A method and system for energy efficiency management of hydrogen cogeneration systems oriented towards a circular economy

Abstract

This invention relates to the field of hydrogen energy technology and discloses an energy efficiency management method and system for a hydrogen cogeneration system oriented towards a circular economy. The method includes: introducing a thermal energy carrier and a metal-based active material into a reaction environment at a preset ratio to undergo a self-heating catalytic hydrolysis reaction, generating a first hydrogen gas stream and releasing reaction heat; converting the collected reaction heat and residual heat from the thermal energy carrier into electrical energy; monitoring the real-time flow rate of the first hydrogen gas stream and determining the flow rate deviation; using the converted electrical energy to drive the electrolysis reaction, adjusting the execution power of the electrolysis reaction in real time according to the flow rate deviation to generate a second hydrogen gas stream; separating the catalytically active component from the solid byproducts produced by the hydrolysis reaction and re-introducing the catalytically active component into the hydrolysis reaction step. This invention achieves dynamic matching of hydrogen supply load and optimization of system energy efficiency by linking thermochemical and electrochemical hydrogen production processes, recovering reaction heat for power generation, and recycling catalytic components.

Description

Technical Field

[0001] This invention relates to the field of hydrogen energy technology, and in particular to an energy efficiency management method and system for hydrogen cogeneration systems oriented towards a circular economy. Background Technology

[0002] Hydrogen energy, as a widely available, clean, and carbon-free secondary energy source, plays a crucial role in the global energy structure transformation and the achievement of carbon neutrality goals. Currently, large-scale industrial hydrogen production mainly relies on two technological pathways: fossil fuel reforming and water electrolysis. However, the former involves significant carbon dioxide emissions during production, contradicting the requirements of green development; while the latter produces pure hydrogen, it is highly dependent on grid power, with production costs significantly affected by electricity price fluctuations, and its final carbon emission level also depends on the grid's power composition, making it difficult to achieve low-carbon or zero-carbon emissions throughout its entire lifecycle. Meanwhile, in many industrial settings such as thermal power plants, steel mills, and chemical plants, there are large amounts of low-grade waste heat resources with temperatures around 150 degrees Celsius, such as reaction waste heat generated during processes and heating exhaust. Due to its low energy density and grade, this heat energy is difficult to recover and utilize efficiently and economically using traditional technologies, and is usually directly discharged into the environment, causing enormous energy waste and thermal pollution. While existing technologies have attempted to produce hydrogen by reacting reactive metals such as aluminum-based alloys with liquid water, these methods often require continuous external heating to start and maintain the reaction, and fail to effectively recover and utilize the large amount of heat energy released during the reaction. More importantly, existing hydrogen production systems typically employ a single production process, resulting in slow system response to fluctuations in downstream hydrogen demand and difficulty in quickly adjusting the hydrogen production rate, leading to poor hydrogen supply stability. Furthermore, the solid byproducts generated by the reaction are not effectively utilized for resource recovery, reducing overall economic efficiency. This fragmented production model, where energy and materials fail to form a closed loop, severely restricts cost control and sustainable development in the hydrogen energy industry. Summary of the Invention

[0003] To address the shortcomings of existing technologies, this invention discloses an energy efficiency management method and system for hydrogen cogeneration systems oriented towards a circular economy. It aims to solve the technical problems of low energy utilization, poor hydrogen supply stability, and low economic efficiency caused by the failure of existing hydrogen production technologies to effectively integrate low-grade waste heat utilization, process waste heat recovery, multi-path hydrogen production linkage control, and material recycling.

[0004] The technical solution of the present invention is as follows: In a first aspect, this invention discloses an energy efficiency management method for a hydrogen cogeneration system oriented towards a circular economy, used for the coordinated regulation of thermochemical hydrogen production and electrochemical hydrogen production. The method includes: A thermal energy carrier with a preset enthalpy value and a metal-based active material are introduced into a reaction environment in a preset ratio. In the reaction environment, the thermal energy carrier and the metal-based active material undergo a self-heating catalytic hydrolysis reaction to generate a first hydrogen gas flow and release the heat of reaction. It collects the heat of reaction and the residual heat of the heat carrier, and converts the collected heat energy into electrical energy; Monitor the real-time flow rate of the first hydrogen gas stream and determine the flow rate deviation of the first hydrogen gas stream relative to the target hydrogen supply load; The converted electrical energy is used to drive the electrolysis reaction, and the execution power of the electrolysis reaction is adjusted in real time according to the flow deviation value to generate a second hydrogen flow to compensate for the hydrogen production gap. The catalytically active component is separated from the solid byproducts generated by the hydrolysis reaction and then reintroduced into the hydrolysis reaction step.

[0005] This technical solution constructs a closed-loop system integrating waste heat utilization, combined heat and power, dual-path hydrogen production, and material recycling. By using low-grade waste heat as start-up energy, generating electricity using the heat of the reaction itself, and using water electrolysis to produce hydrogen as a flexible control method, it achieves cascaded utilization of energy and stable and reliable hydrogen supply. At the same time, through the recycling of catalysts, it significantly improves the overall energy efficiency and economy of the system.

[0006] Furthermore, the step of introducing a heat carrier with a preset enthalpy value and a metal-based active material into the reaction environment in a preset ratio includes: Preheating treatment of metal-based active materials; According to a preset ratio, a heat carrier with a preset enthalpy value is used to atomize and spray the preheated metal-based active material, so that the metal-based active material is suspended in particulate form in the heat carrier and enters the reaction environment.

[0007] Furthermore, the steps of collecting the heat of reaction and the residual heat of the heat carrier, and converting the collected heat energy into electrical energy, include: The heat of reaction in the reaction environment and the residual heat of the heat carrier discharged after the reaction are collected by heat exchange components; The collected heat energy is transferred to the working fluid of the organic Rankine cycle system, and the phase change expansion of the working fluid drives the generator set to generate electricity.

[0008] Furthermore, the steps of monitoring the real-time flow rate of the first hydrogen gas stream and determining the flow rate deviation of the first hydrogen gas stream relative to the target hydrogen supply load include: Obtain the target flow rate value corresponding to the target hydrogen supply load; The target flow rate value is compared with the real-time flow rate of the first hydrogen gas stream to obtain the flow rate deviation value.

[0009] Furthermore, the step of using the converted electrical energy to drive the electrolysis reaction and adjusting the execution power of the electrolysis reaction in real time according to the flow deviation value to generate a second hydrogen gas flow to compensate for the hydrogen production shortfall includes: When the flow deviation value is positive, the power adjustment increment of the electrolysis reaction is determined according to the flow deviation value, and the input electrical energy of the electrolysis reaction is adjusted according to the power adjustment increment so that the flow rate of the second hydrogen gas is matched with the flow deviation value. When the deviation value is zero, or negative and its absolute value is not large enough to trigger the preset deviation threshold, the input of electrical energy to the electrolysis reaction is stopped. When the flow deviation value is negative and its absolute value is greater than the preset deviation threshold, it is determined that the first hydrogen gas flow is in an oversupply state, and the following steps are executed: Stop supplying electrical energy to the electrolysis reaction; The electrical energy is switched from electrolysis to storage in energy storage units; Based on the absolute value of the flow deviation, the flow rate or enthalpy of the heat carrier introduced into the reaction environment is simultaneously reduced, thereby suppressing the hydrogen production rate of the hydrolysis reaction by lowering the energy input level of the reaction environment.

[0010] Furthermore, the steps of separating the catalytically active component from the solid byproducts generated by the hydrolysis reaction and then re-introducing the catalytically active component into the hydrolysis reaction step include: Component analysis was performed on the solid byproducts to identify the catalytically active metal components. The catalytically active metal components are extracted through a separation process, and then introduced into the reaction environment together with fresh metal-based active materials.

[0011] Furthermore, the step of introducing the extracted catalytically active metal component and fresh metal-based active material into the reaction environment includes: Real-time acquisition of the hydrogen production rate per unit mass under the current reaction conditions for the hydrolysis reaction; The hydrogen production rate per unit mass is compared with a preset catalytic activity benchmark value to obtain the activity decay coefficient. The mixing ratio of the catalytic active metal component and the fresh metal-based active material is dynamically adjusted according to the activity decay coefficient. When the activity decay coefficient is lower than the preset threshold, the proportion of the fresh metal-based active material is increased, and the catalytic active metal component is subjected to physical grinding or chemical reduction treatment to restore its surface reaction activity.

[0012] Furthermore, the method also includes: Real-time monitoring of the feed rate of the thermal energy carrier, the hydrogen production rate of the hydrolysis reaction, the power conversion of electrical energy, and the load parameters of the electrolysis reaction; Closed-loop control logic is executed based on the monitored parameters to maintain energy and material balance in the reaction environment.

[0013] Furthermore, the method also includes: Hydrogen leakage and pressure monitoring were conducted on the reaction environment and hydrogen transport path. When a leakage or overpressure signal is detected, safety response actions including inerting protection, emergency pressure relief, and full-process explosion-proof shut-off are executed.

[0014] Secondly, this invention also discloses an energy efficiency management system for a hydrogen cogeneration system oriented towards a circular economy, used to execute any of the aforementioned methods, including: The hydrolysis reaction module is used to introduce a thermal energy carrier with a preset enthalpy value and a metal-based active material into the reaction environment in a preset ratio, and to allow the thermal energy carrier and the metal-based active material to undergo a self-heating catalytic hydrolysis reaction in the reaction environment to generate a first hydrogen gas flow and release the heat of reaction. The energy conversion module is used to collect the heat of reaction and the residual heat of the heat carrier, and convert the collected heat energy into electrical energy. The deviation monitoring module is used to monitor the real-time flow rate of the first hydrogen gas and determine the flow rate deviation value of the first hydrogen gas flow rate relative to the target hydrogen supply load. The linkage control module is used to drive the electrolysis reaction with the converted electrical energy and adjust the execution power of the electrolysis reaction in real time according to the flow deviation value to generate a second hydrogen flow to compensate for the hydrogen production gap. The catalytic recycling module is used to separate the catalytically active components from the solid byproducts generated by the hydrolysis reaction and to reintroduce the catalytically active components into the hydrolysis reaction step.

[0015] This technical solution provides a hardware platform for implementing the above methods, deconstructing complex methodological processes into clearly defined physical modules, and providing a clear system architecture for the engineering implementation of the technology.

[0016] In summary, this invention provides an energy efficiency management method and system for hydrogen cogeneration systems geared towards a circular economy. The method achieves synergistic improvements in technological, economic, and environmental benefits by integrating a dual closed loop of energy and materials. Specifically: First, the method constructs a self-circulating energy system of "low-grade waste heat driving primary hydrogen production—reaction waste heat power generation—green electricity driving hydrogen replenishment," achieving tiered and efficient energy utilization and significantly reducing dependence on external energy sources and overall system energy consumption. Second, the method couples the stability of thermochemical primary hydrogen production with the rapid response capability of electrochemical hydrogen replenishment. Through real-time monitoring and dynamic control, it achieves precise and stable supply to downstream hydrogen loads, significantly enhancing the system's operational flexibility. Finally, the method establishes a fully closed-loop material path of "raw materials—hydrogen production—byproduct recovery—catalyst regeneration," achieving the recycling and reuse of key catalytic components with near-zero loss and resource utilization of solid byproducts, simultaneously achieving cost reduction, efficiency improvement, and near-zero waste emissions. The system is a collection of functional modules used to implement this method. Attached Figure Description

[0017] Figure 1 This is a flowchart illustrating an energy efficiency management method for a hydrogen cogeneration system oriented towards a circular economy, provided by an embodiment of the present invention.

[0018] Figure 2 This is a schematic diagram of the structure of an energy efficiency management system for a hydrogen cogeneration system oriented towards a circular economy, provided as an embodiment of the present invention.

[0019] Labeling Explanation: 210, Hydrolysis Reaction Module; 220, Energy Conversion Module; 230, Deviation Monitoring Module; 240, Linkage Control Module; 250, Catalytic Cycle Module. Detailed Implementation

[0020] The technical solutions of this invention will now be clearly and completely described with reference to the accompanying drawings. Obviously, the described embodiments are merely some, not all, of the embodiments of this invention. The components of this invention described and shown in the accompanying drawings can generally be arranged and designed in various different configurations. Therefore, the following detailed description of the embodiments of the invention provided in the drawings is not intended to limit the scope of the claimed invention, but merely to illustrate selected embodiments of the invention. All other embodiments obtained by those skilled in the art based on the embodiments of this invention without inventive effort are within the scope of protection of this invention.

[0021] It should be noted that similar reference numerals 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. Furthermore, in the description of this invention, terms such as "first," "second," etc., are used only to distinguish descriptions and should not be construed as indicating or implying relative importance.

[0022] In many industrial production scenarios, especially in combined heat and power (CHP) plants or large chemical plants, there are large amounts of low-grade waste heat resources that are difficult to utilize efficiently. For example, the exhaust steam from thermal power plant turbines or the waste steam released from certain chemical reaction processes typically has a temperature of around 150 degrees Celsius and a low energy grade. If directly used for traditional Rankine cycle power generation, it would be inefficient and uneconomical. Therefore, most of it is directly discharged into the atmosphere or cooling water bodies, causing significant energy waste and environmental thermal pollution. At the same time, the demand for high-purity hydrogen is increasing in emerging fields such as hydrogen fuel cell vehicles, distributed hydrogen energy stations, and fine chemicals, and this demand often exhibits dynamic fluctuations. Traditional hydrogen production methods, such as water electrolysis that relies on the power grid, are not only costly, but their carbon footprint is also directly linked to the energy structure of the power grid, making it difficult to guarantee a low-carbon supply. On the other hand, hydrogen production from fossil fuel reforming is accompanied by unavoidable carbon emissions. Therefore, how to convert these waste low-grade heat energies into high-value clean hydrogen energy and flexibly adapt to fluctuating downstream hydrogen demand has become an urgent technical challenge.

[0023] Firstly, please see Figure 1 This invention provides an energy efficiency management method for a hydrogen cogeneration system oriented towards a circular economy, used for the coordinated regulation of thermochemical hydrogen production and electrochemical hydrogen production. The method includes: S1. A thermal energy carrier with a preset enthalpy value and a metal-based active material are introduced into the reaction environment in a preset ratio, and the thermal energy carrier and the metal-based active material undergo a self-heating catalytic hydrolysis reaction in the reaction environment to generate a first hydrogen gas flow and release the heat of reaction. S2, collects the heat of reaction and the residual heat of the heat carrier, and converts the collected heat energy into electrical energy; S3. Monitor the real-time flow rate of the first hydrogen gas flow and determine the flow rate deviation of the first hydrogen gas flow rate relative to the target hydrogen supply load; S4. The electrolysis reaction is driven by the converted electrical energy. The execution power of the electrolysis reaction is adjusted in real time according to the flow deviation value to generate a second hydrogen flow to compensate for the hydrogen production gap. S5. Separate the catalytically active component from the solid byproducts generated by the hydrolysis reaction and reintroduce the catalytically active component into the hydrolysis reaction step.

[0024] Specifically, a heat transfer medium is a fluid medium capable of carrying and transferring heat energy, its core function being to provide the initial energy for the hydrolysis reaction. This medium can participate in the chemical reaction itself or simply serve as a heat transfer medium. In a specific application scenario, such as utilizing waste heat from a thermal power plant, the heat transfer medium can be superheated steam at a temperature of approximately 150 to 250 degrees Celsius. This superheated steam not only carries a considerable enthalpy but is itself a reactant (water) required for the hydrolysis reaction, achieving a unity of heat and mass transfer. In other scenarios, the heat transfer medium can also be a high-temperature inert gas, such as nitrogen, or a molten salt with good thermal conductivity, such as the nitrate mixture used in solar thermal power generation. In the latter case, water needs to be added separately as a reactant to the reaction environment.

[0025] Metal-based active materials refer to one or more classes of reactive metals or their alloys that can undergo vigorous chemical reactions with water under specific conditions to produce hydrogen gas and corresponding metal oxides or hydroxides. To achieve efficient and controllable reactions, pure reactive metals (such as pure aluminum or pure magnesium) are typically not used because their surfaces readily form dense oxide films, hindering the continued reaction. Therefore, these metal-based active materials are usually specially formulated alloy powders. For example, a commonly used material is an aluminum-based alloy containing aluminum and small amounts of one or more catalytically active metals, such as gallium, indium, tin, and bismuth. These low-melting-point metals can disrupt the dense alumina passivation layer on the aluminum surface, forming localized galvanic cells, thereby significantly improving the activity of the aluminum-water reaction. This material is usually present in micron-sized powder form to increase its contact area with the heat carrier.

[0026] Self-heating catalytic hydrolysis refers to the exothermic reaction that occurs between the aforementioned metal-based active materials and water at a certain temperature. The "self-heating" characteristic of this reaction is that once the initial energy is provided by a heat carrier to trigger the reaction, the reaction itself releases a large amount of heat. This heat is sufficient to maintain the temperature of the reaction environment, or even further increase it, allowing the reaction to continue without continuous external heating. For example, the reaction of aluminum with water (2Al + 6H₂O -> 2Al(OH)₃ + 3H₂) is a strongly exothermic reaction. The "catalytic" effect in the reaction process is mainly achieved by components such as gallium and indium added to the alloy. As catalytically active components, they lower the activation energy of the reaction, allowing the reaction to proceed rapidly under relatively mild conditions.

[0027] In one specific embodiment, the execution flow of the method can be managed by an integrated central control system (e.g., based on a programmable logic controller (PLC) or a distributed control system (DCS).

[0028] First, upon system startup, the central control system controls the material conveying unit according to preset process parameters. For example, metal-based active materials (such as aluminum gallium indium tin alloy powder) are stored in a sealed silo and quantitatively conveyed by a precision-controlled screw feeder. Simultaneously, 180°C superheated steam from the exhaust steam pipeline of a thermal power plant serves as the heat energy carrier, and its flow rate is precisely controlled by a proportional-integral-derivative (PID) regulating valve connected to the central control system. The screw feeder's rotational speed and the valve's opening are set to maintain the mass ratio of alloy powder to steam at a preset optimal value, such as 1:10. After initial mixing in a mixing chamber, these two materials are injected together into a vertical or horizontal pressure reactor, which serves as the reaction environment.

[0029] Inside the reactor, high-temperature steam rapidly heats the alloy powder to the reaction temperature, and it participates in the hydrolysis reaction as a reactant. Once the reaction begins, it rapidly releases a large amount of heat, causing the temperature inside the reactor to rise quickly from an initial 180 degrees Celsius to over 250 degrees Celsius. The high-purity hydrogen gas generated by the reaction, i.e., the first hydrogen stream, is discharged from the outlet at the top of the reactor, while the solid byproducts generated (mainly aluminum hydroxide and unreacted catalytic components) are deposited at the bottom of the reactor and periodically discharged through a pneumatic discharge valve.

[0030] Next, the system performs energy recovery and conversion steps. The reactor's outer wall is designed with a heat exchange jacket, or heat exchange coils are arranged inside the reactor. A heat transfer medium, such as thermal oil, circulates between the heat exchange components and a separate power generation unit. As the thermal oil flows through the reactor, it absorbs a large amount of heat released by the hydrolysis reaction, raising its temperature. Simultaneously, the steam discharged after the reaction, still carrying some residual heat, passes through a tail gas heat exchanger after leaving the reactor, transferring its heat to the thermal oil circulation loop. In this way, the heat of reaction and the residual heat of the carrier are collected. The thermal oil, now containing high-temperature heat energy, is pumped to the power generation unit, which can be a small heat engine system, such as a Stirling engine-based system or a small steam turbine system, driving a generator to convert the heat energy into electrical energy.

[0031] Subsequently, the system enters the hydrogen production monitoring and control phase. A high-precision gas mass flow meter is installed on the main pipeline after the first hydrogen stream exits the reactor and before it enters the subsequent purification or storage unit. This flow meter measures the flow rate of the first hydrogen stream in real time and transmits the data to the central control system in the form of a 4-20 mA current signal or a digital communication signal. Simultaneously, the central control system receives a signal representing the current hydrogen demand from downstream hydrogen-consuming units (such as the pressure sensor of a hydrogen storage tank at a hydrogen refueling station or the production management system of a chemical plant). This signal is converted into a target hydrogen supply load, i.e., a target flow rate value. The logic program within the central control system compares the real-time flow rate value with the target flow rate value at fixed intervals (e.g., once per second) to calculate the flow rate deviation. For example, if the target flow rate is 50 standard cubic meters per hour, and the real-time flow rate is 45 standard cubic meters per hour, the flow rate deviation is +5 standard cubic meters, indicating a supply shortage; conversely, if the real-time flow rate is 52 standard cubic meters per hour, the deviation is -2 standard cubic meters, indicating a supply surplus.

[0032] Based on the calculated flow deviation, the system implements coordinated control. The electrical energy converted in the previous step is supplied to a water electrolysis hydrogen production unit, which can be a proton exchange membrane (PEM) electrolyzer, characterized by rapid start-up and a wide load adjustment range. When the flow deviation calculated by the central control system is positive, it means that the hydrogen production of the main reaction is insufficient. The system calculates the amount of hydrogen to be supplemented and the electrical power required to drive the electrolyzer to produce that much hydrogen based on the magnitude of the deviation using a preset mathematical model (e.g., a simple proportional relationship: 0.2 standard cubic meters of hydrogen produced per kilowatt-hour of electricity). Subsequently, the system precisely adjusts the electrical energy supplied to the electrolyzer through a power controller, ensuring that its hydrogen production rate exactly compensates for the hydrogen production shortfall. The hydrogen produced by the electrolyzer, i.e., the second hydrogen stream, is dehumidified and then merged with the first hydrogen stream in a mixer before entering the hydrogen storage tank, jointly meeting the downstream hydrogen demand.

[0033] Finally, the system performs a material recycling step. Solid byproducts discharged from the bottom of the reactor are transported to a separate recycling unit. In this unit, a physical method, such as centrifugation at a specific temperature, is used to separate the molten liquid catalyst alloy from the solid aluminum hydroxide, utilizing the density and melting point differences between the catalytically active component (such as gallium indium tin alloy) and aluminum hydroxide. The separated and purified catalytically active component is returned to the preparation stage of fresh metal-based active materials, mixed with new aluminum powder to produce new alloy powder, thus achieving closed-loop utilization of the high-value catalyst. The separated aluminum hydroxide, as a chemical raw material, can also be sold externally, achieving complete resource utilization.

[0034] Through the coordinated efforts of the above series of steps, the previously discarded low-grade thermal energy has been successfully used to produce clean hydrogen. Furthermore, by linking and regulating cogeneration and dual-path hydrogen production, a stable supply of hydrogen to dynamic loads has been achieved. At the same time, key catalytic materials have been recycled, forming an efficient, flexible, economical, and environmentally friendly energy and material cycle system.

[0035] In a more optimized embodiment, the step of introducing a heat carrier having a preset enthalpy value and a metal-based active material into the reaction environment in a preset ratio includes: Preheating treatment of metal-based active materials; According to a preset ratio, a heat carrier with a preset enthalpy value is used to atomize and spray the preheated metal-based active material, so that the metal-based active material is suspended in particulate form in the heat carrier and enters the reaction environment.

[0036] The reason for this improvement is that, in the basic implementation, the mixing of solid powder conveyed by a screw feeder with steam may not be uniform enough, limiting heat and mass transfer efficiency and potentially leading to a slightly slower reaction start-up or incomplete reaction. This implementation optimizes this process. Before the metal-based active material is fed into the reactor, it first passes through a preheater. This preheater can utilize low-grade waste heat generated by the power generation unit or part of the exhaust steam from the reactor to raise the temperature of the alloy powder from room temperature to, for example, around 100 degrees Celsius. This reduces the need for heat carrier absorption upon entering the reactor, allowing the reaction to be triggered more quickly. A more critical improvement lies in the feeding method. This implementation employs a specially designed coaxial atomizing nozzle. The alloy powder is conveyed to the nozzle outlet through a central channel, while high-speed superheated steam, acting as the heat carrier, is ejected through an annular channel surrounding the central channel. The high-speed steam exerts a strong shearing and entraining effect on the powder flowing out from the center at the nozzle outlet, instantly breaking it down into extremely fine particles, which are then uniformly enveloped in the steam flow, forming a gas-solid two-phase atomized state. When this atomized mixture is sprayed into the reactor, the specific surface area of ​​the metal particles increases significantly, resulting in extremely sufficient contact with water vapor. This leads to an order-of-magnitude increase in the chemical reaction rate, causing the reaction to occur violently almost instantly upon entering the reactor. Consequently, the reactor's hydrogen production efficiency and energy utilization per unit volume are greatly improved.

[0037] In another optimized implementation, the step of collecting the heat of reaction and the residual heat of the heat carrier, and converting the collected heat energy into electrical energy, includes: The heat of reaction in the reaction environment and the residual heat of the heat carrier discharged after the reaction are collected by heat exchange components; The collected heat energy is transferred to the working fluid of the organic Rankine cycle system, and the phase change expansion of the working fluid drives the generator set to generate electricity.

[0038] In the basic implementation, no specific optimal path is given for efficiently converting low-grade thermal energy into electrical energy. Considering that the heat source temperature in this system (e.g., 180 to 300 degrees Celsius) is inefficient for a traditional steam Rankine cycle, this implementation explicitly adopts Organic Rankine Cycle (ORC) technology. This is a more suitable solution. Specifically, the aforementioned heat exchange components (reactor jacket and exhaust gas heat exchanger) constitute the evaporator of the Organic Rankine Cycle system. The working fluid is no longer water, but a low-boiling-point organic compound, such as R245fa or pentane, is selected. After absorbing the heat of reaction and waste heat, this organic working fluid boils at a relatively low temperature and generates high-pressure steam. This high-pressure organic steam then enters a specially designed turbine (expander), driving the turbine to rotate at high speed and powering a coaxially connected generator to generate electricity. The low-pressure organic steam after performing work enters the condenser, where it is cooled and condensed into a liquid state through heat exchange with ambient air or cooling water. The liquid working fluid is then pressurized by a working fluid pump and sent back to the evaporator, completing a closed cycle. Due to the physical properties of organic working fluids, organic Rankine cycles have significantly higher thermoelectric conversion efficiency, simpler system structure, and better operational stability compared to traditional steam turbines in terms of recovering low-grade waste heat for power generation. This allows them to provide more abundant and reliable power for subsequent water electrolysis to produce hydrogen.

[0039] Furthermore, the steps of monitoring the real-time flow rate of the first hydrogen gas stream and determining the flow rate deviation of the first hydrogen gas stream relative to the target hydrogen supply load include: Obtain the target flow rate value corresponding to the target hydrogen supply load; The target flow rate value is compared with the real-time flow rate of the first hydrogen gas stream to obtain the flow rate deviation value.

[0040] This step involves the precise definition of the control logic input. There are several ways to acquire the target flow rate value. In a highly automated factory environment, this target value might be dynamically issued by the factory's Energy Management System (EMS) or Manufacturing Execution System (MES) based on the overall production plan, and transmitted to the central controller of the hydrogen production system via Industrial Ethernet or fieldbus (such as Profibus-DP). For example, a downstream fuel cell forklift charging station might report its hydrogen demand forecast for the next hour to the Energy Management System based on the number of vehicles waiting to be charged. The Energy Management System then converts this demand into a specific flow rate setpoint. In a simpler application, a target flow rate value can be manually entered by a field operator via a Human-Machine Interface (HMI) touchscreen. Regardless of the method, the central control system stores this acquired value in a specific data register as the setpoint (SP). Simultaneously, the real-time flow rate measured by the mass flow meter, as the process value (PV), is also read into another register. The controller's central processing unit performs a simple subtraction operation (deviation = setpoint - process value), and the result is stored in the deviation register and used as the direct input for all subsequent compensation control algorithms. This clear definition ensures that the decision-making basis of the control system is accurate and unambiguous.

[0041] In a more specific embodiment regarding material recycling, the steps of separating the catalytically active component from the solid byproducts generated by the hydrolysis reaction and re-introducing the catalytically active component into the hydrolysis reaction step include: Component analysis was performed on the solid byproducts to identify the catalytically active metal components. The catalytically active metal components are extracted through a separation process, and then introduced into the reaction environment together with fresh metal-based active materials.

[0042] This step refines the specific operations of catalyst recovery. The solid byproducts discharged from the reactor are first sent to an analytical unit. For rapid feedback, online analytical techniques can be employed. For example, an X-ray fluorescence (XRF) spectrometer probe is installed on the byproduct delivery pipeline. As the material flows past the probe, the XRF spectrometer can analyze the content of various elements in the material in real time and non-destructively, such as the mass percentage of aluminum, oxygen, gallium, indium, and tin. The analytical results are transmitted to the central control system, which can then determine the enrichment degree of catalytically active metals (gallium, indium, and tin) in the byproducts.

[0043] After obtaining the component information, the system initiates the corresponding separation process. One efficient separation process is vacuum distillation. Since the boiling points of catalytically active metals (such as gallium, indium, and tin) are much lower than the decomposition temperatures of the reaction products aluminum hydroxide or alumina, the solid byproducts can be heated to a specific temperature (e.g., 800-1000 degrees Celsius under vacuum). At this temperature, the catalytic metal will vaporize, while the alumina remains solid. Collecting and condensing these metal vapors yields a high-purity regenerated catalyst alloy. Another method is hydrometallurgical processing, which utilizes specific acidic or alkaline solutions (such as hydrochloric acid or sodium hydroxide solution) to selectively dissolve the catalytic metal under specific conditions, while alumina remains insoluble. After filtration, the catalytic metal is precipitated from the solution through electrolysis or chemical displacement. The extracted high-purity catalytically active metal components are used to calculate the required amount of fresh aluminum powder based on their recovery rate. This powder is then uniformly mixed in a mixing device and fed into the feeding system, thus achieving a precise and efficient closed-loop recovery process.

[0044] In the basic implementation, the system compensates for the hydrogen production shortfall through electrolysis. However, its control strategy for dealing with hydrogen overproduction and for more precisely matching supply and demand is relatively simple. When hydrogen demand drops sharply, simply stopping the electrolysis reaction may result in a large surplus of hydrogen produced by the main reaction, causing safety risks associated with hydrogen pressurization and wasting energy.

[0045] To address this, the present invention provides a more refined linkage control logic. The steps of using the converted electrical energy to drive the electrolysis reaction and adjusting the execution power of the electrolysis reaction in real time according to the flow deviation value to generate a second hydrogen gas flow to compensate for the hydrogen production shortfall include: When the flow deviation value is positive, the power adjustment increment of the electrolysis reaction is determined according to the flow deviation value, and the input electrical energy of the electrolysis reaction is adjusted according to the power adjustment increment so that the flow rate of the second hydrogen gas is matched with the flow deviation value. When the deviation value is zero, or negative and its absolute value is not large enough to trigger the preset deviation threshold, the input of electrical energy to the electrolysis reaction is stopped. Specifically, when the flow deviation value is negative and its absolute value is greater than a preset deviation threshold, it is determined that the first hydrogen gas flow is in an oversupply state, and the following steps are executed: Stop supplying electrical energy to the electrolysis reaction; The electrical energy is switched from electrolysis to storage in energy storage units; Based on the absolute value of the flow deviation, the flow rate or enthalpy of the heat carrier introduced into the reaction environment is simultaneously reduced, thereby suppressing the hydrogen production rate of the hydrolysis reaction by lowering the energy input level of the reaction environment.

[0046] This multi-level control strategy is implemented in the central control system (DCS or PLC) through specific logic blocks.

[0047] In a specific application scenario, assuming that the downstream hydrogen refueling station is already full, the demand for hydrogen drops sharply from 50 standard cubic meters per hour to 5 standard cubic meters per hour.

[0048] 1. Supply Shortage (Positive Deviation): During normal operation, if the target flow rate is 50 and the real-time flow rate is 48, the deviation is +2. The PID (Proportional-Integral-Derivative) controller in the central control system will calculate a power increment based on this deviation. For example, if the system's electrolysis efficiency is 0.2 cubic meters of hydrogen produced per kilowatt-hour, then to compensate for a 2-cubic-meter shortfall, an additional 10 kilowatts of power is needed. The controller will send a command to the electrolyzer's power module to increase power by 10 kilowatts, ensuring that the flow rate of the second hydrogen gas stream precisely matches the shortfall.

[0049] 2. Supply and demand balance or slight surplus (deviation value close to zero): When the real-time flow rate fluctuates within a small tolerance range of the target flow rate, for example, target 50, real-time 50.5, the deviation value is -0.5. The absolute value of this negative deviation is less than the preset deviation threshold (for example, the threshold is set to 2% of the target flow rate, i.e., 1 cubic meter). In this case, the system determines that supply and demand are basically balanced, and no intervention is required. The controller will send a zero-power command to the electrolytic cell power module to stop it from working, in order to save energy.

[0050] 3. Significant Oversupply (Large Negative Deviation): In the scenario described above where demand sharply decreases, the target flow becomes 5, while the real-time flow of the main response may still remain around 50, resulting in a huge negative deviation of -45. Its absolute value is far greater than the preset threshold. The central control system immediately determines that the system is in a state of severe oversupply and initiates a Level 3 response procedure: Stop electrolysis: Immediately send a command to the electrolytic cell power module to reduce power to zero.

[0051] Energy storage switching: The central control system controls a power switching cabinet via digital output signals. The contactor inside the cabinet actuates, disconnecting the circuit between the organic Rankine cycle generator set and the electrolyzer, while simultaneously closing the circuit between the generator set and an energy storage unit (such as a lithium-ion battery pack and its battery management system, BMS). In this way, the electricity originally intended for electrolysis is diverted to charge the battery, achieving energy recovery and storage for use during subsequent peak hydrogen demand periods.

[0052] Source suppression: This is the most crucial step. To fundamentally address the problem of excessive hydrogen production, the controller calculates the amount of hydrogen produced by the main reaction that needs to be reduced based on the absolute value of the negative deviation (45 cubic meters per hour) using a reverse process model. To achieve this, the controller sends a new, lower setpoint to the flow control valve responsible for delivering the heat carrier (such as superheated steam), for example, reducing the steam flow rate from 1000 kg / h to 100 kg / h. The energy and reactant (water) input levels entering the reactor are significantly reduced, thereby directly suppressing the rate of the hydrolysis reaction and controlling the production of the first hydrogen stream at its source, gradually bringing it closer to the new target demand.

[0053] Through this complete control logic covering "gap filling," "wait and see," and "peak shaving and valley filling," the system can not only respond quickly to increased demand, but also intelligently cope with decreased demand. By combining energy storage and source control, it greatly improves the system's flexibility, security, and overall energy economy.

[0054] Furthermore, while the basic material recycling scheme achieves catalyst recovery and reuse, it does not consider the potential activity degradation of the catalyst after multiple cycles. Indiscriminately mixing deactivated catalyst with fresh materials will cause the hydrogen production efficiency of the main reaction to gradually decrease over time, affecting the system's stability and economics.

[0055] To address this, the present invention further proposes a dynamic management strategy based on activity monitoring. The step of introducing the extracted catalytically active metal component and fresh metal-based active material into the reaction environment includes: Real-time acquisition of the hydrogen production rate per unit mass under the current reaction conditions for the hydrolysis reaction; The hydrogen production rate per unit mass is compared with a preset catalytic activity benchmark value to obtain the activity decay coefficient. The mixing ratio of the catalytic active metal component and the fresh metal-based active material is dynamically adjusted according to the activity decay coefficient. When the activity decay coefficient is lower than the preset threshold, the proportion of the fresh metal-based active material is increased, and the catalytic active metal component is subjected to physical grinding or chemical reduction treatment to restore its surface reaction activity.

[0056] The specific implementation of this dynamic management strategy is as follows: 1. Real-time Activity Calculation: The central control system continuously collects two key data points: the hydrogen mass flow meter reading (real-time flow rate of the first hydrogen stream) and the real-time rotational speed of the metal-based active material screw feeder (converted to mass feed rate). The system's internal program performs a division operation to obtain the "hydrogen production rate per unit mass," with units of (standard cubic meters of hydrogen / kilogram alloy·hour).

[0057] 2. Determination of Attenuation Coefficient: The system stores a "catalytic activity baseline value," which is the standard hydrogen production rate measured under laboratory conditions using 100% new catalyst, for example, 1.5 (m). 3 / kg·h). The system compares the real-time calculated hydrogen production rate per unit mass with this benchmark value to calculate the "activity decay coefficient" = current rate / benchmark rate. This coefficient is a value between 0 and 1, which intuitively reflects the overall activity level of the currently used catalyst (including recovered components).

[0058] 3. Dynamic Proportion Adjustment: The system dynamically adjusts the mixing ratio of the recovered catalyst and fresh aluminum powder based on the activity decay coefficient, using a preset control curve or lookup table. For example: When the decay coefficient is >0.9, it indicates that the recovered catalyst has good activity and the system uses a high proportion of recovered material, such as recovered material: fresh material = 8:2.

[0059] When the attenuation coefficient is between 0.7 and 0.9, the system automatically adjusts the ratio, such as recycled material: fresh material = 6:4.

[0060] When the attenuation coefficient is lower than a preset threshold, such as 0.7, the system determines that the batch of recovered catalyst has been severely deactivated.

[0061] 4. Regeneration Trigger: Once the decay coefficient falls below 0.7, the system will not only adjust the mixing ratio to a more conservative value (e.g., recycled:fresh = 3:7) to ensure stable hydrogen production, but will also trigger a "regeneration" command. The low-activity catalyst separated from the byproducts in this batch will be diverted by a diversion valve to a dedicated regeneration unit, instead of directly entering the mixing silo. In this regeneration unit, one or more of the following processes can be performed: Physical grinding: The deactivated catalyst is fed into a high-energy ball mill for mechanical grinding for several hours. This process breaks up agglomerated particles, removes the passivation layer on the surface, and exposes the fresh, active surface inside.

[0062] Chemical reduction: The ground powder is fed into a tube furnace and, under an inert atmosphere, a reducing gas such as hydrogen is introduced and the process is carried out at a certain temperature to reduce any metal oxides that may be formed into elemental metals, thereby restoring their catalytic activity.

[0063] After regeneration, the activity of this batch of catalyst was restored, and it can be reused as a highly active recycled material. This meticulous management ensures that the main reaction always operates within its efficient range, maintaining the system's long-term stable hydrogen production capacity.

[0064] To ensure the stable operation of the entire complex coupled system, this invention also includes a higher-level monitoring and balancing logic: Real-time monitoring of the feed rate of the thermal energy carrier, the hydrogen production rate of the hydrolysis reaction, the power conversion of electrical energy, and the load parameters of the electrolysis reaction; Closed-loop control logic is executed based on the monitored parameters to maintain energy and material balance in the reaction environment.

[0065] Specifically, real-time monitoring and correlation analysis include, but are not limited to, the feed rate and enthalpy of the thermal energy carrier, the real-time hydrogen production rate and reaction temperature of the hydrolysis reaction, the power generation of the energy conversion module, and the real-time load and input power of the electrolysis hydrogen replenishment module. Based on the above correlation parameters, the overall energy flow balance and material balance of the system are evaluated in real time through a built-in system dynamic model, and the future short-term state evolution trend is predicted. When any key parameter disturbance is detected (such as changes in heat source temperature, fluctuations in power generation efficiency, or sudden changes in downstream demand), or when it is predicted that the system will deviate from the equilibrium state, the control strategy will initiate cross-module coordinated adjustment commands. Its decision-making logic is not to provide independent feedback to a single module, but to calculate and execute a set of optimal operations that can pull the entire system back to the equilibrium state. For example, it may be possible to fine-tune the input of the thermal energy carrier while compensating for changes in power generation through reverse linkage adjustment, so as to coordinate and stabilize the entire energy conversion chain and hydrogen production output.

[0066] This is equivalent to a system's "general manager." It doesn't just focus on a single aspect, but rather on the overall picture. For example, if the system detects that the power generation (electrical energy conversion power) of the organic Rankine cycle has slightly decreased due to rising ambient temperature, while the electrolysis reaction is operating at high load, this overall control logic will determine that without intervention, the hydrogen production of the electrolyzer will decrease, potentially leading to a hydrogen supply shortage. In response, it might take a proactive measure: slightly increasing the feed rate of the heat carrier to enhance the heat generation of the hydrolysis reaction, thereby increasing the power generation and ensuring a stable power supply to the electrolyzer, ultimately maintaining the energy and material balance of the entire system.

[0067] Finally, considering the flammable and explosive nature of hydrogen, system safety is of paramount importance in the design. This invention also includes a complete set of safety safeguards: Hydrogen leakage and pressure monitoring were conducted on the reaction environment and hydrogen transport path. When a leakage or overpressure signal is detected, safety response actions including inerting protection, emergency pressure relief, and full-process explosion-proof shut-off are executed.

[0068] This is a safety instrumented system (SIS) that is independent of conventional process control.

[0069] Monitoring: Explosion-proof hydrogen leak detectors are installed at the reactor flange connections, valve assemblies, hydrogen compressor, and storage tank area. Additionally, redundant pressure transmitters are installed on the reactor and high-pressure hydrogen storage pipelines.

[0070] Response: Once any detector detects that the hydrogen concentration exceeds a preset safety threshold (e.g., 25% LEL), or the pressure transmitter detects an abnormal increase in pressure, the safety instrumented system will immediately and independently execute the following interlocking actions without intervention from the central control system: Inerting protection: Instantly opens the solenoid valve connected to the high-pressure nitrogen cylinder group, rapidly charging a large amount of nitrogen into the reactor and related pipelines, diluting the hydrogen concentration and disrupting the conditions for combustion and explosion.

[0071] Emergency pressure relief: If an overpressure signal is detected, the system will trigger a rupture disc or quickly open a safety relief valve to guide the high-pressure gas in the system to a safe flare for combustion or high-altitude discharge.

[0072] Full-process explosion-proof shut-off: This is the highest level of safety action. The safety instrumented system will cut off the main power supply to the entire system (while maintaining power to the necessary explosion-proof equipment), close all material (steam, alloy powder) feed valves, and stop all rotating equipment (pumps, compressors), bringing the entire system into a completely static and isolated safe state.

[0073] This series of designs ensures that the system can be protected in a timely and effective manner under any foreseeable abnormal operating conditions, thus safeguarding the safety of personnel and equipment.

[0074] Secondly, see Figure 2 This invention also provides an energy efficiency management system for a hydrogen cogeneration system oriented towards a circular economy. This system functionalizes and materializes the various steps in the aforementioned methods, forming a collaborative and organic whole for executing any of the aforementioned methods, including: The hydrolysis reaction module 210 is used to introduce a thermal energy carrier with a preset enthalpy value and a metal-based active material into the reaction environment in a preset ratio, and to cause the thermal energy carrier and the metal-based active material to undergo a self-heating catalytic hydrolysis reaction in the reaction environment to generate a first hydrogen gas flow and release the heat of reaction. The energy conversion module 220 is used to collect the reaction heat and residual heat of the heat carrier, and convert the collected heat energy into electrical energy. Deviation monitoring module 230 is used to monitor the real-time flow rate of the first hydrogen gas flow and determine the flow deviation value of the first hydrogen gas flow rate relative to the target hydrogen supply load. The linkage control module 240 is used to drive the electrolysis reaction with the converted electrical energy and adjust the execution power of the electrolysis reaction in real time according to the flow deviation value to generate a second hydrogen flow to compensate for the hydrogen production gap. The catalytic recycling module 250 is used to separate the catalytically active component from the solid byproducts generated by the hydrolysis reaction and to reintroduce the catalytically active component into the hydrolysis reaction step.

[0075] Each module in this system physically corresponds to a specific set of devices and control units.

[0076] The hydrolysis reaction module 210 is the core hydrogen production unit of the entire system. It mainly comprises one or more high-pressure reactors and a corresponding material conveying system. The material conveying system includes a sealed silo for storing the metal-based active material, a screw feeder or weighing hopper for precise metering, and pipes, valves, and flow control devices for introducing the heat carrier. This module can be further integrated with an atomizing injection system to achieve efficient mixing and rapid reaction of the reactants. The reactor itself is designed with interfaces for discharging hydrogen, unloading solid byproducts, and exchanging heat.

[0077] The energy conversion module 220 is crucial for achieving internal energy self-sufficiency within the system. The core component of this module is a heat-to-work converter. In a preferred embodiment, this is a complete Organic Rankine Cycle (ORC) power generation unit, including an evaporator (i.e., a heat exchange assembly coupled to the hydrolysis reaction module 210), a turboexpander, a generator, a condenser, and a working fluid pump. The module also includes all the piping and valves connecting these devices, as well as sensors for monitoring the state of the circulating working fluid (temperature, pressure). Its function is to efficiently convert the low-to-medium grade heat energy released by the hydrolysis reaction module 210 into usable electrical energy.

[0078] The deviation monitoring module 230 is part of the system's "eyes" and "brain," responsible for sensing the supply and demand status. Hardware-wise, this module includes a high-quality flow meter installed on the first hydrogen gas flow line and a communication interface for receiving downstream hydrogen demand signals. Software-wise, it is implemented as a functional block in the central control system, which continuously executes algorithms for data acquisition, comparison, and deviation calculation, providing a basis for subsequent control decisions.

[0079] The linkage control module 240 acts as the system's "hands" and "feet," responsible for executing specific regulatory actions. This module includes a water electrolysis hydrogen production unit (such as a PEM electrolyzer), a power controller capable of precisely adjusting output power, a power switching cabinet for energy flow switching, and an energy storage unit (such as a battery pack and its management system). Furthermore, this module is connected to the material conveying system of the water electrolysis reaction module 210 via control signals to achieve source control of the main reaction rate. All these devices receive instructions from the central control system and, based on the results of the deviation monitoring module 230, perform operations such as hydrogen production compensation, energy storage, or hydrogen production suppression.

[0080] The catalytic recycling module 250 embodies the circular economy characteristics of the system. This module is a stand-alone material handling unit that may include an online spectrometer for component analysis, physical or chemical processing units (such as vacuum distillation furnaces or leaching reactors) for separating catalysts from byproducts, and equipment for mixing recovered catalysts with fresh feedstocks. Its function is to achieve closed-loop utilization of high-value catalysts, reducing costs and waste.

[0081] These modules are not isolated but tightly integrated through pipes, cables, and a unified central control system (such as a DCS or PLC). The central control system, acting as the "nerve center" of the entire system, integrates the control logic, algorithm models, and safety interlocking procedures from all the aforementioned methods and steps, coordinating the collaborative work of each module to fully realize the efficient, flexible, and cyclical hydrogen cogeneration and energy efficiency management proposed in this invention. The above descriptions are merely embodiments of the present invention and are not intended to limit the scope of protection of the present invention. For those skilled in the art, the present invention can have various modifications and variations. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. An energy efficiency management method for a hydrogen cogeneration system oriented towards a circular economy, used for the coordinated regulation of thermochemical hydrogen production and electrochemical hydrogen production, characterized in that, The method includes: A thermal energy carrier with a preset enthalpy value and a metal-based active material are introduced into a reaction environment in a preset ratio. In the reaction environment, the thermal energy carrier and the metal-based active material undergo a self-heating catalytic hydrolysis reaction to generate a first hydrogen gas flow and release the heat of reaction. The heat of reaction and the residual heat of the heat carrier are collected, and the collected heat energy is converted into electrical energy. Monitor the real-time flow rate of the first hydrogen gas stream and determine the flow rate deviation of the first hydrogen gas stream relative to the target hydrogen supply load; The electrolysis reaction is driven by the converted electrical energy, and the execution power of the electrolysis reaction is adjusted in real time according to the flow deviation value to generate a second hydrogen flow to compensate for the hydrogen production gap. The catalytically active component is separated from the solid byproducts generated by the hydrolysis reaction and then reintroduced into the hydrolysis reaction step.

2. The energy efficiency management method for a hydrogen cogeneration system oriented towards a circular economy as described in claim 1, characterized in that, The step of introducing a heat energy carrier with a preset enthalpy value and a metal-based active material into the reaction environment in a preset ratio includes: The metal-based active material is preheated. According to the preset ratio, the preheated metal-based active material is atomized and sprayed using a thermal energy carrier with a preset enthalpy value, so that the metal-based active material is suspended in particulate form in the thermal energy carrier and enters the reaction environment.

3. The energy efficiency management method for a hydrogen cogeneration system oriented towards a circular economy according to claim 1, characterized in that, The step of collecting the reaction heat and the residual heat of the heat carrier, and converting the collected heat energy into electrical energy includes: The heat of reaction in the reaction environment and the residual heat of the heat carrier discharged after the reaction are collected using heat exchange components. The collected thermal energy is transferred to the circulating working fluid of the organic Rankine cycle system, and the phase change expansion of the circulating working fluid drives the generator set to generate electrical energy.

4. The energy efficiency management method for a hydrogen cogeneration system oriented towards a circular economy according to claim 1, characterized in that, The step of monitoring the real-time flow rate of the first hydrogen gas stream and determining the flow rate deviation of the first hydrogen gas stream relative to the target hydrogen supply load includes: Obtain the target flow rate value corresponding to the target hydrogen supply load; The target flow rate value is compared with the real-time flow rate of the first hydrogen gas stream to obtain the flow rate deviation value.

5. The energy efficiency management method for a hydrogen cogeneration system oriented towards a circular economy according to claim 4, characterized in that, The step of using the converted electrical energy to drive the electrolysis reaction, and adjusting the execution power of the electrolysis reaction in real time according to the flow deviation value to generate a second hydrogen flow to compensate for the hydrogen production shortfall includes: When the flow deviation value is positive, the power adjustment increment of the electrolysis reaction is determined according to the flow deviation value, and the input electrical energy of the electrolysis reaction is adjusted according to the power adjustment increment so that the flow rate of the second hydrogen gas is matched with the flow deviation value. When the deviation value is zero, or negative and its absolute value is not large enough to exceed a preset deviation threshold, the input of electrical energy to the electrolysis reaction is stopped. When the flow deviation value is negative and its absolute value is greater than a preset deviation threshold, it is determined that the first hydrogen gas flow is in an oversupply state, and the following steps are executed: Stop supplying electrical energy to the electrolysis reaction; The electrical energy is switched from the electrolysis reaction to the energy storage unit for storage; based on the absolute value of the flow deviation, the flow rate or enthalpy value of the heat carrier introduced into the reaction environment is simultaneously reduced, thereby suppressing the hydrogen production rate of the hydrolysis reaction by reducing the energy input level of the reaction environment.

6. The energy efficiency management method for a hydrogen cogeneration system oriented towards a circular economy according to claim 1, characterized in that, The step of separating the catalytically active component from the solid byproducts generated by the hydrolysis reaction and then re-introducing the catalytically active component into the hydrolysis reaction step includes: The solid byproducts were subjected to component analysis to identify the catalytically active metal components. The catalytically active metal component is extracted through a separation process, and the extracted catalytically active metal component is introduced into the reaction environment together with the fresh metal-based active material.

7. The energy efficiency management method for a hydrogen cogeneration system oriented towards a circular economy as described in claim 6, characterized in that, The step of introducing the extracted catalytically active metal component and the fresh metal-based active material into the reaction environment includes: The rate of hydrogen production per unit mass under the current reaction conditions is obtained in real time. The hydrogen production rate per unit mass is compared with a preset catalytic activity benchmark value to obtain the activity decay coefficient; The mixing ratio of the catalytically active metal component and the fresh metal-based active material is dynamically adjusted according to the activity decay coefficient. When the activity decay coefficient is lower than a preset threshold, the proportion of the fresh metal-based active material is increased, and the catalytically active metal component is subjected to physical grinding or chemical reduction treatment to restore its surface reactivity.

8. The energy efficiency management method for a hydrogen cogeneration system oriented towards a circular economy according to claim 1, characterized in that, The method also includes: The feed rate of the thermal energy carrier, the hydrogen production rate of the hydrolysis reaction, the power conversion of the electrical energy, and the load parameters of the electrolysis reaction are monitored in real time. Closed-loop control logic is executed based on the monitored parameters to maintain energy and material balance in the reaction environment.

9. The energy efficiency management method for a hydrogen cogeneration system oriented towards a circular economy according to claim 1, characterized in that, The method also includes: Hydrogen leakage and pressure monitoring were performed on the reaction environment and hydrogen transport path. When a leakage or overpressure signal is detected, safety response actions including inerting protection, emergency pressure relief, and full-process explosion-proof shut-off are executed.

10. An energy efficiency management system for a hydrogen cogeneration system oriented towards a circular economy, used to execute the method described in any one of claims 1 to 9, characterized in that, include: The hydrolysis reaction module is used to introduce a thermal energy carrier with a preset enthalpy value and a metal-based active material into a reaction environment in a preset ratio, and to cause the thermal energy carrier and the metal-based active material to undergo a self-heating catalytic hydrolysis reaction in the reaction environment to generate a first hydrogen gas flow and release the heat of reaction. An energy conversion module is used to collect the reaction heat and the residual heat of the heat carrier, and convert the collected heat energy into electrical energy. The deviation monitoring module is used to monitor the real-time flow rate of the first hydrogen gas flow and determine the flow deviation value of the first hydrogen gas flow rate relative to the target hydrogen supply load. The linkage control module is used to drive the electrolysis reaction with the converted electrical energy and adjust the execution power of the electrolysis reaction in real time according to the flow deviation value to generate a second hydrogen flow to compensate for the hydrogen production gap. A catalytic recycling module is used to separate the catalytically active component from the solid byproducts generated by the hydrolysis reaction and to reintroduce the catalytically active component into the hydrolysis reaction step.

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