type E101 from MEL-Chemicals), 8.66 percent by weight of a polysulphone, 1.10 percent by weight of glycerol; and 41.17 percent by weight of N-ethyl pyrrolidone (NEP).
Instead of the above described pre-metered slot die system, also a simple doctor blade (or bar) coater with adjustable distance between bar and substrate can be used. In this case, the coated weight is depending on gap distance, rheological properties of paste, coating speed and properties of the substrate. When using the pre-metered slot die, the coating weight depends only on the flow dosed by the feeding pump, the coating width and the coating speed and not on the rheology of the paste or properties of the substrate.
Phase inversion can be realized by inversion, coagulation and washing by immersion in a water bath at a temperature of 60° C. to remove the solvents N-ethyl-pyrrolidone and glycerol followed by rinsing. Pore sizes in the range of 50 nm to 100 nm were thereby realized. Finally the resulting porous layers were dried at 40° C. for 60 minutes.
Samples of assemblies according to the first aspect of the invention have been made using different porous metal gas diffusion substrates. A first group of porous metallic gas diffusion substrates are sintered stainless steel fiber web comprising two layers. The first layer is 150 gram per square meter of 6.5 μm diameter stainless steel fibers on top of 450 gram per square meter of 8 μm diameter stainless steel fibers. This composition was compressed and sintered into two samples with different porosity values: 60% (having an average pore size of 8 μm) and 80% (having an average pore size of 16 μm).
A second group of porous metallic gas diffusion substrates are sintered stainless steel fiber web comprising two layers. The first layer is 600 gram per square meter of 12 μm diameter stainless steel fibers on top of 450 gram per square meter of 22 μm diameter stainless steel fibers. This composition was compressed and sintered into two samples with different porosity values: 60% (having an average pore size of 15 μm) and 80% (having an average pore size of 30 μm).
A third group of porous metallic gas diffusion substrates are sintered stainless steel fiber web comprising two layers. The first layer is 600 gram per square meter of 22 μm diameter stainless steel fibers on top of 600 gram per square meter of 30 μm diameter stainless steel fibers. This composition was compressed and sintered into two samples with different porosity values: 60% (having an average pore size of 27.5 μm) and 80% (having an average pore size of 55 μm).
Assemblies of porous gas metal diffusion substrates and polymeric separator membranes have been made via coating a suitable paste onto the porous metallic gas diffusion substrates. Samples have been made with a dry coating weight of the separator membrane on the porous gas metal diffusion substrate between 200 and 400 gram per square meter.
A paste has been made comprising the following ingredients:
The polysulphone (P-1800 NT 11-Solvay) was first dissolved in a mixture of glycerol and N-ethyl pyrrolidone with stirring over 30 minutes followed by adding the zirconium oxide and stirring for a further 120 minutes.
In order to make the test samples, a similar coating and coagulation set up as described in
By adjusting the distance between substrate and the doctor blade, different thicknesses of the paste were applied. Depending also on paste temperature, coating speed, gap provided by the doctor blade and properties of porous metal substrate, different total coating weights of membrane were obtained. Part of the total applied paste was penetrating into the porous substrate depending on the parameters mentioned.
A laboratory electrolyser test set up was built in order to evaluate the assemblies of porous gas metal diffusion substrates and polymeric separator membranes (according to the first aspect of the invention) that have been produced. Potassium hydroxide in water was used as electrolyte. The exposed test sample was a square of 3 cm by 3 cm (or 9 square cm). This test sample (according to the first aspect of the invention) served as the cathode of the electrolyser cell, with the separator membrane facing a platinum coated titanium counter electrode (the anode). An EA source type PS 3016-20B was used to apply an electrical voltage to the anode and cathode of the electrolyser cell with as settings a constant current of 4 Ampere, meaning 0.44 Ampere/square cm sample surface. The temperature of the electrolyte was controlled and held at 70° C. The electrolyte was stirred in a constant way during the experiments. During the electrolysis experiment at constant current, the total power consumption as well as the volume of produced gas (hydrogen and oxygen) was continuously measured.
Electrolysis experiments with the test samples according to the invention used as cathode have shown to result in a 25% lower power consumption (measured in Watt) for the same gas production rate (measured in volume of gas produced per unit time) compared to when the test sample (cathode) was replaced with an identical porous metallic gas diffusion substrate which is brought in close contact (through applying pressure) with an identical polymeric separator membrane.
| Number | Date | Country | Kind |
|---|---|---|---|
| 12161650.2 | Mar 2012 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2013/054882 | 3/11/2013 | WO | 00 |
| Number | Date | Country | |
|---|---|---|---|
| 61616437 | Mar 2012 | US |
