An adaptive multi-energy coupling adaptive hierarchical collaborative SOEC hydrogen production system

Abstract

An adaptive multi-energy coupled adaptive hierarchical collaborative SOEC hydrogen production system is disclosed, relating to the fields of hydrogen production technology and integrated energy utilization. It includes a high-temperature heat source supply module, an electrolysis hydrogen production module, a multi-source power supply module, a temperature detection module, an actuator group, and a controller. The high-temperature heat source supply module provides a high-temperature heat medium, and the multi-source power supply module provides electrical energy, jointly maintaining the high-temperature electrolysis hydrogen production reaction in the electrolysis hydrogen production module. The controller has a pre-stored rated operating temperature and executes control logic based on temperature deviation segments: when the deviation is small, it performs basic adjustment in a first mode; when the deviation is large, it switches to a second mode, coordinating the heat medium flow regulation mechanism, power regulation mechanism, and raw material flow regulation valve according to preset weights until the temperature returns to the allowable fluctuation range. This invention achieves high-precision control of the SOEC operating temperature through multi-energy coupling and hierarchical collaborative control, making it suitable for large-scale low-carbon hydrogen production scenarios.

Description

Technical Field

[0001] This invention relates to the field of hydrogen production technology and integrated energy utilization, specifically to an adaptive multi-energy coupling adaptive hierarchical collaborative SOEC hydrogen production system. Background Technology

[0002] Solid oxide electrolyzers (SOECs) can efficiently electrolyze water vapor into hydrogen and oxygen at high temperatures, with significantly higher efficiency than alkaline electrolysis and proton exchange membrane electrolysis. This represents a crucial technological direction for large-scale low-carbon hydrogen production. The key bottleneck restricting the large-scale industrial application of SOEC hydrogen production lies in the fact that SOECs require a continuous and stable high-temperature heat source and power supply to maintain their operating temperature. The inherent intermittency and volatility of renewable energy sources such as wind and solar power, along with the limitations of single-energy nuclear coupling methods and their sluggish response in thermal-electric regulation, make it difficult to meet the stringent temperature stability requirements of SOECs.

[0003] Current technologies attempt to couple nuclear energy with SOEC (Solar Electrolysis Electrolysis), utilizing the high-temperature waste heat generated by the nuclear reactor to provide a heat source for SOEC. However, such solutions only use nuclear energy as a single energy source, failing to fully utilize the complementary potential of renewable energy sources such as wind and solar power, and do not address the problem of large temperature fluctuations caused by the lag in the response of the nuclear thermal system. Other technologies couple nuclear power generation with renewable energy generation to power the electrolysis system, but only focus on the complementary allocation on the power side, without addressing the direct utilization of high-temperature waste heat from nuclear energy, nor providing a thermal management solution for SOEC, and even less addressing the coordinated control of multiple physical quantities. Regarding SOEC control, while existing technologies employ multi-parameter coordinated control methods, their control objects are limited to parameters such as solar panel tilt angle, water vapor flow rate, and air flow rate, without involving the coordinated linkage between nuclear thermal medium flow rate and electrolysis power and raw material flow rate. Furthermore, the control strategy is conventional feedback regulation, lacking an adaptive coordinated control mechanism based on temperature deviation grading. In terms of thermal management, while existing technologies offer waste heat utilization solutions, the heat source is industrial waste heat rather than high-temperature waste heat from nuclear energy, and a system-level heat-electricity-material coordinated architecture under multi-energy complementarity conditions has not been formed.

[0004] In summary, existing SOEC hydrogen production systems suffer from the following technical problems: They rely on a single energy source or are merely simple additions to the power supply, failing to achieve deep coupling and synergistic utilization of nuclear high-temperature waste heat with wind and photovoltaic power at the heat-power-storage level; the combination of heat source response lag and power fluctuations results in a lack of a tiered, coordinated control strategy that integrates heat transfer fluid flow, electrolysis power, and feedstock flow, making it difficult to stably control the SOEC operating temperature within a precise range; and the system integration is low, with insufficient tiered waste heat recovery, undeveloped product added value, and a lack of safety protection and intelligent operation and maintenance, making it difficult to meet the comprehensive requirements of stability, economy, and safety for large-scale industrial hydrogen production. Summary of the Invention

[0005] The purpose of this invention is to provide an adaptive multi-energy coupled adaptive hierarchical cooperative SOEC hydrogen production system to address the shortcomings mentioned in the background art.

[0006] To achieve the above objectives, the present invention provides the following technical solution: an adaptive multi-energy coupling adaptive hierarchical collaborative SOEC hydrogen production system, comprising: a high-temperature heat source supply module for providing a high-temperature heat medium;

[0007] An electrolytic hydrogen production module is connected to the high-temperature heat source supply module, and uses the high-temperature heat medium and electrical energy to carry out a high-temperature electrolytic hydrogen production reaction;

[0008] A multi-source power supply module is electrically connected to the electrolysis hydrogen production module and is used to provide the electrolysis hydrogen production module with electrical energy.

[0009] A temperature detection module is located inside the electrolysis hydrogen production module and is used to obtain the actual operating temperature of the electrolysis hydrogen production module in real time.

[0010] The actuator assembly includes at least a heat medium flow regulating mechanism, a power regulating mechanism, and a raw material flow regulating valve; and,

[0011] The controller is electrically connected to both the temperature detection module and the actuator assembly. It has a pre-stored rated operating temperature and executes the following control logic:

[0012] When the absolute value of the deviation between the actual operating temperature and the rated operating temperature is less than a first preset threshold, the actuator group is subjected to basic adjustment in the first mode.

[0013] When the absolute value of the deviation is greater than or equal to the first preset threshold, the system switches to the second mode and controls the heat medium flow regulating mechanism, the power regulating mechanism, and the raw material flow regulating valve to work together according to preset weights until the actual working temperature returns to the allowable fluctuation range of the rated working temperature.

[0014] Preferably, the controller includes a model reference adaptive control module and an online parameter self-tuning module;

[0015] The model reference adaptive control module uses the thermodynamic model of the electrolytic hydrogen production module as a reference benchmark, and takes the rated operating temperature and the actual operating temperature as inputs. It generates a temperature tracking error by comparison, calculates the adaptive control law in real time based on the temperature tracking error, generates the preliminary adjustment amount of each actuator, and outputs it.

[0016] The online parameter self-tuning module takes the deviation and rate of change between the actual operating temperature and the rated operating temperature as input, performs fuzzy inference according to the preset fuzzy rule base, outputs the control parameter correction amount of the controller, superimposes the control parameter correction amount onto the control parameters of the adaptive control law, corrects the initial adjustment amount, and outputs it to each of the actuators.

[0017] Preferably, the high-temperature heat source supply module is a high-temperature gas-cooled reactor, and its coolant is helium, with a coolant outlet temperature of not less than 950°C.

[0018] The heat medium flow regulation mechanism is provided between the coolant outlet of the high-temperature gas-cooled reactor and the heat medium inlet of the electrolysis hydrogen production module.

[0019] The high-temperature gas-cooled reactor is also equipped with a waste heat buffer tank. The inlet of the waste heat buffer tank is connected to the coolant outlet of the high-temperature gas-cooled reactor, and the outlet of the waste heat buffer tank is connected to the inlet of the heat medium flow regulating mechanism. When the high-temperature gas-cooled reactor is unloaded, the helium in the waste heat buffer tank is transported to the electrolysis hydrogen production module through the heat medium flow regulating mechanism.

[0020] Preferably, the multi-source power supply module includes a wind power generation unit, a photovoltaic power generation unit, and an energy storage subunit;

[0021] The output terminals of the wind power generation unit and the photovoltaic generation unit are respectively electrically connected to the input terminal of the energy storage subunit;

[0022] The output terminal of the energy storage subunit is electrically connected to the power supply terminal of the electrolysis hydrogen production module via the power regulation mechanism;

[0023] The energy storage subunit is a flow battery pack, which includes independent power units and capacity units, and an electrolyte circulation pipeline is provided between the power units and the capacity units.

[0024] Preferably, the wind power generation unit is equipped with a wind power output prediction module and a blade folding protection mechanism, and the photovoltaic power generation unit is equipped with a photovoltaic output prediction module;

[0025] The output terminals of the wind power output prediction module and the photovoltaic power output prediction module are respectively connected to the input terminal of the controller, and the predicted power generation is sent to the controller.

[0026] The controller issues a storage and discharge command to the energy storage sub-unit or a trigger command to the blade folding protection mechanism based on the predicted power generation.

[0027] Preferably, the electrolytic hydrogen production module is a solid oxide electrolytic cell stack, comprising a nickel-based anode, a yttrium oxide-stabilized zirconium oxide electrolyte, and a lanthanum-strontium-cobalt-iron cathode stacked sequentially. The electrolytic cell stack has a modular disassembly and assembly structure, and each electrolytic cell can be replaced independently.

[0028] The heat medium inlet of the solid oxide electrolytic cell stack is connected to the high-temperature heat source supply module, the raw material inlet is connected to the raw material supply pipeline, and the power supply end is electrically connected to the output end of the power regulation mechanism.

[0029] Preferably, the first preset threshold is 4℃, and the allowable fluctuation range is ±0.5℃;

[0030] When the absolute value of the deviation is less than 4°C, the controller controls the heat medium flow regulating mechanism, the power regulating mechanism and the raw material flow regulating valve to operate synchronously with a preset fine adjustment range. The preset fine adjustment range is 1 / 3 to 1 / 2 of the corresponding adjustment range in the second mode.

[0031] When the absolute value of the deviation is greater than or equal to 4°C and the actual working temperature is lower than the rated working temperature, the controller simultaneously increases the output of the heat medium flow regulating mechanism to the first regulating range, increases the output of the power regulating mechanism to the second regulating range, and decreases the output of the raw material flow regulating valve to the third regulating range, wherein the first regulating range > the second regulating range > the third regulating range;

[0032] When the absolute value of the deviation is greater than or equal to 4°C and the actual working temperature is higher than the rated working temperature, the controller synchronously executes to reduce the output of the heat medium flow regulating mechanism to the fourth regulating range, reduce the output of the power regulating mechanism to the fifth regulating range, and increase the output of the raw material flow regulating valve to the sixth regulating range, and the fourth regulating range > the fifth regulating range > the sixth regulating range.

[0033] Preferably, it also includes a waste heat recovery module, which includes a first heat exchanger and a second heat exchanger;

[0034] The first heat exchanger is located on the return pipeline of the high-temperature heat source supply module. The raw material supply pipeline passes through the first heat exchanger and then enters the raw material inlet of the electrolysis hydrogen production module. The first heat exchanger uses the waste heat of the high-temperature heat medium to heat the raw material.

[0035] The second heat exchanger is located on the oxygen production pipeline of the electrolytic hydrogen production module. The hydrogen production outlet pipeline of the electrolytic hydrogen production module is connected to the subsequent purification device after passing through the second heat exchanger. The second heat exchanger uses the waste heat of the high-temperature oxygen produced by electrolysis to heat the hydrogen production mixture.

[0036] Preferably, it also includes a hydrogen purification module, which is located at the hydrogen production outlet of the electrolytic hydrogen production module and includes a first-stage purification unit and a second-stage purification unit.

[0037] The first-stage purification unit is a pressure swing adsorption unit, whose inlet is connected to the hydrogen production outlet of the electrolytic hydrogen production module, and whose outlet is connected to the inlet of the second-stage purification unit. The pressure swing adsorption unit is equipped with an online adsorbent regeneration pipeline.

[0038] The second-stage purification unit is a palladium membrane separator, the outlet of which is connected to the hydrogen storage and transportation unit.

[0039] Preferably, it also includes a product comprehensive utilization module, which includes a hydrogen storage and transportation subunit and an oxygen processing subunit;

[0040] The hydrogen storage and transportation subunit includes a hydrogen buffer tank, a compressor, and a high-pressure hydrogen storage tank group connected in sequence. The inlet of the hydrogen buffer tank is connected to the outlet of the hydrogen purification module, and the storage pressure of the high-pressure hydrogen storage tank group is 35 MPa.

[0041] The oxygen processing subunit is located at the oxygen production outlet of the electrolytic hydrogen production module, and includes a cooler, a dryer, a compressor and a high-pressure oxygen storage tank connected in sequence. The storage pressure of the high-pressure oxygen storage tank is 15 MPa.

[0042] Compared with the prior art, the beneficial effects of the present invention are:

[0043] This invention organically integrates the high-temperature waste heat of a high-temperature gas-cooled reactor with wind power, photovoltaic power generation, and flow battery energy storage to form a multi-energy coupled thermal-electrical-storage collaborative energy supply architecture. This reduces the system's dependence on a single energy source and improves the continuity and stability of energy supply. Based on this, the invention proposes a dual-mode control strategy based on temperature deviation segmentation. When the deviation is small, each actuator independently adjusts according to a preset fine-tuning range to avoid system oscillation. When the deviation is large, it automatically switches to a three-mechanism linkage and collaborative mode, executing corresponding collaborative actions in the appropriate direction depending on whether the temperature is too low or too high. This is combined with model reference adaptation and parameter self-tuning. The integrated control system enables real-time correction of control parameters according to changes in operating conditions, improving temperature control accuracy to ±0.5℃. In the coordinated operation mode, the heat medium flow regulation mechanism, power regulation mechanism, and raw material flow regulation valve work together with differentiated ranges of "main adjustment to determine direction, fast adjustment to save time, and fine adjustment to improve accuracy," achieving a balance between rapid response and high-precision steady state. In addition, the system reduces energy consumption in the raw material heating section through two-stage waste heat recovery, and improves hydrogen purity and pressurizes and stores by-product oxygen through two-stage purification of "pressure swing adsorption + palladium membrane," realizing the dual production of hydrogen and oxygen and the full development of product added value. Attached Figure Description

[0044] Figure 1 This is a schematic diagram of the system structure of the present invention; Figure 2 The figure shows the simulation curve of the temperature response of the SOEC stack under the hierarchical collaborative control of this invention. Detailed Implementation

[0045] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0046] Please see Figure 1 In this embodiment, to address the technical problems of existing SOEC hydrogen production systems, such as the single energy form and insufficient synergy between heat, electricity, and storage, a multi-energy coupled adaptive hierarchical collaborative SOEC hydrogen production system is constructed. The system as a whole includes a high-temperature heat source supply module, a feedstock heating section (whose function corresponds to the heat transfer path between the high-temperature heat source supply module and the electrolysis hydrogen production module, i.e., the process of transferring heat from the high-temperature heat medium to the feedstock), an electrolysis hydrogen production module, a multi-source power supply module (including a wind power generation unit, a photovoltaic power generation unit, and an energy storage sub-unit), a temperature detection module, an actuator group (including a heat medium flow regulation mechanism, a power regulation mechanism, and a feedstock flow regulation valve), and a controller; it also includes a waste heat recovery module (including a first heat exchanger and a second heat exchanger), a hydrogen purification module, a product comprehensive utilization module, a safety protection module, and an intelligent operation and maintenance management module. All modules are connected through pipelines, circuits, or control lines to form a complete closed-loop hydrogen production system integrating hydrogen production, purification, storage and transportation, waste heat utilization, and safety protection.

[0047] In this embodiment, to achieve deep coupling between high-temperature waste heat from nuclear energy and renewable energy power, a high-temperature gas-cooled reactor (HTGR) is selected as the high-temperature heat source supply module. Helium is used as the coolant, and the coolant outlet temperature is constant at 950°C. A physical isolation barrier and grounding lightning protection mechanism are installed between the nuclear heat exchange area and the electrical area of ​​the HTGR to prevent electrical faults from affecting the stable operation of the nuclear equipment. A heat medium flow regulation mechanism is installed between the coolant outlet of the HTGR and the heat medium inlet of the feedstock heating section. This mechanism is used to regulate the flow rate of helium entering the feedstock heating section. The HTGR is also equipped with a waste heat buffer tank. The inlet of the waste heat buffer tank is connected to the coolant outlet of the HTGR, and the outlet of the waste heat buffer tank is connected to the inlet of the heat medium flow regulation mechanism. When the HTGR temporarily reduces its load, the high-temperature helium stored in the waste heat buffer tank can continue to be transported to the feedstock heating section through the heat medium flow regulation mechanism, thereby maintaining the temperature of the SOEC electrolysis hydrogen production module from dropping sharply due to the reduction in nuclear heat source load. Here, "reduction in load" refers to the operating state of the HTGR temporarily reducing its output power due to peak shaving or maintenance needs.

[0048] In this embodiment, to achieve the preparation of 750℃ high-temperature water, the raw material heating section adopts a shell-and-tube heat exchanger structure and uses a counter-current heat exchange method. The inner tube is made of Hastelloy C276, and the outer tube is made of 310S stainless steel. The outer tube is wrapped with a composite insulation layer of nano-aerogel and aluminum silicate fiber, with a heat insulation efficiency of not less than 90%. High-temperature helium gas flows on the outside of the shell, and the water to be heated flows on the inside of the shell. The two flow in opposite directions to exchange heat. After the water is stably heated to 750℃, it is transported to the electrolytic hydrogen production module through the raw material supply pipeline. The heat exchanger is also equipped with an ultrasonic online descaling module. This module can descale the heat exchange tube wall without stopping the system. The descaling frequency can be set according to the water quality, for example, once every 24 hours. A raw material flow regulating valve is set at the inlet of the raw material heating section. This valve is used to precisely control the water flow entering the raw material heating section, and works with the subsequent controller to achieve fine adjustment of the water flow.

[0049] In this embodiment, to achieve stable supply and complementary dispatch of multi-source power, the multi-source power supply module includes a wind power generation unit, a photovoltaic power generation unit, and an energy storage sub-unit. The output terminals of the wind power generation unit and the photovoltaic power generation unit are electrically connected to the input terminal of the energy storage sub-unit via their respective power regulation modules. The electrical energy generated by wind and photovoltaic power is preferentially stored in the energy storage sub-unit. The energy storage sub-unit uses a flow battery pack, preferably a vanadium redox flow battery pack, which includes independent power units and capacity units. An electrolyte circulation pipeline is provided between the power units and capacity units. The power units determine the output power capability of the battery pack, while the capacity units determine the energy storage capacity through the amount and concentration of the electrolyte. This decoupled arrangement allows the energy storage capacity to be flexibly expanded according to demand. The battery pack is installed in the system's independent energy storage compartment, in an ambient temperature range of 10℃ to 40℃. Within this temperature range, the battery charge / discharge efficiency is maintained at 82% to 88%. When the ambient temperature exceeds 25℃±5℃, the system automatically activates an independent air-cooling and liquid-cooling combined temperature control device to stabilize the battery operating temperature between 15℃ and 35℃. The output of the energy storage sub-unit is electrically connected to the power supply of the electrolysis hydrogen production module via a power regulation mechanism. The power regulation mechanism is used to adjust the DC power output from the energy storage sub-unit to the operating voltage and current required by the electrolysis hydrogen production module. The system is also equipped with a backup small... The auxiliary power generation module automatically activates to supplement the power gap when wind and solar power output is insufficient and the energy storage subunit's power level falls below a preset threshold. When wind and solar power output is excessive, the power regulation module switches the excess power to auxiliary equipment in the system, such as water pumps, wind turbines, and nitrogen purging devices, replacing external grid power. The wind power generation unit is equipped with a wind power output prediction module and a blade folding protection mechanism, while the solar power generation unit is equipped with a solar power output prediction module. The wind power output prediction module predicts wind power output 24 hours in advance based on meteorological big data, with prediction accuracy not specified. If the power generation is below 85%, the photovoltaic power output prediction module predicts the photovoltaic power output 24 hours in advance based on meteorological and solar data, with a prediction accuracy of no less than 80%. The output terminals of the wind power output prediction module and the photovoltaic power output prediction module are respectively connected to the input terminal of the controller to send the predicted power generation to the controller. The controller issues storage and discharge commands to the energy storage sub-unit according to the predicted power generation, such as charging the energy storage sub-unit to full charge in advance when predicting a windless period or a cloudy and rainy period with weak sunlight; or issuing trigger commands to the blade folding protection mechanism, such as triggering the blade folding protection of the wind turbine when predicting extreme wind speeds such as typhoons.

[0050] In this embodiment, to achieve efficient electrolytic hydrogen production from high-temperature steam, a solid oxide electrolytic cell stack with a flat-plate structure is selected for the hydrogen production module. The electrolytic cell stack includes a nickel-based anode, a yttrium-stabilized zirconium oxide electrolyte, and a lanthanum-strontium-cobalt-iron cathode stacked sequentially. The yttrium-stabilized zirconium oxide electrolyte material has excellent oxygen ion conductivity, the nickel-based anode provides catalytic activity and electron conduction, and the lanthanum-strontium-cobalt-iron cathode exhibits mixed ion-electron conductivity. The electrolytic cell stack has a modular, disassembled structure, allowing for independent replacement of individual electrolytic cells. When a single electrolytic cell experiences performance degradation, it can be replaced without disassembling the entire stack. The heat transfer medium inlet of the hydrogen production module is connected to the high-temperature heat source supply module to receive 750°C high-temperature water from the raw material heating section. The raw material inlet is connected to the raw material supply pipeline to receive preheated raw material water. The power supply terminal is electrically connected to the output terminal of the power regulation mechanism to receive the DC power required for electrolysis. The internal operating temperature of the electrolytic hydrogen production module is 750℃, which is maintained by three sources of heat: the sensible heat of the 750℃ high-temperature water, the heat of reaction released during the electrochemical reaction, and the auxiliary heat fed back by the waste heat recovery module. Therefore, no additional electrical energy is required for heating. An electrochemical reaction occurs inside the electrolytic hydrogen production module, and the reaction equation is as follows: The product is a mixture of hydrogen and oxygen.

[0051] In this embodiment, to achieve high-precision real-time temperature monitoring and adaptive closed-loop control, the temperature detection module employs a temperature sensor with an armored, sealed, welded sleeve structure. These sensors are arranged at multiple locations within the single-cell inlet, middle, and outlet of the electrolytic hydrogen production module's stack. For example, three sensors are arranged at each of the inlet, middle, and outlet, for a total of nine monitoring points. This through-type installation method allows for direct measurement of the stack temperature without compromising the stack's airtightness. The temperature sensor has a detection accuracy of ±0.2℃ and is used to acquire the actual operating temperature of the electrolytic hydrogen production module in real time, transmitting the temperature signal to the controller. The controller is a programmable logic controller (PLC) with a pre-stored rated operating temperature of 750℃, and executes segmented, coordinated control logic based on temperature deviation.

[0052] In this embodiment, to address the issue of significant temperature fluctuations caused by the combined effects of nuclear thermal system response lag and renewable energy fluctuations, the controller is configured to switch between different control modes based on the magnitude of the absolute value of the temperature deviation. When the absolute value of the deviation between the actual operating temperature and the rated operating temperature is less than a first preset threshold, the controller performs basic adjustments to the actuator group in the first mode. When the absolute value of the deviation is greater than or equal to the first preset threshold, the controller switches to the second mode and coordinates the operation of the heat medium flow regulating mechanism, the power regulating mechanism, and the raw material flow regulating valve according to preset weights until the actual operating temperature returns to the allowable fluctuation range of the rated operating temperature. The essence of this segmented control logic is that each actuator independently fine-tunes during small deviations to avoid frequent system oscillations, while the three mechanisms work together during large deviations to quickly pull the temperature back to the allowable range.

[0053] Specifically, the first preset threshold is set to 4℃, and the allowable fluctuation range is set to ±0.5℃. When the absolute value of the deviation is less than 4℃, the controller controls the heat medium flow regulating mechanism, the power regulating mechanism, and the raw material flow regulating valve to operate synchronously with a preset fine adjustment range. This preset fine adjustment range is one-third to one-half of the corresponding adjustment range in the second mode. Here, "corresponding adjustment range" refers to the adjustment range when the same actuator performs the corresponding action in the second mode. For example, if the adjustment range of the heat medium flow regulating mechanism in the second mode is the first adjustment range, then its fine adjustment range in the first mode is one-third to one-half of the first adjustment range.

[0054] In this embodiment, the adjustment range is determined as follows: the controller calculates the adjustment range of each actuator according to a preset proportional relationship based on the specific value of the current temperature deviation. For example, under rated operating conditions, when the absolute value of the deviation is greater than or equal to 4°C, the adjustment range of the heat medium flow regulating mechanism in the second mode is 10% of the valve opening. When the absolute value of the deviation is less than 4°C, the preset fine-tuning range of the mechanism in the first mode is 3.3% to 5% of the valve opening, which is one-third to one-half of the adjustment range in the second mode. The preset fine-tuning ranges of the power regulating mechanism and the raw material flow regulating valve are determined according to one-third to one-half of their respective adjustment ranges in the second mode, so that the fine-tuning range in the first mode and the adjustment range in the second mode maintain a clear quantitative correspondence.

[0055] When the absolute value of the deviation is greater than or equal to 4℃ and the actual operating temperature is lower than the rated operating temperature, the controller synchronously increases the output of the heat medium flow regulating mechanism to the first regulating range, increases the output of the power regulating mechanism to the second regulating range, and decreases the output of the raw material flow regulating valve to the third regulating range. The first regulating range is greater than the second regulating range, and the second regulating range is greater than the third regulating range. The relationship between the regulating ranges here reflects the weight distribution of each regulating channel in the coordinated action—the heat medium flow regulating mechanism undertakes the largest regulating range and acts as the dominant channel; the power regulating mechanism undertakes the medium-amplitude rapid response; and the raw material flow regulating valve undertakes the smallest fine-tuning.

[0056] When the absolute value of the deviation is greater than or equal to 4℃ and the actual working temperature is higher than the rated working temperature, the controller synchronously executes to reduce the output of the heat medium flow regulating mechanism to the fourth regulating range, reduce the output of the power regulating mechanism to the fifth regulating range, and increase the output of the raw material flow regulating valve to the sixth regulating range, and the fourth regulating range is greater than the fifth regulating range, and the fifth regulating range is greater than the sixth regulating range.

[0057] It should be noted that in this embodiment, "output" has corresponding physical meanings in different actuators: the output of the heat medium flow regulating mechanism refers to its opening command or flow setpoint; the output of the power regulating mechanism refers to its voltage command or current command; and the output of the raw material flow regulating valve refers to its valve opening command. All of the above "outputs" are control signals sent by the controller to each actuator, and each actuator performs corresponding actions based on the received control signals.

[0058] In this embodiment, the controller further includes a model reference adaptive control module and an online parameter self-tuning module. The model reference adaptive control module uses the thermodynamic model of the electrolysis hydrogen production module as a reference, and the rated operating temperature and actual operating temperature as inputs, generating a temperature tracking error through comparison. This module establishes three independent model reference adaptive control channels for the three actuators, each channel using a rated operating temperature of 750℃ as the command signal and the actual operating temperature as the feedback. Each channel has a built-in first-order reference model, and the desired closed-loop system behavior is characterized by the following transfer function: ,in, The Laplace operator represents the frequency domain (i.e., the system's response speed characteristics to changes). The poles of the reference model (to ensure the stability of the reference model) Take a positive number such that the pole is Located in the left half of the complex plane). The gain is used as a reference model. The controlled object in each channel is described using the following first-order nominal model: ,

[0059] in This refers to the actual operating temperature. For the first Control input for each channel ( =1,2,3 correspond to the heat medium flow regulating mechanism, the power regulating mechanism, and the raw material flow regulating valve, respectively. For the extreme points of the controlled object, To control the gain, This addresses the uncertainties and external disturbances present in the system. Based on the aforementioned reference model and nominal model, the controller employs a direct model reference adaptive control structure, with the control laws for each channel as follows:

[0060] ,

[0061] in This refers to the actual operating temperature. This is the command signal for the rated operating temperature. and The first Each channel features online adjustable feedback and feedforward gain. The controller calculates the actual operating temperature. Compared with the reference model output The tracking error between them is:

[0062] Based on this tracking error, each channel uses the following adaptive law to update the feedback gain in real time. and feedforward gain :

[0063] , ;

[0064] in and For the first The adaptive learning rate for each channel is used to control the adaptive speed of the gain of each channel. The controller calculates the adaptive rate of each channel in real time according to the above adaptive law. and Substitute the current value into the control law. The initial adjustment values ​​for the three actuators are generated and output respectively.

[0065] The online parameter self-tuning module takes the deviation and rate of change between the actual operating temperature and the rated operating temperature as input, performs fuzzy inference based on a preset fuzzy rule base, and outputs the learning rate of the adaptive law in three channels respectively. and The correction amount is added to the current learning rate, and the initial adjustment amount is corrected before being output to each actuator.

[0066] The fuzzy rule base is constructed as follows: Temperature deviation *e* and deviation change rate *ec* are divided into seven fuzzy subsets: negative large, negative medium, negative small, zero, positive small, positive medium, and positive large. Each fuzzy subset corresponds to a membership function, which uses a triangular or trapezoidal function. Based on prior knowledge and operational experience of SOEC stack temperature control, a rule table containing 49 fuzzy rules is established. The rule format is "If *e* is Ai and *ec* is Bj, then the learning rate correction is Cij," where Ai and Bj are the fuzzy subsets of *e* and *ec*, respectively, and Cij is the corresponding output fuzzy subset. The inference result is defuzzified using the centroid method, and the specific learning rate correction value is output. It should be noted that in this embodiment, the three channels... and As a time-varying gain that changes with time, the rate of change of each gain in the above adaptive law is adjusted online according to temperature error and reference command, so that the control gain of the three channels automatically adapts to changes in operating conditions during system operation.

[0067] In this embodiment, to achieve cascaded energy recovery and utilization, the system also includes a waste heat recovery module; the waste heat recovery module includes a first heat exchanger and a second heat exchanger. The first heat exchanger is located on the return pipeline of the high-temperature heat source supply module, specifically on the helium outlet pipeline of the raw material heating section; the raw material supply pipeline passes through the first heat exchanger and then enters the raw material inlet of the electrolysis hydrogen production module; after the high-temperature helium completes the heating of the water in the raw material heating section, the temperature drops to about 300°C, and the helium at about 300°C enters the hot side of the first heat exchanger, while the raw material water (room temperature tap water) enters the cold side of the first heat exchanger. After heat exchange, the raw material water is preheated to about 200°C, and then sent to the raw material heating section for further heating to 750°C.

[0068] Thus, the first heat exchanger utilizes the waste heat from the high-temperature heat medium reflux to preheat the raw materials, reducing the heating load of the raw material heating section. The second heat exchanger is located on the oxygen production pipeline of the electrolytic hydrogen production module. The hydrogen production outlet pipeline of the electrolytic hydrogen production module passes through the second heat exchanger before connecting to the subsequent hydrogen purification module. The by-product oxygen produced by the electrolytic hydrogen production module has a temperature of 750°C. This high-temperature oxygen enters the hot side of the second heat exchanger, while the hydrogen-oxygen mixture output from the hydrogen production outlet of the electrolytic hydrogen production module enters the cold side of the second heat exchanger. The high-temperature oxygen preheats the hydrogen-oxygen mixture, preventing a sudden drop in the temperature of the hydrogen-oxygen mixture from causing water vapor condensation in the pipeline. At the same time, the sensible heat of the high-temperature oxygen is recovered to help maintain the system temperature environment.

[0069] In this embodiment, to achieve high-purity hydrogen purification, the system also includes a hydrogen purification module. The hydrogen purification module is located at the hydrogen production outlet of the electrolytic hydrogen production module and includes a first-stage purification unit and a second-stage purification unit. The first-stage purification unit is a pressure swing adsorption (PSA) unit, whose inlet is connected to the hydrogen production outlet of the electrolytic hydrogen production module, and whose outlet is connected to the inlet of the second-stage purification unit. The PSA unit utilizes the difference in the adsorption capacity of the adsorbent for hydrogen and impurity gases (oxygen, water vapor) under different pressures, adsorbing impurities under high pressure and desorbing and regenerating under low pressure, thereby increasing the hydrogen purity to 99.9%. The PSA unit is equipped with an online adsorbent regeneration pipeline, which automatically switches to desorption and regeneration when the adsorbent is saturated, achieving regeneration without downtime.

[0070] The second-stage purification unit is a palladium membrane separator. The palladium membrane has selective permeability to hydrogen. Hydrogen molecules dissociate into hydrogen atoms on the membrane surface and diffuse through the palladium membrane. They recombine into hydrogen molecules on the other side of the membrane, while other gas molecules cannot pass through. After treatment by this unit, the purity of hydrogen is further improved to no less than 99.999%. The outlet of the second-stage purification unit is connected to the hydrogen storage and transportation unit.

[0071] In this embodiment, in order to achieve the dual production of hydrogen and oxygen and the large-scale storage and transportation of the products, the system also includes a product comprehensive utilization module; the product comprehensive utilization module includes a hydrogen storage and transportation subunit and an oxygen processing subunit. The hydrogen storage and transportation subunit includes a hydrogen buffer tank, a compressor, and a high-pressure hydrogen storage tank group connected in sequence. The inlet of the hydrogen buffer tank is connected to the outlet of the hydrogen purification module. The hydrogen buffer tank is used to buffer the hydrogen pressure fluctuations from the purification module and maintain the output pressure between 0.8 and 1.0 MPa. The compressor pressurizes the hydrogen and sends it to the high-pressure hydrogen storage tank group, which is a carbon fiber wound tank with a storage pressure of 35 MPa. The hydrogen metering module is set on the outlet pipeline of the compressor to count the hydrogen production in real time and realize accurate calculation of energy consumption and hydrogen production. The oxygen treatment subunit is set at the oxygen production outlet of the electrolysis hydrogen production module and includes a cooler, a dryer, a compressor, and a high-pressure oxygen storage tank connected in sequence. The high-temperature oxygen produced by electrolysis is first cooled to room temperature by the cooler, then the moisture is removed by the dryer, and then the pressure is increased to 15 MPa by the compressor before being stored in the high-pressure oxygen storage tank.

[0072] In this embodiment, to ensure the system's safe operation in a high-temperature, high-pressure hydrogen-containing environment, the system also includes a safety protection module. This module includes a hydrogen leak monitoring subunit, an over-temperature and over-pressure protection subunit, and an emergency interlock subunit. The hydrogen leak monitoring subunit is equipped with hydrogen concentration sensors at key nodes in the electrolytic hydrogen production module, hydrogen purification module, and hydrogen delivery pipeline, with a detection accuracy not exceeding 100 ppm, and is equipped with a nitrogen purging mechanism and an explosion-proof ventilation device. The over-temperature and over-pressure protection subunit is equipped with over-temperature protection switches in the raw material heating section and electrolytic hydrogen production module, with an over-temperature protection threshold of 800℃. Pressure sensors and safety relief valves are installed in the fluid pipelines and purification device, with a working pressure of 1.2 MPa and a pressure relief threshold of 1.5 MPa. The emergency interlock subunit is electrically connected to the controller. When the hydrogen concentration is detected to exceed 4% of the lower explosive limit, the system will activate the emergency interlock subunit. When the temperature exceeds 800℃ or the pressure exceeds 1.5MPa, the controller immediately triggers the emergency interlock protection: cuts off the power supply to the electrolytic hydrogen production module, closes the valves of the relevant pipelines, starts the nitrogen purging mechanism to purge the leak area or pipeline exceeding the standard with nitrogen, starts the explosion-proof exhaust device to reduce the hydrogen concentration on site, and if it is an over-temperature fault, it simultaneously starts the emergency cooling pipeline to introduce low-temperature helium for rapid cooling. All fault signals are simultaneously issued with on-site audible and visual alarms and remote early warning signals. In order to meet the safety replacement requirements of residual hydrogen and oxygen under the high temperature condition of 750℃ inside the electrolytic hydrogen production module, the nitrogen purging is designed based on the piston flow gas replacement model.

[0073] The "piston flow gas displacement model" here refers to the assumption that nitrogen gas is orderly propelled along the fuel cell stack channel in a plug flow manner, gradually displacing the residual gas from the inlet to the outlet, thus avoiding the local accumulation caused by violent mixing of nitrogen and residual gas. The purging process is configured according to the hydrogen-oxygen explosion-proof engineering design criteria and high-temperature thermal-hydraulic characteristics. Nitrogen gas is introduced in a gradient manner—first at a lower flow rate to balance the internal pressure of the fuel cell stack, and then gradually increased to the target purging flow rate. Simulation analysis has verified that the concentration of residual hydrogen and oxygen gas inside the system can be sufficiently diluted to outside the explosion limit, while avoiding excessive thermal stress damage to the fuel cell stack structure caused by airflow impact or sudden temperature changes.

[0074] In this embodiment, to achieve intelligent operation and maintenance management, the system also includes an intelligent operation and maintenance management module. The intelligent operation and maintenance management module is wirelessly connected to the controller and includes a full-parameter online monitoring subunit, a cloud-based remote management subunit, and a fault self-diagnosis and early warning subunit. The full-parameter online monitoring subunit uses various types of sensors installed in each module to monitor multiple parameters online, such as temperature, pressure, flow rate, hydrogen concentration, current, voltage, battery state of charge, light intensity, and wind speed. The data is transmitted in real time to the controller's visual touchscreen terminal. The cloud-based remote management subunit uploads system operation data to a cloud server based on 5G or IoT technology, supporting remote monitoring via computers and mobile phones, with a data storage period of no less than one year. The fault self-diagnosis and early warning subunit has a built-in fault diagnosis algorithm that can automatically identify fault types and locations. For minor faults such as sensor drift or slight shading of photovoltaic modules, it automatically calibrates or issues early warnings. For serious faults such as equipment damage or hydrogen leakage, it issues multiple early warnings and provides fault handling suggestions.

[0075] In this embodiment, to adapt to different hydrogen demand and extreme operating conditions, the controller incorporates three load regulation modes: full load, half load, and low load. The controller automatically switches load modes based on actual hydrogen demand, controlling the coolant flow rate of the high-temperature gas-cooled reactor, the output power of the energy storage subunit, and adjusting the number of electrolyzers in the hydrogen electrolysis module during the switching process, achieving stepless adjustment of the hydrogen production load. The system also includes a low-temperature start-up preheating program and a gradient shutdown program. The low-temperature start-up preheating program controls the high-temperature gas-cooled reactor to operate at a low load during system startup, outputting a small amount of high-temperature helium to preheat the feedstock heating section and the hydrogen electrolysis module. When the temperature sensor detects that the internal temperature of the hydrogen electrolysis module has risen to 500°C, the coolant output flow rate of the high-temperature gas-cooled reactor is gradually increased. Simultaneously, wind and solar power are activated to charge the energy storage subunit, waiting for the internal temperature of the hydrogen electrolysis module to reach 500°C. When the temperature stabilizes at 750℃ and the state of charge of the energy storage subunit is not lower than 80%, the system enters normal operating condition. After the shutdown command is issued, the gradient shutdown procedure gradually reduces the coolant output flow rate of the high-temperature gas-cooled reactor and the output power of the energy storage subunit, and gradually reduces the number of electrolyzers put into the electrolysis hydrogen production module, so that the internal temperature of the electrolysis hydrogen production module gradually decreases. When the temperature drops to 200℃, all valves and power supplies of the high-temperature gas-cooled reactor, the feed heating section and the electrolysis hydrogen production module are shut down. At the same time, the nitrogen purging mechanism is started to perform a comprehensive nitrogen purging of the hydrogen delivery pipeline, oxygen delivery pipeline, electrolysis hydrogen production module and hydrogen purification module to remove residual hydrogen and oxygen gas in the pipelines and equipment. After the purging is completed, the system is completely shut down.

[0076] Please see Figure 2In this embodiment, to verify the temperature control performance of the above-mentioned hierarchical collaborative control method, a simulation verification environment was built based on the system thermodynamic model. The simulation conditions closely match the operating characteristics of this system, in which the wind power and photovoltaic output are smoothly stabilized by the vanadium redox flow battery energy storage unit, without power fluctuation disturbances. Only the thermal disturbance scenarios caused by the residual heat of the high-temperature gas-cooled reactor and the small heat transfer deviation of the heat exchanger are simulated, that is, to verify the effectiveness of the basic regulation strategy under the first mode (absolute deviation less than 4℃).

[0077] Figure 2 The vertical axis represents temperature in °C, and the horizontal axis represents time in seconds. The red dashed line in the graph represents the 750 °C rated operating temperature baseline, the green dashed line represents the ±0.5 °C steady-state allowable fluctuation range, and the blue solid line represents the actual operating temperature of the SOEC stack. The total simulation time is 35 seconds, with step thermal disturbances of +1 °C, -1.5 °C, +2 °C, -2.5 °C, +3 °C, and -3.5 °C applied sequentially. The amplitudes of these disturbances are all within 4 °C, corresponding to the operating range of the controller's first mode. Figure 2 As can be seen, under each step thermal disturbance, the actual temperature did not exceed the allowable fluctuation range of ±0.5℃, and the time for the temperature to recover to steady state after each disturbance was less than 3 seconds. Here, "recovery time" refers to the time elapsed from the moment the disturbance was applied until the actual temperature entered and remained within the allowable fluctuation range of ±0.5℃. The above simulation results verify the effectiveness of the first-mode basic regulation strategy based on temperature deviation segmentation in suppressing small thermal disturbances. When the temperature deviation exceeds 4℃, the controller will automatically switch to the second mode and initiate a triple-linked deep-level regulation of coolant flow rate, electrolysis power, and inlet water flow rate to ensure that the temperature can also quickly recover to the allowable fluctuation range under large thermal disturbances.

[0078] In this embodiment, the complete workflow of the system is as follows: Upon system startup, a low-temperature start-up preheating procedure is triggered. The high-temperature gas-cooled reactor operates at low load, outputting high-temperature helium to preheat the electrolysis hydrogen production module to 500°C, which is then gradually increased to 750°C. Simultaneously, wind and solar power are activated to charge the energy storage subunit. After the high-temperature gas-cooled reactor reaches full load operation, 950°C helium enters the feedstock heating section via a heat transfer medium flow regulation mechanism. Tap water, preheated to 200°C by the first heat exchanger, enters the feedstock heating section and is heated to 750°C via counter-current heat exchange before being fed into the electrolysis hydrogen production module. The energy storage subunit provides DC power to the electrolysis hydrogen production module via a power regulation mechanism. The electrolysis hydrogen production module operates at 750°C. An electrochemical reaction produces a hydrogen-oxygen mixture. A temperature sensor collects the internal temperature of the hydrogen electrolysis module in real time and transmits it to the controller. The controller maintains the temperature stably at 750℃±0.5℃ according to the aforementioned hierarchical collaborative control logic. The hydrogen-oxygen mixture is preheated by the second heat exchanger and then enters the hydrogen purification module. After two stages of purification—pressure swing adsorption and palladium membrane purification—hydrogen with a purity of not less than 99.999% is obtained. This hydrogen is then pressurized by a hydrogen buffer tank and a compressor and stored in a 35MPa high-pressure hydrogen storage tank group. The high-temperature oxygen produced as a byproduct of electrolysis is recovered from its waste heat by the second heat exchanger and then enters the oxygen treatment subunit. After cooling, drying, and compression, it is stored in a 15MPa high-pressure oxygen storage tank. Throughout the operation, the safety protection module continuously monitors the hydrogen concentration, temperature, and pressure, while the intelligent operation and maintenance management module records and uploads all operating parameters in real time. When a shutdown is required, a gradient shutdown procedure is triggered to gradually cool the temperature to 200℃ before shutting down all units. Nitrogen is then introduced for piston-flow purging before complete shutdown.

[0079] It will be apparent to those skilled in the art that the present invention is not limited to the details of the exemplary embodiments described above, and that the invention can be implemented in other specific forms without departing from its spirit or essential characteristics. Therefore, the embodiments should be considered in all respects as exemplary and non-limiting, and the scope of the invention is defined by the appended claims rather than the foregoing description. Thus, all variations falling within the meaning and scope of equivalents of the claims are intended to be included within the present invention. No reference numerals in the claims should be construed as limiting the scope of the claims.

Claims

1. An adaptive multi-energy coupled adaptive hierarchical cooperative SOEC hydrogen production system, characterized in that, include: High-temperature heat source supply module, used to provide high-temperature heat medium; An electrolytic hydrogen production module is connected to the high-temperature heat source supply module, and uses the high-temperature heat medium and electrical energy to carry out a high-temperature electrolytic hydrogen production reaction; A multi-source power supply module is electrically connected to the electrolysis hydrogen production module and is used to provide the electrolysis hydrogen production module with electrical energy. A temperature detection module is located inside the electrolysis hydrogen production module and is used to obtain the actual operating temperature of the electrolysis hydrogen production module in real time. The actuator assembly includes at least a heat medium flow regulating mechanism, a power regulating mechanism, and a raw material flow regulating valve; and, The controller is electrically connected to both the temperature detection module and the actuator assembly. It has a pre-stored rated operating temperature and executes the following control logic: When the absolute value of the deviation between the actual operating temperature and the rated operating temperature is less than a first preset threshold, the actuator group is subjected to basic adjustment in the first mode. When the absolute value of the deviation is greater than or equal to the first preset threshold, the system switches to the second mode and controls the heat medium flow regulating mechanism, the power regulating mechanism, and the raw material flow regulating valve to work together according to preset weights until the actual working temperature returns to the allowable fluctuation range of the rated working temperature.

2. The adaptive multi-energy coupling adaptive hierarchical cooperative SOEC hydrogen production system according to claim 1, characterized in that, The controller is equipped with a model reference adaptive control module and an online parameter self-tuning module; The model reference adaptive control module uses the thermodynamic model of the electrolytic hydrogen production module as a reference benchmark, and takes the rated operating temperature and the actual operating temperature as inputs. It generates a temperature tracking error by comparison, calculates the adaptive control law in real time based on the temperature tracking error, generates the preliminary adjustment amount of each actuator, and outputs it. The online parameter self-tuning module takes the deviation and rate of change between the actual operating temperature and the rated operating temperature as input, performs fuzzy inference according to the preset fuzzy rule base, outputs the control parameter correction amount of the controller, superimposes the control parameter correction amount onto the control parameters of the adaptive control law, corrects the initial adjustment amount, and outputs it to each of the actuators.

3. The adaptive multi-energy coupling adaptive hierarchical cooperative SOEC hydrogen production system according to claim 1, characterized in that, The high-temperature heat source supply module is a high-temperature gas-cooled reactor, and its coolant is helium, with a coolant outlet temperature of not less than 950°C. The heat medium flow regulation mechanism is provided between the coolant outlet of the high-temperature gas-cooled reactor and the heat medium inlet of the electrolysis hydrogen production module. The high-temperature gas-cooled reactor is also equipped with a waste heat buffer tank. The inlet of the waste heat buffer tank is connected to the coolant outlet of the high-temperature gas-cooled reactor, and the outlet of the waste heat buffer tank is connected to the inlet of the heat medium flow regulating mechanism. When the high-temperature gas-cooled reactor is unloaded, the helium in the waste heat buffer tank is transported to the electrolysis hydrogen production module through the heat medium flow regulating mechanism.

4. The adaptive multi-energy coupling adaptive hierarchical cooperative SOEC hydrogen production system according to claim 1, characterized in that, The multi-source power supply module includes a wind power generation unit, a photovoltaic power generation unit, and an energy storage sub-unit; The output terminals of the wind power generation unit and the photovoltaic generation unit are respectively electrically connected to the input terminal of the energy storage subunit; The output terminal of the energy storage subunit is electrically connected to the power supply terminal of the electrolysis hydrogen production module via the power regulation mechanism; The energy storage subunit is a flow battery pack, which includes independent power units and capacity units, and an electrolyte circulation pipeline is provided between the power units and the capacity units.

5. The adaptive multi-energy coupling adaptive hierarchical cooperative SOEC hydrogen production system according to claim 4, characterized in that, The wind power generation unit is equipped with a wind power output prediction module and a blade folding protection mechanism, and the photovoltaic power generation unit is equipped with a photovoltaic output prediction module. The output terminals of the wind power output prediction module and the photovoltaic power output prediction module are respectively connected to the input terminal of the controller, and the predicted power generation is sent to the controller. The controller issues a storage and discharge command to the energy storage sub-unit or a trigger command to the blade folding protection mechanism based on the predicted power generation.

6. The adaptive multi-energy coupling adaptive hierarchical cooperative SOEC hydrogen production system according to claim 1, characterized in that, The electrolytic hydrogen production module is a solid oxide electrolytic cell stack, comprising a nickel-based anode, a yttrium oxide-stabilized zirconium oxide electrolyte, and a lanthanum-strontium-cobalt-iron cathode stacked sequentially. The electrolytic cell stack has a modular disassembly and assembly structure, and each electrolytic cell can be replaced independently. The heat medium inlet of the solid oxide electrolytic cell stack is connected to the high-temperature heat source supply module, the raw material inlet is connected to the raw material supply pipeline, and the power supply end is electrically connected to the output end of the power regulation mechanism.

7. The adaptive multi-energy coupling adaptive hierarchical cooperative SOEC hydrogen production system according to claim 1, characterized in that, The first preset threshold is 4℃, and the allowable fluctuation range is ±0.5℃; When the absolute value of the deviation is less than 4°C, the controller controls the heat medium flow regulating mechanism, the power regulating mechanism and the raw material flow regulating valve to operate synchronously with a preset fine adjustment range. The preset fine adjustment range is 1 / 3 to 1 / 2 of the corresponding adjustment range in the second mode. When the absolute value of the deviation is greater than or equal to 4°C and the actual working temperature is lower than the rated working temperature, the controller simultaneously increases the output of the heat medium flow regulating mechanism to the first regulating range, increases the output of the power regulating mechanism to the second regulating range, and decreases the output of the raw material flow regulating valve to the third regulating range, wherein the first regulating range > the second regulating range > the third regulating range; When the absolute value of the deviation is greater than or equal to 4°C and the actual working temperature is higher than the rated working temperature, the controller synchronously executes to reduce the output of the heat medium flow regulating mechanism to the fourth regulating range, reduce the output of the power regulating mechanism to the fifth regulating range, and increase the output of the raw material flow regulating valve to the sixth regulating range, and the fourth regulating range > the fifth regulating range > the sixth regulating range.

8. The adaptive multi-energy coupling adaptive hierarchical cooperative SOEC hydrogen production system according to claim 1, characterized in that, It also includes a waste heat recovery module, which includes a first heat exchanger and a second heat exchanger; The first heat exchanger is located on the return pipeline of the high-temperature heat source supply module. The raw material supply pipeline passes through the first heat exchanger and then enters the raw material inlet of the electrolysis hydrogen production module. The first heat exchanger uses the waste heat of the high-temperature heat medium to heat the raw material. The second heat exchanger is located on the oxygen production pipeline of the electrolytic hydrogen production module. The hydrogen production outlet pipeline of the electrolytic hydrogen production module is connected to the subsequent purification device after passing through the second heat exchanger. The second heat exchanger uses the waste heat of the high-temperature oxygen produced by electrolysis to heat the hydrogen production mixture.

9. The adaptive multi-energy coupling adaptive hierarchical cooperative SOEC hydrogen production system according to claim 1, characterized in that, It also includes a hydrogen purification module, which is located at the hydrogen production outlet of the electrolytic hydrogen production module and includes a first-stage purification unit and a second-stage purification unit. The first-stage purification unit is a pressure swing adsorption unit, whose inlet is connected to the hydrogen production outlet of the electrolytic hydrogen production module, and whose outlet is connected to the inlet of the second-stage purification unit. The pressure swing adsorption unit is equipped with an online adsorbent regeneration pipeline. The second-stage purification unit is a palladium membrane separator, the outlet of which is connected to the hydrogen storage and transportation unit.

10. An adaptive multi-energy coupled adaptive hierarchical cooperative SOEC hydrogen production system according to claim 9, characterized in that, It also includes a product comprehensive utilization module, which includes a hydrogen storage and transportation subunit and an oxygen processing subunit. The hydrogen storage and transportation subunit includes a hydrogen buffer tank, a compressor, and a high-pressure hydrogen storage tank group connected in sequence. The inlet of the hydrogen buffer tank is connected to the outlet of the hydrogen purification module, and the storage pressure of the high-pressure hydrogen storage tank group is 35 MPa. The oxygen processing subunit is located at the oxygen production outlet of the electrolytic hydrogen production module, and includes a cooler, a dryer, a compressor and a high-pressure oxygen storage tank connected in sequence. The storage pressure of the high-pressure oxygen storage tank is 15 MPa.

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