An electrolyzed water device and a biomass solar combined supply system using the same

Abstract

An electrolyzed water device and a biomass solar combined supply system using the same, comprising: a solar concentrating photovoltaic-thermal system, a solar photovoltaic system, an electrolyzed water device, a biomass gasification system, a methanation reactor, an internal combustion engine, a heat pump, a bromine machine, a water removal device, a heat storage device, and a water storage tank. The present invention proposes a concept of a renewable energy "zero-carbon" synthetic natural gas system based on solar energy and biomass energy. In this application, the H2 and O2 generated by photovoltaic electrolysis of water are introduced into the process of biological oxygen-enriched directional gasification and methanation to empower biomass and synthesize natural gas; this application neither requires an air separation device in conventional biomass oxygen-enriched gasification nor requires purification of the biomass gasification syngas, improving the economic efficiency of energy utilization.

Description

Technical Field

[0001] The present application relates to an electrolytic water device and a biomass solar combined supply system using the device. Background Art

[0002] With the increasing awareness of the environmental impact and limited resources of fossil fuels, in order to obtain high-quality gaseous energy, people have begun to study natural gas preparation processes. As a renewable energy source that can achieve zero-carbon utilization, biomass energy can undergo pyrolysis, oxidation, and reduction reactions through biomass gasification technology to be converted into combustible gases such as carbon monoxide and hydrogen, and then further convert the carbon source into high-calorie methane through methanation technology to obtain high-quality gaseous energy.

[0003] At the same time, due to the characteristics of solar energy such as volatility, unpredictability, and seasonality, its accommodation problem is prominent. The use of biomass can alleviate the uncertainty of solar energy. That is, through the power-to-gas technology, the surplus electric energy of solar energy utilization technology can be converted into hydrogen, and then converted into methane gas through gasification and methanation technologies. The proton exchange membrane electrolytic water technology in the power-to-gas technology avoids the disadvantages of using strong alkaline liquid electrolytes in alkaline electrolytic cells, and has the advantages of high efficiency, high gas purity, and stability, and can provide pure oxygen and hydrogen for gasification and methanation technologies. The concentrating photovoltaic-thermal technology combines concentrating technology with photovoltaic-thermal and photovoltaic technologies to efficiently utilize solar energy, generating electricity and hot water simultaneously, and can be used in conjunction with the proton exchange membrane electrolytic water technology. The combination of these technologies can achieve the rational utilization of renewable energy. In the process of coupling biomass and solar energy, in addition to the overall series design, the most important thing is how to use the proton exchange membrane to obtain oxygen more efficiently, and the existing electrolysis system is slightly insufficient. Summary of the Invention

[0004] To solve the above problems, on the one hand, the present application discloses an electrolytic water device, including:

[0005] A power source for providing direct current;

[0006] An electrolytic cell with an electrolyte provided therein;

[0007] A water electrolysis membrane is further provided in the electrolytic cell, and an anode and a cathode connected to the power source are respectively provided on both sides of the water electrolysis membrane;

[0008] A gas collection part for collecting oxygen from the anode on the electrolytic cell and hydrogen from the cathode;

[0009] The water electrolysis membrane includes a proton exchange membrane, with a cathode catalyst layer and an anode catalyst layer respectively disposed on both sides of the proton exchange membrane. A cathode porous transport layer is disposed outside the cathode catalyst layer, and an anode porous transport layer is disposed outside the anode catalyst layer. A transition oxidation reaction layer is disposed between the proton exchange membrane and the anode catalyst layer and between the proton exchange membrane and the cathode catalyst layer. The transition oxidation reaction layer provided in this application is essentially a semi-membrane structure. Its essential function is first to avoid the mixing of oxygen and hydrogen discharged from the system. Even if mixing occurs, it can catalytically oxidize the two at the primary stage to avoid safety impacts.

[0010] Preferably, the water electrolysis membrane is obtained in the following manner:

[0011] The proton exchange membrane is a Nafion 117 membrane;

[0012] The transition oxidation reaction layer is obtained in the following manner:

[0013] Pd / C is ultrasonically dispersed in an acetone solution, and then sprayed onto the proton exchange membrane at a spraying amount of 0.2 mg / cm 2 , and then dried at room temperature;

[0014] The anode catalyst layer is prepared in the following manner:

[0015] Ir, Nafion solution, polyacrylic acid, and graphene oxide are mixed and then disposed on a polytetrafluoroethylene template, and then transferred onto the transition oxidation reaction layer;

[0016] The cathode catalyst layer is prepared in the following manner:

[0017] Pt and Nafion solution are mixed and then disposed on a polytetrafluoroethylene template, and then transferred onto the other side of the proton exchange membrane relative to the anode catalyst layer;

[0018] The transfer is carried out in the following manner: The polytetrafluoroethylene template containing the anode catalyst layer or the cathode catalyst layer is attached to the proton exchange membrane, and the attachment transfer treatment is carried out at 120 - 130 °C and 3 - 4 MPa. The electrolytic water device of this application uses a novel water electrolysis membrane. First, it can reduce the oxygen content in hydrogen, thus ensuring safety; second, it can improve the service stability of the water electrolysis membrane itself, and it also has a relatively long available time under high efficiency.

[0019] Preferably, the anode porous transport layer is a porous titanium metal plate; the cathode porous transport layer is a porous carbon paper.

[0020] On the other hand, a biomass solar combined heat and power supply system is also disclosed, which includes: a solar concentrating photovoltaic and thermal system (CPV / T), a solar photovoltaic system (PV), an electrolytic water device, a biomass gasification system, a methanation reactor, an internal combustion engine, a heat pump, a bromine machine, a water removal device, a heat storage device, and a water storage tank. The present invention proposes a concept of a renewable energy "zero-carbon" synthetic natural gas system based on solar energy and biomass energy. In this application, the H2 and O2 generated by photovoltaic electrolysis of water are introduced into the process of bio-oxygen-enriched directional gasification and methanation to empower biomass and synthesize green natural gas; this application neither requires an air separation device in conventional biomass oxygen-enriched gasification nor requires purification of the biomass gasification syngas, improving the economy; based on the principle of cascade utilization of energy, this application integrates CPV / T, electrolysis-gasification-methanation technology, the thermoelectric conversion of an internal combustion engine, a heat pump, and heat storage into an efficient and controllable combined cooling, heating, power, and gas supply system, thus having integrated innovation. This application also utilizes the flexibility of the internal combustion engine to make up for the instability of CPV / T to obtain a stable and controllable output, breaking through the bottleneck problems faced in the cogeneration system, and forming an independent technology for zero-carbon regional combined heat and power supply with complementary biomass and solar energy.

[0021] Preferably, the electric energy generated by the solar concentrating photovoltaic and thermal system and the solar photovoltaic system absorbing solar energy respectively enters the electrolytic water device as a power source and is supplied to the heat pump and users; the solar concentrating photovoltaic and thermal system absorbs solar energy to heat external water, and the heated warm water enters the heat pump.

[0022] The heat pump receives the electric energy of the solar concentrating photovoltaic and thermal system and the solar photovoltaic system, heats the warm water of the solar concentrating photovoltaic and thermal system into hot water to supply the electrolytic water device, and the rest is stored in the water storage tank to meet the domestic hot water demand of users.

[0023] Preferably, the electrolytic water device receives the electric energy of the solar concentrating photovoltaic and thermal system and the solar photovoltaic system, and electrolyzes the hot water of the heat pump to generate oxygen and hydrogen, which are used to supply the biomass gasification system and the methanation reactor respectively, and the excess oxygen is stored or sold.

[0024] Preferably, the water removal device includes a water removal device 1 and a water removal device 2; the biomass gasification system receives biomass raw materials and oxygen generated by the electrolytic water device, reacts to generate gasified gas, and the gasified gas enters the water removal device 1 for cooling and water removal. After water removal, the gasified gas enters the methanation reactor, and the heat released by the water removal device 1 enters the converging pipeline through circulating hot water; the methanation reactor receives the gasified gas from the biomass gasification system and hydrogen generated by the electrolytic water device, undergoes a methanation reaction to generate methane gas and releases heat, and the gas enters the water removal device 2 for cooling and water removal. After water removal, the gas enters the internal combustion engine. If there is surplus gas, it is introduced into the gas network; if the gas is insufficient, it is introduced from the gas network; the heat released by the methanation reaction and the heat released by the cooling of the gas by the water removal device 2 enter the converging pipeline through circulating hot water.

[0025] Preferably, the internal combustion engine receives the fuel gas from the methanation reactor or the gas network to generate electric energy and heat energy. The electric energy is supplied to users, and if there is any surplus, it is sent to the power grid. The heat of the cylinder jacket water of the internal combustion engine enters the converging pipeline. In the refrigeration season, the flue gas of the internal combustion engine enters the bromine machine for refrigeration, and the remaining flue gas is discharged. In the non-refrigeration season, the flue gas of the internal combustion engine directly enters the heat exchanger for cooling, and the released heat enters the converging pipeline through the circulating hot water, and the remaining flue gas after heat exchange is discharged.

[0026] Preferably, the hot water pipeline combines the water removal device 1, the methanation reactor, the water removal device 2, the cylinder jacket water of the internal combustion engine and the heat of the heat exchanger to meet the heat demand of users in the non-refrigeration season. In the refrigeration season, the hot water in the hot water pipeline and the flue gas of the internal combustion engine are sent to the bromine machine for refrigeration to meet the cold demand of users.

[0027] The heat storage device is connected to the hot water pipeline. When the heat supply is greater than the heat demand of users or the bromine machine, the excess heat is stored in the heat storage device. When the heat supply is less than the heat demand, the heat is extracted from the heat storage device for supplementation.

[0028] Preferably, if the electric energy generated by the solar concentrating photovoltaic-thermal system, the solar photovoltaic system and the internal combustion engine is insufficient, power is taken from the power grid to meet the electric demand of users.

[0029] The present application can bring the following beneficial effects:

[0030] 1. The present application provides a transition oxidation reaction layer which is essentially a semi-membrane structure. Its essential function is first to prevent the mixing of oxygen and hydrogen in the exhaust system. Even if mixing occurs, it can catalytically oxidize both of them at the primary stage to avoid safety hazards.

[0031] 2. The electrolyzer of the present application uses a new type of water electrolysis membrane. First, it can reduce the oxygen content in hydrogen to ensure safety. Second, it can improve the use stability of the water electrolysis membrane itself, and it can have a relatively long available time even under high efficiency.

[0032] 3. The present invention proposes a concept of a renewable energy "zero-carbon" synthetic natural gas system based on solar energy and biomass energy. The present application introduces the H2 and O2 generated by photovoltaic electrolysis of water into the process of biological oxygen-enriched directional gasification and methanation, endows biomass, and synthesizes green natural gas. The present application neither requires an air separation device in conventional biomass oxygen-enriched gasification nor requires purification of biomass gasification syngas, improving the economic efficiency of energy utilization. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] The drawings described herein are used to provide a further understanding of the present application and form a part of the present application. The schematic embodiments and descriptions thereof of the present application are used to explain the present application and do not constitute an improper limitation to the present application. In the drawings:

[0034] Figure 1 It is a schematic diagram of a biomass solar combined supply system. Specific embodiments

[0035] To clearly illustrate the technical features of this solution, the present application will be elaborated in detail through specific embodiments below.

[0036] For the water electrolysis device, it includes: a power source for providing direct current; an electrolytic cell with an electrolyte arranged inside; a water electrolysis membrane is also arranged inside the electrolytic cell, and an anode and a cathode connected to the power source are respectively arranged on both sides of the water electrolysis membrane; a gas collection part for collecting oxygen from the anode on the electrolytic cell and hydrogen from the cathode; the water electrolysis membrane includes a proton exchange membrane, a cathode catalytic layer and an anode catalytic layer are respectively arranged on both sides of the proton exchange membrane, a cathode porous transport layer is arranged outside the cathode catalytic layer, an anode porous transport layer is arranged outside the anode catalytic layer, and a transition oxidation reaction layer is arranged between the proton exchange membrane and the anode catalytic layer and between the proton exchange membrane and the cathode catalytic layer.

[0037] Example 1:

[0038] The water electrolysis membrane is obtained in the following way:

[0039] The proton exchange membrane is a Nafion 117 membrane;

[0040] The transition oxidation reaction layer is obtained in the following way:

[0041] The transition oxidation reaction layer is spray-coated on both the front and back sides of the Nafion 117 membrane, specifically including:

[0042] Pd / C is ultrasonically dispersed in an acetone solution, and then Pd is spray-coated onto the proton exchange membrane at a spray coating amount of 0.2 mg / cm 2 , and then dried at room temperature to complete the modification of the Nafion117 membrane;

[0043] The anode catalytic layer is prepared in the following way:

[0044] Yttrium oxide, Nafion solution (5wt%), polyacrylic acid, and graphene oxide are mixed in a mass ratio of yttrium oxide: Nafion solution (5wt%): polyacrylic acid: graphene oxide = 0.1∶10∶0.2∶0.05, then set on a polytetrafluoroethylene template, and then transferred onto the transition oxidation reaction layer, where the yttrium loading is 2 mg / cm 2 ;

[0045] The cathode catalytic layer is prepared in the following way:

[0046] Pt / C and Nafion solution (5 wt%) were mixed and placed on a polytetrafluoroethylene template, and then transferred to the other side of the proton exchange membrane relative to the anode catalyst layer; the mass ratio of each substance, Pt / C: Nafion solution (5 wt%) = 0.1:10, and the loading amount of Pt after loading was 0.5 mg / cm 2 .

[0047] The transfer was performed as follows: a polytetrafluoroethylene template including an anode catalyst layer or a cathode catalyst layer was laminated to a proton exchange membrane, and a lamination transfer treatment was performed at 130° C. and 3 MPa.

[0048] The anode porous transport layer is a porous titanium metal plate; the cathode porous transport layer is a porous carbon paper.

[0049] Electrode plates are arranged on both sides of the water electrolysis membrane to form a positive electrode and a negative electrode, and are placed in the same water electrolysis device to measure their performance.

[0050] It was measured that after 5 minutes of hydrolysis reaction, the oxygen content in the hydrogen was 13 ppm.

[0051] After 100 h of use, the electrolysis voltage increased by 15.2%.

[0052] Embodiment 2:

[0053] The water electrolysis membrane is obtained as follows:

[0054] The proton exchange membrane is Nafion 117 membrane;

[0055] The transition oxidation reaction layer is obtained as follows:

[0056] The transition oxidation reaction layer is sprayed on both sides of the Nafion 117 membrane, including:

[0057] Pd / C was ultrasonically dispersed into acetone solution, and then Pd was concentrated to 0.2 mg / cm 2 After spraying onto the proton exchange membrane, the membrane was dried at room temperature, thereby completing the modification of the Nafion 117 membrane.

[0058] The anode catalyst layer was prepared as follows:

[0059] Yttrium oxide, Nafion solution (5 wt%), polyacrylic acid, and graphene oxide were mixed in a mass ratio of yttrium oxide: Nafion solution (5 wt%): polyacrylic acid: graphene oxide = 0.1:10:0.2:0.05 and set on a polytetrafluoroethylene template, and then transferred to the transition oxidation reaction layer, wherein the yttrium loading is 2 mg / cm 2 ;

[0060] The cathode catalyst layer was prepared as follows:

[0061] Pt / C and Nafion solution (5 wt%) were mixed and placed on a polytetrafluoroethylene template, and then transferred to the other side of the proton exchange membrane relative to the anode catalyst layer; the mass ratio of each substance, Pt / C: Nafion solution (5 wt%) = 0.1:10, and the loading amount of Pt after loading was 0.5 mg / cm 2 .

[0062] The transfer is performed as follows: a polytetrafluoroethylene template containing an anode catalyst layer or a cathode catalyst layer is laminated to a proton exchange membrane, and a lamination transfer treatment is performed at 120° C. and 4 MPa.

[0063] The anode porous transport layer is a porous titanium metal plate; the cathode porous transport layer is a porous carbon paper.

[0064] Electrode plates are arranged on both sides of the water electrolysis membrane to form a positive electrode and a negative electrode, and are placed in the same water electrolysis device to measure their performance.

[0065] It was measured that after 5 minutes of hydrolysis reaction, the oxygen content in the hydrogen was 17 ppm.

[0066] After 100 h of use, the electrolysis voltage increased by 11.8%.

[0067] In order to characterize the possible effects of each substance, the following comparative examples were made:

[0068] Comparative Example 1:

[0069] No transition oxidation reaction layer was set on both sides of the Nafion 117 membrane. Other preparation and operation methods were the same as those in Example 2. It was measured that after 5 minutes of hydrolysis reaction, the oxygen content in the hydrogen was 97 ppm.

[0070] After 100 h of use, the electrolysis voltage increased by 28.8%.

[0071] Comparative Example 2:

[0072] Polyacrylic acid and graphene oxide were not placed in the cathode catalyst layer. Other preparation and operation methods were the same as those in Example 2. It was measured that after 5 minutes of hydrolysis reaction, the oxygen content in the hydrogen was 25 ppm.

[0073] After 100 h of use, the electrolysis voltage increased by 49.1%.

[0074] For the application of the electrolytic cell, this application also provides an application scenario, such as Figure 1As shown in the figure, a biomass solar combined supply system includes: a solar concentrating photovoltaic-thermal system (CPV / T), a solar photovoltaic system (PV), an electrolyzer, a biomass gasification system, a methanation reactor, an internal combustion engine, a heat pump, a bromine machine, a water removal device, a heat storage device, and a water storage tank. The electric energy generated by the solar concentrating photovoltaic-thermal system and the solar photovoltaic system absorbing solar energy respectively enters the electrolyzer as a power source and is supplied to the heat pump and users; the solar concentrating photovoltaic-thermal system absorbs solar energy to heat external water, and the heated warm water enters the heat pump; the heat pump receives the electric energy of the solar concentrating photovoltaic-thermal system and the solar photovoltaic system, heats the warm water of the solar concentrating photovoltaic-thermal system into hot water for supplying the electrolyzer, and the rest is stored in the water storage tank to meet the domestic hot water demand of users. The water removal device includes a water removal device 1 and a water removal device 2. The electrolyzer receives the electric energy of the solar concentrating photovoltaic-thermal system and the solar photovoltaic system, and electrolyzes the hot water of the heat pump to produce oxygen and hydrogen, which are used to supply the biomass gasification system and the methanation reactor respectively, and the excess oxygen is stored or sold. The biomass gasification system receives the biomass raw material and the oxygen generated by the electrolyzer, reacts to produce gasified gas, the gasified gas enters the water removal device 1 for cooling and water removal, the gasified gas after water removal enters the methanation reactor, and the heat released by the water removal device 1 enters the converging pipeline through the circulating hot water; the methanation reactor receives the gasified gas from the biomass gasification system and the hydrogen generated by the electrolyzer, undergoes a methanation reaction to generate methane gas and releases heat, the gas enters the water removal device 2 for cooling and water removal, and the gas after water removal enters the internal combustion engine. If there is surplus gas, it is introduced into the gas network; if the gas is insufficient, it is introduced from the gas network; the heat released by the methanation reaction and the heat released by the gas cooled by the water removal device 2 enter the converging pipeline through the circulating hot water. The internal combustion engine receives the gas from the methanation reactor or the gas network and burns to generate electric energy and heat energy, the electric energy is supplied to users, and if there is surplus, it is sent to the power grid; the heat of the jacket water of the internal combustion engine enters the converging pipeline, and the flue gas of the internal combustion engine enters the bromine machine for refrigeration in the refrigeration season, and the remaining flue gas is discharged; the flue gas of the internal combustion engine directly enters the heat exchanger for cooling in the non-refrigeration season, the heat released enters the converging pipeline through the circulating hot water, and the remaining flue gas after heat exchange is discharged. The hot water pipeline combines the heat of the water removal device 1, the methanation reactor, the water removal device 2, the jacket water of the internal combustion engine and the heat exchanger, and meets the heat demand of users in the non-refrigeration season; in the refrigeration season, the hot water in the hot water pipeline and the flue gas of the internal combustion engine are sent to the bromine machine for refrigeration to meet the cold demand of users; the heat storage device is connected to the hot water pipeline. When the heat supply is greater than the heat demand of users or the bromine machine, the excess heat is stored in the heat storage device; when the heat supply is less than the heat demand, heat is extracted from the heat storage device for supplementation. If the electric energy generated by the solar concentrating photovoltaic-thermal system, the solar photovoltaic system and the internal combustion engine is insufficient, power is taken from the power grid to meet the electric demand of users.

[0075] This system can provide electricity, gas, heat, cold and domestic hot water for the outside world.

[0076] CPV / T and PV absorb solar energy for power generation. Part of the generated electricity meets the power demand of the electrolyzer, part is supplied to the heat pump, and part is supplied to users. The warm water generated by the CPV / T system absorbing solar energy is heated into hot water by the heat pump. Part of the hot water meets the water consumption of the electrolyzer, and the other part enters the water storage tank for storage for domestic hot water.

[0077] The electrolyzer uses the electricity generated by the CPV / T and PV systems to electrolyze the hot water from the heat pump to produce hydrogen and oxygen. Among them, oxygen is supplied to the gasification system, and the excess oxygen is stored or sold; all the hydrogen is supplied to the methanation reactor.

[0078] The biomass raw material and oxygen react in the gasification system to produce syngas. The syngas enters the water removal device 1 for cooling and water removal and then is introduced into the methanation reactor. The gasification system is a self-heating system, and the heat released by the syngas cooled and dewatered by the water removal device 1 is recorded as the heat release amount 1.

[0079] The syngas generated by the gasification system and the hydrogen generated by the electrolyzer react in the methanation reactor. This reaction is an exothermic reaction, recorded as the heat release amount 2; the reaction produces methane gas, and the gas is cooled and dewatered by the water removal device 2. At this time, the heat release is recorded as the heat release amount 3; part of the dewatered gas is introduced into the internal combustion engine, and the excess gas is sent to the gas network.

[0080] Due to the periodic change of the external energy demand, starting from the actual demand, this application divides the external demand into a heating season, a cooling season, and a transition season.

[0081] (1) Heating season:

[0082] The methane gas is introduced into the gas internal combustion engine for combustion to generate electric energy and heat energy. The generated electricity is supplied to users; the heat energy is in the high-temperature flue gas and the jacket water. The heat of the jacket water is recorded as the heat release amount 4; the high-temperature flue gas recovers heat through the heat exchanger, and the recovered heat is recorded as the heat release amount 5, and the remaining flue gas after heat exchange is discharged.

[0083] The user's electricity load is met by the electricity generated by the CPV / T and PV systems and the electricity generated by the internal combustion engine. If the power supply is insufficient and the internal combustion engine has not reached the rated power, gas is purchased from the gas network. If the power supply is still insufficient under the rated working condition of the internal combustion engine, electricity is taken from the power grid to meet the user's electricity demand.

[0084] The user's heating load is jointly met by the heat release amount 1 of the combined syngas cooling, the heat release amount 2 of the methanation reaction, the heat release amount 3 of the gas cooling, the heat release amount 4 of the jacket water, and the heat release amount 5 of the high-temperature flue gas. If the heat supply is greater than the heating load, the excess heat is stored in the heat storage device; if the heat supply is insufficient, it is extracted from the heat storage device for supplementation.

[0085] The user's domestic hot water is provided by the CPV / T linked heat pump.

[0086] (2) Cooling season:

[0087] The power supply mode and domestic hot water supply mode of the user are the same as those in the heating season.

[0088] Methane gas is introduced into a gas internal combustion engine for combustion, generating electric energy and heat energy. The generated electricity is supplied to the user; its heat energy is in the high-temperature flue gas and the jacket water. The heat of the jacket water is recorded as the heat release 4, and the heat of the high-temperature flue gas sent to the bromine machine is recorded as the heat 6.

[0089] The cooling load of the user is borne by the refrigeration of the bromine machine. The heat sources of the bromine machine include the heat 6 of the high-temperature flue gas of the internal combustion engine, and the heat release 1 of the combined gasification gas cooling heat release, the heat release 2 of the methanation reaction, the heat release 3 of the gas cooling, and the heat release 4 of the jacket water. If each heat release is greater than the heat demand of the bromine machine, the excess heat is stored in the heat storage device; if the refrigeration capacity of the bromine machine is less than the cooling load, heat is extracted from the heat storage device to supplement the bromine machine.

[0090] (3) Transition season:

[0091] In the transition season, since there is no heating or cooling load, only electric load and domestic hot water load exist. At this time, the internal combustion engine, heat pump, bromine machine, and smoke-water heat exchanger do not work.

[0092] The power supply mode and domestic hot water supply mode of the user are the same as those in the heating season and the refrigeration season.

[0093] During the transition season, the methane gas generated by the methanation reactor is directly sent into the gas network, and the heat release 1 of the gasification gas cooling heat release, the heat release 2 of the methanation reaction, and the heat release 3 of the gas cooling are directly stored in the heat storage device.

[0094] The above are only the embodiments of the present application and are not used to limit the present application. For those skilled in the art, various changes and modifications can be made to the present application. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application shall be included within the scope of the claims of the present application.

Claims

1. An electrolyzed water device, characterized in that: include: A power supply for providing direct current; Electrolytic cell, a cell containing electrolyte; A water electrolysis membrane is also arranged in the electrolytic cell, and an anode and a cathode connected to a power source are arranged on both sides of the water electrolysis membrane respectively; A gas collection unit, used to collect oxygen from the anode and hydrogen from the cathode of the electrolytic cell; The water electrolysis membrane comprises a proton exchange membrane, a cathode catalyst layer and an anode catalyst layer are respectively arranged on both sides of the proton exchange membrane, a cathode porous transport layer is arranged on the outer side of the cathode catalyst layer, an anode porous transport layer is arranged on the outer side of the anode catalyst layer, and a transition oxidation reaction layer is arranged between the proton exchange membrane and the anode catalyst layer, and between the proton exchange membrane and the cathode catalyst layer; The water electrolysis membrane is obtained as follows: The proton exchange membrane is a Nafion 117 membrane; The transition oxidation reaction layer is obtained as follows: Disperse Pd / C ultrasonically into an acetone solution, and then spray it onto the proton exchange membrane at a spraying rate of 0.2 mg / cm 2 , and then dry it at room temperature; The anode catalyst layer is prepared as follows: Ir, Nafion solution, polyacrylic acid, and graphene oxide are mixed and set on a polytetrafluoroethylene template, and then transferred to the transition oxidation reaction layer; The cathode catalyst layer is prepared as follows: The Pt and Nafion solutions are mixed and set on a polytetrafluoroethylene template, and then transferred to the other side of the proton exchange membrane relative to the anode catalyst layer; The transfer is performed as follows: a polytetrafluoroethylene template containing an anode catalyst layer or a cathode catalyst layer is laminated to a proton exchange membrane, and a lamination transfer treatment is performed at 120-130° C. and 3-4 MPa.

2. An electrolytic water device according to claim 1, characterized in that: The anode porous transport layer is a porous titanium metal plate; the cathode porous transport layer is a porous carbon paper.

3. A biomass solar combined supply system using the electrolytic water device described in claim 1 or 2, characterized in that, include: Solar concentrating photovoltaic and thermal systems, solar photovoltaic systems, water electrolysis devices, biomass gasification systems, methanation reactors, internal combustion engines, heat pumps, bromine machines, water removal devices, heat storage devices, and water storage tanks.

4. The biomass solar combined supply system according to claim 3, wherein: The solar concentrating photovoltaic system and the solar photovoltaic system absorb the electricity generated by the solar energy and enter the water electrolysis device as a power source and provide it to the heat pump and users respectively; the solar concentrating photovoltaic system absorbs the solar energy to heat the external water, and the heated warm water enters the heat pump; The heat pump receives electricity from the solar concentrating photovoltaic thermal system and the solar photovoltaic system, heats the warm water from the solar concentrating photovoltaic thermal system into hot water to supply the electrolytic water device, and stores the rest in the water storage tank to meet the user's domestic hot water needs.

5. The biomass solar combined supply system according to claim 4, wherein: The water electrolysis device receives electricity from the solar concentrating photovoltaic thermal system and the solar photovoltaic system, and electrolyzes the hot water of the heat pump to produce oxygen and hydrogen, which are used to supply the biomass gasification system and the methanation reactor respectively. The excess oxygen is stored or sold.

6. The biomass solar combined supply system according to claim 5, wherein: The dehydration device comprises a first dehydration device and a second dehydration device; the biomass gasification system receives the biomass raw material and oxygen generated by the water electrolysis device, reacts to generate gasified gas, the gasified gas enters the first dehydration device for cooling and dehydration, the gasified gas after dehydration enters the methanation reactor, and the heat released by the first dehydration device enters the convergence pipeline through circulating hot water; The methanation reactor receives the gasified gas from the biomass gasification system and the hydrogen generated by the electrolytic water device, undergoes a methanation reaction to generate methane gas and release heat. The gas enters the second water removal device for cooling and water removal. After water removal, the gas enters the internal combustion engine. If there is surplus gas, it is fed into the gas network; if the gas is insufficient, it is introduced from the gas network. The heat released by the methanation reaction and the heat released by the cooling of the gas through the second water removal device enter the converging pipeline through the circulating hot water.

7. The biomass solar combined supply system according to claim 6, characterized in that: The internal combustion engine receives the gas from the methanation reactor or the gas network, burns to generate electric energy and heat energy. The electric energy is supplied to users, and if there is surplus, it is sent to the power grid. The heat of the cylinder jacket water of the internal combustion engine enters the converging pipeline. The flue gas of the internal combustion engine enters the bromine chiller for refrigeration in the cooling season, and the remaining flue gas is discharged. The flue gas of the internal combustion engine directly enters the heat exchanger for cooling in the non-cooling season, and the released heat enters the converging pipeline through the circulating hot water, and the remaining flue gas after heat exchange is discharged.

8. The biomass solar combined heat and power supply system according to claim 7, wherein: The hot water pipeline combines the heat of the first water removal device, the methanation reactor, the second water removal device, the cylinder jacket water of the internal combustion engine and the heat exchanger to meet the heat demand of users in the non-cooling season; in the cooling season, the hot water in the hot water pipeline and the flue gas of the internal combustion engine are sent to the bromine chiller together to meet the cooling demand of users. The heat storage device is connected to the hot water pipeline. When the heat supply is greater than the heat demand of users or the bromine chiller, the excess heat is stored in the heat storage device. When the heat supply is less than the heat demand, heat is extracted from the heat storage device for supplementation.

9. The biomass solar combined supply system according to claim 8, wherein: If the electric energy generated by the solar concentrating photovoltaic-thermal system, the solar photovoltaic system and the internal combustion engine is insufficient, power is taken from the power grid to meet the electric demand of users.

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