EA041695B1 - CATALYTIC COMPOSITION AND METHOD FOR ITS PRODUCTION - Google Patents

Description

Technical field

The present invention relates to the catalytic combustion of fuel mixtures. In particular, the present invention relates to the catalytic combustion of pure fuel mixtures.

State of the art

Various types of fuel are used to use energy. Traditionally, most fuels are derived from fossil fuels. However, the use of fossil fuels can lead to emissions of carbon dioxide and other greenhouse gases. It is increasingly clear that these emissions can contribute to anthropogenic climate change and to a decrease in overall air quality.

In response to these discoveries, attempts have been made to change energy sources from fossil fuels to fuels derived from cleaner sources. For example, in many countries coal-fired equipment has been shut down to reduce emissions to improve air quality. Such equipment can be found, for example, at power plants or district heating stations. These stations may include other equipment, such as steam equipment and/or turbines, which may be converted to use other fuels to generate electricity or heat.

One possible source of clean energy is hydrogen. Hydrogen can be produced by a number of methods, including steam reforming or electrolysis. If the electricity for electrolysis comes from clean sources such as nuclear, wind, tidal or solar power, the resulting hydrogen does not generate carbon emissions. Hydrogen reacts with oxygen to form water and release energy.

This reaction has been used in fuel cells to produce electricity directly. However, factors such as membrane degradation and complex fuel cell fabrication methods hinder the introduction of hydrogen as a fuel. Hydrogen has also been used as a fuel in internal combustion engines. However, such systems can be complex and have disadvantages related to the safe handling of said systems.

Catalytic combustion systems have been used, but such systems often require complex or expensive self-sustaining reaction initiation systems, such as preheating systems. Even after starting self-sustaining reactions, such systems often require limitations on the temperatures that can be used due to ablation of the catalytic material and fuel ignition problems in the bulk.

There is a need for improved systems and methods for using clean energy sources.

Brief description of the invention

In one aspect, a catalytic composition is provided comprising a continuous phase containing a hydrogen oxidation catalyst (KOV); and a discrete phase containing an oxygen reduction catalyst (ORC) deposited on the substrate so that a catalytic surface is formed, in which the ratio of the surface area of the OTC to the surface area of the OCR is from 9:1 to 4:1, and the catalytic composition is made with the possibility of low-temperature activation hydrogen combustion reactions. In some embodiments, the ratio of the surface area of the KOV to the surface area of the CVC is about 20:3. In some embodiments, the implementation of KOV and KVK obtained by electrodeposition. In some embodiments, the catalyst is configured to activate the combustion of hydrogen at a temperature below about 140°C. In some embodiments, the catalyst is configured to activate the combustion of hydrogen at a temperature below 20°C. In some embodiments, the KOV is a noble metal. In some embodiments, the KOV is platinum or palladium. In some embodiments, the KOV is palladium. In some embodiments, the CVC is stannous oxide.

In one aspect, a method for producing a catalyst composition is provided, comprising applying the catalyst composition to a substrate to form a catalytic surface, such that the continuous phase deposited on the substrate contains a hydrogen oxidation catalyst (OHC), and the discontinuous phase deposited on the substrate contains an oxygen reduction catalyst (ORC), moreover, the obtained catalytic surface contains a section of KOV and a section of KVK, the ratio of the areas of which is from 9:1 to 4:1, and moreover, the catalytic surface is made with the possibility of low-temperature activation of the hydrogen combustion reaction.

In some embodiments, the ratio of the area of the KOV plot to the area of the KVC plot is about 20:3. In some embodiments, the application of the catalyst composition includes the application of KOV and the application of CVC. In some embodiments, the implementation of the CVC is applied after the application of KOV. In some embodiments, the application of the catalyst composition includes the electrodeposition of KOV, KVK or both of these catalysts on the substrate. In some embodiments, application of the catalyst composition includes electrodeposition of the KOH onto the substrate. In some embodiments, application of the catalyst composition includes electrodeposition of the CVC onto the CCA supported substrate. In some embodiments, prior to applying the catalyst compo

- 1 041695 position on the substrate is applied to the precursor, and the specified precursor enhances the adhesion of the catalytic composition to the substrate. In some embodiments, the precursor is nickel or copper. In some embodiments, application of the precursor comprises electrodeposition of the precursor onto the substrate. In some embodiments, a method for thermally treating a supported catalyst substrate is provided.

In one aspect, a catalytic reactor is provided, comprising a catalytic surface containing said catalytic composition.

Brief description of the drawings

Below, the present invention will be described with reference to the accompanying drawings.

Fig. 1A is a schematic diagram illustrating a catalytic surface showing a continuous phase containing a hydrogen oxidation catalyst and a discontinuous phase containing an oxygen reduction catalyst.

Fig. 1B is a schematic diagram illustrating a catalyst surface showing a continuous phase containing a hydrogen oxidation catalyst and a discrete phase containing an oxygen reduction catalyst, with the total area of the discrete phase being the same as shown in FIG. 1A, but with a larger phase contact perimeter.

Fig. 2 is a flow chart illustrating a method for applying a catalyst composition according to one embodiment of the present invention.

Fig. 3 is a cross-sectional perspective view of a heat exchanger according to one embodiment of the present invention.

Fig. 4 is a flow chart illustrating a method for heating a heat exchange medium according to one embodiment of the present invention.

Fig. 5A is a schematic diagram illustrating catalyst particles sprayed onto a substrate.

Fig. 5B is a schematic diagram illustrating a catalyst deposited on a substrate by electrodeposition according to one embodiment of the present invention.

Fig. 6A is an SEM image showing the presence of palladium and tin on a coated substrate according to one embodiment of the present invention.

Fig. 6B is an SEM image showing the presence of palladium on a coated substrate according to one embodiment of the present invention.

Fig. 6C is an SEM image showing the presence of palladium and tin on a coated substrate according to one embodiment of the present invention.

Fig. 7 is a graph showing the temperature of a system operated according to a method according to one embodiment of the present invention.

Fig. 8 is a cross-sectional perspective view of a heat exchanger according to one embodiment of the present invention. One pair of fuel and oxidizer inlets is shown.

Fig. 9 is a cross-sectional view of a heating element according to the heat exchanger embodiment shown in FIG. 8.

Detailed description of the invention

In the following description, specific details are provided for the purpose of providing a more complete understanding to those skilled in the art. However, well-known elements may not be shown or described in detail in order to avoid unnecessary confusion in understanding the present description. Therefore, the description and drawings are to be considered illustrative and not restrictive.

catalytic composition.

In one aspect, a catalyst composition is provided comprising a hydrogen oxidation catalyst (OHC) and an oxygen reduction catalyst (ORC). The catalytic composition is made with the possibility of low-temperature activation of the hydrogen combustion reaction.

In some embodiments, the ROC is a material on the surface of which molecular hydrogen dissociates into hydrogen radicals. In some embodiments, the KOV is a noble metal. In some embodiments, the noble metal is palladium or platinum. In some embodiments, the noble metal is palladium.

In some embodiments, the implementation of the CVC is a material on the surface of which molecular oxygen dissociates into oxygen radicals. In some embodiments, the CVC is iron, zinc, silver, copper, tin, oxides of these metals, or any combination of these materials. In some embodiments, the implementation of the CVC is SnO ₂ .

In some embodiments, after the introduction of molecular hydrogen and molecular oxygen into the catalyst composition, the KOH causes the molecular hydrogen to dissociate into a radical

- 2 041695 ly hydrogen, and KVK causes the dissociation of molecular oxygen into oxygen radicals. The transfer of two hydrogen radicals to one of the oxygen radicals on the surface of the catalyst leads to the formation of water. In general, the reaction is exothermic and can be considered as catalytic combustion of hydrogen. The energy released during the catalytic combustion of hydrogen can be used for other purposes. In some embodiments, the energy released in the reaction is used to heat the heat exchange medium. In other implementations, the energy released in the reaction is converted into work.

In some embodiments, the catalyst composition lowers the activation energy of the hydrogen combustion reaction so that the reaction proceeds at low temperatures. For example, the activation energy of the reaction can be reduced so that the reaction proceeds at a temperature below 140, 100, 50, 30, 20, 15°C, or even below 10°C. In some embodiments, the hydrogen combustion reaction occurring on the surface of the catalyst does not ignite bulk molecular hydrogen. In such embodiments, the catalytic combustion is flameless catalytic combustion.

In some embodiments, the KOV and KVK are located so as to have a high phase contact perimeter. In some embodiments, the ratio of the surface area of the KOV to the surface area of the CVC is between 9:1 and 4:1. In some embodiments, the ratio of the surface area of the KOV to the surface area of the CVC is about 20:3. In some embodiments, the above ratios of the surface areas of the CFC and CCR provide a sufficient contact perimeter of the phases and the amount of catalytic materials to reduce the activation energy of the reaction so that the hydrogen combustion reaction can proceed at lower temperatures.

In some embodiments, as shown in FIG. 1A and 1B, on the surface of the catalyst 100, the ROC forms a continuous surface area 110, and the CRC forms discrete surface areas 120. In some embodiments, the CTC and CRC are positioned to increase the overall phase contact perimeter between the continuous surface area and the discrete surface areas. For example, reducing the size of each of the areas of the discrete surfaces 120' while increasing the number of areas of the discrete surfaces results in an increase in the total phase contact perimeter for the same total area of the discrete surfaces.

When the activation energy of the hydrogen catalytic combustion reaction is reduced so that the reaction can proceed at low temperatures, such as room temperature, the reaction can be initiated simply by introducing hydrogen and oxygen into the catalyst composition without the need for preheating or other initiation step. By eliminating preheating, the complexity and cost of the hydrogen catalytic combustion system can be reduced. In addition, preheating leads to the potential risk of undesired premature combustion of hydrogen, which can lead to reduced efficiency or safety issues.

Obtaining a catalyst.

In some embodiments, the catalyst composition is prepared according to the method described below. In some embodiments, the catalyst composition is obtained by electrodeposition.

In one aspect, a method 200 is provided for preparing a catalyst composition. As shown in FIG. 2, the method includes providing a substrate in step 202. In step 208, the catalyst composition is applied to the substrate to form a catalyst surface. The catalytic composition includes a hydrogen oxidation catalyst (KOV) and an oxygen reduction catalyst (ORC). The catalytic surface is made with the possibility of low-temperature activation of the hydrogen combustion reaction.

In some embodiments, the catalyst composition contains a KOV region and a CVC region. In some embodiments, the catalytic surface comprises a KOH region and a CVR region, with their area ratio being from about 9:1 to about 4:1. In some embodiments, the ratio of KOV area to KVK area is about 20:3.

In some embodiments, the substrate is resistant to hydrogen embrittlement. In some embodiments, the substrate is graphite, a ceramic material, austenitic stainless steel, aluminum, an aluminum alloy, or a copper alloy. In some embodiments, the substrate is graphite, a ceramic material, austenitic stainless steel, or a copper alloy. In some embodiments, the substrate is graphite or austenitic stainless steel. In some embodiments, the substrate is graphite. In some embodiments, the substrate is 316 stainless steel. In some embodiments, the substrate is a heat conductor. The thermal conductivity of the substrate can reduce the accumulation of heat in the reaction area, which in turn reduces the formation of hot spots.

In some embodiments, the application of the catalyst composition includes the application of the CFC at step 208A and the application of the CFC at step 208B. In some embodiments, the KOV is applied prior to the application of the KVK. In some embodiments, the implementation of the CVC is applied before applying the KOV. In not

- 3 041695 which embodiments of KOV and KVK are applied at one stage. In some embodiments, the application of the catalyst composition includes coating the substrate with KOV, KVK, or both of these materials. In some embodiments, coating includes electrodeposition or the application of molten catalytic material to a substrate. In some embodiments, the coating application includes electrodeposition.

In some embodiments, the application of the catalyst composition results in the formation of a protective surface. For example, in some embodiments, the catalyst composition inhibits oxidation of the substrate. Therefore, in some cases, the use of a catalyst may allow a wider range of substrate materials to be used.

In some embodiments, applying the catalyst composition includes applying precursors or a sublayer. In one embodiment, applying the precursor includes applying a base layer prior to applying the catalyst composition. In some embodiments, the base layer is a sublayer. As used herein, undercoat refers to a layer applied between a substrate and a catalyst to promote bonding or adhesion between the catalyst and the substrate. In one embodiment, the sublayer is nickel. In other embodiments, the sublayer is copper, zinc, or copper. In embodiments involving the application of a sublayer, the method includes one or more final steps, including heat treatment.

In some embodiments, the substrate has a textured surface. The textured surface can provide improved adhesion of the catalytic material to the substrate. The surface texture makes it possible to find a balance between the adhesion of the catalytic material to the substrate and thermal conductivity and structural requirements. In some embodiments, the surface of the substrate has a roughness R _a of approximately 12.5 µm, or an ISO roughness of N10.

In some embodiments, the substrate is roughened at 204 prior to the application of any catalytic material to provide the desired texture. In some embodiments, the substrate is roughened by mechanical processing such as grinding, sandblasting, filing, notching, and rolling.

In some embodiments, the substrate is cleaned at 206 before or during the application of any catalytic material. Cleaning removes contaminants from the surface of the substrate to improve adhesion of the catalytic material. In some embodiments, surface contaminants include grease, residue from mechanical roughening, or both. In some embodiments, cleaning includes electrolytic cleaning, solvent washing, or both. In some embodiments, cleaning includes chemical cleaning, ultrasonic cleaning, or both.

In one preferred embodiment, a base layer is applied at step 207 to the substrate prior to application of the catalyst composition at step 208. In some embodiments, the base layer is a nickel base coat. In one embodiment, the nickel base coating is applied electrolytically using a NiCl salt in a boric acid solvent to a depth of 100 to 500 µm, at a voltage of 3-10 V and a current of 2-5 A. The coating of the substrate is checked using a scanning electron microscope (SEM) / X-ray analysis of variance (RDA). Preferably, a smooth, continuous base coat is applied to a substrate with a coating of greater than 80%, greater than 90%, greater than 95%, greater than 99%, or 100% of the substrate. The nickel base layer promotes the binding of the catalyst to the substrate. In one embodiment, the nickel base layer improves the adhesion of the KOV to the stainless steel substrate because the nickel base layer has a strong affinity or bonding capacity for both the stainless steel substrate and the KOV. In some embodiments, the nickel base layer significantly improves the adhesion of the catalyst to the heating element plates in the reactor and increases the durability of the material.

In other embodiments, applying the KOV in step 208A involves directly coating the catalyst on the substrate. In some embodiments, the coating application comprises electrodeposition of the KOH onto the substrate. In some embodiments, electrodeposition involves applying a current to a substrate immersed in a KOH electrodeposition solution containing a KOH salt and a solvent.

In some embodiments, the implementation of the application of KOV includes applying a coating to a substrate having a coating of the base layer. In one embodiment, the base layer is nickel. In some embodiments, the implementation of the coating includes the electrodeposition of KOV on the substrate, having a coating of the base layer. In some embodiments, electrodeposition includes applying a current to a base layer coated substrate immersed in a KOH electrodeposition solution containing a KOH salt and a solvent.

In some embodiments, the KOV salt is an ammonium salt or chloride. In some embodiments, the KOV salt is palladium ammonium chloride or palladium chloride.

- 4 041695 boat. In some embodiments, the salt is palladium chloride. In some embodiments, the KOH salt is present at a concentration of about 5 to about 15 mM. In some embodiments, the KOH salt is present at a concentration of about 7 to about 10 mM. In some embodiments, the KOH salt is present at a concentration of about 8.8 mM.

In some embodiments, the solvent includes aqueous ammonia.

In some embodiments, the KOH electrodeposition solution contains an agent to improve electrical conductivity. In some embodiments, the conductive agent comprises NaCl.

In some embodiments, electrodeposition includes applying a voltage of about 5 to about 32 V. In some embodiments, electrodeposition includes applying a current of about 0.3 to about 3 A. In some embodiments, electrodeposition is performed for about 15 minutes.

In some embodiments, the thickness of the KOV layer applied to the substrate is from about 100 to about 1000 microns. In some embodiments, the thickness of the KOV layer applied to the substrate is about 250 microns.

In some embodiments, after electrodeposition of the KOV, the substrate is subjected to a treatment to stabilize the KOV. In some embodiments, the stabilizing treatment comprises heating the substrate onto which the KOV has been electrodeposited. In some embodiments, the heating is carried out at a temperature of about 100°C.

In some embodiments, applying the CVC in step 208B includes coating the substrate. In some embodiments, the implementation of the application of the CVC includes the direct application of the CVC to the substrate. In other embodiments, applying the CVC includes applying the CVC to a CCA-coated substrate. In some embodiments, the coating comprises electrodeposition of the CVC onto the substrate. In some embodiments, electrodeposition includes applying a current to a substrate immersed in an KVA electrodeposition solution containing an KVA salt and a solvent.

In some embodiments, the KVC salt is a chloride salt. In some embodiments, the KVC salt is stannous chloride. In some embodiments, the KVA salt is present at a concentration of about 5 to about 10 mM. In some embodiments, the KVA salt is present at a concentration of about 6.6 mM.

In some embodiments, the salt is prepared by dissolving the KVC salt precursor in a solvent. In some embodiments, the KVC salt precursor is an oxide. In some embodiments, the oxide is SnO ₂ .

In some embodiments, the solvent contains hydrochloric acid. In some embodiments, the KVC electrodeposition solution is prepared by dissolving SnO ₂ in HCl. In some embodiments, the KVC electrodeposition solution is prepared by dissolving 1 g of SnO ₂ in 800 ml of 32% HCl.

In some embodiments, electrodeposition includes applying a voltage of about 5 to about 32 V. In some embodiments, electrodeposition includes applying a current of about 0.3 to about 3 A. In some embodiments, electrodeposition is performed for about 7 minutes.

In some embodiments, the thickness of the CVC layer deposited on the substrate is from about 100 to about 1000 microns. In some embodiments, the thickness of the CVC layer applied to the substrate is about 250 microns.

In some embodiments, the substrate is inspected after application of the KOV or KVK to confirm the coverage area of the KOV or KVK. In some embodiments, the substrate is checked using SEM/RDA. In some embodiments, if an insufficient area of coverage is obtained, reapplying the KOV or KVK is carried out. In some embodiments, the heat treatment (described below) results in a reduction in the CVR relative to the ROC. For example, while up to 40% of the surface of a substrate can be coated with CVC after it has been applied (i.e., a 6:4 ratio of CCA surface to CCA surface), only 30% of the surface can be coated with CCA after heat treatment. A pre-heat treatment test can be used to determine if the pre-heat treatment CVC coverage is sufficient to obtain the desired CVC coverage after heat treatment. Therefore, in some embodiments, the target ratio between CVR and ROC after application of the catalytic material is higher than after heat treatment.

A surface coated with CFC, CFC, or a combination thereof, or electrodeposited with CFC, CFC, or a combination thereof, may exhibit less formation of hot spots during catalytic combustion compared to a surface coated with catalyst pellets or particles. Without wishing to be bound by any theory, and with reference to FIGS. 5A and 5B, it is believed that the application of the catalyst 510 in the form of granules or particles results in relatively small areas of contact with the underlying substrate 520. In contrast, electrodeposition of the catalyst material results in a thin layer of KOV and KVK 540 deposited on the KOV layer, whereby warm

- 5 041695 is easily transferred to the substrate. When a fuel mixture containing a fuel and an oxidizer is supplied to the catalytic surface, the fuel undergoes a combustion process to generate heat. If heat is not removed from the catalyst, localized hot spots may form, which may ablate the catalyst from the surface or ignite the fuel mixture, which may cause a fire or explosion. By increasing the area of contact between the catalyst and the underlying substrate, heat can be more effectively removed from the catalyst, which reduces the formation of hot spots. More uniform heat distribution may allow higher operating temperatures to be applied.

In some embodiments, the substrate to which the CCB and CVC has been deposited is subjected to one or more finishing steps 210. In some embodiments, one or more finishing steps include heat treatment. In some embodiments, the heat treatment is carried out in an atmosphere of air or N2. In some embodiments, the heat treatment is carried out in air. In some embodiments, the heat treatment is carried out after the application of the CCA to the substrate, after the application of the CCA to the substrate, or after the application of both catalysts. In some embodiments, the heat treatment includes a KOH heat treatment and a CVC heat treatment.

In some embodiments, the heat treatment of the KOH is carried out after the stabilizing treatment. In some embodiments, the heat treatment of the KOV is carried out at a temperature of from about 800 to about 1200°C. In some embodiments, the heat treatment of the KOV is carried out at a temperature of about 900°C. In some embodiments, the heat treatment is carried out for a period of time from about 30 minutes to about 4 hours. In some embodiments, the heat treatment is carried out for about 1 hour. In some embodiments, the heat treatment causes annealing of the KOV deposited on the substrate. In some embodiments, the heat treatment causes annealing of the KOV deposited on the base layer.

In some embodiments, the CVC heat treatment is carried out after the stabilizing treatment. In some embodiments, the implementation of the heat treatment of the CVC is carried out at a temperature of from about 200 to about 600°C. In some embodiments, the heat treatment of the CVC is carried out at a temperature of about 400°C. In some embodiments, the heat treatment is carried out for a period of time from about 30 minutes to about 4 hours. In some embodiments, the heat treatment is carried out for about 1 hour.

In some embodiments, the heat treatment activates or increases the catalytic activity of the KOV, KVK, or both catalysts. In some embodiments, the heat treatment activates or increases the activity of the CCA. In some embodiments, the heat treatment calcines the KOV, KVK, or both catalysts. In some embodiments, the CFC precursor is applied and the heat treatment causes the formation of the CFC, particularly by converting the CFC precursor to the CFC.

In some embodiments, tin is applied to the substrate and heat treatment causes the formation of stannous oxide.

Reactors.

According to FIG. 3, in one aspect, a reactor 300 is provided. In one embodiment, the reactor is a heat exchanger. The reactor 300 includes a conduit 310 having an inlet 312 for receiving a first fluid material and an outlet 314; and a housing 330 surrounding conduit 310 and having an inlet 332 for receiving a second fluid material and an outlet 334. One of the first fluid material and the second fluid material is a fuel mixture. The other of the first fluid material and the second fluid material is a heat exchange medium. The conduit 310 includes a heating element 316 coated with a catalyst composition comprising a hydrogen oxidation catalyst (OHC) and an oxygen reduction catalyst (ORC). The heating element 316 is configured to carry out catalytic combustion of the fuel mixture and transfer the energy released during catalytic combustion to the heat exchange medium. In some embodiments, the catalyst composition lowers the activation energy of catalytic combustion so that it proceeds at low temperatures.

In some embodiments, the catalyst composition is the catalyst composition described above. In some embodiments, the heating element 316 includes a substrate on which CFCs and CFCs have been applied. In some embodiments, the implementation of KOV and KVK applied to the substrate using the method described above. In some embodiments, the ratio of the surface area of KOV and KVK is from about 9:1 to about 4:1. In some embodiments, the ratio of the surface area of KOV and KVK is about 20:3.

In some embodiments, the fuel mixture contains a fuel and an oxidizer. In some embodiments, the fuel contains hydrogen, a hydrocarbon material, or a mixture of these materials. In some embodiments, the hydrocarbon material is a renewable hydrocarbon material such as biodiesel, biogas, or algal fuel. In some

- 6 041695 embodiments, the fuel is hydrogen. In some embodiments, the oxidant comprises oxygen, oxygen-enriched air, or air. In some embodiments, the oxidizing agent is oxygen.

In some embodiments, the fuel mixture inlet includes a fuel inlet and an oxidizer inlet. Thus, there is no pre-mixing of fuel and oxidizer. By introducing the components of the fuel mixture into the reactor, the composition of the fuel mixture can be better controlled. Any changes in the composition of the fuel mixture introduced into the reactor are carried out more quickly because transport delays can be minimized. Also, if there is no oxidizer in the fuel, transporting the fuel and oxidizer separately may be relatively safer than transporting a fuel mixture.

In some embodiments, the heat exchange medium contains water or helium. In some embodiments, the heat exchange medium contains or is water. In some embodiments, the catalytic combustion of the fuel mixture provides water heating. In some embodiments, water is heated to produce steam. The steam produced in the heat exchanger 300 can be used for various purposes. For example, steam can be used to drive turbines to generate electricity, to provide power for central heating, or for other applications that require steam.

In some embodiments, at least a portion of the heating element 316 is an integral part of the surface of the conduit 310. In some embodiments, at least a portion of the heating element 316 is connected to the surface of the conduit 310.

In some embodiments, heating element 316 includes a plurality of fins 318. The addition of fins can increase the surface area on which catalytic combustion of hydrogen can occur. In some embodiments, one or more of the fins is grooved or bellows-shaped to further increase surface area. In some embodiments, a plurality of fins 318 are connected to conduit 310. Such connection of fins facilitates heat transfer, such as by conduction, from fins 318 to conduit 310 and any material in contact therewith. For example, if the catalytic combustion of the fuel mixture occurs on the surface of the fins 318, the heat generated by the reaction may be transferred to the heat exchange medium through conduit 310.

In some embodiments, the reactor 300 includes a distributor 320 for distributing the fuel mixture near the heating element 316. Distributing the fuel mixture to the heating element 316 may better supply unburned hydrogen to the surface of the heating element 316. In some embodiments, the distributor 320 is in fluid communication with the inlet ( 312 or 332) into which the fuel mixture is supplied. In some embodiments, distributor 320 includes a plurality of curved tubes, each of which forms holes for delivering fuel mixture to heating element 316. individually selected fuel mixture. For example, each of the plurality of pipes may deliver an independent fuel mixture.

In some embodiments, conduit 310 includes a plurality of tubes 322. Thus, the rate of heat transfer to the heat exchange medium is increased by maximizing the surface area to volume ratio. In some embodiments, tubes 322 are arranged in a one-way design in which fluid entering one end of conduit 310 is conducted to the other end. In some embodiments, the tubes are arranged in a multi-pass arrangement in which fluid entering one end of the conduit is conducted to the other end and back to the first end, optionally multiple times.

In some embodiments, conduit 310 receives the heat exchange medium and housing 330 receives the fuel mixture. In such embodiments, the heating element 316 is located on the outside of the conduit 310 and is in contact with the interior of the housing 330. The heat generated during the catalytic combustion of the fuel mixture is transferred to the heat exchange medium located inside the conduit 310.

In some embodiments, the catalytic combustion of the fuel mixture provides heat to the housing 330. In some embodiments, the preheater 340 in contact with the outer surface of the housing 330 transfers heat generated by the catalytic combustion of the fuel mixture, fuel mixture, or heat exchange medium prior to their introduction into the pipeline 310 or housing 330. In some embodiments, preheater 340 is located upstream of conduit 310 and preheats the heat transfer fluid before it is introduced into conduit 310 upstream. In some embodiments, the heat exchange medium is heated to a temperature of about 90° C. before being introduced into the inlet.

In some embodiments, the unreacted fuel in the fuel mixture is returned back to the heat exchanger. Fuel recycling reduces the amount of unburned fuel that

- 7 041695 must be processed or stored. In some embodiments, a downstream condenser (not shown) removes water from the combustion products. By removing water from the combustion products, the recycled fuel can contain less thermal diluent. The thermal diluent may cause a decrease in operating temperature or an increase in the formation of condensate on the catalytic surface, which may reduce or inhibit combustion.

In some of the embodiments where the fuel is hydrogen, the hydrogen-contactable components are made from materials that are resistant to hydrogen embrittlement. For example, materials resistant to hydrogen embrittlement include austenitic stainless steel, copper, copper alloys, aluminium, aluminum alloys, and ceramic materials.

In some of the embodiments where the housing 330 receives the fuel mixture, the interior of the housing is lined with reflective material to reduce or minimize heat radiation losses. In some embodiments, the heat exchanger includes insulation surrounding the housing. In some embodiments, the insulation is glass wool.

As shown in FIG. 8, another embodiment of a reactor 800 with improved conduction heat transfer is provided. In some embodiments, the interweaving of the heating elements and the first and second fluid conduits allows greater heat transfer, as well as the ability to scale with large volumes of fluid and fuel.

The reactor 800 includes a conduit 810 having an inlet 812 for receiving the first fluid material and an outlet 814. The conduit 810 is connected to a heating element 816, on which a catalyst composition containing a hydrogen oxidation catalyst (HOX) and an oxygen reduction catalyst (ORC) is applied. The heating element 816 is configured to perform catalytic combustion of the fuel mixture and transfer the energy released during catalytic combustion to the heat exchange medium. In some embodiments, the catalyst composition lowers the activation energy of catalytic combustion so that it proceeds at low temperatures. Conduit 810 and heating element 816 are located in a reaction cavity surrounded by housing 830. Housing 830 has one or more inlets for receiving a second fluid material. In one embodiment, the first fluid material is a heat exchange medium and the second fluid material is a fuel and an oxidizer. In some embodiments, the second fluid material is a mixture of fuel and oxidizer. In preferred embodiments, fuel and oxidizer are fed separately and are not premixed. In some embodiments, the fuel is a mixture of one or more different types of fuel.

In one embodiment, the housing includes a pair of inlets 832a, 832b for receiving the fuel mixture into the reaction cavity. In some embodiments, the second fluid material includes a fuel and an oxidizer. One of the inlets 832a, 832b is for receiving fuel and the other is for receiving oxidizer. In some embodiments, the fuel is the fuel described above. In some embodiments, the heat exchange medium is the heat exchange medium described above.

In some embodiments, the catalyst composition is a catalyst composition as described above. As shown in FIG. 9, in some embodiments, heating element 816 includes a plurality of horizontal plates 950a, 950b, 950c, which are coated with CFC and CFC. In some embodiments, KOV and KVK are applied to the plates using the method described above. In some embodiments, the ratio of the surface area of KOV and KVK is from about 9:1 to about 4:1. In some embodiments, the ratio of the surface area of KOV and KVK is about 20:3.

In some embodiments, heating element 816 includes a plurality of plates, including corrugated plates. In some embodiments, some of the plurality of plates are corrugated. In some embodiments, a plurality of corrugated plates are stacked. In some embodiments, conduit 810 is located adjacent to the area where one plate contacts another.

In some embodiments, each plate has a cross-sectional shape including alternating projections 952 and recesses 954. Examples of cross-sectional shapes include, but are not limited to, sine waves, zigzag, curved, scalloped, and scalloped. In preferred embodiments, each plate is connected to an adjacent plate by one or more joints 956. In some embodiments, one or more joints hold adjacent plates at some distance from one another. In one embodiment, the first side of the connection is attached to the top surface of the protrusion on one plate, and the second side of the connection is attached to the bottom surface of the recess on the other plate. In some embodiments, each connection occupies the entire width of the plate and contains a clearance 958 to accommodate the pipe.

- 8 041695 conduit 810. In one embodiment, the connection is formed by two connection elements, each of which contains an elongated open channel, while one of the elements is welded to one plate, and the second is welded to an adjacent plate. When the two plates are stacked, the two elongate open channels are connected to form a continuous lumen 958 to receive conduit 810. In other embodiments, the connection includes a recess to receive conduit 810.

In some embodiments, a plurality of horizontal plates are stacked and held together by a compressive force provided, for example, by a clamp or bolts. In some embodiments, a plurality of horizontal plates and joints are held together by a compressive force provided, for example, by a clamp or bolts. In an alternative implementation, a plurality of horizontal plates and joints are welded or interconnected. In another embodiment, a plurality of plates are directly welded or connected to each other, without connecting elements, and contain an elongated cavity in the area where adjacent plates contact or are interconnected to accommodate the pipeline.

In some embodiments, the plurality of stacked plates have a common cross-sectional shape, such as a lattice, honeycomb, or damask pattern.

In one embodiment, the heating element comprises a plurality of plates stacked, where each plate measures approximately 30mm by 400mm. In another embodiment, the heating element comprises six plates stacked, where each plate measures approximately 100mm by 200mm.

In some embodiments, conduit 810 weaves through gaps in connections, forming a loop 860 at the region where conduit exits one gap and enters the next gap. In some embodiments, loop 860 extends beyond the width of the plurality of plates. In some embodiments, the conduit is positioned in a one-way structure across the lumen such that fluid entering one end of the lumen is conducted to the other end of the lumen. In some embodiments, conduit 810 is arranged in a multi-way arrangement through the lumen such that fluid entering one end of the lumen is conducted to the other end of the lumen and back to the first end, and optionally multiple times.

In some embodiments, a plurality of plates are flat and each plate is connected to an adjacent plate by a plurality of elongated joints that extend the full width of the plates and keep the plates spaced apart. In this embodiment, the connections comprise a lumen through which conduit 810 is weaved.

In some embodiments, each tubing segment 910 passing through the lumen is separated from the next segment by a distance w, where w is at least 10, at least 20, at least 30, preferably at least 40 mm. In one embodiment, w is at least 42 mm. In some embodiments, each row of conduit intertwined between a pair of plates is separated from the next row by a distance h, where h is at least 10, at least 15, at least 20, preferably at least 25 mm. In one embodiment, h is at least 26 mm.

In some embodiments, a plurality of plates are integral with the surface of conduit 810. In some embodiments, at least a portion of the plurality of plates are connected to the surface of conduit 810.

In some embodiments, reactor 800 includes a distributor 820 for distributing fuel and oxidizer near the plates. The distribution of fuel and oxidizer to the plates can provide a better supply of unburned hydrogen to the surface of the plates. In some embodiments, distributor 820 is in fluid communication with one or more inlets that receive fuel and oxidizer. The distributor extends along the width of the plates through a cavity 970 formed by the protrusion of one plate and the depression of the other plate. In some embodiments, distributor 820 includes fuel mixture delivery ports in cavities 970 formed between the plates. In some embodiments, the distributor 820 includes a plurality of holes of the same or different sizes along the length of the distributor extending along the width of the plates. In some embodiments, the size of the holes along the length of the distributor varies to provide some balance in flow rate. For example, the opening closest to the inlet end of the distributor is smaller than the openings at the end of the distributor farthest from the inlet. Other sizes are also possible and known to those skilled in the art.

In some embodiments, a pair of distributors 920a, 920b are in fluid communication with a corresponding pair of inlets 832a, 832b, which respectively receive fuel and oxidizer. Both distributors in a pair pass through a cavity 970 defined by a protrusion of one plate and a recess of the other plate, thereby allowing both fuel and oxidizer to be delivered to cavity 970. 972, and the second of a pair of distributors is located

- 9 041695 lies closer to or substantially within the portion of the cavity formed by recess 974. In some embodiments, each of the pair of distributors 920a, 920b contains a plurality of holes of the same or different sizes along the length of the distributor, which is located along the width of the plates. The holes along one of the distributors in the pair coincide in longitudinal arrangement and are opposite the corresponding holes in the second distributor in the pair. The gaseous fuel and oxidizer, meeting each other at the outlet of the distributors located opposite the feed tubes, mix turbulently, forming a mixture of fuel and oxidizer, which comes into contact with the surrounding catalytic surface of the plates. One of the advantages of feeding the fuel and oxidizer separately and mixing them in the reactor as late as possible is that it allows for more efficient combustion, with minimal pollutant emissions and maximum fuel burn.

In some embodiments, the distributor has a diameter of 3-10, 5-8, 6-7, preferably 6.35 mm. In some embodiments, the holes have a size in the range of 0.1-2, 0.5-1.5, preferably 1 mm. Other sizes are also possible.

In some embodiments, the reactor contains a network of distributors or a plurality of pairs of distributors for distributing fuel and oxidizers into various cavities formed between the plates. In preferred embodiments, each cavity houses a pair of distributors in fluid communication with a corresponding pair of inlets. In such embodiments, there are a plurality of pairs of inlets and a corresponding plurality of pairs of distributors. In some embodiments, the distributor has an open end in fluid communication with the fuel mixture inlet and a closed end. Thus, the fuel mixture is introduced through the inlets, then it exits through the holes serving as outlets. In some embodiments, each of the pair of distributors has an open end and a closed end, and openings through which fuel and oxidizer exit to achieve a high degree of mixing of the fuel and oxidizer before they come into contact with the surface of the plates. In alternative embodiments, a distributor or a pair of distributors intertwine through various cavities formed between the plates.

In some embodiments, the reactor is a modular unit having its own housing, heating element, heat exchange fluid conduit, and fuel inlet. In one embodiment, the catalytic combustion system comprises a plurality of modular reactors. In one embodiment, each block, which is a modular reactor, contains a heating element with 30 heating plates with a diameter of 400 mm and a thickness of about 1 mm. In some embodiments, the catalytic combustion system comprises more than 3, more than 5, more than 10, or more than 20 modular reactor units. In one embodiment, the catalytic combustion system comprises 4 to 6 modular reactor units. In one embodiment, the units, which are modular reactors, are stacked. Providing reactors in modules has many advantages, including the ability to replace one module independently of the others, for maintenance or repair.

In some embodiments of the catalytic combustion system, the pipeline is a separate pipeline for each element of the modular reactor. In some embodiments, the catalytic combustion system comprises a network of conduits arranged in parallel or in series to deliver a heat exchange medium to each of the modular reactor elements. In some embodiments where the catalytic combustion system comprises stacked modular reactor elements, the conduit is configured to supply the heat exchange medium through the conduit inlet located at the bottom of the modular reactor and withdraw it through the conduit outlet located at the top. modular reactor. The outlet of the conduit of the first modular reactor in the stack is in fluid communication with the inlet of the conduit of the second modular reactor in the stack. Thus, the number of elements of the modular reactor in the catalytic combustion system can be changed depending on the desired output of the heat exchange medium from the uppermost unit, which is a modular reactor.

In some embodiments, the reactor according to the present description contains a plurality of heating elements, each of which contains a plurality of plates. In some embodiments, the reactor according to the present disclosure comprises a modular heating element, with each modular unit comprising a plurality of plates.

Heat exchange.

In prior art heat exchangers, a hot medium is typically provided within the conduit and a cold medium is provided to transfer heat from the hot medium to the cold medium. To maximize fuel combustion and simultaneously maximize heat transfer, improved reactors and catalytic surfaces according to the present disclosure have been developed that are more efficient when a cold environment (i.e. heat exchange medium) is provided inside the tube.

- 10 041695 wire surrounded by a hot medium (i.e. a heating element coated with a catalytic composition).

In addition, during the initial start-up of the heat exchanger, early heat loss due to conduction heat transfer to the heat exchange medium can reduce the efficiency of the catalytic composition-supported heating element at the start of combustion. To avoid significant delay or slow initial temperature rise, the reactors of the present disclosure also have the advantage of more effectively controlling these early start-up heat losses by entangling tubing between the plates and looping the tubing outside the width of the plates so that the looping portion is not in contact with the plates.

In one aspect, a method 400 for heating a heat exchange medium is provided, as shown in FIG. 4. 402 shows a catalytic surface containing a hydrogen oxidation catalyst (OHC) and an oxygen reduction catalyst (ORC). The catalytic surface is configured to reduce the activation energy of combustion of the fuel mixture containing fuel and oxidizer, resulting in combustion proceeding at low temperatures. At 404, the fuel mixture is supplied to the catalytic surface. In step 406, the fuel mixture is burned on the catalytic surface. In step 408, the heat generated by the catalytic combustion is transferred to the heat exchange medium.

In some embodiments, KOV and KVK are present in a ratio of from about 9:1 to about 4:1 by surface area. In some embodiments, KOV and KVK are present in a ratio of about 20:3.

In some embodiments, the fuel mixture contains a fuel and an oxidizer. In some embodiments, the fuel contains hydrogen, a hydrocarbon material, or a mixture of these materials. In some embodiments, the hydrocarbon material is a renewable hydrocarbon material such as biodiesel, biogas, or algal fuel. In some embodiments, the fuel is hydrogen. In some embodiments, the oxidant comprises oxygen, oxygen-enriched air, or air. In some embodiments, the oxidizing agent is oxygen.

In some embodiments, the combustion products from catalytic combustion contain water. The accumulation of water on the catalytic surface reduces the surface available for catalysis of the combustion of the fuel mixture. In some embodiments, catalytic combustion occurs at low pressure. Low pressures can lower the boiling point of water. The reduced boiling point can reduce the accumulation of liquid water on the catalytic surface by increasing the rate of water evaporation.

In some embodiments, the implementation of the supply of the fuel mixture includes changing the composition of the fuel mixture. In some implementations, the supply of the fuel mixture includes a start-up phase 404A, an operating phase 404B, or both of these phases.

During the startup phase 404A, the catalytic surface is at an initial temperature. In some embodiments, the initial catalyst surface temperature is below 100, 50, 30, 20, 15, or even below 10°C. In some embodiments, the fuel mixture provided during the startup phase 404A is relatively enriched in oxygen. The relatively oxygen-enriched fuel mixture can undergo catalytic combustion at a lower temperature than the fuel-rich mixture. In some embodiments, the ratio of oxygen to fuel in the fuel mixture supplied during the startup phase is from about 1:2 to about 1:1. In some embodiments, the ratio of oxygen to fuel in the fuel mixture supplied during the startup phase is about 11:14. Catalytic combustion leads to heating of the catalytic surface. In some embodiments, the startup phase lasts up to 1 hour, 45 minutes, 30 minutes, or even 20 minutes.

As shown in FIG. 7, in a specific embodiment of the present invention, the fuel mixture is fed into the reactor. The initial temperature was equal to the ambient temperature (about 25°C). The temperature rose slowly over about 10 seconds until reaching about 35°C, after which it continued to rise much faster. Without wishing to be bound by theory, it is believed that at the initial temperature, the activation energy was sufficient to activate the reaction, but with a relatively slow reaction rate. As the reaction proceeded, energy was released due to the exothermic catalytic combustion reaction. This resulted in an observable increase in temperature and provided additional energy, resulting in increased reaction rates and resulted in a faster temperature rise. In contrast, in a system fed with the same fuel mixture but with palladium as the only catalytic material in a similar heating element, no temperature rise above ambient temperature was observed even after more than 1 hour.

In some embodiments, once the catalytic surface temperature has exceeded about 140°C, the process enters operation phase 404B. In some embodiments, the fuel mixture composition is relatively rich in fuel. In some implementations, the catalog

- 11 041695 Thermal combustion of a fuel mixture relatively rich in fuel can proceed at higher operating temperatures because there is no excess oxidizer acting as a thermal diluent. In some embodiments, the ratio of oxygen to fuel in the fuel mixture supplied during the operating phase is from about 2:5 to about 2:3. In some embodiments, the ratio of oxygen to fuel in the fuel mixture supplied during the operating phase is about 3:4. In some embodiments, catalytic combustion during the operating phase occurs on a catalytic surface with an operating temperature of greater than 300, 400, 500, or even greater than 600°C. In some embodiments, the operating temperature exceeds 600°C. Higher catalytic surface temperatures result in a larger temperature gradient with the heat exchange medium, which increases the amount of heat transferred to the heat exchange medium.

In some embodiments, the fuel mixture contains limited or no thermal diluent. For example, air is a mixture of gases including nitrogen, oxygen and carbon dioxide. All gases in the air, other than oxygen, have limited reactivity and can serve as thermal diluents that absorb some of the heat generated during catalytic combustion, due to which the temperatures that can be achieved with catalytic combustion of the fuel mixture will be lower than if the fuel mixture contained a limited amount or did not contain a thermal diluent. In addition, at high operating temperatures, the presence of nitrogen can lead to the formation of undesirable NOx. Therefore, in some embodiments, the oxidant is oxygen-enriched air or oxygen. In some embodiments, the oxidizing agent is oxygen.

In some embodiments, catalytic combustion is carried out at subatmospheric pressure. In some embodiments, catalytic combustion is carried out at pressures below 100, 90, 80, 70, 60, or even below 50 kPa. At a pressure below atmospheric pressure, the boiling point of water decreases, thereby reducing the likelihood of accumulation of liquid water on the catalytic surface. In addition, at lower pressures, the ability of the fuel mixture to burn in volume can be reduced, which can provide greater safety.

In some embodiments, the heat exchange medium is water, a traditional cooled helium loop, pCO ₂ (superheated carbon dioxide). In some embodiments, the transfer of heat to water results in the formation of steam. Steam can be used, for example, to drive turbines, to power central heating systems, or in desalination operations.

In some embodiments, the catalytic surface is at least a portion of the heating element surface of the heat exchanger described above. In some embodiments, the catalytic surface is obtained using the method described above. In some embodiments, the catalyst surface contains the catalyst composition described above.

In one aspect, a catalytic combustor is provided. The catalytic combustion chamber contains a catalytic surface. The catalytic surface contains the catalytic composition described above or obtained using the method described above.

In some embodiments, the heat generated by the operation of the catalytic combustor is used as a heat source to produce work. In some embodiments, the heat generated from the operation of the catalytic combustor is used to drive a Stirling engine, a turbine, an air conditioning phase change operation, a central heating system, or a desalination system. For example, in some embodiments, the catalytic combustor is a heating element included with reactor 300. In another embodiment, the catalytic combustor is a graphite block with an opening configured to receive a Stirling engine expansion cylinder. In some embodiments, the heat generated from the operation of the catalytic combustor is used to generate steam. For example, the catalytic combustion chamber may be part of the reactor described above.

In one aspect, a method for catalytically combusting a fuel mixture is provided. The fuel mixture containing the fuel and the oxidant is fed into the above-described catalytic combustion chamber and subjected to catalytic combustion on the catalytic surface of the catalytic combustion chamber. In some embodiments, catalytic combustion is performed similarly to heating the heat exchange medium described above, except that heat is not necessarily transferred to the heat exchange medium.

Examples

Example 1. Obtaining a catalytic composition.

A 0.8 mm thick disc was cut from a 316 stainless steel sheet. Mounting holes were drilled in the disk. The disc surfaces were mechanically roughened to ISO N10 roughness using carborundum paper with gradually decreasing grit from 30 to 800.

- 12 041695

A solution for electrodeposition of KOV was obtained by dissolving 1 g of PdCl in 800 ml of 30% ammonia. A disk and a palladium electrode of the same area were mechanically suspended in the solution and an electric current of 1 A at 30 V was applied for 15 min. The goal was to obtain a uniform palladium coating with a thickness of approximately 250 µm.

After coating was completed, the disc was removed, washed with distilled water, and gently blotted with a soft cloth to remove excess remaining liquid. The disc was then heated in a commercial oven at 100° C. for about 15 minutes to remove any remaining electrodeposition solution.

Conducted a visual inspection of the surface to confirm the application of a homogeneous coating without visible substrate. If the coverage was marginal, a multipoint SEM/RDA study was performed. Electroplating was repeated if necessary.

After coating was confirmed, the disc was annealed at 900°C for 1 h and then allowed to cool to room temperature.

Solution for electrodeposition KVK was obtained by dissolving 1 g of SnO ₂ in 800 ml of 32% HCl.

The cooled disk was mechanically suspended in the KVK electrodeposition solution and an electric current of 10 V 3 A was passed through the disk and a similarly sized palladium electrode for 7 min.

After completion of CVC electrodeposition, the disc was removed and washed with distilled water. The test was repeated to confirm that tin electrodeposition had occurred on at least 30% of the surface.

After confirmation of the coating, the disk was annealed at 400°С for 1 h.

An SEM/XRD image showing the catalyst composition applied to the substrate is shown in FIG. 6A-C. The following parameters were used to obtain the image:

accelerating voltage: 15.0 kV, resolution: 512x512 dots, visible resolution: 50%, processing time: 5, image width: 1.567 mm, mixed circuit: Lal palladium (red), Lal tin (green).

Example 2 Catalytic Combustion Using a Catalyst Composition.

A reactor was used with a catalyst composition applied to a heater located in the reactor as shown in FIG. 3. The system operated in such a way that water entered the pipeline, and the fuel mixture entered the housing.

Water was pumped through the system from the reservoir using a pump until water began to flow from the water/steam outlet through the open valve. Then the outlet valve of the water subsystem was closed. The pressure in the internal environment of the case was lowered to obtain a vacuum of about 2 kPa (abs). Then hydrogen and oxygen were introduced into the internal cavity through a regulator, controlled by a mass flow meter. Initially, the flow was set to provide a supply of hydrogen and oxygen in a ratio of about 14:11. A number of thermocouples were used to monitor internal and external temperatures.

As shown in FIG. 7, the initial internal temperature was about 25°C. A relatively slow initial rise in temperature was observed over about 10 seconds. After reaching a temperature in the range of about 40 to 60°C, the rate of temperature increase increased significantly. The temperature reached an equilibrium value in the range from about 350 to 400°C.

Water was circulated in the subsystem and the steam pressure was controlled by opening an outlet valve to keep the steam pressure below 800 kPa.

The fuel mixture flow rate was then adjusted to increase the amount of H2 injected and then the amount of O2 injected, until the internal pressure in the vacuum system could no longer be maintained below about 100 kPa (abs).

The temperature was raised to about 600° C. and high quality steam was obtained.

Example 3 Catalytic Combustion Using a Catalyst Composition Spread on Corrugated Heating Plates.

A reactor was used with the catalyst composition deposited on a plurality of corrugated plates arranged in the reactor as shown in FIG. 8. The system was operated in such a way that water entered the pipeline, and hydrogen and oxygen entered the casing through two separate inlets. Water was pumped through the system, and then hydrogen and oxygen were introduced into the internal cavity in the same way as described in example 2 above.

The initial internal temperature was about 11°C (data not shown) and the system exhibited a temperature rise profile or trend similar to that shown in FIG. 7, with the formation of high quality steam.

While a number of exemplary aspects and implementations have been described above, one skilled in the art will appreciate that certain modifications, changes, additions, and subcombinations are possible.

-

Claims (21)

tion. In the above description, for the purpose of explanation, numerous details are shown to provide a thorough understanding of the present invention. However, the person skilled in the art will understand that these specific details are not necessary for the practice of the present invention. Although certain dimensions and materials are described for carrying out the described exemplary embodiments, other suitable dimensions and/or materials may be used within the scope of the present invention. All such modifications and variations, including all relevant current and future changes in technology, are considered to be within the scope and scope of the present invention. All references mentioned in the present description, fully incorporated in the present description by reference. CLAIM 1. Catalytic composition containing a continuous phase containing a hydrogen oxidation catalyst (KOV); and a discrete phase containing an oxygen reduction catalyst (ORC); deposited on the substrate so that a catalytic surface is formed, in which the ratio of the surface area of the KOV to the surface area of the CVC is from 9:1 to 4:1; moreover, the catalytic composition is made with the possibility of low-temperature activation of the hydrogen combustion reaction. 2. Catalyst composition according to claim 1, characterized in that the ratio of the surface area of the KOV to the surface area of the KVK is about 20:3. 3. Catalyst composition according to claim 1 or 2, characterized in that KOV and KVK are obtained by electrodeposition. 4. Catalyst composition according to any one of claims 1 to 3, characterized in that the catalyst is adapted to activate the combustion of hydrogen at a temperature below about 140°C. 5. Catalyst composition according to claim 4, characterized in that the catalyst is configured to activate the combustion of hydrogen at a temperature below 20°C. 6. Catalyst composition according to any one of claims 1 to 5, characterized in that the KOH is a noble metal. 7. Catalyst composition according to claim 6, characterized in that the KOV is platinum or palladium. 8. Catalyst composition according to claim 7, characterized in that the KOV is palladium. 9. Catalyst composition according to any one of claims 1 to 8, characterized in that the CVC is iron, zinc, silver, copper, tin, oxides of these elements or combinations of these materials. 10. Catalyst composition according to claim 9, characterized in that the CVC is a stannous oxide. 11. A method for producing a catalytic composition, which includes applying the catalytic composition to a substrate to form a catalytic surface so that the continuous phase deposited on the substrate contains a hydrogen oxidation catalyst (KOV), and the discrete phase deposited on the substrate contains an oxygen reduction catalyst (ORC); moreover, the obtained catalytic surface contains the plot KOV and plot KVK, the ratio of the areas of which is from 9:1 to 4:1; and the catalytic surface is configured to low-temperature activation of the hydrogen combustion reaction. 12. The method according to claim 11, characterized in that the ratio of the area of the KOV section to the area of the KVK section is approximately 20:3. 13. The method according to claim 11 or 12, characterized in that the application of the catalyst composition includes the application of KOV and the application of KVK. 14. The method according to claim 13, characterized in that the KVK is applied after the application of the KOV. 15. The method according to any one of claims 11 to 14, characterized in that the application of the catalyst composition comprises the electrodeposition of KOV, KVK or both of these catalysts on the substrate. 16. The method according to claim 15, characterized in that the application of the catalytic composition includes the electrodeposition of KOV on the substrate. 17. The method according to claim 16, characterized in that the application of the catalytic composition includes the electrodeposition of KVK on the substrate with applied KOV. 18. The method according to any one of claims 11 to 17, further comprising applying a precursor to the substrate prior to applying the catalyst composition, said precursor enhancing the adhesion of the catalyst composition to the substrate. 19. The method according to claim 18, characterized in that the precursor is nickel or copper. 20. The method according to claim 18 or 19, wherein the application of the precursor comprises electrodeposition of the precursor onto the substrate. 21. The method according to any one of claims 11-20, further comprising heat treatment of the substrate -