Hydrogen production device and hydrogen production method

Abstract

The invention provides a hydrogen production device and a hydrogen production method, and relates to the technical field of water electrolysis hydrogen production. Wherein the air compressor, the anode heat exchanger and the anode of the SOEC galvanic pile in the device form an anode loop, and the cathode of the SOEC galvanic pile, the cathode heat exchanger, the mixer, the separator and the hydrogen circulator form a cathode loop; the gas-water heat exchanger is connected with the steam generator and the anode heat exchanger; the light condensation and heat collection loop comprises a light condensation tower, a first-stage heat exchanger, a heat storage tank, a cold storage tank, a second-stage heat exchanger and a steam generator. According to the device, heat is supplied to an SOEC loop through an internal indirect thermal coupling light condensation and heat collection system, meanwhile, the SOEC loop is provided with double loops capable of conducting deep waste heat recovery, thorough decoupling of short-time fluctuation of solar irradiation and steam generation is achieved, and it is guaranteed that steam entering the SOEC loop is kept stable in temperature and flow; and meanwhile, the degree of freedom of overheating and fine tuning of the SOEC loop is reserved, so that the control difficulty in the hydrogen production process of the solid oxide electrolytic tank is reduced, and the equipment stability is improved.

Description

Technical Field

[0001] This application relates to the field of hydrogen production technology through water electrolysis, and in particular to a hydrogen production device and a hydrogen production method. Background Technology

[0002] Hydrogen production through water electrolysis is a technology that uses direct current to drive water molecules to undergo a redox reaction at electrodes, converting electrical energy into the chemical energy of hydrogen. This technology offers a clean solution for energy transition and carbon neutrality.

[0003] Current hydrogen production methods using water electrolysis are gradually replacing traditional fossil fuel-based hydrogen production with solid oxide electrolysis cells (SOECs), which have greater potential in terms of efficiency and scalable unit power density. Specifically, SOEC hydrogen production involves the electrolysis of water vapor through an oxygen ion conductor under high-temperature steam conditions.

[0004] However, when using the above-mentioned solid oxide electrolyzer hydrogen production scheme, there are strict requirements for temperature difference, pressure difference, composition boundary, and steam quality in the solid oxide electrolyzer system during the hydrogen production process. If the variable parameters such as stack temperature, anolyte oxygen volume fraction, steam conversion rate, and inlet gauge pressure are not properly controlled, it can easily lead to rapid aging or damage of the system equipment, making the hydrogen production process difficult to control and resulting in insufficient equipment stability. Summary of the Invention

[0005] The main purpose of this application is to propose a hydrogen production device and method, which aims to reduce the control difficulty in the hydrogen production process of solid oxide electrolyzers and improve equipment stability.

[0006] In a first aspect, the present invention provides a hydrogen production device, comprising: a solid oxide electrolyzer (SOEC) circuit, a concentrating solar collector circuit, and a controller, wherein the SOEC circuit comprises: an air compressor (102), an anode heat exchanger (103), an SOEC stack (101), a cathode heat exchanger (104), a mixer (105), a separator (106), a hydrogen circulator (107), and a gas-water heat exchanger (108); the concentrating solar collector circuit comprises: a concentrating tower (109), a primary heat exchanger (110), a hot storage tank (111), a cold storage tank (112), a secondary heat exchanger (113), and a steam generator (114). The air inlet of the air compressor (102) is connected to the outside, and the air outlet of the air compressor (102) is connected to the air inlet of the anode heat exchanger (103). The air outlet of the anode heat exchanger (103) is connected to the anode air inlet of the SOEC stack (101) and the air inlet of the gas-water heat exchanger (108). The anode air outlet of the SOEC stack (101) is also connected to the air inlet of the anode heat exchanger (103). The outlet of the gas-water heat exchanger (108) is connected to the outside, and the inlet of the gas-water heat exchanger (108) is connected to an external deionized water source. The outlet of the gas-water heat exchanger (108) is connected to the steam generator (114), and the outlet of the steam generator (114) is connected to the inlet of the cathode heat exchanger (104). The outlet of the cathode heat exchanger (104) is connected to the inlet of the mixer (105) and the inlet of the separator (106), respectively. The outlet of the mixer (105) is connected to the cathode inlet of the SOEC, the outlet of the SOEC cathode is also connected to the inlet of the cathode heat exchanger (104), the outlet of the separator (106) is connected to an external water storage device, the outlet of the separator (106) is connected to an external gas collection device and the inlet of the hydrogen circulator (107), and the outlet of the hydrogen circulator (107) is connected to the inlet of the mixer (105). The concentrating tower (109) and the first-stage heat exchanger (110) are connected in series to form a loop, the hot storage tank (111) and the cold storage tank (112) are connected in series to form a loop, and the second-stage heat exchanger (113) and the heat exchange end of the steam generator (114) form a loop. The primary heat exchanger (110) is located between the outlet of the hot storage tank (111) and the inlet of the cold storage tank (112) to exchange the heat in the circulation loop formed by the concentrating tower (109) and the primary heat exchanger (110) in series with the circulation loop formed by the hot storage tank (111) and the cold storage tank (112) in series. The secondary heat exchanger (113) is located between the outlet of the cold storage tank (112) and the inlet of the hot storage tank (111), and is used to exchange the heat in the circulation loop formed by the hot storage tank (111) and the cold storage tank (112) in series to the circulation loop formed by the heat exchange end of the secondary heat exchanger (113) and the steam generator (114). The controller is communicatively connected to the air compressor (102), the SOEC stack (101), the hydrogen circulator (107), and the steam generator (114). The controller is used to respond to a hydrogen production command to control the air compressor (102), the SOEC stack (101), the hydrogen circulator (107), and the steam generator (114) to operate according to preset boundary conditions, control the steam generator (114) to generate saturated steam at a preset pressure and preset temperature, and control the hydrogen circulator (107) to introduce hydrogen into the mixer (105) according to a preset first volume fraction. The preset boundary conditions include: anode-side oxygen volume conditions, SOEC stack (101) temperature gradient conditions, SOEC stack (101) inlet pressure conditions, and bilateral pressure relationship.

[0007] In an optional embodiment, the heat transfer medium filled in the circulation loop formed by the concentrating tower (109) and the first-stage heat exchanger (110) in series, and the circulation loop formed by the heat exchange end of the second-stage heat exchanger (113) and the steam generator (114) is heat transfer oil. The heat-conducting medium filled in the circulation loop formed by the hot storage tank (111) and the cold storage tank (112) connected in series is molten salt.

[0008] In an optional embodiment, the hydrogen production device further includes: an anode heater (115), a cathode heater (116), a hydrogen heater (117), and a thermal oil heater (118); the anode heater (115), the cathode heater (116), the hydrogen heater (117), and the thermal oil heater (118) are all communicatively connected to the controller; The anode heater (115) is located between the outlet of the anode heat exchanger (103) and the anode inlet of the SOEC stack (101). The cathode heater (116) is located between the outlet of the mixer (105) and the cathode inlet of the SOEC. The hydrogen heater (117) is located between the outlet of the hydrogen circulator (107) and the inlet of the mixer (105). The thermal oil heater (118) is located between the oil outlet of the secondary heat exchanger (113) and the heat exchange end oil inlet of the steam generator (114).

[0009] In an optional embodiment, the SOEC stack (101), the anode heater (115), the cathode heater (116), the hydrogen heater (117), the thermal oil heater (118), and the air compressor (102) are all powered by an external photovoltaic power supply circuit and a grid power supply circuit in parallel.

[0010] In an optional embodiment, the steam generator (114) is a shell-side open steam generator.

[0011] In a second aspect, the present invention provides a hydrogen production method, applied to a controller of a hydrogen production apparatus according to any of the foregoing embodiments, the method comprising: In response to a hydrogen production command, the air compressor, SOEC stack, hydrogen circulator, and steam generator are controlled to operate according to preset boundary conditions. The steam generator is controlled to generate saturated steam at a preset pressure and temperature, and the hydrogen circulator is controlled to introduce hydrogen into the mixer according to a preset first volume fraction. The preset boundary conditions include: anode-side oxygen volume condition, SOEC stack temperature gradient condition, SOEC stack inlet pressure condition, and bilateral pressure relationship.

[0012] In an optional implementation, the method further includes: The gas temperature at the outlet of the anode heat exchanger is collected. If the gas temperature does not reach the target gas temperature at the anode inlet of the SOEC stack, the anode heater is controlled to start supplementary heating. The hydrogen temperature at the outlet of the hydrogen circulator is collected. If the hydrogen temperature does not reach the target hydrogen temperature at the inlet of the mixer, the hydrogen heater is controlled to start for supplemental heating. The water vapor temperature at the outlet of the mixer is collected. If the water vapor temperature does not reach the target water vapor temperature at the cathode inlet of the SOEC stack, the cathode heater is controlled to start for supplemental heating. The temperature of the heat transfer oil at the outlet of the secondary heat exchanger is collected. If the temperature of the heat transfer oil does not reach the target temperature of the heat transfer oil at the inlet of the heat exchange end of the steam generator, the heat transfer oil heater is controlled to start supplementary heating.

[0013] In an optional implementation, the method further includes: Based on the preset optimization parameter algorithm, the preset optimization objective, and the preset boundary conditions, the optimal set of operating parameters is calculated using a preset solution algorithm. The preset optimization parameter algorithm includes: an electric hydrogen production efficiency algorithm, a solar hydrogen production efficiency algorithm, and a thermal storage-to-heat ratio algorithm. The hydrogen production unit is controlled to operate based on multiple optimal operating parameters from the set of optimal operating parameters.

[0014] In an optional implementation, the method further includes: In response to the hot standby command, the power supply to the SOEC stack is cut off, and the air compressor, the hydrogen circulator, and the steam generator are controlled to operate according to preset boundary conditions. The steam generator is controlled to generate saturated steam at a preset pressure and preset temperature, and the hydrogen circulator is controlled to introduce hydrogen into the mixer according to a first preset volume fraction.

[0015] In an optional implementation, the method further includes: In response to the shutdown order, the power supply to the SOEC stack is cut off, the steam generator is controlled to stop operating, the air compressor, the hydrogen circulator, and the steam generator are controlled to operate according to preset boundary conditions, and the hydrogen circulator is controlled to introduce nitrogen-hydrogen mixed gas into the mixer according to a second preset volume fraction.

[0016] Thirdly, the present invention provides an electronic device, comprising: a processor, a storage medium, and a bus, wherein the storage medium stores machine-readable instructions executable by the processor, and when the electronic device is running, the processor communicates with the storage medium via the bus, and the processor executes the machine-readable instructions to perform the steps of any of the methods described in the foregoing embodiments.

[0017] Fourthly, the present invention provides a computer-readable storage medium storing a computer program, which, when executed by a processor, performs the steps of the method as described in any of the foregoing embodiments.

[0018] The beneficial effects of this application are: The hydrogen production device provided in this application includes: a solid oxide electrolyzer (SOEC) circuit, a concentrating solar collector circuit, and a controller. The SOEC circuit includes: an air compressor (102), an anode heat exchanger (103), an SOEC stack (101), a cathode heat exchanger (104), a mixer (105), a separator (106), a hydrogen circulator (107), and a gas-water heat exchanger (108). The concentrating solar collector circuit includes: a concentrating tower (109), a primary heat exchanger (110), a thermal storage tank (111), and a cold storage tank (108). 12) Secondary heat exchanger (113), steam generator (114); air compressor (102), anode heat exchanger (103), and the anode of SOEC stack (101) form the anode circuit; the cathode of SOEC stack (101), cathode heat exchanger (104), mixer (105), separator (106), and hydrogen circulator (107) form the cathode circuit; gas-water heat exchanger (108) is connected to steam generator (114) and anode heat exchanger (103); the concentrating tower (109) in the concentrating solar collector circuit is connected to the primary heat exchanger ( 110) The heat energy is circulated and exchanged to the circulation loop consisting of the hot storage tank (111) and the cold storage tank (112). The circulation loop consisting of the hot storage tank (111) and the cold storage tank (112) circulates and exchanges the heat energy to the heat exchange end of the steam generator (114) through a secondary heat exchanger (113). The controller is communicatively connected to the air compressor (102), the SOEC stack (101), the hydrogen circulator (107), and the steam generator (114). The controller is used to control the air compressor (102) in response to the hydrogen production command. The SOEC stack (101), the hydrogen circulator (107), and the steam generator (114) operate according to preset boundary conditions. The steam generator (114) is controlled to generate saturated steam at a preset pressure and a preset temperature, and the hydrogen circulator (107) is controlled to introduce hydrogen into the mixer (105) according to a preset first volume fraction. The preset boundary conditions include: anode-side oxygen volume condition, SOEC stack (101) temperature gradient condition, SOEC stack (101) inlet pressure condition, and bilateral pressure relationship. In this embodiment, a concentrating solar thermal system, thermally coupled between an internal concentrating tower and two molten salt storage tanks, supplies heat to the SOEC loop. Simultaneously, the SOEC loop, through a dual-loop system with cathode and anode capable of deep waste heat recovery, completely decouples short-term fluctuations in solar irradiance from steam generation, ensuring stable temperature and flow rates for the steam entering the SOEC loop. Furthermore, it retains the SOEC loop's freedom to perform superheating and fine-tuning through tail gas heat exchange, thereby reducing the control difficulty in the hydrogen production process of the solid oxide electrolyzer and improving equipment stability. Attached Figure Description

[0019] To more clearly illustrate the technical solutions of the embodiments of this application, the accompanying drawings used in the embodiments of this application will be briefly introduced below. It should be understood that the following drawings only show some embodiments of this application and should not be regarded as a limitation of the scope. For those skilled in the art, other related drawings can be obtained based on these drawings without creative effort.

[0020] Figure 1 This is a schematic diagram of the structure of a hydrogen production apparatus provided in one embodiment of this application; Figure 2 A schematic flowchart of a hydrogen production method provided in an embodiment of this application; Figure 3 A schematic flowchart of a hydrogen production method provided in another embodiment of this application; Figure 4 This is a schematic diagram of the structure of an electronic device provided in an embodiment of this application.

[0021] Figure reference numerals: 101-SOEC fuel cell stack; 102-Air compressor; 103-Anode heat exchanger; 104-Cathode heat exchanger; 105-Mixer; 106-Separator; 107-Hydrogen circulator; 108-Gas-water heat exchanger; 109-Concentrating tower; 110-First-stage heat exchanger; 111-Hot storage tank; 112-Cold storage tank; 113-Second-stage heat exchanger; 114-Steam generator; 115-Anode heater; 116-Cathode heater; 117-Hydrogen heater; 118-Heat transfer oil heater. Detailed Implementation

[0022] To make the objectives, technical solutions, and advantages of the embodiments of this application clearer, the technical solutions of the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this application, and not all embodiments. The components of the embodiments of this application described and shown in the accompanying drawings can generally be arranged and designed in various different configurations.

[0023] Therefore, the following detailed description of the embodiments of this application provided in the accompanying drawings is not intended to limit the scope of the claimed application, but merely to illustrate selected embodiments of the application. All other embodiments obtained by those skilled in the art based on the embodiments of this application without inventive effort are within the scope of protection of this application.

[0024] It should be noted that similar labels and letters in the following figures indicate similar items. Therefore, once an item is defined in one figure, it does not need to be further defined and explained in subsequent figures.

[0025] It should be noted that, in this document, relational terms such as "first" and "second" are used only to distinguish one entity or operation from another, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Furthermore, the terms "comprising," "including," or any other variations thereof are intended to cover non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements includes not only those elements but also other elements not expressly listed, or elements inherent to such a process, method, article, or apparatus. Without further limitations, an element defined by the phrase "comprising one..." does not exclude the presence of other identical elements in the process, method, article, or apparatus that includes said element.

[0026] The following detailed description of some embodiments of this application is provided in conjunction with the accompanying drawings. Unless otherwise specified, the following embodiments and features can be combined with each other.

[0027] Current hydrogen production methods using water electrolysis are increasingly replacing traditional fossil fuel-based hydrogen production with solid oxide electrolyzers (SOECs), which offer greater potential in terms of efficiency and scalable unit power density. Specifically, SOECs achieve water vapor electrolysis under high-temperature steam conditions through an oxygen ion conductor. However, current SOEC systems face stringent requirements regarding temperature difference, pressure difference, compositional boundaries, and steam quality. Improper control of parameters such as stack temperature, anode oxygen volume fraction, steam conversion rate, and inlet gauge pressure can lead to rapid aging or damage to the system equipment. Furthermore, using concentrated solar power (CSP) to heat the SOEC system results in unstable heat supply, and the current SOEC systems also have low utilization rates of waste heat from exhaust gases. Therefore, current SOEC hydrogen production methods present significant challenges in process control and suffer from insufficient equipment stability.

[0028] To address the aforementioned issues, the main objective of this application is to propose a hydrogen production device and method, aiming to reduce the control difficulty in the hydrogen production process of solid oxide electrolyzers and improve equipment stability.

[0029] Figure 1 Please refer to the schematic diagram of a hydrogen production apparatus provided in one embodiment of this application. Figure 1The hydrogen production unit includes: a solid oxide electrolyzer (SOEC) circuit, a concentrating solar collector circuit, and a controller. The SOEC circuit includes: an air compressor 102, an anode heat exchanger 103, an SOEC stack 101, a cathode heat exchanger 104, a mixer 105, a separator 106, a hydrogen circulator 107, and a gas-water heat exchanger 108. The concentrating solar collector circuit includes: a concentrating tower 109, a primary heat exchanger 110, a hot storage tank 111, a cold storage tank 112, a secondary heat exchanger 113, and a steam generator 114.

[0030] The air inlet of the air compressor 102 is connected to the outside, the air outlet of the air compressor 102 is connected to the air inlet of the anode heat exchanger 103, the air outlet of the anode heat exchanger 103 is connected to the anode air inlet of the SOEC stack 101 and the air inlet of the gas-water heat exchanger 108, and the anode air outlet of the SOEC stack 101 is also connected to the air inlet of the anode heat exchanger 103.

[0031] The outlet of the gas-water heat exchanger 108 is connected to the outside, and the inlet of the gas-water heat exchanger 108 is connected to an external deionized water source. The outlet of the gas-water heat exchanger 108 is connected to the steam generator 114. The outlet of the steam generator 114 is connected to the inlet of the cathode heat exchanger 104. The outlet of the cathode heat exchanger 104 is connected to the inlet of the mixer 105 and the inlet of the separator 106. The outlet of the mixer 105 is connected to the cathode inlet of the SOEC. The cathode outlet of the SOEC is also connected to the inlet of the cathode heat exchanger 104. The outlet of the separator 106 is connected to an external water storage device. The outlet of the separator 106 is connected to an external gas collection device and the inlet of the hydrogen circulator 107. The outlet of the hydrogen circulator 107 is connected to the inlet of the mixer 105.

[0032] The aforementioned concentrating tower 109 is connected in series with the aforementioned primary heat exchanger 110 to form a circulation loop, the aforementioned hot storage tank 111 and the aforementioned cold storage tank 112 are connected in series to form a circulation loop, and the aforementioned secondary heat exchanger 113 and the aforementioned steam generator 114 form a circulation loop.

[0033] The aforementioned primary heat exchanger 110 is disposed between the outlet of the aforementioned hot storage tank 111 and the inlet of the aforementioned cold storage tank 112, and is used to exchange the heat in the circulation loop formed by the aforementioned concentrating tower 109 and the aforementioned primary heat exchanger 110 in series to the circulation loop formed by the aforementioned hot storage tank 111 and the aforementioned cold storage tank 112 in series.

[0034] The secondary heat exchanger 113 is disposed between the outlet of the cold storage tank 112 and the inlet of the hot storage tank 111, and is used to exchange the heat in the circulation loop formed by the hot storage tank 111 and the cold storage tank 112 in series to the circulation loop formed by the secondary heat exchanger 113 and the heat exchange end of the steam generator 114.

[0035] For example, the internal structure of the aforementioned hydrogen production device may be connected by pipelines with the same or different material specifications. The material of the pipeline may be, for example, stainless steel, ceramic, or other materials with strong thermal stability, but this is not a limitation. Furthermore, the flow rate and temperature may vary at different loop locations within different hydrogen production devices. In addition to the material being the same or different, the different specifications of the pipeline may also include the same or different lengths, the same or different inner diameters, the same or different wall thicknesses, the same or different shapes, and the same or different interface types. However, the above are only possible examples, and the actual pipeline specifications can be adjusted and determined according to the actual situation. No specific restrictions are imposed here.

[0036] The circuit formed by the air compressor 102 → anode heat exchanger 103 → SOEC stack 101 anode can be called an anode circuit, for example. The anode circuit can be filled with air, which can be pumped into the anode circuit by the air compressor 102. The air can refer to air with the same composition as the outside air, or it can refer to air with a different composition than the outside air, such as air with a lower oxygen volume fraction than the outside air. No specific limitation is made here.

[0037] The circuit including the cathode heat exchanger 104, mixer 105, and SOEC stack 101 cathode can be referred to as the cathode circuit. When the hydrogen production unit produces hydrogen, the cathode circuit can be filled with a mixture of water vapor and hydrogen. Of course, when the hydrogen production unit is shut down, the cathode circuit can also be filled with a mixture of nitrogen and hydrogen, etc., but it is not limited to this. The volume fraction ratio of water vapor and hydrogen, and the volume fraction ratio of nitrogen and hydrogen in the nitrogen-hydrogen mixture can be adjusted and determined according to the actual situation, and are not limited here.

[0038] In addition, various interfaces and pipelines inside the aforementioned hydrogen production device can be equipped with sensors such as temperature sensors, flow sensors, and pressure sensors to monitor the temperature and flow rate of the medium inside these interfaces and pipelines. For example, gas temperature sensors, gas flow sensors, and gas pressure sensors can be installed at the anode inlet of the aforementioned SOEC stack 101, the cathode inlet of the aforementioned SOEC stack 101, the inlet of the cathode heat exchanger 104, and the inlet of the anode heat exchanger 103. However, the specific types, numbers, and locations of the sensors are not limited to the examples mentioned above. It is understood that these sensors can communicate with the aforementioned controller via wired or wireless communication connections, and the specific communication connection method is not limited here.

[0039] The controller is communicatively connected to the air compressor 102, the SOEC stack 101, the hydrogen circulator 107, and the steam generator 114.

[0040] The controller described above is used to respond to a hydrogen production command to control the air compressor 102, the SOEC stack 101, the hydrogen circulator 107, and the steam generator 114 to operate according to preset boundary conditions. The controller controls the steam generator 114 to generate saturated steam at a preset pressure and a preset temperature, and controls the hydrogen circulator 107 to introduce hydrogen into the mixer 105 according to a preset first volume fraction. The preset boundary conditions include: anode-side oxygen volume condition, SOEC stack temperature gradient condition, SOEC stack inlet pressure condition, and bilateral pressure relationship.

[0041] For example, the controller mentioned above can be a device with computing and processing functions such as an embedded calculator, a microcontroller, or a server. However, the specific type of controller is not limited to the examples mentioned above. The hydrogen production command can be issued by relevant personnel through the input device of the controller, such as a button, mouse, or keyboard. However, the specific source and content of the hydrogen production command can be adjusted according to the different types and forms of controllers, and no specific restrictions are imposed here.

[0042] The aforementioned oxygen volume condition on the anode side may refer, for example, to a threshold condition used to limit the oxygen volume fraction in the air in the anode circuit, such as the oxygen volume fraction in the air in the anode circuit should be <33% to reduce the safety risks of material degradation and abnormal leakage.

[0043] The aforementioned SOEC stack temperature gradient condition may refer, for example, to a threshold condition for limiting the temperature gradient of the aforementioned SOEC stack 101. For example, the temperature gradient of the aforementioned SOEC stack 101 should be ≤50°C to suppress thermal stress and active layer degradation.

[0044] The aforementioned SOEC stack inlet pressure conditions may refer, for example, to threshold conditions used to limit the anode inlet and cathode inlet of the SOEC stack 101. For example, the pressure at both the anode inlet and cathode inlet of the SOEC stack 101 should be <0.04 bar, thereby controlling the airtightness risk and mechanical load within an appropriate range.

[0045] The aforementioned two-sided pressure relationship can refer to, for example, the conditions used to limit the relationship between the gas pressure in the anode circuit and the gas pressure in the cathode circuit. For example, the gas pressure in the anode circuit should be less than or equal to the gas pressure in the cathode circuit to prevent air from leaking from the anode circuit into the cathode circuit and causing safety hazards.

[0046] Of course, the above content is only one possible example of the anode-side oxygen volume condition, SOEC stack temperature gradient condition, SOEC stack inlet pressure condition, and bilateral pressure relationship. The actual preset boundary conditions may include other conditions, and the above-mentioned anode-side oxygen volume condition, SOEC stack temperature gradient condition, SOEC stack inlet pressure condition, and bilateral pressure relationship are not limited to the above examples. The preset boundary conditions of the above-mentioned anode-side oxygen volume condition, SOEC stack temperature gradient condition, SOEC stack inlet pressure condition, and bilateral pressure relationship are set with the aim of ensuring the safe and stable operation of the hydrogen production unit and reducing the lifespan loss of various parts of the hydrogen production unit. Specific details are not limited here.

[0047] In the hydrogen production device provided in this application embodiment, a concentrating solar thermal system, thermally coupled between an internal concentrating tower and two molten salt storage tanks, supplies heat to the SOEC loop. Simultaneously, the SOEC loop, through a dual-loop system with cathode and anode capable of deep waste heat recovery, completely decouples short-term fluctuations in solar irradiance from steam generation, ensuring stable temperature and flow rates for the steam entering the SOEC loop. Furthermore, the SOEC loop retains the freedom to superheat and fine-tune through methods such as tail gas heat exchange, thereby reducing the control difficulty in the hydrogen production process of the solid oxide electrolyzer and improving equipment stability.

[0048] Optionally, the heat transfer medium filled in the circulation loop formed by the concentrating tower 109 and the primary heat exchanger 110 connected in series, and the circulation loop formed by the secondary heat exchanger 113 and the heat exchange end of the steam generator 114, is heat transfer oil. The heat transfer medium filled in the circulation loop formed by the hot storage tank 111 and the cold storage tank 112 connected in series is molten salt.

[0049] In addition, the aforementioned hydrogen production device also includes: an anode heater 115, a cathode heater 116, a hydrogen heater 117, and a thermal oil heater 118. The anode heater 115, the cathode heater 116, the hydrogen heater 117, and the thermal oil heater 118 are all communicatively connected to the aforementioned controller.

[0050] The anode heater 115 is disposed between the outlet of the anode heat exchanger 103 and the anode inlet of the SOEC stack 101; the cathode heater 116 is disposed between the outlet of the mixer 105 and the cathode inlet of the SOEC; the hydrogen heater 117 is disposed between the outlet of the hydrogen circulator 107 and the inlet of the mixer 105; and the thermal oil heater 118 is disposed between the oil outlet of the secondary heat exchanger 113 and the heat exchange end oil inlet of the steam generator 114.

[0051] For example, the anode heater 115 can be turned on under the control of the controller when the air temperature flowing out of the outlet of the anode heat exchanger 103 does not reach the corresponding temperature threshold, thereby consuming electrical energy to supplement the heat of the air flowing out of the outlet of the anode heat exchanger 103.

[0052] Similarly, the cathode heater 116 can be used, for example, to turn on under the control of the controller when the temperature of the gas mixture of water vapor and hydrogen flowing out of the outlet of the mixer 105 does not reach the corresponding temperature threshold, thereby consuming electrical energy to reheat the gas mixture of water vapor and hydrogen flowing out of the outlet of the mixer 105.

[0053] The hydrogen heater 117 described above can be used, for example, to turn on under the control of a controller when the temperature of the hydrogen flowing out of the outlet of the hydrogen circulator 107 does not reach the corresponding temperature threshold, thereby consuming electrical energy to reheat the hydrogen flowing out of the outlet of the hydrogen circulator 107.

[0054] The aforementioned heat transfer oil heater 118 can, for example, be turned on under the control of a controller when the temperature of the heat transfer oil flowing out of the oil outlet of the aforementioned secondary heat exchanger 113 does not reach the corresponding temperature threshold, thereby consuming electrical energy to supplement the heat transfer oil flowing out of the oil outlet of the aforementioned secondary heat exchanger 113.

[0055] It should be noted that the temperature threshold corresponding to the air flowing out of the outlet of the anode heat exchanger 103, the temperature threshold corresponding to the gas mixture of water vapor and hydrogen flowing out of the outlet of the mixer 105, the temperature threshold corresponding to the hydrogen flowing out of the outlet of the hydrogen circulator 107, and the temperature threshold corresponding to the heat transfer oil flowing out of the outlet of the secondary heat exchanger 113 can be the same or different temperature thresholds. The specific temperature threshold values ​​are not specifically limited here and can be adjusted and determined according to the actual situation.

[0056] Optionally, the SOEC stack 101, the anode heater 115, the cathode heater 116, the hydrogen heater 117, the thermal oil heater 118, and the air compressor 102 are all powered by an external photovoltaic power supply circuit and a grid power supply circuit connected in parallel.

[0057] Such a power supply design can, for example, improve the independent controllability of the power supply device and the stable coupling within the hydrogen production device.

[0058] Optionally, the steam generator 114 described above can be, for example, an open-shell steam generator, but the specific type of steam generator 114 is not limited thereto.

[0059] in addition, Figure 2 This is a schematic flowchart of a hydrogen production method provided in one embodiment of this application. This hydrogen production method can, for example, be used in the controller of the hydrogen production apparatus in any of the above embodiments, such as... Figure 2 As shown, the hydrogen production method may include: S201, in response to the hydrogen production command, control the air compressor 102, SOEC stack 101, hydrogen circulator 107, and steam generator 114 to operate according to preset boundary conditions, and control the steam generator 114 to generate saturated steam at preset pressure and preset temperature.

[0060] S202. Control the hydrogen circulator 107 to introduce hydrogen into the mixer 105 according to a preset first volume fraction, wherein the preset boundary conditions include: anode side oxygen volume condition, SOEC stack temperature gradient condition, SOEC stack inlet pressure condition, and bilateral pressure relationship.

[0061] For example, the saturated steam with the preset pressure and preset temperature can refer to saturated steam at 3 bar and 133 degrees Celsius, but is not limited thereto. The hydrogen gas introduced into the mixer 105 according to the preset first volume fraction can refer to the hydrogen gas introduced into the mixer 105 according to the preset first volume fraction, for example, to the hydrogen gas introduced into the mixer 105 according to the preset first volume fraction, thereby forming a mixed gas with a water vapor volume fraction of 90% and a hydrogen gas volume fraction of 10%. Of course, the preset first volume fraction is not limited to 10%, and even if the preset first volume fraction is 10%, the mixed gas formed in the mixer 105 is not limited to a mixed gas with a water vapor volume fraction of 90% and a hydrogen gas volume fraction of 10%, but may also include a mixed gas with other components. The specific components are not limited here.

[0062] Figure 3 Please refer to the schematic flowchart of another embodiment of the hydrogen production method provided in this application. Figure 3 Furthermore, in the above Figure 2 Based on the embodiments, the above method may further include: S301. Collect the gas temperature at the outlet of the anode heat exchanger 103. If the gas temperature does not reach the target gas temperature at the anode inlet of the SOEC stack 101, control the anode heater 115 to start supplementary heating.

[0063] S302. Collect the hydrogen temperature at the outlet of the hydrogen circulator 107. If the hydrogen temperature does not reach the target hydrogen temperature at the inlet of the mixer 105, control the hydrogen heater 117 to start supplementary heating.

[0064] S303. Collect the water vapor temperature at the outlet of the mixer 105. If the water vapor temperature does not reach the target water vapor temperature at the cathode inlet of the SOEC stack 101, control the cathode heater 116 to start supplementary heating.

[0065] S304. Collect the temperature of the heat transfer oil at the outlet of the secondary heat exchanger 113. If the above-mentioned heat transfer oil temperature does not reach the target heat transfer oil temperature at the heat exchange end inlet of the steam generator 114, control the heat transfer oil heater 118 to start supplementary heating.

[0066] For example, the above-mentioned acquisition of the gas temperature at the outlet of the anode heat exchanger 103, the hydrogen temperature at the outlet of the hydrogen circulator 107, the water vapor temperature at the outlet of the mixer 105, and the heat transfer oil temperature at the outlet of the secondary heat exchanger 113 can be achieved by temperature sensors set at corresponding positions. The acquisition of the gas temperature at the outlet of the anode heat exchanger 103, the hydrogen temperature at the outlet of the hydrogen circulator 107, the water vapor temperature at the outlet of the mixer 105, and the heat transfer oil temperature at the outlet of the secondary heat exchanger 113 by temperature sensors can be, for example, continuous real-time acquisition, or acquisition according to a preset acquisition frequency, such as acquisition twice per second, but is not limited to this, and can be adjusted and determined according to actual needs.

[0067] It should be noted that in steps S301-S304 above, the gas temperature at the outlet of the anode heat exchanger 103, the hydrogen temperature at the outlet of the hydrogen circulator 107, the water vapor temperature at the outlet of the mixer 105, and the heat transfer oil temperature at the outlet of the secondary heat exchanger 113 can be collected simultaneously. The anode heater 115, cathode heater 116, hydrogen heater 117, and heat transfer oil heater 118 can also be started simultaneously. The step numbers S301-S304 are not used to restrict the order of the corresponding steps.

[0068] In addition, in the above Figure 2Based on the embodiments, the above-mentioned hydrogen production method may further include: calculating and obtaining the optimal set of operating parameters using a preset solution algorithm according to a preset optimization parameter algorithm, a preset optimization target, and the above-mentioned preset boundary conditions, wherein the above-mentioned preset optimization parameter algorithm includes: an electric hydrogen production efficiency algorithm, a solar hydrogen production efficiency algorithm, and a thermal storage-to-heat ratio algorithm. The operation of the hydrogen production unit is controlled based on multiple optimal operating parameters from the aforementioned set of optimal operating parameters.

[0069] For example, the aforementioned optimal operating parameters may refer to the load of each part of the hydrogen production unit, the anode scavenging gas volume of the anode circuit, the cathode scavenging gas volume of the cathode circuit, the threshold parameters corresponding to the preset boundary conditions, etc., but are not limited to these. The aforementioned multiple optimal operating parameters may be stored in a point set in the form of operating points, and the point set is the aforementioned optimal operating parameter set, but the form of the optimal operating parameters and the optimal operating parameter set is not limited to these.

[0070] The aforementioned solution algorithm can be, for example, a solver or an optimizer. The aforementioned calculation of the optimal set of operating parameters using the preset solution algorithm based on the preset optimization parameter algorithm, the preset optimization objective, and the aforementioned preset boundary conditions can, for example, refer to the solver or optimizer using the aforementioned preset optimization parameter algorithm to solve for multiple optimal operating parameters that satisfy the aforementioned preset optimization objective and preset boundary conditions, thereby forming the aforementioned optimal set of operating parameters.

[0071] The above-mentioned algorithm for the efficiency of hydrogen production by electricity can be expressed as, for example, the following formula:

[0072] Among them, the above For the efficiency of electro-hydrogen production, the above The above refers to the mass flow rate of hydrogen (H2) in the hydrogen production unit. The lower calorific value of hydrogen can be directly obtained from a database. For the electrical power of the aforementioned SOEC stack 101, the aforementioned The input electrical power of the anode heater 115 is as described above. This refers to the input electrical power of the cathode heater 116.

[0073] The above-mentioned hydrogen mass flow rate For example, the molar flow rate of hydrogen in a hydrogen production device can be calculated. The molar flow rate of hydrogen can be calculated using the following formula:

[0074] Among them, the above The above refers to the molar flow rate of hydrogen in the hydrogen production unit. The current density can be directly acquired or read by the controller. The effective area of ​​a single cell in the aforementioned SOEC stack 101 can be obtained directly from the parameters of the hydrogen production device. The number of solar cells in SOEC stack 101 can also be obtained by directly querying the parameters of the hydrogen production unit. is Faraday's constant.

[0075] After obtaining the molar flow rate of hydrogen in the hydrogen production unit, the mass flow rate of hydrogen can be obtained by multiplying the molar flow rate of hydrogen by the molar mass of hydrogen. .

[0076] The above and For example, it can be calculated using the following formula:

[0077] Among them, the above That is, the above. or The above The equivalent thermal power of the heater (for the input electrical power of the anode heater 115) The equivalent thermal power of this heater is the same as the equivalent thermal power of the anode heater 115, and the input electrical power of the cathode heater 116 is... The equivalent thermal power of this heater is the same as the equivalent thermal power of the cathode heater 116. Similarly, the heating efficiency can be divided into the heating efficiency of the anode heater 115 and the heating efficiency of the cathode heater 116, both of which can be obtained through experimental measurement or by referring to tables.

[0078] Meanwhile, the above It is also determined by the corresponding heat exchanger performance, which can be calculated using, for example, the following formula:

[0079] Among them, the above This refers to the heat exchanger performance, including the performance of the anode heat exchanger 103 and the cathode heat exchanger 104. Regarding the performance of the anode heat exchanger 103, the above... The mass flow rate of the medium in the anode circuit is given. For the efficiency of cathode heat exchanger 104, the above... The mass flow rate of the medium in the cathode circuit is calculated in the same way as described above. The same applies, so I won't repeat it here. The above... and These are the corresponding hot and cold flow rates of the heat exchanger, respectively. and These are the specific heat capacities of the corresponding hot and cold streams of the heat exchanger, respectively. and The inlet temperatures of the corresponding hot and cold streams of the heat exchanger are not specified above. , , , All of these can be obtained through experimental measurement or by looking up tables.

[0080] Through the efficiency of anode heat exchanger 103 or cathode heat exchanger 104 The temperature of the medium output after heat exchange by the anode heat exchanger 103 or the cathode heat exchanger 104 can be determined. This allows us to ascertain the difference between the temperature of the medium output after heat exchange by the anode heat exchanger 103 or the cathode heat exchanger 104 and the corresponding temperature threshold, thereby determining the equivalent thermal power of the corresponding anode heater 115 or cathode heater 116. The value when and If it is known, then it can be determined. That is, the above and .

[0081] The electrical power of the aforementioned SOEC stack 101 For example, it can be calculated using the following formula:

[0082] Among them, the above The voltage of a single cell in SOEC stack 101 can be calculated using, for example, the following formula:

[0083] Among them, the above For the reversible potential of a single cell, the above Let T be the equivalent area resistance of a single cell at temperature T. and All of these can be obtained through experimental measurement or by looking up tables, and no specific restrictions are imposed here.

[0084] The above-mentioned solar hydrogen production efficiency algorithm can be expressed as, for example, the following formula:

[0085] Among them, the above For the efficiency of solar-powered hydrogen production, the above The efficiency of the above-mentioned concentrating heat collection circuit, The efficiency of the photovoltaic system (concentrating tower 109) in the concentrating solar thermal circuit can be obtained through experimental measurement or by looking up tables, etc. That is, the above The above The power of the steam generator 114 can be calculated, for example, using the following formula:

[0086] Among them, the above and These are the specific enthalpies of liquid water and gaseous water under pressure P, respectively, both of which can be obtained through experimental measurement or by referring to tables. The mass flow rate of water (H2O) is calculated in the same way as described above. The same applies, so I won't go into details here.

[0087] The above-mentioned calculation method for the heat storage-to-heat ratio can be expressed as, for example, the following formula:

[0088] Among them, the above The heat storage and supply ratio of the hydrogen production unit over one year, where 8760 refers to 8760 hours per year. The above refers to the power of the steam generator at 114 units per hour. The total heat power per hour of the hot storage tank 111 and the aforementioned cold storage tank 112 connected in series to form a circulating loop can be obtained through experimental measurement or by looking up a table.

[0089] Based on the above, the aforementioned preset optimization objective could be, for example, >80%, and, >10%, and, >50%, but not limited to this.

[0090] In addition to satisfying the above-mentioned preset optimization objectives and the above-mentioned preset boundary conditions, the voltage drop of the above-mentioned cathode circuit and anode circuit can also be calculated using the following formula:

[0091] Among them, the above That is, the voltage drop in the cathode circuit or the voltage drop in the anode circuit, as mentioned above. The above refers to the cathode circuit gas diffusion layer resistance coefficient corresponding to the voltage drop in the cathode circuit, or the anode circuit gas diffusion layer resistance coefficient corresponding to the voltage drop in the anode circuit. For the corresponding mass flow rate of the medium in the anode circuit or the mass flow rate of the medium in the cathode circuit, the above... For the corresponding standard gas density of the medium in the anode circuit or the standard gas density of the medium in the cathode circuit, the above... For the corresponding standard gas viscosity of the medium in the anolyte circuit or the standard gas viscosity of the medium in the cathode circuit, the above... This refers to the density of the gas in the corresponding anolyte circuit at temperature T or the density of the gas in the corresponding cathode circuit at temperature T. This refers to the viscosity of the gas medium in the corresponding anolyte circuit at temperature T or the viscosity of the gas medium in the corresponding cathode circuit at temperature T. , , , , All of these can be obtained through experimental measurement or by looking up tables; no specific restrictions are imposed here.

[0092] Through the above It can be deduced whether the pressure at the anode inlet and cathode inlet of the SOEC stack 101 after the pressure drop meets the inlet pressure condition of the SOEC stack 101, and whether the gas pressure in the anode circuit and the gas pressure in the cathode circuit meet the pressure relationship between the two sides. If there are preset boundary conditions that cannot be met, the current operating parameters cannot be the optimal operating parameters.

[0093] Optionally, in Figure 2 Based on the embodiments, the above method may further include: In response to the hot standby command, the power supply to the SOEC stack 101 is cut off, and the air compressor 102, the hydrogen circulator 107, and the steam generator 114 are controlled to operate according to preset boundary conditions. The steam generator 114 is controlled to generate saturated steam at a preset pressure and preset temperature, and the hydrogen circulator 107 is controlled to introduce hydrogen into the mixer 105 according to a first preset volume fraction.

[0094] Similar to the hydrogen production command mentioned above, the hot standby command can also be issued by relevant personnel through the input device of the controller, such as a button, mouse, or keyboard. However, the specific source and content of the hot standby command can be adjusted according to the type and form of the controller, and no specific restrictions are imposed here.

[0095] Compared to the hydrogen production command, the hot standby command cuts off the power supply to SOEC stack 101, stopping hydrogen production, but keeps the rest of the components running to ensure that hydrogen production can be quickly resumed. It is suitable for short-term shutdowns of less than 1 hour.

[0096] In addition, the above methods may also include: In response to the shutdown order, the power supply to the SOEC stack 101 is cut off, the steam generator 114 is stopped, the air compressor 102, the hydrogen circulator 107, and the steam generator 114 are controlled to operate according to preset boundary conditions, and the hydrogen circulator 107 is controlled to introduce nitrogen-hydrogen mixed gas into the mixer 105 according to the second preset volume fraction.

[0097] Similar to the hydrogen production command and hot standby command mentioned above, the shutdown command can also be issued by relevant personnel through the input device of the controller, such as a button, mouse, or keyboard. However, the specific source and content of the shutdown command can be adjusted according to the type and form of the controller, and no specific restrictions are imposed here.

[0098] Compared to the hydrogen production command, the shutdown command cuts off the power supply to the SOEC stack 101, stops the steam generation of the steam generator 114, and replaces the medium in the cathode circuit with a nitrogen-hydrogen mixture with a second preset volume fraction (for example, a nitrogen-hydrogen mixture with a nitrogen component of 80% and a hydrogen component of 20% at room temperature). However, it maintains the operation of the other components to eliminate the risks of water treatment and condensation during the shutdown process and reduce the heat storage burden. It also ensures a rapid restart of the hydrogen production unit when hydrogen production resumes. It is suitable for long-term shutdowns of 1 to 16 hours.

[0099] Of course, the specific content and scope of application of the above-mentioned standby and shutdown instructions are not limited to the examples above, and can be adjusted according to the actual situation.

[0100] Figure 4 This is a schematic diagram of the structure of an electronic device provided in an embodiment of this application. The electronic device can be a device with computing and processing functions, such as the aforementioned embedded calculator, microcontroller, or server. Figure 4 As shown, the device 400 includes: The processor 410, storage medium 420, and bus 430 are connected and communicate with each other via bus 430.

[0101] The storage medium 420 stores machine-readable instructions that can be executed by the processor 410. When the electronic device is running, the processor 410 executes the machine-readable instructions to perform the hydrogen production method.

[0102] It should be understood that, Figure 4 The structure shown is only a schematic diagram of an electronic device; the electronic device may also include components that are larger than those shown. Figure 4 The more or fewer components shown, or having the same Figure 4 The different configurations shown. Figure 4 The components shown can be implemented using hardware, software, or a combination thereof.

[0103] This application also provides a computer-readable storage medium storing a computer program that, when executed by a processor, implements the hydrogen production method described in the above method embodiments.

[0104] Computer-readable storage media can be electronic storage devices such as flash memory, EEPROM (Electrically Erasable Programmable Read-Only Memory), EPROM, hard disk, or ROM. Optionally, computer-readable storage media includes non-transitory computer-readable storage medium. The computer-readable storage medium has storage space for program code that performs any of the method steps described above. This program code can be read from or written to one or more computer program exhibits. The program code can be compressed, for example, in a suitable form.

[0105] In the several embodiments provided in this application, it should be understood that the disclosed apparatus and methods can also be implemented in other ways. The apparatus embodiments described above are merely illustrative. For example, the flowcharts and block diagrams in the accompanying drawings illustrate the architecture, functionality, and operation of possible implementations of apparatus, methods, and computer program exhibits according to various embodiments of this application. In this regard, each block in a flowchart or block diagram may represent a module, segment, or portion of code, which contains one or more executable instructions for implementing a specified logical function. It should also be noted that in some alternative implementations, the functions marked in the blocks may occur in a different order than those marked in the drawings. For example, two consecutive blocks may actually be executed substantially in parallel, and they may sometimes be executed in reverse order, depending on the functions involved. It should also be noted that each block in a block diagram and / or flowchart, and combinations of blocks in block diagrams and / or flowcharts, can be implemented using a dedicated hardware-based system that performs the specified function or action, or using a combination of dedicated hardware and computer instructions.

[0106] In addition, the functional modules in the various embodiments of this application can be integrated together to form an independent part, or each module can exist independently, or two or more modules can be integrated to form an independent part.

[0107] If the functionality is implemented as a software module and sold or used as an independent exhibit, it can be stored in a computer-readable storage medium. Based on this understanding, the technical solution of this application, in essence, or the part that contributes to the prior art, or a portion of the technical solution, can be embodied in the form of a software exhibit. This computer software exhibit is stored in a storage medium and includes several instructions to cause a computer device (which may be a personal computer, server, or network device, etc.) to execute all or part of the steps of the methods of the various embodiments of this application. The aforementioned storage medium includes various media capable of storing program code, such as USB flash drives, portable hard drives, read-only memory (ROM), random access memory (RAM), magnetic disks, or optical disks.

[0108] The above description is merely a preferred embodiment of this application and does not limit the patent scope of this application. Any equivalent structural transformations made based on the inventive concept of this application and the contents of the specification and drawings of this application, or direct / indirect applications in other related technical fields, are included within the patent protection scope of this application.

Claims

1. A hydrogen production apparatus, characterized in that, include: The solid oxide electrolytic cell (SOEC) circuit, the concentrating solar collector circuit, and the controller are provided. The SOEC circuit includes an air compressor (102), an anode heat exchanger (103), an SOEC stack (101), a cathode heat exchanger (104), a mixer (105), a separator (106), a hydrogen circulator (107), and a gas-water heat exchanger (108). The concentrating solar collector circuit includes a concentrating tower (109), a primary heat exchanger (110), a hot storage tank (111), a cold storage tank (112), a secondary heat exchanger (113), and a steam generator (114). The air inlet of the air compressor (102) is connected to the outside, and the air outlet of the air compressor (102) is connected to the air inlet of the anode heat exchanger (103). The air outlet of the anode heat exchanger (103) is connected to the anode air inlet of the SOEC stack (101) and the air inlet of the gas-water heat exchanger (108). The anode air outlet of the SOEC stack (101) is also connected to the air inlet of the anode heat exchanger (103). The outlet of the gas-water heat exchanger (108) is connected to the outside, and the inlet of the gas-water heat exchanger (108) is connected to an external deionized water source. The outlet of the gas-water heat exchanger (108) is connected to the steam generator (114), and the outlet of the steam generator (114) is connected to the inlet of the cathode heat exchanger (104). The outlet of the cathode heat exchanger (104) is connected to the inlet of the mixer (105) and the inlet of the separator (106), respectively. The outlet of the mixer (105) is connected to the cathode inlet of the SOEC, the outlet of the SOEC cathode is also connected to the inlet of the cathode heat exchanger (104), the outlet of the separator (106) is connected to an external water storage device, the outlet of the separator (106) is connected to an external gas collection device and the inlet of the hydrogen circulator (107), and the outlet of the hydrogen circulator (107) is connected to the inlet of the mixer (105). The concentrating tower (109) and the first-stage heat exchanger (110) are connected in series to form a loop, the hot storage tank (111) and the cold storage tank (112) are connected in series to form a loop, and the second-stage heat exchanger (113) and the heat exchange end of the steam generator (114) form a loop. The primary heat exchanger (110) is located between the outlet of the hot storage tank (111) and the inlet of the cold storage tank (112) to exchange the heat in the circulation loop formed by the concentrating tower (109) and the primary heat exchanger (110) in series with the circulation loop formed by the hot storage tank (111) and the cold storage tank (112) in series. The secondary heat exchanger (113) is located between the outlet of the cold storage tank (112) and the inlet of the hot storage tank (111), and is used to exchange the heat in the circulation loop formed by the hot storage tank (111) and the cold storage tank (112) in series to the circulation loop formed by the heat exchange end of the secondary heat exchanger (113) and the steam generator (114). The controller is communicatively connected to the air compressor (102), the SOEC stack (101), the hydrogen circulator (107), and the steam generator (114). The controller is used to respond to a hydrogen production command to control the air compressor (102), the SOEC stack (101), the hydrogen circulator (107), and the steam generator (114) to operate according to preset boundary conditions, control the steam generator (114) to generate saturated steam at a preset pressure and preset temperature, and control the hydrogen circulator (107) to introduce hydrogen into the mixer (105) according to a preset first volume fraction. The preset boundary conditions include: anode-side oxygen volume conditions, SOEC stack (101) temperature gradient conditions, SOEC stack (101) inlet pressure conditions, and bilateral pressure relationship.

2. The hydrogen production apparatus according to claim 1, characterized in that, The circulating loop formed by the concentrating tower (109) and the first-stage heat exchanger (110) in series, and the circulating loop formed by the heat exchange end of the second-stage heat exchanger (113) and the steam generator (114) are filled with heat transfer oil as the heat transfer medium. The heat-conducting medium filled in the circulation loop formed by the hot storage tank (111) and the cold storage tank (112) connected in series is molten salt.

3. The hydrogen production apparatus according to claim 1, characterized in that, The hydrogen production device further includes: an anode heater (115), a cathode heater (116), a hydrogen heater (117), and a thermal oil heater (118); the anode heater (115), the cathode heater (116), the hydrogen heater (117), and the thermal oil heater (118) are all communicatively connected to the controller; The anode heater (115) is located between the outlet of the anode heat exchanger (103) and the anode inlet of the SOEC stack (101). The cathode heater (116) is located between the outlet of the mixer (105) and the cathode inlet of the SOEC. The hydrogen heater (117) is located between the outlet of the hydrogen circulator (107) and the inlet of the mixer (105). The thermal oil heater (118) is located between the oil outlet of the secondary heat exchanger (113) and the heat exchange end oil inlet of the steam generator (114).

4. The hydrogen production apparatus according to claim 1, characterized in that, The SOEC stack (101), the anode heater (115), the cathode heater (116), the hydrogen heater (117), the thermal oil heater (118), and the air compressor (102) are all powered by an external photovoltaic power supply circuit and a grid power supply circuit in parallel.

5. The hydrogen production apparatus according to claim 1, characterized in that, The steam generator (114) is a shell-side open steam generator.

6. A hydrogen production method, applied to the controller of the hydrogen production apparatus according to any one of claims 1-5, characterized in that, The method includes: In response to a hydrogen production command, the air compressor, SOEC stack, hydrogen circulator, and steam generator are controlled to operate according to preset boundary conditions. The steam generator is controlled to generate saturated steam at a preset pressure and temperature, and the hydrogen circulator is controlled to introduce hydrogen into the mixer according to a preset first volume fraction. The preset boundary conditions include: anode-side oxygen volume condition, SOEC stack temperature gradient condition, SOEC stack inlet pressure condition, and bilateral pressure relationship.

7. The method according to claim 6, characterized in that, The method further includes: The gas temperature at the outlet of the anode heat exchanger is collected. If the gas temperature does not reach the target gas temperature at the anode inlet of the SOEC stack, the anode heater is controlled to start supplementary heating. The hydrogen temperature at the outlet of the hydrogen circulator is collected. If the hydrogen temperature does not reach the target hydrogen temperature at the inlet of the mixer, the hydrogen heater is controlled to start for supplemental heating. The water vapor temperature at the outlet of the mixer is collected. If the water vapor temperature does not reach the target water vapor temperature at the cathode inlet of the SOEC stack, the cathode heater is controlled to start for supplemental heating. The temperature of the heat transfer oil at the outlet of the secondary heat exchanger is collected. If the temperature of the heat transfer oil does not reach the target temperature of the heat transfer oil at the inlet of the heat exchange end of the steam generator, the heat transfer oil heater is controlled to start supplementary heating.

8. The method according to claim 6, characterized in that, The method further includes: Based on the preset optimization parameter algorithm, the preset optimization objective, and the preset boundary conditions, the optimal set of operating parameters is calculated using a preset solution algorithm. The preset optimization parameter algorithm includes: an electric hydrogen production efficiency algorithm, a solar hydrogen production efficiency algorithm, and a thermal storage-to-heat ratio algorithm. The hydrogen production unit is controlled to operate based on multiple optimal operating parameters from the set of optimal operating parameters.

9. The method according to claim 6, characterized in that, The method further includes: In response to the hot standby command, the power supply to the SOEC stack is cut off, and the air compressor, the hydrogen circulator, and the steam generator are controlled to operate according to preset boundary conditions. The steam generator is controlled to generate saturated steam at a preset pressure and preset temperature, and the hydrogen circulator is controlled to introduce hydrogen into the mixer according to a first preset volume fraction.

10. The method according to claim 6, characterized in that, The method further includes: In response to the shutdown order, the power supply to the SOEC stack is cut off, the steam generator is controlled to stop operating, the air compressor, the hydrogen circulator, and the steam generator are controlled to operate according to preset boundary conditions, and the hydrogen circulator is controlled to introduce nitrogen-hydrogen mixed gas into the mixer according to a second preset volume fraction.

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