Solar radiation energy grading and residual light energy thermal complementary coupling electro / thermochemical gradient hydrogen production system and method

Abstract

The invention provides an electro / thermochemical gradient hydrogen production system and method for solar radiation energy grading and residual light energy thermal complementary coupling. The system comprises a light condensation assembly; the frequency division assembly is used for grading solar spectrum radiation; a photovoltaic cell power generation device; the methane oxygen-enriched combustion high-temperature photovoltaic power generation device is used for realizing oxygen-enriched combustion of natural gas by utilizing residual heat heat energy and generating power by utilizing radiation energy generated by high-temperature flue gas generated after combustion; the solid oxide electrolytic tank device is used for pushing solid oxide to electrolyze water to produce hydrogen by utilizing heat energy and electric energy contained in the high-temperature flue gas step by step; and the thermal chemical reaction device is used for promoting each step of thermal chemical reaction by utilizing heat energy and electric energy contained in the high-temperature flue gas step by step. The energy source of the system is solar radiation and natural gas, hydrogen and electricity are produced, the system utilizes different energy conversion modes to achieve temperature gradient ordered conversion and utilization of residual light energy after solar frequency division, and complementary coupling of different qualities is achieved on the basis of energy gradient conversion.

Description

Technical Field

[0001] The present invention belongs to the technical field of new energy preparation, and particularly relates to an electro / thermal chemical cascade hydrogen production system and method for solar radiation energy grading and waste light energy heat complementary coupling. Background Art

[0002] Due to the advantages of solar energy such as being clean, sustainable, and having huge energy, it is regarded as an important direction for future energy development. However, due to its objective discontinuity, there is a large-scale problem of abandoned light, and the medium and low-grade solar energy cannot be effectively utilized, resulting in difficulties in improving the utilization and conversion efficiency of solar energy. Hydrogen energy is a secondary energy source with high calorific value and no pollution. Converting solar energy into hydrogen energy through water decomposition for storage and utilization is a very promising energy utilization method, and using solar energy to produce hydrogen energy is also considered one of the most ideal hydrogen production routes in the future. Photovoltaic power generation is an efficient photoelectric conversion method, but photovoltaic cells can only convert high-grade solar energy within a specific wavelength range into electrical energy, and a large amount of solar energy is wasted. The spectral splitting technology can decompose solar radiation energy into different bands, enabling each band to be effectively utilized. The high-grade solar radiation energy is directly converted into electrical energy through photovoltaic power generation; while the low-grade remaining band energy can be complemented with fossil fuels to achieve a large increase in energy grade. However, there is still a lack of a single way to fully and efficiently utilize high-grade thermal energy at present. Therefore, cascaded conversion and utilization of energy is a scientific and effective way.

[0003] In terms of hydrogen production technology, both solid oxide electrolytic cell water decomposition for hydrogen production and copper-chlorine cycle hydrogen production are clean and efficient hydrogen production methods. There are no greenhouse gas emissions during the hydrogen production process, and both require input of electrical energy and thermal energy of different grades. The difference is that the solid oxide electrolytic cell for water decomposition to produce hydrogen needs to maintain a high-temperature environment of 700 - 800 °C, while the highest temperature required in the copper-chlorine cycle is only 530 °C. The energy required by both can match the solar radiation energy grading and waste light energy heat complementary cascaded conversion utilization method (power generation and heat supply), realizing the coupling of different quality energies, and providing an efficient solar hydrogen production route. Summary of the Invention

[0004] Aiming at the above technical status quo, the present invention aims to provide an electro / thermal chemical cascade hydrogen production system and method for solar radiation energy grading and waste light energy heat complementary coupling, which frequency-divides natural sunlight for utilization. The high-grade sunlight is directly used for photovoltaic power generation, the low-grade solar waste light is complemented with natural gas to improve the energy grade, and different energy conversion methods are used to orderly convert and utilize the waste light in a temperature cascade manner and match and couple with solid oxide fuel cells and copper-chlorine cycles to efficiently output hydrogen energy, greatly improving the energy utilization efficiency.

[0005] On the one hand, the present application proposes an electro / thermochemical cascaded hydrogen production system with hierarchical solar radiation energy and complementary thermal energy of residual light, including a concentrating component, a frequency-dividing component, a photovoltaic power generation device, a high-temperature photovoltaic power generation device for methane oxy-fuel combustion, a solid oxide electrolyzer device, and a thermochemical reaction device;

[0006] The concentrating component concentrates sunlight, and the frequency-dividing component divides the concentrated light beam. Among them, the frequency band suitable for photovoltaic power generation is reflected to the photovoltaic power generation device for photovoltaic power generation, and the remaining frequency bands are secondarily concentrated by the concentrating component to the high-temperature photovoltaic power generation device for methane oxy-fuel combustion;

[0007] The high-temperature photovoltaic power generation device for methane oxy-fuel combustion uses a tubular receiver to convert the secondarily concentrated sunlight into heat energy to preheat the oxygen-rich air. The preheated oxygen-rich air and natural gas are input into the combustion chamber for oxy-fuel combustion to generate the first-stage high-temperature flue gas. The high-temperature photovoltaic power generation device for methane oxy-fuel combustion uses the radiant energy of the first-stage high-temperature flue gas for photovoltaic power generation, and the second-stage high-temperature flue gas is discharged from the combustion chamber to the solid oxide electrolyzer device;

[0008] The solid oxide electrolyzer device uses a three-stage heat exchanger and a solid oxide electrolyzer to gradually utilize the heat of the high-temperature flue gas. Among them, the solid oxide electrolyzer uses the electric energy generated by the system and the heat contained in the high-temperature flue gas for high-temperature electrolytic hydrogen production, and discharges the fourth-stage high-temperature flue gas to supply the thermochemical cycle device;

[0009] The pyrolysis reaction chamber, hydrolysis reaction chamber, and drying reaction chamber of the thermochemical cycle device gradually utilize the heat energy contained in the high-temperature flue gas to drive the reaction. The entire thermochemical cycle device uses the heat energy contained in the high-temperature flue gas and the electric energy generated by the system to achieve a copper-chlorine cycle and produce hydrogen.

[0010] In particular, by regulating the ratio of air to oxygen entering the tubular receiver, that is, regulating the oxygen content in the oxygen-rich air, the instability of solar energy can be balanced to ensure the self-sustaining operation of the system day and night.

[0011] On the other hand, the present application also proposes a method for electro / thermochemical cascaded hydrogen production with hierarchical solar radiation energy and complementary thermal energy of residual light, which specifically includes the following steps: natural sunlight is first concentrated and then reaches the frequency-dividing component, the beam whose reflected energy can be efficiently utilized by the photovoltaic power generation device is reflected, and the remaining solar residual light in other bands is transmitted. The residual light is secondarily concentrated and then reaches the tubular receiver;

[0012] The oxygen-rich air is preheated by the concentrated solar afterglow in the tubular receiver and then fed into the combustion chamber together with natural gas for combustion, generating the first-stage high-temperature flue gas with a temperature of 2000 - 2500 °C; the methane oxy-fuel combustion high-temperature photovoltaic power generation device utilizes the radiant energy contained in the first-stage high-temperature flue gas with a temperature of 2000 - 2500 °C for thermophotovoltaic power generation, converting it into the second-stage high-temperature flue gas with a temperature of 850 - 1000 °C and feeding it into the solid oxide electrolysis cell device;

[0013] The solid oxide electrolysis cell device heats the electrolysis reaction raw materials by utilizing the heat energy contained in the second-stage high-temperature flue gas with a temperature of 850 - 1000 °C through the third-stage heat exchanger, converting it into the third-stage high-temperature flue gas with a temperature of 750 - 850 °C and feeding it into the solid oxide electrolysis cell; the solid oxide electrolysis cell utilizes the third-stage high-temperature flue gas with a temperature of 750 - 850 °C and the electric energy generated by the system's photovoltaic power generation to drive the solid oxide electrolysis of water to produce hydrogen, converting the third-stage high-temperature flue gas into the fourth-stage high-temperature flue gas with a temperature of 530 - 680 °C and feeding it into the thermochemical reaction device;

[0014] In the thermochemical reaction device, the pyrolysis reaction chamber utilizes the heat energy contained in the fourth-stage high-temperature flue gas to drive the pyrolysis reaction, converting it into the fifth-stage high-temperature flue gas with a temperature of 400 - 460 °C and feeding it into the hydrolysis reaction chamber; the hydrolysis reaction chamber utilizes the heat energy contained in the fifth-stage high-temperature flue gas to drive the hydrolysis reaction, converting it into the sixth-stage high-temperature flue gas with a temperature of 130 - 200 °C and feeding it into the drying reaction chamber; the drying reaction chamber utilizes the heat energy contained in the sixth-stage high-temperature flue gas to drive the drying reaction, converting it into low-temperature flue gas and discharging it; the electrolysis reaction chamber utilizes the electric energy generated by the system's photovoltaic power generation to carry out the electrolysis reaction to produce hydrogen.

[0015] The system and method proposed in this application have the following advantages or beneficial effects:

[0016] 1. By decoupling photovoltaic conversion and thermophotovoltaic conversion through concentrated frequency division, the hierarchical utilization of solar radiant energy is realized, and the energy utilization efficiency is improved.

[0017] 2. Complement the low-grade solar afterglow with natural gas, and obtain the first-stage high-temperature flue gas with a temperature of 2000 - 2500 °C through oxy-fuel combustion, effectively improving the energy grade.

[0018] 3. Based on the principle of energy quality matching, directly generate electricity by high-grade solar energy through photovoltaic power generation, and carry out high-temperature thermophotovoltaic power generation using the first-stage high-temperature flue gas; supply different-quality electric / thermal energy in stages for the high-temperature electrolysis reaction of solid oxide and the thermochemical cycle to produce hydrogen, realizing the complementary coupling of different qualities on the basis of energy cascade conversion.

[0019] 4. The oxygen generated by the electrolysis of water reaction and the pyrolysis reaction can be used as a raw material for oxy-fuel combustion. By regulating the oxygen content in the oxy-fuel air, the instability of solar energy can be balanced to ensure the stable operation of the system day and night.

[0020] 5. A heat recovery device is added inside the system. Through reasonable design and layout, the heat released in the system is maximally recovered, effectively reducing the energy loss of the system.

[0021] 6. Introducing an appropriate amount of hydrogen into the cathode of the solid oxide electrolyzer can effectively prevent the cathode material from being oxidized under high-temperature and high-humidity conditions. Description of the Drawings

[0022] Figure 1 is a schematic diagram of the structure of an electric / thermal chemical cascaded hydrogen production system with solar radiation energy grading and waste heat energy thermal complementarity coupling according to an embodiment of the present application;

[0023] Among them, 1 - primary concentrator assembly, 2 - frequency division assembly, 3 - secondary concentrator assembly, 4 - first-stage photovoltaic cell, 5 - waste heat utilization device of the first-stage photovoltaic cell, 6 - tubular receiver, 7 - combustion chamber, 8 - emitter, 9 - filter, 10 - second-stage photovoltaic cell, 11 - waste heat utilization device of the second-stage photovoltaic cell, 12 - first-stage heat exchanger, 13 - second-stage heat exchanger, 14 - third-stage heat exchanger, 15 - solid oxide electrolyzer, 16 - pyrolysis reaction chamber, 17 - hydrolysis reaction chamber, 18 - drying reaction chamber, 19 - electrolysis reaction chamber, 20 - hydrogen storage tank, 21 - oxygen storage tank, 22 - hydrogen separator, 23 - storage battery. Detailed Embodiments

[0024] In order to better understand the technical solution of the present application, the embodiments of the present application will be described in detail below with reference to the drawings.

[0025] The technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention and are intended to explain the inventive concept. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present application without creative efforts shall fall within the protection scope of the present invention.

[0026] Unless otherwise clearly specified and limited, the terms "high temperature", "low temperature", etc. used in the description are only used to describe relative characteristics and do not indicate or imply that the technical characteristics referred to must have specific indicators.

[0027] Unless otherwise clearly specified and defined, the terms "primary", "secondary", "first level", "second level", etc. used in the description are for descriptive purposes only, in order to distinguish between similar components or devices with different purposes, and should not be construed as indicating or implying relative importance or implicitly specifying the indicated technical features.

[0028] Unless otherwise clearly specified and defined, the terms "connected" and "coupled" used in the description should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or integrated; it can be a mechanical connection, an electrical connection; it can be directly connected, indirectly connected through an intermediate medium; it can be the internal communication of two components or the interaction relationship between two components. For those of ordinary skill in the art, the specific meanings of the above terms in the embodiments can be understood according to specific circumstances.

[0029] The embodiments of the present application provide an electric / thermal chemical cascaded hydrogen production system for solar radiation energy grading and residual light energy thermal complementary coupling, and a method for cascaded hydrogen production using this system.

[0030] See Figure 1 , in a specific embodiment of the present application, there is provided an electric / thermal chemical cascaded hydrogen production system for solar radiation energy grading and residual light energy thermal complementary coupling, including a concentrating component, a frequency division component 2, a photovoltaic power generation device, a high-temperature photovoltaic power generation device for methane oxy-fuel combustion, a solid oxide electrolyzer device, and a thermochemical reaction device; wherein, the concentrating component concentrates sunlight, the frequency division component 2 frequency-divides the concentrated light beam, and the frequency band suitable for photovoltaic power generation is reflected to the photovoltaic power generation device for photovoltaic power generation, and the remaining frequency bands are secondarily concentrated by the concentrating component to the high-temperature photovoltaic power generation device for methane oxy-fuel combustion;

[0031] The high-temperature photovoltaic power generation device for methane oxy-fuel combustion uses a tubular receiver 6 to convert the secondarily concentrated sunlight into heat energy to preheat the oxygen-rich air, and the preheated oxygen-rich air and natural gas are input into a combustion chamber 7 for oxy-fuel combustion to generate first-stage high-temperature flue gas. The high-temperature photovoltaic power generation device for methane oxy-fuel combustion uses the radiant energy of the first-stage high-temperature flue gas for photovoltaic power generation, and the second-stage high-temperature flue gas is discharged from the combustion chamber 7 to the solid oxide electrolyzer device;

[0032] The solid oxide electrolyzer device uses a three-stage heat exchanger 14 and a solid oxide electrolyzer 15 to gradually utilize the heat of the high-temperature flue gas. Among them, the solid oxide electrolyzer 15 uses the electric energy generated by the system and the heat contained in the high-temperature flue gas for high-temperature electrolysis hydrogen production, and discharges the fourth-stage high-temperature flue gas to supply a thermochemical cycle device;

[0033] The pyrolysis reaction chamber 16, hydrolysis reaction chamber 17, and drying reaction chamber 18 of the thermochemical cycle device successively utilize the thermal energy contained in the high-temperature flue gas to drive reactions. The entire thermochemical cycle device utilizes the thermal energy contained in the high-temperature flue gas and the electric energy generated by the system to achieve a copper-chlorine cycle and produce hydrogen.

[0034] As Figure 1 shown, the system of the present invention has an air / flue gas pipeline for heat transfer. This pipeline is successively connected to a tubular receiver 6, a combustion chamber 7, a heat exchanger 14, a solid oxide electrolyzer 15, a pyrolysis reaction chamber 16, a hydrolysis reaction chamber 17, and a drying reaction chamber 18 to achieve the cascade conversion of the energy of the high-temperature flue gas and the mutual coupling between systems.

[0035] In a specific embodiment of the present invention, the concentrating assembly includes a primary concentrating assembly 1 and a secondary concentrating assembly 3 for enhancing the solar radiation intensity. The primary concentrating assembly 1 concentrates natural sunlight to the frequency division assembly 2. The secondary concentrating assembly 3 concentrates the remaining light after frequency division to the tubular receiver 6. Preferably, the primary concentrating assembly 1 and the secondary concentrating assembly 3 adopt point-focus Fresnel concentrating assemblies, which are mature products and inexpensive.

[0036] The frequency division assembly 2 of the present invention is used to reflect the first light beam that can be efficiently utilized by the photovoltaic cell and transmit the remaining solar light of other bands to the secondary concentrating assembly 3. The solar spectrum is divided into two parts according to photon energy for different energy-efficient conversion paths. Preferably, the material of the frequency division assembly is a nano-film stacked with multi-layer polymer or semiconductor. By adjusting the position of the frequency division assembly, the specific bands of the first light beam and the remaining solar light can be regulated.

[0037] In an embodiment of the present invention, the photovoltaic power generation device includes a first-stage photovoltaic cell 4 and a first-stage photovoltaic cell waste heat utilization device 5. The first-stage photovoltaic cell 4 is used to receive the first light beam for photovoltaic power generation to provide electric energy for subsequent electrolytic hydrogen production. The first-stage photovoltaic cell waste heat utilization device 5 recovers the thermal energy of the first-stage photovoltaic cell 4 to preheat water, and obtains hot water with a temperature of 40-60 °C as the raw material for the pyrolysis reaction in the thermochemical cycle, while avoiding the temperature rise of the photovoltaic cell due to a large amount of radiant energy. Preferably, the first-stage photovoltaic cell waste heat utilization device 5 is provided with an inlet for cold water and an outlet for discharging hot water. Preferably, the first-stage photovoltaic cell 4 adopts a gallium arsenide (GaAs) photovoltaic cell with a cut-off wavelength of 900 nm. This type of photovoltaic cell has a high photoelectric conversion efficiency, can withstand high temperatures and high-concentration ratio light, and better meets the system requirements.

[0038] In one embodiment of the present invention, the high-temperature photovoltaic power generation device for oxy-fuel combustion of methane includes a tubular receiver 6, a combustion chamber 7, a transmitter 8, a filter 9, a secondary photovoltaic cell 10, and a waste heat utilization device 11 for the secondary photovoltaic cell. A photo-thermal absorber is fixed inside the tubular receiver 6 to absorb the sunlight focused by the secondary concentrating assembly 3 and convert it into heat energy to preheat the oxy-fuel air, generating oxy-fuel air at a temperature of 600 - 700 °C. Natural gas and the preheated oxy-fuel air are input into the combustion chamber 7 together for oxy-fuel combustion, generating a first-stage high-temperature flue gas at a temperature of 2000 - 2500 °C. The first-stage high-temperature flue gas generates radiant energy through the transmitter 8, and the radiant energy selectively passes through the filter 9 and is absorbed by the secondary photovoltaic cell 10 to generate electric energy. The radiant energy that does not match the secondary photovoltaic cell returns to the combustion chamber 7. Subsequently, the first-stage high-temperature flue gas is converted into a second-stage high-temperature flue gas at a temperature of 850 - 1000 °C and discharged from the combustion chamber 7 to supply the tertiary heat exchanger 14 of the solid oxide electrolysis cell device; the waste heat utilization device 11 for the secondary photovoltaic cell recovers the heat energy of the secondary photovoltaic cell 10 to preheat water, obtaining hot water at a temperature of 40 - 60 °C as the raw material for the pyrolysis reaction in the thermochemical cycle, improving the energy utilization efficiency and avoiding the temperature rise of the photovoltaic cell due to a large amount of radiant energy. Preferably, the tubular receiver 6 is provided with an inlet for introducing air, an inlet for introducing oxygen, and an outlet for discharging the preheated oxy-fuel air, and the inlet for introducing oxygen is connected to the outlet of the oxygen storage tank 21; the combustion chamber 7 is provided with an inlet for introducing oxy-fuel air and an outlet for discharging the second-stage high-temperature flue gas, and the inlet for introducing oxy-fuel air is connected to the oxy-fuel air outlet of the tubular receiver 6; the waste heat utilization device 11 for the secondary photovoltaic cell is provided with an inlet for introducing cold water and an outlet for discharging hot water. Preferably, the secondary photovoltaic cell 10 uses a gallium antimonide (GaSb) photovoltaic cell with a cut-off wavelength of 1800 nm. This type of photovoltaic cell has a relatively large cut-off wavelength and can withstand a relatively high intensity of thermal radiation, which better meets the system requirements.

[0039] In an embodiment of the present invention, the solid oxide electrolysis cell device includes a primary heat exchanger 12, a secondary heat exchanger 13, a tertiary heat exchanger 14, and a solid oxide electrolysis cell 15. The heat energy and electrical energy contained in the secondary high-temperature flue gas and the tertiary high-temperature flue gas after heat exchange in the tertiary heat exchanger 14 are utilized to achieve high-temperature electrolysis at 700-800 °C. By recovering heat, the temperature of the raw material (water) is gradually increased and the phase state is changed, thereby improving the energy utilization efficiency. The primary heat exchanger 12 is used to recover the heat of the high-temperature hydrogen and water vapor discharged from the cathode of the solid oxide electrolysis cell 15 to further heat the hot water (~60 °C) discharged from the secondary photovoltaic cell waste heat utilization device 11; the secondary heat exchanger 13 is used to recover the heat of the high-temperature oxygen discharged from the anode of the solid oxide electrolysis cell 15 to further heat the hot water vapor discharged from the primary heat exchanger 12; the tertiary heat exchanger 14 is used to utilize the heat contained in the secondary high-temperature flue gas at a temperature of 850-1000 °C to further heat the hot water vapor discharged from the secondary heat exchanger 13. The heated high-temperature water vapor (700-800 °C) is introduced into the cathode of the solid oxide electrolysis cell 15 as the raw material for the electrolysis reaction. The tertiary high-temperature flue gas at a temperature of 750-850 °C after heat exchange in the tertiary heat exchanger 14 is supplied to the solid oxide electrolysis cell 15; the solid oxide electrolysis cell 15 is used to perform high-temperature electrolysis to produce hydrogen by using the electrical energy generated by the photovoltaic cell and the heat contained in the tertiary high-temperature flue gas. The required electrical energy is provided by the storage battery 23. High-temperature hydrogen and un-electrolyzed high-temperature water vapor are produced at the cathode, and high-temperature oxygen is produced at the anode. The fourth-stage high-temperature flue gas at a temperature of 530-680 °C after heat exchange in the solid oxide electrolysis cell 15 is supplied to the thermochemical cycle device.

[0040] Preferably, the hot water / water vapor pipeline is sequentially connected to the primary heat exchanger 12, the secondary heat exchanger 13, the tertiary heat exchanger 14, and the solid oxide electrolysis cell 15; the inlet for introducing the high-temperature hydrogen and water vapor mixture of the primary heat exchanger 12 is connected to the cathode outlet of the solid oxide electrolysis cell 15, and the inlet for introducing hot water is connected to the hot water outlet of the secondary photovoltaic cell waste heat utilization device 11; the inlet for introducing high-temperature oxygen of the secondary heat exchanger 13 is connected to the anode outlet of the solid oxide electrolysis cell 15, and the inlet for introducing hot water vapor is connected to the hot water vapor outlet of the primary heat exchanger 12; the inlet for introducing the secondary high-temperature flue gas of the tertiary heat exchanger 14 is connected to the high-temperature flue gas outlet of the combustion chamber 7, and the inlet for introducing hot water vapor is connected to the hot water vapor outlet of the secondary heat exchanger 13; the solid oxide electrolysis cell 15 is provided with an inlet for introducing the tertiary high-temperature flue gas and an outlet for discharging the fourth-stage high-temperature flue gas. The inlet for introducing the tertiary high-temperature flue gas is connected to the high-temperature flue gas outlet of the tertiary heat exchanger 14. The cathode is provided with an inlet for introducing high-temperature water vapor, an inlet for introducing hydrogen, and an outlet for discharging high-temperature hydrogen and water vapor. The inlet for introducing high-temperature water vapor is connected to the high-temperature water vapor outlet of the tertiary heat exchanger 14. The anode is provided with an outlet for discharging high-temperature oxygen.

[0041] Further preferably, the solid oxide electrolyzer device is further provided with a hydrogen separator 22, which is used to separate hydrogen and water from the mixed gas at the outlet of the first-stage heat exchanger 12. The separated water enters the photovoltaic power generation device for cooling, and a part of the separated hydrogen is supplied to the cathode of the solid oxide electrolyzer 15. Hydrogen effectively prevents the cathode material from being oxidized under high-temperature and high-humidity conditions.

[0042] In an embodiment of the present invention, the thermochemical reaction device includes a pyrolysis reaction chamber 16, a hydrolysis reaction chamber 17, a drying reaction chamber 18, and an electrolysis reaction chamber 19. The pyrolysis reaction chamber 16 utilizes the heat contained in the fourth-stage high-temperature flue gas to promote the pyrolysis reaction, so that the temperature in the pyrolysis reaction chamber 16 is maintained at 500-530°C. After heat exchange, the fourth-stage high-temperature flue gas is converted into the fifth-stage high-temperature flue gas with a temperature of 400-460°C and supplied to the hydrolysis reaction chamber 17; the chemical reaction equation of the pyrolysis reaction is Cu2OCl2(s) → 2CuCl(l) + 0.5O2(g). The hydrolysis reaction chamber 17 utilizes the heat contained in the fifth-stage high-temperature flue gas to promote the hydrolysis reaction, so that the temperature in the hydrolysis reaction chamber is maintained at 370-400°C. After heat exchange, the fifth-stage high-temperature flue gas is converted into the sixth-stage high-temperature flue gas with a temperature of 130-200°C and supplied to the drying reaction chamber 18; the chemical reaction equation of the hydrolysis reaction is 2CuCl2(s) + H2O(g) → 2HCl(g) + Cu2OCl2(s), and the product HCl gas is supplied to the electrolysis reaction chamber 19 as a raw material for the electrolysis reaction. The drying reaction chamber 18 utilizes the heat contained in the sixth-stage high-temperature flue gas to promote the drying reaction, evaporates the water in the CuCl2 solution to form solid CuCl2, and maintains the temperature in the drying reaction chamber at 100-130°C. After heat exchange, the sixth-stage high-temperature flue gas is converted into low-temperature flue gas and discharged. The electrolysis reaction chamber 19 utilizes a part of the electric energy generated by the photovoltaic cells stored in the storage battery 22 to promote the electrolysis reaction. The chemical reaction equation is 2CuCl(aq) + 2HCl(g) → H2(g) + 2CuCl2(aq). The thermochemical reaction constitutes a complete cycle, that is, a four-step copper-chlorine cycle, and its net reaction is the decomposition of water into hydrogen and oxygen. The thermochemical reaction device sequentially utilizes the thermal energy contained in the fourth, fifth, and sixth-stage high-temperature flue gases and a part of the electric energy generated by the photovoltaic cells to meet the different reaction temperature conditions and the required energy types, which is conducive to the full progress of the reaction and enables the energy to be effectively utilized in a cascaded manner. Preferably, the fourth-stage high-temperature flue gas inlet of the pyrolysis reaction chamber 16 is connected to the high-temperature flue gas outlet of the heat exchanger 8, the fifth-stage high-temperature flue gas inlet of the hydrolysis reaction chamber 17 is connected to the high-temperature flue gas outlet of the pyrolysis reaction chamber 16, and the sixth-stage high-temperature flue gas inlet of the drying reaction chamber 18 is connected to the high-temperature flue gas outlet of the hydrolysis reaction chamber 17.

[0043] In a specific embodiment, the system of the present invention further includes a solid-liquid material transfer system. Through the solid-liquid material transfer system, the solid Cu2OCl2 and HCl gas generated by the reaction in the hydrolysis reaction chamber 17 are respectively transported into the pyrolysis reaction chamber 16 and the electrolysis reaction chamber 19, the liquid CuCl generated by the reaction in the pyrolysis reaction chamber 16 is transported into the electrolysis reaction chamber 19, the CuCl2 solution generated by the reaction in the electrolysis reaction chamber 19 is transported into the drying reaction chamber 18, and the CuCl2 solid generated by the reaction in the drying reaction chamber 18 is transported into the hydrolysis reaction chamber 17. The solid-liquid material transfer system recovers and transports the reusable solid-liquid products generated in each device, realizes the recycling of materials in the hydrogen production system, reduces the production cost, and also avoids polluting the environment.

[0044] As Figure 1 shown, the system of the present invention further includes a hydrogen storage tank 20, an oxygen storage tank 21, and a storage battery 22. Among them, the hydrogen storage tank 20 and the oxygen storage tank 21 are respectively used to store the hydrogen and oxygen generated by the SOEC electrolytic water hydrogen production reaction and the thermochemical cycle. The hydrogen storage tank 20 is connected to the hydrogen separator 22 and the hydrogen outlet of the electrolysis reaction chamber 19, and the oxygen storage tank 21 is connected to the secondary heat exchanger 13 and the oxygen outlet of the pyrolysis reaction chamber 16. The storage battery 22 is used to store the electric energy generated by the photovoltaic cell and is connected to the primary photovoltaic cell 4 and the secondary photovoltaic cell 10.

[0045] The embodiment of the present application also provides an electro / thermal chemical cascade hydrogen production method for solar radiation energy grading and waste heat energy thermal complementarity coupling, which specifically includes the following steps: The natural sunlight is concentrated once and then reaches the frequency division component 2. The light beam that can be efficiently utilized by the photovoltaic cell is reflected to the photovoltaic power generation device, and the remaining solar waste light in other bands is transmitted. The waste light is concentrated again and then reaches the tubular receiver 6. The electric energy generated by the photovoltaic power generation device is stored in the storage battery 23; The oxygen-rich air is preheated by the concentrated solar waste light in the tubular receiver 6 and then enters the combustion chamber 7 together with natural gas for combustion, generating the first-stage high-temperature flue gas with a temperature of 2000-2500°C; The high-temperature photovoltaic power generation device for methane oxygen-rich combustion utilizes the radiant energy contained in the first-stage high-temperature flue gas for thermophotovoltaic power generation, converts it into the second-stage high-temperature flue gas with a temperature of 700-1000°C and introduces it into the solid oxide electrolysis cell device. The generated electric energy is stored in the storage battery 23; The third-stage heat exchanger 14 uses the heat energy contained in the second-stage high-temperature flue gas to heat the electrolysis reaction raw material to 700-800°C, converts it into the third-stage high-temperature flue gas with a temperature of 750-850°C and introduces it into the solid oxide electrolysis cell device; The solid oxide electrolyzer 15 uses the third-stage high-temperature flue gas and a part of the electric energy stored in the storage battery 23 to drive the SOEC electrolysis of water to produce hydrogen, converts it into the fourth-stage high-temperature flue gas with a temperature of 530-680°C and introduces it into the pyrolysis reaction chamber 16, so that the temperature in the solid oxide electrolyzer 15 is maintained at 700-800°C; The pyrolysis reaction chamber 16 uses the heat energy contained in the fourth-stage high-temperature flue gas to drive the pyrolysis reaction, converts it into the fifth-stage high-temperature flue gas with a temperature of 400-460°C and introduces it into the hydrolysis reaction chamber 17, so that the temperature in the pyrolysis reaction chamber 16 is maintained at 500-530°C; The hydrolysis reaction chamber 17 uses the heat energy contained in the fifth-stage high-temperature flue gas to drive the hydrolysis reaction, converts it into the sixth-stage high-temperature flue gas with a temperature of 130-200°C and introduces it into the drying reaction chamber 18, so that the temperature in the hydrolysis reaction chamber 17 is maintained at 370-400°C; The drying reaction chamber 18 uses the heat energy contained in the sixth-stage high-temperature flue gas to drive the drying reaction, converts it into low-temperature flue gas and discharges it, so that the temperature in the drying reaction chamber 18 is maintained at 100-130°C.

[0046] In a specific embodiment, the method further includes the following steps: The liquid CuCl produced by the pyrolysis reaction is supplied as the raw material for the electrolysis reaction to the electrolysis reaction chamber 19, and the produced oxygen leaves the cycle; The solid Cu2OCl2 produced by the hydrolysis reaction is supplied as the raw material for the pyrolysis reaction to the pyrolysis reaction chamber 16; The solid CuCl2 produced by the drying reaction is supplied as the product of the hydrolysis reaction to the hydrolysis reaction chamber 17; The CuCl2 solution produced by the electrolysis reaction is supplied as the raw material for the drying reaction to the drying reaction chamber 18, and the produced hydrogen leaves the cycle.

[0047] In a specific embodiment, the method further includes the following steps: using a part of the electric energy stored in the storage battery 23 through the electrolysis reaction chamber 19 to carry out electrolysis reaction to produce hydrogen, and storing the produced hydrogen in the hydrogen storage tank 20; storing the oxygen generated by the reaction in the solid oxide electrolyzer 15 and the pyrolysis reaction chamber 16 in the oxygen storage tank 21, and partially introducing it into the tubular receiver 6 to be mixed with air to form oxygen-enriched air; by regulating the ratio of air and oxygen entering the tubular receiver 6, that is, regulating the oxygen content in the oxygen-enriched air, to balance the instability of solar energy and ensure the stable operation of the system day and night.

[0048] In a specific embodiment, it further includes the following steps: the hydrogen separator 22 separates hydrogen and water from the mixed gas at the outlet of the primary heat exchanger 12, and the separated water and the newly input cooling water of the system are merged into the primary photovoltaic cell waste heat utilization device 5 together. Part of the separated hydrogen is supplied to the cathode of the solid oxide electrolyzer 15, and an appropriate amount of hydrogen can effectively prevent the cathode material from being oxidized under high temperature and high humidity conditions.

[0049] In a specific embodiment, the required electricity / heat ratio for hydrogen production by the solid oxide electrolyzer is about 2 (under the condition of 800 °C). The four-step copper-chlorine cycle requires thermal energy of 349.96 kJ / (mol H2) and electric energy of 57.76 kJ / (mol H2). Excess preheated hot water is introduced to ensure the full progress of the reaction. To ensure safety, the temperature of the oxygen-enriched air preheated by concentrated solar energy does not exceed 700 °C, and the natural gas feed power is 15 kW. The power generation power of the photovoltaic power generation device is 1.03 kW, and the power generation power of the high-temperature photovoltaic power generation device for methane oxygen-enriched combustion is 7.48 kW; the hydrogen production power of the solid oxide electrolyzer device is 9.03 kW, the hydrogen production power of the thermochemical reaction device is 3.46 kW, and the hydrogen production efficiency of the system is 60.86%. From the above embodiments, it can be seen that the energy sources utilized by the system and method of the present invention are solar radiation and natural gas, and the outputs are hydrogen and electricity. The system utilizes natural sunlight by frequency division. High-quality sunlight is directly used for photovoltaic power generation, and low-quality solar afterglow is complementary to natural gas to improve the energy grade. Different energy conversion methods are used to realize the orderly conversion and utilization of the temperature gradient of the afterglow after solar energy frequency division. And based on the principle of energy quality matching, different-quality electric / thermal energies are supplied to the solid oxide electrolyzer and the thermochemical cycle in stages to produce hydrogen, realizing the complementary coupling of different qualities on the basis of energy cascade conversion, and providing an efficient solar energy cascade hydrogen production approach.

[0050] The foregoing are only the preferred embodiments of the present application and are not intended 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 protection scope of the present application.

Claims

1. An electric / thermochemical cascade hydrogen production system with solar radiation energy classification and residual light energy thermal complementary coupling, characterized in that: It comprises a light collecting component, a frequency dividing component (2), a photovoltaic power generation device, a methane oxygen-enriched combustion high-temperature photovoltaic power generation device, a solid oxide electrolysis cell device and a thermochemical reaction device; The focusing component focuses sunlight, and the frequency division component (2) divides the frequency of the focused light beam, wherein the frequency band suitable for photovoltaic power generation is reflected to the photovoltaic power generation device for photovoltaic power generation, and the remaining frequency bands are secondary focused by the focusing component to the methane oxygen-enriched combustion high-temperature photovoltaic power generation device; The methane oxygen-enriched combustion high-temperature photovoltaic power generation device utilizes a tubular receiver (6) to convert secondary concentrated sunlight into heat energy to preheat oxygen-enriched air. The preheated oxygen-enriched air and natural gas are input into a combustion chamber (7) for oxygen-enriched combustion to generate first-stage high-temperature flue gas. The methane oxygen-enriched combustion high-temperature photovoltaic power generation device utilizes the radiation energy of the first-stage high-temperature flue gas to generate photovoltaic power. The second-stage high-temperature flue gas is discharged from the combustion chamber (7) to the solid oxide electrolysis cell device. The solid oxide electrolysis cell device utilizes the heat of the high-temperature flue gas step by step by using the three-stage heat exchanger (14) and the solid oxide electrolysis cell (15), wherein the solid oxide electrolysis cell (15) utilizes the electric energy generated by the system and the heat contained in the high-temperature flue gas to perform high-temperature electrolysis to produce hydrogen, and discharges the fourth-stage high-temperature flue gas to supply the thermochemical circulation device; The pyrolysis reaction chamber (16), the hydrolysis reaction chamber (17) and the drying reaction chamber (18) of the thermochemical cycle device use the heat energy contained in the high-temperature flue gas to drive the reaction step by step. The entire thermochemical cycle device uses the heat energy contained in the high-temperature flue gas and the electrical energy generated by the system to realize the copper-chlorine cycle and generate hydrogen.

2. The electric / thermochemical cascade hydrogen production system of solar radiation energy classification and afterglow energy thermal complementary coupling as claimed in claim 1 is characterized by: The light-collecting assembly comprises a primary light-collecting assembly (1) and a secondary light-collecting assembly (3); the primary light-collecting assembly (1) is used to collect natural sunlight to a frequency-dividing assembly (2); the frequency-dividing assembly (2) reflects a first light beam that can be efficiently utilized by a photovoltaic cell, and transmits sunlight residual light in other bands to the secondary light-collecting assembly (3); the secondary light-collecting assembly (3) is used to collect the residual light after frequency division to a tubular receiver (6).

3. The electric / thermochemical cascade hydrogen production system of solar radiation energy classification and afterglow energy thermal complementary coupling as claimed in claim 1 is characterized by: The photovoltaic power generation device comprises a primary photovoltaic cell (4) and a primary photovoltaic cell waste heat utilization device (5); the primary photovoltaic cell (4) is used to receive the frequency band reflected by the frequency division component (2) to perform photovoltaic power generation, thereby providing electrical energy for subsequent electrolytic hydrogen production; The primary photovoltaic cell waste heat utilization device (5) recovers the heat energy of the primary photovoltaic cell (4) to preheat water as a raw material for a thermochemical reaction, while avoiding the temperature rise of the primary photovoltaic cell; the primary photovoltaic cell waste heat utilization device (7) is provided with an inlet for introducing cold water and an outlet for discharging hot water.

4. The electric / thermochemical cascade hydrogen production system of solar radiation energy classification and afterglow energy thermal complementary coupling as claimed in claim 1 is characterized by: The methane oxygen-enriched combustion high-temperature photovoltaic power generation device comprises a tubular receiver (6), a combustion chamber (7), a transmitter (8), a filter (9), a secondary photovoltaic cell (10) and a secondary photovoltaic cell waste heat utilization device (11); a photothermal absorber is fixed inside the tubular receiver (6) for absorbing focused sunlight and converting it into heat energy to preheat oxygen-enriched air, and the natural gas and the preheated oxygen-enriched air are input into the combustion chamber (7) for combustion; the first-stage high-temperature flue gas generated by the oxygen-enriched combustion of natural gas in the combustion chamber (7) generates radiation energy through the transmitter (8), and the radiation energy selectively passes through the filter (9) and is absorbed by the secondary photovoltaic cell (10) to generate electrical energy; the secondary photovoltaic cell waste heat utilization device (11) recovers the heat energy of the secondary photovoltaic cell (10) to preheat water as a raw material for the solid oxide water electrolysis hydrogen production reaction, while avoiding the temperature rise of the secondary photovoltaic cell.

5. The electric / thermochemical cascade hydrogen production system of solar radiation energy classification and residual light energy thermal complementary coupling as claimed in claim 1 is characterized by: The solid oxide electrolysis cell device comprises a primary heat exchanger (12), a secondary heat exchanger (13), a tertiary heat exchanger (14) and a solid oxide electrolysis cell (15); the primary heat exchanger (12) recovers the heat of high-temperature hydrogen and water vapor discharged from the cathode of the solid oxide electrolysis cell (15) to further heat the hot water discharged from the secondary photovoltaic cell waste heat utilization device (11); the secondary heat exchanger (13) recovers the heat of high-temperature oxygen discharged from the anode of the solid oxide electrolysis cell (15) to further heat the hot water vapor discharged from the primary heat exchanger (12); the tertiary heat exchanger (14) utilizes the second high-temperature flue gas to heat the hot water vapor discharged from the secondary photovoltaic cell waste heat utilization device (11) The heat contained in the gas is used to further heat the hot water vapor discharged from the secondary heat exchanger (13). The heated high-temperature water vapor is introduced into the cathode of the solid oxide electrolytic cell (15) as a raw material for the electrolysis reaction. The third-stage high-temperature flue gas after heat exchange in the tertiary heat exchanger (14) is supplied to the solid oxide electrolytic cell (15); the solid oxide electrolytic cell (15) uses the electricity generated by the photovoltaic cell and the heat contained in the third-stage high-temperature flue gas to perform high-temperature electrolysis to produce hydrogen. The required electricity is provided by the photovoltaic power generation of the system. High-temperature hydrogen and high-temperature water vapor that is not electrolyzed are produced at the cathode, and high-temperature oxygen is produced at the anode. The fourth-stage high-temperature flue gas after heat exchange is supplied to the thermochemical circulation device.

6. The electric / thermochemical cascade hydrogen production system of solar radiation energy classification and residual light energy thermal complementary coupling as claimed in claim 1, characterized in that: The solid oxide electrolysis cell device has a hot water / water vapor pipeline, which is connected to a primary heat exchanger (12), a secondary heat exchanger (13), a tertiary heat exchanger (14) and a solid oxide electrolysis cell (15) in sequence; the hot side inlet of the primary heat exchanger (12) is connected to the cathode outlet of the solid oxide electrolysis cell (15), and the cold side inlet is connected to the hot water outlet of the secondary photovoltaic cell waste heat utilization device (11); the hot side inlet of the secondary heat exchanger (13) is connected to the anode outlet of the solid oxide electrolysis cell (15), and the cold side inlet is connected to the cold side outlet of the primary heat exchanger (12); the cold side inlet of the tertiary heat exchanger (14) is connected to the cold side outlet of the secondary heat exchanger (13); the cathode of the solid oxide electrolysis cell (15) is provided with an inlet for introducing high-temperature water vapor, an inlet for introducing hydrogen and an outlet for discharging high-temperature hydrogen and water vapor, and the anode is provided with an outlet for discharging high-temperature oxygen; The solid oxide electrolytic cell device is also provided with a hydrogen separator (22), which is used to separate hydrogen and water in the mixed gas at the outlet of the primary heat exchanger (12). The separated water enters the photovoltaic power generation device for cooling, and part of the separated hydrogen is supplied to the cathode of the solid oxide electrolytic cell (15). The hydrogen effectively prevents the cathode material from being oxidized under high temperature and high humidity conditions.

7. The electric / thermochemical cascade hydrogen production system of claim 1 with solar radiation energy classification and residual light energy thermal complementary coupling, characterized in that: The thermochemical reaction device comprises a pyrolysis reaction chamber (16), a hydrolysis reaction chamber (17), a drying reaction chamber (18) and an electrolysis reaction chamber (19). The pyrolysis reaction chamber (16) utilizes the heat contained in the third-stage high-temperature flue gas to promote the pyrolysis reaction. After heat exchange, the third-stage high-temperature flue gas is converted into a fourth-stage high-temperature flue gas with a temperature of 400 to 460° C. and supplied to the hydrolysis reaction chamber (17). The chemical reaction equation of the pyrolysis reaction is Cu2OCl2(s)→2CuCl(l)+0.5O2(g). The hydrolysis reaction chamber (17) utilizes the heat contained in the fourth-stage high-temperature flue gas to promote the hydrolysis reaction. After heat exchange, the fourth-stage high-temperature flue gas is converted into the fifth-stage high-temperature flue gas with a temperature of 130 to 200° C. and supplied to the drying reaction chamber (18). The chemical reaction equation of the hydrolysis reaction is 2CuCl2(s)+H2O(g)→2HCl(g)+Cu2OCl2(s). The product HCl gas is supplied to the electrolysis reaction chamber (19) as a raw material for the electrolysis reaction. The drying reaction chamber (18) utilizes the heat contained in the fifth-stage high-temperature flue gas to promote the drying reaction, evaporates the water in the CuCl2 solution to form solid CuCl2, and after heat exchange, the fifth-stage high-temperature flue gas is converted into low-temperature flue gas for discharge; The electrolytic reaction chamber (19) utilizes part of the electricity generated by the methane oxygen-enriched combustion high-temperature photovoltaic power generation device to promote the electrolytic reaction, and the chemical reaction equation is 2CuCl(aq)+2HCl(g)→H2(g)+2CuCl2(aq); The thermochemical reaction device constitutes a complete four-step copper-chlorine cycle, and its net reaction is the decomposition of water into hydrogen and oxygen.

8. The electric / thermochemical cascade hydrogen production system of solar radiation energy classification and residual light energy thermal complementary coupling as claimed in claim 1 is characterized in that: The system further comprises a solid-liquid material transport system, through which solid Cu2OCl2 and HCl gas produced by the reaction in the hydrolysis reaction chamber (17) are transported to the pyrolysis reaction chamber (16) and the electrolysis reaction chamber (19) respectively, liquid CuCl2 produced by the reaction in the pyrolysis reaction chamber (16) is transported to the electrolysis reaction chamber (19), CuCl2 solution produced by the reaction in the electrolysis reaction chamber (19) is transported to the drying reaction chamber (18), and solid CuCl2 produced by the reaction in the drying reaction chamber (18) is transported to the hydrolysis reaction chamber (17).

9. The electric / thermochemical cascade hydrogen production system of claim 1 with solar radiation energy classification and residual light energy thermal complementary coupling, characterized in that: The system also includes a hydrogen storage tank (20), an oxygen storage tank (21) and a battery (23), wherein the hydrogen storage tank (20) is used to store hydrogen produced by the solid oxide electrolysis cell device and the thermochemical reaction device, and the oxygen storage tank (21) is used to store oxygen produced by the solid oxide electrolysis cell device and the thermochemical reaction device; the battery (23) is used to store electricity generated by photovoltaic cells of the photovoltaic power generation device and the methane oxygen-rich combustion high-temperature photovoltaic power generation device, and to provide power for the electrolysis process of the solid oxide electrolysis cell device and the thermochemical reaction device.

10. An electric / thermochemical stepwise hydrogen production method based on the solar radiation energy classification and the afterlight energy thermal complementary coupling of the system according to any one of claims 1 to 9, characterized in that: The natural sunlight is divided into different frequencies for use, high-quality sunlight is used directly for photovoltaic power generation, low-quality residual sunlight is used to complement natural gas to improve energy quality, different energy conversion methods are used to achieve orderly conversion and utilization of residual light temperature gradients after solar energy frequency division, and complementary coupling of different qualities is achieved based on the principle of energy quality matching; the specific steps include the following: The natural sunlight is concentrated once and reaches the frequency division component (2), which reflects the light beam that can be efficiently utilized by the photovoltaic power generation device and transmits the residual sunlight in the remaining bands. The residual light is concentrated twice and reaches the tubular receiver (6); The oxygen-enriched air is preheated by concentrated solar residual light in the tubular receiver (6) and then introduced into the combustion chamber (7) together with the natural gas for combustion, thereby generating a first-stage high-temperature flue gas with a temperature of 2000-2500° C.; the radiation energy contained in the first-stage high-temperature flue gas with a temperature of 2000-2500° C. is used by the methane oxygen-enriched combustion high-temperature photovoltaic power generation device to perform thermal photovoltaic power generation, and the radiation energy is converted into a second-stage high-temperature flue gas with a temperature of 850-1000° C. and introduced into the solid oxide electrolysis cell device; The solid oxide electrolysis cell device utilizes the heat energy contained in the second-stage high-temperature flue gas with a temperature of 850 to 1000° C. to heat the electrolysis reaction raw materials through the third-stage heat exchanger (14), converting the second-stage high-temperature flue gas with a temperature of 750 to 850° C. into the third-stage high-temperature flue gas, which is then introduced into the solid oxide electrolysis cell (15); the solid oxide electrolysis cell (15) utilizes the third-stage high-temperature flue gas with a temperature of 750 to 850° C. and the electricity generated by the photovoltaic power generation of the system to drive the solid oxide electrolysis water to produce hydrogen, converting the third-stage high-temperature flue gas into the fourth-stage high-temperature flue gas with a temperature of 530 to 680° C., which is then introduced into the thermochemical reaction device; In the thermochemical reaction device, the pyrolysis reaction chamber (16) uses the heat energy contained in the fourth-level high-temperature flue gas to drive the pyrolysis reaction, converting it into the fifth-level high-temperature flue gas with a temperature of 400-460°C and passing it into the hydrolysis reaction chamber (17); the hydrolysis reaction chamber (17) uses the heat energy contained in the fifth-level high-temperature flue gas to drive the hydrolysis reaction, converting it into the sixth-level high-temperature flue gas with a temperature of 130-200°C and passing it into the drying reaction chamber (18); the drying reaction chamber (18) uses the heat energy contained in the sixth-level high-temperature flue gas to drive the drying reaction, converting it into low-temperature flue gas for discharge; the electrolysis reaction chamber (19) uses the electric energy generated by the photovoltaic power generation of the system to carry out electrolysis reaction to produce hydrogen.

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