Zero-carbon emission device and process for generating hot air or high-temperature steam or producing pure water

Abstract

The present invention discloses a zero-carbon emission device and process for generating hot air or high-temperature steam or producing pure water, including a gas storage unit, a gas guiding device, a reaction chamber, and a heating guiding device. The gas storage unit is used to store hydrogen gas and oxygen gas or air respectively. The gas storage unit is respectively connected to the reaction chamber through the gas guiding device. The gas guiding device is used to transport the oxygen gas or air and hydrogen gas of the gas storage unit into the reaction chamber. The reaction chamber is further provided with a wet hot air outlet connected to the heating guiding device. The reaction chamber is provided with a plurality of layers of sequentially connected pipes, and the pipes are filled or coated with a catalyst to form a catalyst bed layer. Oxygen gas or air and hydrogen gas respectively enter the reaction chamber from the oxygen gas or air intake and the hydrogen gas intake, react in contact with the catalyst in the reaction chamber, and the formed wet hot air is directionally guided by the heating guiding device to the space that requires heating. The device can not only heat the room and humidify the air, but also play the role of purifying the air.

Description

Technical Field

[0001] The present invention relates to the field of indoor heating technology or the field of production of warm water and pure water, and specifically relates to a zero-carbon emission device and process for generating hot air or high-temperature steam or producing pure water.

Background Art

[0002] At present, the development of new energy in the world is urgent. The reason is that the energy used, such as oil, natural gas, coal, and oil gas, all belong to non-renewable resources, and their reserves on the earth are limited. However, since energy is essential for human survival, new energy must be explored. As the consumption of fossil fuels increases, their reserves are decreasing, and it is urgently necessary to find new energy-containing substances with abundant reserves that do not rely on fossil fuels. Hydrogen is exactly such a secondary energy. Hydrogen is located at the top of the periodic table, has an atomic number of 1, is gaseous at normal temperature and pressure, and is liquid at ultra-low temperature and high pressure. As an ideal new energy-containing substance, it has the following characteristics.

[0003] 1. Lightest in weight: Under standard conditions, its density is 0.0899 g / L, and it can become liquid at -252.7 °C. If the pressure is increased to several hundred atmospheres, liquid hydrogen can become metallic hydrogen. 2. Best in thermal conductivity: It is 10 times higher than the thermal conductivity of many gases. 3. Abundant in storage: It is estimated to constitute 75% of the cosmic mass, mainly stored in water in the form of compounds, and water is the most widespread substance on Earth. If all the hydrogen in seawater is extracted, the total heat generated is estimated to be 9000 times greater than the heat released by all the fossil fuels on Earth. 4. Recycling: The waste discharged from hydrogen energy vehicles is only water, so hydrogen can be decomposed again and recycled. 5. Ideal calorific value: The calorific value of hydrogen other than nuclear fuel is the highest among all fossil fuels, chemical fuels, and biofuels, at 142351 kJ / kg, which is 3 times the calorific value of gasoline. 6. Excellent combustion performance: It has a fast ignition speed, a wide flammable range when mixed with air, a high flash point, and a fast combustion speed. 7. Environmentally friendly: Compared with other fuels, hydrogen combustion is the cleanest. Except for the generation of water and a small amount of ammonia gas, it does not generate environmentally harmful pollutants such as carbon monoxide, carbon dioxide, hydrocarbons, lead compounds, and dust particles. If a small amount of ammonia gas is properly treated, it will not pollute the environment. Replacing fossil fuels with hydrogen can weaken the greenhouse effect to the greatest extent. 8. Diverse utilization forms: It can not only generate thermal energy by combustion and generate mechanical work in a heat engine, but also be used as an energy material in a fuel cell or be converted into solid hydrogen and used as a structural material. 9. Multiple forms: It appears in gaseous, liquid, or solid metal hydride forms and can adapt to the different requirements of storage, transportation, and various application environments. 10. Low consumption: It can cancel long-distance high-voltage power transmission, transport hydrogen through short- and long-distance pipelines, relatively improve safety, and reduce energy loss. 11. High utilization rate: Hydrogen eliminates the risk of noise sources and energy pollution in internal combustion engines and has a high utilization rate.12. Easy to transport: Hydrogen can reduce the weight of the fuel, increase the payload of the carrier, and thus reduce the transportation cost. Considering the overall profit of the whole process, the total social benefit is superior to other energies.

[0004] Currently, in terms of household use, hydrogen energy mainly focuses on hydrogen gas boilers. Hydrogen gas boilers often burn hydrogen gas instead of natural gas (or methane) in the air. However, it is not much different from the combustion method of natural gas boilers. Hydrogen gas boilers utilize oxygen gas and hydrogen gas radicals in the air for combustion, and obtain hot water through the heat exchange of the boiler. Since the combustion exhaust gas contains carbon dioxide, carbon monoxide, VOCs, and water vapor, it is discharged outdoors together with the exhaust gas, taking away some heat at the same time. At the same time, because the combustion temperature of hydrogen gas is too high, when high-concentration hydrogen gas (5 vol%) burns in air, NOx is generated, causing huge pollution to the environment and triggering the greenhouse effect. All current combustion heating methods adopt electronic ignition, and it is necessary to operate with natural gas or hydrogen gas and natural gas mixtures above the explosion concentration limit, which is carried out by radical combustion and has a high risk factor.

Summary of the Invention

Problems to be Solved by the Invention

[0005] In order to overcome the deficiencies of the prior art, one of the objectives of the present invention is to provide a zero-carbon emission device that generates hot air or high-temperature steam, or produces pure water, which can increase the contact area between the catalyst in the reaction chamber and hydrogen gas and oxygen gas, and the wet hot air generated by the reaction of hydrogen gas and oxygen gas can be introduced into the room through a heating and guiding device for heating, purifying, and humidifying the air. The second objective of the present invention is to provide a zero-carbon emission process that generates hot air or high-temperature steam, or produces pure water, passing hydrogen gas and oxygen gas or air through a catalyst bed layer, allowing the hydrogen gas to fully react with the oxygen gas in the air, and simultaneously catalytically oxidizing some of the VOCs such as formaldehyde and carbon monoxide present in the air into water and carbon dioxide, thereby obtaining water and wet hot air. The wet hot air may be directly and directionally guided to a space that requires heating, or may be heated using the heat of the wet hot air, or the water vapor in the wet hot air may be condensed to produce ultrapure water.

Means for Solving the Problems

[0006] One of the objectives of the present invention is achieved by the following technical solutions. A zero-carbon emission device that generates hot air or high-temperature steam or produces pure water, comprising a gas storage unit, a gas guiding device, a reaction chamber, and a heating guiding device. The gas storage unit is used to store hydrogen gas and oxygen gas or air respectively. The gas storage unit is connected to the reaction chamber via the gas guiding device. The gas guiding device is used to transport the oxygen gas or air and hydrogen gas of the gas storage unit into the reaction chamber. The reaction chamber is further provided with a purified wet hot air outlet connected to the heating guiding device. The reaction chamber has a plurality of layers of sequentially connected pipes. The reaction chamber is used for generating hydrogen gas, and the temperature can be controlled by controlling the flow rate of hydrogen gas and the ratio of hydrogen gas to oxygen gas. There is no reaction to generate water and heat. The pipes are filled or coated with a catalyst to form a catalyst bed layer. Here, the catalyst includes a carrier and an active component supported on the surface of the carrier. The active component contains one or more metal elements of transition metals in Groups 7, 8, 9, 10, or 11.

[0007] Specifically, the device of the present invention can be used for indoor heating. Its principle is similar to that of an electric heater in the room. Since pure hydrogen is adopted, no carbon-containing oxides are generated and exhaust is not required. All the hot air accumulates in the room, and the indoor air also circulates into the device and enters the reaction chamber through the catalyst bed layer. A mixture of hydrogen gas and air below the explosion limit passes through the catalyst bed layer to carry out a hydrogen-oxygen gas reaction to generate water vapor. Since the hydrogen-oxygen gas reaction is an exothermic reaction, the temperature of the catalyst bed layer can be increased and can reach above 100°C. The high temperature can exert a sterilization and disinfection effect on the air in the reaction chamber, generate heat, and heat the air. Therefore, the device can purify the pollutants in the air, thereby forming completely clean and warm air in the room and achieving the purpose of indoor heating. At the same time, when the wet hot air generated by the hydrogen-oxygen gas catalytic reaction is discharged from the device and exchanges heat with the cooling air in the room, the water vapor in the wet hot air plays a role of moistening the indoor air in the room.

[0008] Furthermore, the device further includes a water tank connected to the heating guide device, which can contain a large amount of water vapor in the wet and hot air, condense to form pure water, and be collected in the water tank. Or use the heat in the wet and hot air to heat the water in the water tank.

[0009] Furthermore, the device includes a heating device connected to the reaction chamber, and the heating device is used to improve the reaction temperature of the reaction chamber.

[0010] Furthermore, the device further includes a renewable energy power generation device and a water electrolysis cell. The renewable energy power generation device is electrically connected to the water electrolysis cell, and the water electrolysis cell is connected to the gas storage unit. Here, the renewable energy power generation device is used to supply energy to the water electrolysis cell, the water electrolysis cell is used to generate hydrogen gas and oxygen gas, and the renewable energy power generation device is a solar power generation device or a wind power generation device.

[0011] Furthermore, the active ingredient contains one or more elements among Fe, Co, Ni, Cu, Tc, Ru, Rh, Pd, Ag, Re, Os, Ir, Pt, and Au. More preferably, the metal is selected from Groups 8, 9, 10, and / or 11 of the periodic table. Suitable Group 8, 9, 10, or 11 metals include Ni, Ir, Pd, Ru, Rh, and Pt. Most preferably, the metal is platinum or palladium. Two or more metals may be present in the catalyst in combination. Here, the content of the active ingredient in the catalyst may be 0.001 wt% to 100 (wt)%, preferably the content of the active metal does not exceed 20 wt%, and it is more desirable that the metal content does not exceed 5 wt%.

[0012] The carrier contains one or a combination of two or more of alumina, modified alumina, spinel oxide, perovskite, silica, modified silica, magnesium oxide, titanium oxide, zirconium oxide, zeolite, aluminate, and manganese oxide. Considering its stability, spinel oxides such as alumina, silica-aluminum molecular sieve, and calcium hexaaluminate are preferred. These porous materials may be used alone or in combination. Depending on the desired final product, molecular sieves such as zeolite can also be selected. The carrier is preferably porous. Its particle size is preferably 0.01 mm to 10 mm, more preferably 0.02 mm to 4 mm. The surface area of the carrier material is desirably more than 1.0 m2 / g, preferably more than 5 m2 / g, and a single carrier or a mixture of at least two carriers can be used.

[0013] Specifically, the method for manufacturing the catalyst includes the following steps: The method for manufacturing the catalyst includes an impregnation method or a coprecipitation method. Here, the impregnation method is as follows: Step 1) of dissolving the active ingredient containing a metal salt and / or a metal oxide in water, adjusting the pH to 4 to 14 to adjust the isoelectric point on the surface of the carrier, and preparing a solution; Step 2) of immersing the carrier in the solution and further drying and calcining the immersed carrier; Step 3) of further activating the calcined carrier by passing hydrogen gas through it to obtain an eggshell-type catalyst. The active ingredient of the eggshell-type catalyst is distributed on the outer surface of the carrier, which is advantageous for the catalytic reaction. The method for manufacturing the coprecipitate is as follows: Step 1) of preparing a metal solution A containing the active ingredient and a solution B containing the carrier component; Step 2) of mixing solution A and solution B, uniformly stirring and mixing them, adjusting the pH to 3 to 10 to precipitate the metal of the active ingredient and the carrier component, and allowing it to stand to form layers; Step 4) of taking out the precipitate in the lower layer, washing it, and then drying it; Step 4) of baking the dried precipitate and then forming it, and then reducing it by passing hydrogen gas to obtain the catalyst.

[0014] Furthermore, a temperature sensor and a gas flow meter are provided in the reaction chamber, the heating and guiding device is a directional injection pipe, and the purified hot air containing water vapor can be transported to objects such as a crowd of people or a living room that require heating through the hot air injection pipe at the end, with a more focused target.

[0015] The second object of the present invention is achieved by the following technical solutions. A zero-carbon emission process for generating hot air, or high-temperature steam, or producing pure water, based on the zero-carbon emission device for generating hot air, or high-temperature steam, or producing pure water described above. Step 1) of introducing hydrogen gas and air from the gas storage unit into the reaction chamber, bringing them into contact with the catalyst bed layer of the pipe, initiating the reaction between hydrogen gas and oxygen gas to generate water vapor and obtain wet hot air. Including step 2) of discharging the wet hot air from the wet hot air outlet to the heating and guiding device for heating, purifying, and humidifying the air.

[0016] Furthermore, it further includes step 3) of transporting the wet hot air to a normal temperature water tank through the heating and guiding device to condense the water vapor in the wet hot air, obtain pure water, and collect it.

[0017] Even further, when the device is used for the production of pure water, it further includes step 4) of immersing the device in seawater, reacting the hydrogen gas flow and the air flow or oxygen gas flow through the catalyst bed layer to generate heat inside and evaporate the seawater.

[0018] Furthermore, in step 1), when the temperature of the reaction chamber is less than 10°C, the reaction chamber is heated, the heating temperature is 50 - 95°C, and the addition amount of hydrogen gas is 0.1 - 8% of the air flow rate in the pipe.

Advantages of the Invention

[0019] Compared with the prior art, the beneficial effects of the present invention are as follows. (1) A zero-carbon emission device that generates hot air or high-temperature steam or produces pure water, including a gas storage unit, a gas guiding device, a reaction chamber, and a heating guiding device. The gas storage unit is used to store hydrogen gas and oxygen gas or air respectively. The gas storage unit is connected to the reaction chamber through the gas guiding device. The gas guiding device is used to transport the oxygen gas or air and hydrogen gas of the gas storage unit into the reaction chamber. The reaction chamber is further provided with a wet hot air outlet connected to the heating guiding device. The reaction chamber has a plurality of layers of sequentially connected pipes. The reaction chamber is used to generate a reaction that generates hydrogen gas and oxygen gas to produce water and heat. The pipes are filled or coated with a catalyst to form a catalyst bed layer. Oxygen gas or air and hydrogen gas enter the reaction chamber from the oxygen gas inlet and the hydrogen gas inlet respectively, are sufficiently mixed in the reaction chamber, contact and react with the catalyst, and the formed wet hot air is directionally guided to a space in need of heating through the heating guiding device or used for heating a medium. Since the high temperature of the wet hot air can play a role in sterilization and disinfection, the device of the present invention can not only be used to heat the indoor space and humidify the air, but also play a role in purifying the air. (2) The device of the present invention can further include a water tank. The heating guiding device is connected to the water tank, passes the wet hot air directly through the water tank, and after washing the cold water in the water tank, takes away the heat of the wet hot air and condenses the moisture in the wet hot air into the water tank, and can be used to produce ultrapure water. (3) The device of the present invention can further include a renewable energy power generation device and a water electrolysis cell. The renewable energy power generation device supplies energy to the water electrolysis cell. The water electrolysis cell converts surplus unstable light energy, wind energy or valley electricity into oxygen gas and hydrogen gas, and transmits and stores them to the gas storage unit, and can send them to the reaction chamber for reaction when needed, achieving the effects of energy conservation, environmental friendliness and reduction of energy loss. (4) In the device of the present invention, the hydrogen gas inlet and the air inlet of the reaction chamber should be at least two, and hydrogen gas can be added step by step during the reaction. The added amount of hydrogen gas in each stage should not exceed 8% (volume ratio) of the air flow rate in the pipeline. The minimum amount can be as low as 0.1% (vol). Specifically, the added amount of hydrogen gas is adjusted according to the addition rate in the chamber. It is desirable that the hydrogen gas is green hydrogen without other heteroatom gases. According to experiments, after the completion of the hydrogen gas reaction in the first stage, the subsequent temperature shows that after adding hydrogen gas with a volume concentration of 1%, the temperature in the pipeline of the reaction chamber increases by 50 - 70 °C. Furthermore, according to the need for heating in the chamber, it is necessary to replenish hydrogen gas in a timely manner in the second stage to continue the reaction. Similarly, after consuming 1 (vol)% of hydrogen gas, the temperature in the pipeline should be 50 - 70 °C. The oxygen concentration in the air in the reaction tube decreases according to the amount of hydrogen gas added, and hot water vapor is generated in the air. More importantly, through the catalyst, the incoming hydrogen gas completely reacts with oxygen gas, and the hydrogen gas at the outlet is less than 10 ppm. Even when 0.4 (vol)% of H2 passes through the catalyst bed layer in the air, the temperature of the catalyst bed layer can be increased by 8 - 20 °C, which is related to the gas flow rate. (5) The process of the present invention includes: Step 1) introducing hydrogen gas and air from a gas storage unit into a reaction chamber, bringing them into contact with a catalyst bed layer in a pipe, initiating a reaction between the hydrogen gas and oxygen gas to generate water vapor and obtain humid hot air; and Step 2) discharging the humid hot air from a humid hot air outlet to a heating and guiding device in order to heat the interior, purify and humidify the air. In the reaction between hydrogen gas and oxygen gas, if the reaction temperature is higher than 10°C, the reaction proceeds smoothly. If the room temperature catalyst bed layer is less than 10°C, depending on the properties of the catalyst, it may be necessary to supply a small amount of heat to initiate the reaction. After the reaction is initiated, since the reaction is exothermic, even without heating, as long as the catalyst exists, the hydrogen gas and oxygen gas in the reaction chamber can continue to react completely to generate water vapor. Since the reaction chamber is provided with a multi-stage pipe, after passing through one or more stages of reaction, the residual amount of oxygen (hydrogen gas is the main gas flow) or hydrogen gas (oxygen gas or air is the main gas flow) in the hot air stream usually does not exceed 50 ppm, and even can be as low as 1 ppm. When the reaction is initiated, it is a hydrogen-oxygen gas reaction. However, this device can ensure that the volume concentration of oxygen gas in hydrogen gas or air is lower than the explosion limit from the beginning according to the gas flow rate of the gas storage unit. Also, since a catalyst is used to catalyze the reaction between hydrogen gas and oxygen gas, it is not necessary to increase the amount of hydrogen gas above the explosion limit to initiate the reaction. The device and process based on the present invention can guarantee the safety and reliability of the reaction. (6) When used for pure water generation, the device of the present invention can be immersed in a seawater container or a cold water container. A gas stream containing oxygen gas or pure oxygen gas and hydrogen gas passes through the catalyst bed layer, generates heat from the inside, and evaporates the seawater. At the same time, the water generated by the hydrogen-oxygen gas reaction passing through the catalyst bed layer is directly collected by cooling.

Brief Description of the Drawings

[0020]

Figure 1

Figure 2

Figure 3

Figure 4

Figure 5

Figure 6

Modes for Carrying Out the Invention

[0021] Hereinafter, the present invention will be further described based on the accompanying drawings and specific embodiments. It should be noted that new embodiments can be arbitrarily combined on the premise that there is no conflict between the following described embodiments or between the technical features.

[0022] When heating or producing ultrapure water (e.g., in water-scarce regions) using the device of the present invention, the flow of hydrogen gas and oxygen gas or air generally has a pure hydrogen gas flow passing through the main pipe 41, with the main pipe 41 filled with a catalyst or the catalyst coated on the pipe wall. Oxygen gas (air) is added into the pipe 41 from the dividing part. The reaction chamber 4 of the present invention can be spiral, in series tubular form, or a discharge pipe. The inner surface of the pipe 41 is loaded or coated with a catalyst to form a catalyst bed layer 42. Hydrogen gas flows through the catalyst bed layer 42, and oxygen gas not exceeding 5% of the hydrogen gas flow rate in the main pipe 41, preferably 4% or less, is introduced from the side pipe. After gas mixing, it passes through the catalyst bed layer 42, where hydrogen gas and oxygen gas react to generate hot steam and a hot gas stream. When it is necessary to further heat or produce more water, oxygen gas (volume ratio) not exceeding 5% of the residual hydrogen gas flow rate in the main pipe 41 can be introduced again at the next stage, and in this way, more heat and steam can be generated. Each time oxygen gas accounting for 1% of the hydrogen gas flow rate in the main pipe 41 is added to the main pipe 41, after passing through the catalyst bed layer 42, the oxygen gas can basically undergo a catalytic reaction and be completely converted into water. Here, the residual amount of oxygen gas does not exceed 100 ppm. When oxygen gas is added to the hydrogen gas bed layer and passes through the catalyst bed layer 42, the temperature can be raised by 100 - 140 °C for every 1% of the consumed oxygen. The obtained steam and the gas stream rich in hot hydrogen gas pass directly through water from the other end of the main reaction pipe through the heating guide device 5 for heat exchange with water. Their hot steam remains in the water phase, and the hydrogen gas can carry away the trace amount of oxygen gas originally dissolved in the water, playing the role of oxygen gas removal and preventing corrosion of the equipment. The unreacted hydrogen gas concentrated in the water tank 6 is further compressed from the upper end of the sealed water tank 6 and returns to the hydrogen gas tank 1 of the gas storage unit or enters the main reaction pipe 41.

[0023] Specifically, hydrogen gas and oxygen gas pass through the catalyst bed layer 42 in the pipe 41 and react. The generated water and excess hydrogen gas flow out from the spiral pipe. The water accumulates in the sealed water tank 6 filled with cold water, and the excess hydrogen gas returns to the hydrogen gas tank 1 at the tip of the water tank.

[0024] Of course, in the catalytic reaction for producing ultrapure water, oxygen gas may be passed through the main pipe 41 filled with or coated with a catalyst, and hydrogen gas accounting for 4% (volume ratio) of the oxygen gas flow rate in the main pipe 41 may be introduced into the side pipe 41 for reaction. However, in this process, after the outflow of hydrogen gas from the main pipe 41, excessive oxygen gas may increase the dissolved oxygen concentration in water, which may be disadvantageous to the corrosion prevention system of the water tank 6 and the pipe 41.

[0025] The chemical reaction of the present invention can be expressed as follows. 2H2 + O2 → 2H2O + heat, When used for indoor heating, the catalyst bed layer also has a purification effect on indoor pollutants, and there is a possibility that reactions such as the oxidation of VOCs such as formaldehyde into water and carbon dioxide may occur. Such reactions may include other reactions, for example, CH2O + 1 / 2O2 → CO2 + H2O, CO + 1 / 2O2 → CO2.

[0026] When used for indoor heating, the volume ratio of hydrogen gas to oxygen gas in the air is preferably 1:5 to 200, and preferably 1:(5 to 20). In the case of indoor heating, even if a large excess of oxygen gas is used, the mixture in the reaction chamber 4 can be ensured within the safe range of the explosion limit. Also, even if hydrogen gas is consumed to generate heat and hot air, the oxygen gas content in the hot air does not decrease significantly, so it can all be circulated indoors, and efficient heating of the room can be ensured without being affected by the concentration of oxygen gas.

[0027] Here, as shown in FIG. 2, FIG. 2 is a laboratory apparatus for evaluating the catalyst used in the present invention. Its operating principle is that both air and hydrogen gas can adjust their flow rates. Four hydrogen gas inlets are provided in the catalyst bed layer, and there is one air inlet. The air flows along the catalyst bed layer, adding hydrogen gas step by step to ensure that the introduced amount of hydrogen gas at each step does not exceed the explosion limit of the mixed gas. On the catalyst, air and hydrogen gas react in the catalyst bed layer to generate water. Here, four thermocouples are provided in the catalyst bed layer to monitor the temperature of the catalyst bed layer during the reaction. As can be seen from the above apparatus, when hydrogen gas and oxygen gas react to generate water, the temperature rises, thereby heating the air passing through the catalyst bed layer to form hot air.

[0028] As shown in FIG. 3, in FIG. 3, hydrogen gas and air are contained in a mixed gas container, and the volume concentration of hydrogen gas is limited to be <8%. Then the mixed gas enters the catalyst bed layer through a flow rate adjusting valve, and the mixed gas is reacted by the action of the catalyst to generate water. Similarly, since this reaction is an exothermic reaction, the mixed gas in the catalyst bed layer is heated to form a hot air flow.

[0029] From the above, it can be proved that both of the above two apparatuses can demonstrate that the catalyst of the present invention can play a role in catalyzing the hydrogen-oxygen gas reaction. When hydrogen gas and air (oxygen gas) are mixed, a good catalytic effect can be obtained in either case when they enter the catalyst bed layer respectively. Since this reaction is an exothermic reaction, the air flow passing through the catalyst bed layer is heated, thus obtaining a hot air flow.

[0030] Example 1 As shown in Fig. 4, the apparatus of this embodiment is an indoor chemical zero-carbon heating system, which includes a hydrogen gas tank 1, an oxygen gas tank 2, a gas guiding device 3, a reaction chamber 4, and a heating guiding device 5. A plurality of layers of pipes 41 are sequentially connected to the reaction chamber 4. One oxygen gas intake port 43 is provided on the side line of each layer of the pipe 41. At least one hydrogen gas intake port 44 is further provided in the reaction chamber 4. The pipe 41 is filled with a catalyst to form a catalyst bed layer 42. The hydrogen gas tank 1 and the oxygen gas tank 2 are respectively connected to the oxygen gas intake port 43 and the hydrogen gas intake port 44 of the reaction chamber 4 through the gas guiding device 3. The reaction chamber 4 is further provided with a wet and hot air outlet 45 connected to the heating guiding device 5.

[0031] A zero-carbon emission process that generates hot air, or high-temperature steam, or produces pure water, Step 1): Introduce the hydrogen gas and air from the gas storage unit into the reaction chamber 4, bring them into contact with the catalyst bed layer 42 of the pipe 41, initiate the reaction between the hydrogen gas and the oxygen gas, generate water vapor, and obtain wet and hot air; Step 2): Collect from the wet and hot air outlet 45 that can be used for indoor heating, air purification, and humidification to the heating guiding device 5.

[0032] Here, the catalyst of Example 1 is manufactured using the metal salt impregnation wet method and includes the following steps: 1) Obtained by manufacturing an H2PtCl4 solution with a Pt metal content of 0.2 wt% and an H2PdCl4 solution with a Pd content of 0.6 wt%; 2) First, drop ammonia water into 2.5 ml of the H2PtCl4 solution to adjust the pH value to 9. After mixing the solution, immerse it in a gamma γ-Al2O3 carrier dried at 120 °C. Use the immersed carrier to dry it in an oven at 100 °C overnight. Then, wash the catalyst with water until no chlorine ions are detected, and further dry it. Then, put the dried sample into a muffle furnace and calcine it in air at a heating rate of 5 °C / min to 500 °C for 2 h. 3) Take 3 ml of 0.6% H2PdCl4 solution, adjust the pH to 9 with aqueous ammonia, immerse the above-mentioned calcined Pt / Al2O3 sample, let it stand for 24 hours, dry it overnight at 100 °C in an oven, wash it with distilled water until no chloride ions are detected, and then put the dried sample into a muffle furnace. Bake it at 500 °C for 2 h in air at a heating rate of 5 °C / min. 4) The finally calcined support is activated under H2 at 500 °C with a heating rate of 2 °C / min for 2 hours, which is an intermediate drying step of drying at 150 °C for 1 hour in the downstream of the tubular furnace. The flow rate is 2 L / h / g of hydrogen. At the end of the reduction, the residual hydrogen gas in the pipeline is blown away with N2 to avoid explosion. 5) Screen the catalyst to an appropriate particle size, preferably 200 - 355 μm, to obtain an eggshell-type catalyst as shown in Figure 1. Generally, the active component of the eggshell-type catalyst is distributed on the outer surface of the support, avoiding the hysteresis reaction of hydrogen and oxygen gas molecules caused by the wide contact surface with hydrogen and oxygen gas reactants and the large difference in diffusion coefficients.

[0033] Here, the pipe 41 is a spiral pipe. The pipe 41 has a length of 1.5 m and an inner diameter of 5 mm. The thickness of the catalyst bed layer 42 is 20 mm. The oxygen gas tank 2 stores air, and 50 L / min of air is introduced into the oxygen gas intake port 43 of the copper pipe. Two hydrogen gas intake ports 44 are provided on the side line of the copper pipe. The hydrogen gas flow rate in the first path is 1.8 L / min. After introducing the hydrogen gas in the first path, at 20 cm from the hydrogen gas inlet of the first path, it is measured that the gas temperature in the pipeline is 180 °C. After introducing the hydrogen gas in the second stage into the reaction chamber 4, at a location 20 cm after the hydrogen gas in the second stage, the measured airflow temperature is 260 °C. Finally, the wet and hot air is cut off from the wet and hot air outlet 45, and hydrogen gas sensor and mass analysis are performed. It is found that the hydrogen gas content in the wet and hot air is 10 ppm or less. The wet and hot air is transmitted from the wet and hot air outlet 45 through the heating and guiding device 5 (directional injection pipe) to a 6 m3 room. It is measured that the temperature of this room rises from 12 °C to 20 °C within 15 minutes, and at the same time, the humidity of the room also increases to 86%.

[0034] Example 2 Catalyst production 100 g of α-Al2O3 balls (specific surface area: 4.9 m2 / g, manufactured by Boyinghe Chemical Industry Co., Ltd.) dried at 120 °C for 4 hours were immersed in a 30 ml aqueous solution of Pt(NH3)4(NO3)2 and Fe(NO3)2 containing 2.0 g of Fe and 0.1 g of Pt, allowed to stand at room temperature for 2 hours, dried in an oven at 80 °C for 4 hours, and then calcined in a muffle furnace at 500 °C for 4 hours to obtain an alumina-supported catalyst precursor containing platinum oxide and iron oxide. This catalyst was further heated to 600 °C at a rate of 2 °C / min in a mixed gas stream of 1H2 / 3Ar at 100 ml / min and held for 4 hours to obtain a workable catalyst. When this catalyst is used for in-tube coating, it is necessary to grind the catalyst to less than 120 mesh, mix it with a small amount of water to form a fluid gel, and apply it by air pressure.

[0035] As shown in FIG. 5, the apparatus of this example is a chemical pure water production and seawater heating system, which includes a hydrogen gas tank 1, an oxygen gas or air tank 2, a gas guiding device 3, a reaction chamber 4, a heating guiding device 5, and a water tank 6. A plurality of layers of pipes 41 are sequentially connected to the reaction chamber 4, and one air or oxygen gas intake port 43 is provided on the side line of each layer of pipes 41. At least one hydrogen gas intake port 44 is further provided in the reaction chamber 4. A catalyst is coated in the pipes 41, and catalyst particles of 100 - 1000 um may be randomly dispersed in the pipes 41 to form a catalyst bed layer 42. The hydrogen gas tank 1, the oxygen gas or air tank 2 are respectively connected to the air or oxygen gas intake port 43 and the hydrogen gas intake port 44 of the reaction chamber 4 through the gas guiding device 3. The reaction chamber 4 is further provided with a wet and hot air outlet 45 connected to the heating guiding device 5. The water tank 6 is connected to the heating guiding device 5 and is used to store seawater and collect pure water.

[0036] Here, the pipe 41 is a spiral copper pipe. The pipe 41 has a length of 5 m and an inner diameter of 6 mm, and the thickness of the catalyst bed layer 42 is 2 mm. First, the heating guide device 5 is extended into the water tank 6 filled with 2 L of water. Seawater is put into the water tank 6, air is stored in the oxygen gas tank 2, 50 L / min of air is introduced from the oxygen gas intake port 43 of the copper pipe, and hydrogen gas is introduced from the hydrogen gas intake port 44 of the copper pipe, with a flow rate of 30 L / min. First, oxygen gas is introduced into the oxygen gas intake port 43 of the first-layer pipe 41, with the amount of oxygen gas being 1 lL / min. At a point 30 cm after the contact point of the amount of oxygen gas, it was measured that the temperature of the air flow was 320°C. Then, (0.8 - 1) L O2 / min was introduced into the oxygen gas intake port 43 of the pipes 41 from the second to the fifth layers respectively. After three-stage oxygen gas addition, it was measured that the temperature of the hydrogen gas flowing out from the wet and hot air outlet 45 in the pipe 41 reached 600°C. After passing the wet and hot air through the water tank 6 via the heating guide device 5, the temperature of 258°C was measured in the water tank 6. Also, water and oxygen gas are contained in the wet and hot air, which has a high temperature and is directly passed into the water tank 6. The seawater in the water tank 6 evaporates. After standing, the temperature of the water tank 6 decreases, the water in the wet and hot air condenses into water, and hydrogen gas enters the tip of the water tank 6. After 10 minutes, the temperature of the water in the water tank 6 becomes 89°C, and the amount of water also increases from 2 liters to 2.08 liters. It can be seen from this process that first, seawater is evaporated to obtain distilled water, and the air flow containing hot steam is cooled by seawater. Here, the hot steam is condensed into clean liquid water, which is easy to collect.

[0037] Example 3 As shown in FIG. 6, the device of Example 3 adds a water electrolysis cell 7 based on Example 2. The water electrolysis cell 7 can electrolyze water into hydrogen gas and oxygen gas using surplus solar energy, wind energy, or off-peak electricity as energy, serving as the hydrogen and oxygen gas source in this example.

[0038] The above embodiments are merely preferred embodiments of the present invention and do not limit the technical scope of the present invention thereby. Any non-substantial modifications and substitutions made by those skilled in the art based on the present invention all fall within the scope of the claims of the present invention.

Description of Reference Numerals

[0039] 1 Hydrogen gas tank, 2 Oxygen gas tank, 3 Gas guiding device, 4 Reaction chamber, 41 Pipe, 42 Catalyst bed layer, 43 Oxygen gas intake port, 44 Hydrogen gas intake port, 45 Humid and hot air outlet, 5 Heating and guiding device, 6 Water tank, 7 Water electrolyzer.

Claims

1. A zero-carbon emission device for generating hot air, or high-temperature steam, or producing pure water, comprising a gas storage unit, a gas guiding device, a reaction chamber, a heating guiding device and a water tank. The gas storage unit is used to store hydrogen gas and oxygen gas or air respectively. The gas storage unit is respectively connected to the reaction chamber via the gas guiding device. The gas guiding device is used to transport the oxygen gas or air and hydrogen gas of the gas storage unit into the reaction chamber. The reaction chamber is further provided with a humid hot air outlet connected to the heating guiding device. The water tank is connected to the heating guiding device. The reaction chamber is provided with a plurality of layers of sequentially connected pipes, and a catalyst is filled or coated in the pipes to form a catalyst bed layer. The catalyst bed layer is used to promote the reaction of hydrogen gas and oxygen gas to generate water and heat. Here, the catalyst includes a carrier and an active component supported on the surface of the carrier, and the active component contains one or more metal elements of transition metals of Group 7, 8, 9, 10 or 11. A zero-carbon emission device for generating hot air, or high-temperature steam, or producing pure water, characterized in that.

2. The device includes a heating device connected to the reaction chamber, and the heating device is used to improve the reaction temperature of the reaction chamber. A zero-carbon emission device for generating hot air, or high-temperature steam, or producing pure water according to Claim 1, characterized in that.

3. The device further includes a renewable energy power generation device and a water electrolysis cell. The renewable energy power generation device is electrically connected to the water electrolysis cell, and the water electrolysis cell is connected to the gas storage unit. Here, the renewable energy power generation device is used to supply energy to the water electrolysis cell, and the water electrolysis cell is used to generate hydrogen gas and oxygen gas. The renewable energy power generation device is a solar power generation device or a wind power generation device. A zero-carbon emission device for generating hot air, or high-temperature steam, or producing pure water according to Claim 1, characterized in that.

4. The active ingredient contains one or more elements among Fe, Co, Ni, Cu, Tc, Ru, Rh, Pd, Ag, Re, Os, Ir, Pt, and Au, and the carrier contains one or a combination of two or more among alumina, modified alumina, spinel oxide, perovskite, silica, modified silica, magnesium oxide, titanium oxide, zirconium oxide, zeolite, aluminate, and manganese oxide. The zero-carbon emission device according to claim 1, which generates hot air or high-temperature steam, or produces pure water.

5. The method for manufacturing the catalyst includes an impregnation method or a coprecipitation method. Here, the impregnation method is as follows: Step 1) of dissolving an active ingredient containing a metal salt and / or a metal oxide in water, adjusting the pH to 4 to 14 to adjust the isoelectric point on the surface of the carrier, and preparing a solution; Step 2) of immersing the carrier in the solution and further drying and calcining the immersed carrier; Step 3) of further activating the calcined carrier by passing hydrogen gas through it to obtain an eggshell-type catalyst. The method for manufacturing the coprecipitate is as follows: Step 1) of preparing a metal solution A containing an active ingredient and a solution B containing a carrier component; Step 2) of mixing solution A and solution B, uniformly stirring and mixing them, adjusting the pH to 3 to 10, causing the metal of the active ingredient and the carrier component to precipitate, and allowing it to stand in layers; Step 3) of taking out the precipitate in the lower layer, washing it, and then drying it; Step 4) of roasting the dried precipitate, then forming it, and then reducing it by passing hydrogen gas through it to obtain the catalyst. The zero-carbon emission device according to claim 1 or 4, which generates hot air or high-temperature steam, or produces pure water.

6. A temperature sensor and a gas flow meter are provided in the reaction chamber, and the heating and guiding device is a directional injection pipe. The zero-carbon emission device according to claim 1, which generates hot air or high-temperature steam, or produces pure water.

7. A zero-carbon emission process for generating hot air or high-temperature steam, or producing pure water, based on the zero-carbon emission device according to any one of claims 1 to 6. Step 1) of introducing hydrogen gas and air from the gas storage unit into the reaction chamber, bringing them into contact with the catalyst bed layer of the pipeline, starting the reaction between hydrogen gas and oxygen gas to generate water vapor, and obtaining wet hot air. Step 2) of discharging from the humid hot air outlet to the heating guide device for heating the room, purifying the air, and humidifying it, included in a zero-carbon emission process for generating hot air or high-temperature steam or producing pure water, characterized in that.

8. The zero-carbon emission process for generating hot air or high-temperature steam or producing pure water according to claim 7, further comprising step 3) of transporting the humid hot air to a normal-temperature water tank via a heating guide device in order to condense the water vapor in the humid hot air, obtain pure water, and collect it, characterized in that.

9. When the device is used for the production of pure water, the zero-carbon emission process for generating hot air or high-temperature steam or producing pure water according to claim 8, further comprising step 4) of immersing the device in seawater, reacting a hydrogen gas stream with an air stream or an oxygen gas stream through a catalyst bed layer to generate heat inside and evaporate the seawater, characterized in that.

10. In step 1), when the temperature of the reaction chamber is less than 10°C, heating the reaction chamber, the heating temperature being 50 to 95°C, and the addition amount of hydrogen gas being 0.1 to 8% of the air flow rate in the pipe, the zero-carbon emission device for generating hot air or high-temperature steam or producing pure water according to claim 1, characterized in that.

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