Amino multi-energy complementary energy storage power generation system and control method thereof

Abstract

The invention provides an amino multi-energy complementary energy storage power generation system and a control method thereof, and relates to the technical field of new energy power generation and comprehensive utilization, and the amino multi-energy complementary energy storage power generation system comprises a photovoltaic photo-thermal integrated subsystem, an ammonia energy subsystem, a waste heat cascade recovery subsystem and a control unit. The system generates power through the photovoltaic module and recovers waste heat by using a cooling medium, so that the power generation efficiency is improved; chemical storage of surplus electric energy is realized through electrolytic hydrogen production and ammonia synthesis, and reverse power generation is carried out by utilizing a direct ammonia fuel cell during power shortage; the flue gas hot water type lithium bromide unit and the multi-stage heat exchanger are used for carrying out cascade heat recovery on the synthetic ammonia high-temperature reaction gas; the control unit switches the working modes of the system in real time according to the photovoltaic power and the load demand, and cooperatively dispatches the electric energy, the thermal energy and the chemical energy. The problems that the photovoltaic power generation efficiency is low, the synthetic ammonia waste heat utilization rate is low, step-free recovery is achieved, a multi-energy conversion path is isolated, scheduling is lacked, and consequently supply is unstable are solved, and the effects of improving the energy comprehensive utilization efficiency and achieving cross-period zero-carbon stable energy supply are achieved.

Description

Technical Field

[0001] This application relates to the field of new energy power generation and comprehensive utilization technology, and in particular to an amino-based multi-energy complementary energy storage power generation system and its control method. Background Technology

[0002] With the continued advancement of the "dual carbon" goals, the transformation of the energy system towards cleaner, more efficient, and low-carbon energy has become an inevitable trend. The scale of renewable energy generation, represented by photovoltaics, is constantly expanding, but its inherent volatility and intermittency pose severe challenges to the grid's regulation and absorption capacity. Among related technologies, photovoltaic modules can only utilize a limited band of the solar spectrum to generate electricity, with a large amount of energy dissipated as waste heat, leading to module temperature rise and efficiency decline. Simultaneously, high-grade waste heat generated from chemical processes such as ammonia synthesis has not been efficiently recovered in a cascade manner, resulting in overall low energy utilization efficiency. Furthermore, the conversion paths between electricity, heat, and chemical energy are relatively isolated, lacking coordinated dispatch and multi-energy complementarity mechanisms, making it difficult to achieve cross-period energy balance and stable supply. Summary of the Invention

[0003] This application provides an ammonia multi-energy complementary energy storage power generation system and its control method, which can solve the problems in related technologies such as the need to improve the efficiency of photovoltaic power generation systems, the low utilization rate of waste heat from ammonia synthesis reactions and the lack of a cascade recovery system, and the lack of unified scheduling due to the isolated electrical / thermal / chemical energy conversion paths, resulting in insufficient stability of terminal supply.

[0004] According to a first aspect of this application, an amino-based multi-energy complementary energy storage and power generation system is provided, comprising: Photovoltaic-thermal integrated subsystem, ammonia energy subsystem, waste heat cascade recovery subsystem, and control unit; The photovoltaic-thermal integrated subsystem is used to acquire the light and heat energy of sunlight and to recover the heat energy and waste heat generated by photovoltaic power generation through a heat exchange medium. The ammonia energy subsystem is connected to the DC power output terminal of the photovoltaic-thermal integrated subsystem. It is used to convert electrical energy into ammonia for chemical energy storage when there is excess photovoltaic power generation, and to convert the chemical energy of ammonia back into electrical energy output through electrochemical reaction when there is insufficient photovoltaic power generation. The waste heat cascade recovery subsystem is connected to the high-temperature reaction gas outlet of the ammonia energy subsystem and is used for multi-stage recovery and utilization of the high-grade reaction heat generated during the ammonia synthesis process. The control unit is connected to the photovoltaic-thermal integrated subsystem, the ammonia energy subsystem, and the waste heat cascade recovery subsystem to monitor the photovoltaic power generation and load demand in real time, and control the ammonia multi-energy complementary energy storage power generation system to switch working modes according to the matching relationship between the two.

[0005] Optionally, the photovoltaic-thermal integrated subsystem includes water-cooled photovoltaic modules, multiple DC converters, a DC bus, and a DC vapor compression heat pump; The back of the water-cooled photovoltaic module has a channel for the flow of cooling medium, which is used to simultaneously cool the photovoltaic cells and recover waste heat. The evaporator side of a DC vapor compression heat pump is connected to the circulation loop of the cooling medium to absorb the low-temperature heat energy carried by the cooling medium. The condenser side of a DC vapor compression heat pump is connected to the heating circuit to output high-temperature heat energy to heat users.

[0006] Optionally, the ammonia energy subsystem includes, in sequence, an electrolytic hydrogen production unit, a pressure swing adsorption nitrogen production unit, an ammonia synthesis reactor, a separator, a liquid ammonia storage tank, and a direct ammonia fuel cell; The power input terminals of the electrolytic hydrogen production unit and the pressure swing adsorption nitrogen production unit are respectively connected to the DC bus via DC converters; Ammonia synthesis reactors are used to synthesize ammonia from hydrogen and nitrogen. Direct ammonia fuel cells are used to convert the chemical energy in liquid ammonia into electrical energy, and their DC output is connected to the DC bus through a voltage regulation module.

[0007] Optionally, the waste heat recovery subsystem includes a flue gas hot water type lithium bromide absorption chiller, a first-stage gas-liquid plate heat exchanger, a second-stage gas-liquid plate heat exchanger, and a heat source water circulation loop. The high-temperature heat source input of the flue gas hot water type lithium bromide absorption unit is connected to the high-temperature reaction gas outlet of the ammonia synthesis reactor; The primary gas-liquid plate-and-shell heat exchanger and the secondary gas-liquid plate-and-shell heat exchanger are connected in series on the cooling path of the high-temperature reaction gas to perform multi-stage cooling and recover its sensible and latent heat. The recovered heat energy is used to heat the working fluid in the heat source water circulation loop. The working fluid is used as a driving heat source or a low-temperature heat source and is returned to the lithium bromide unit and heating loop.

[0008] Optionally, the flue gas hot water type lithium bromide absorption chiller includes a high-pressure generator, a low-pressure generator, a condenser, an evaporator, and an absorber; The driving heat source for the high-pressure generator is high-temperature reaction gas at 450~500℃ from the ammonia synthesis reactor; The driving heat source for the low-pressure generator is high-temperature hot water heated to 95°C by a primary gas-liquid plate-shell heat exchanger. The hot side of both the condenser and the absorber is connected to the heating circuit to provide cascade heating for the air conditioning water in the heating circuit.

[0009] Optionally, the control unit is configured to execute the following control logic: Real-time data collection of DC bus voltage, photovoltaic power generation, and real-time demand data of electrical and thermal loads for the photovoltaic-thermal integrated subsystem; The photovoltaic power generation is compared with the electrical load demand, and a mode switching command is sent to the ammonia energy subsystem based on the comparison result: when the photovoltaic power generation is greater than the electrical load demand, the command system enters the energy storage mode and controls the excess electrical energy to flow to the electrolysis hydrogen production and pressure swing adsorption nitrogen production units; when the photovoltaic power generation is less than the electrical load demand, the command system enters the energy release mode and controls the liquid ammonia storage tank to supply fuel to the direct ammonia fuel cell. Based on the heat load demand and the operating status of the waste heat cascade recovery subsystem and the DC vapor compression heat pump, the heat output distribution of each heating device is dynamically adjusted to optimize the overall thermal efficiency of the system. Maintain the stability of the DC bus voltage and perform voltage regulation and power matching of the DC power output from the direct ammonia fuel cell before grid connection.

[0010] According to a second aspect of this application, a control method for an amino-based multi-energy complementary energy storage and power generation system is provided, comprising: It receives light and heat energy from sunlight, and absorbs the heat energy and waste heat generated by photovoltaic power generation through a cooling medium to achieve active cooling of photovoltaic modules; Real-time monitoring of the photovoltaic power generation and real-time load demand of the system; Based on the matching relationship between photovoltaic power generation and electrical load demand, the control system switches the system operation mode.

[0011] Optionally, the cooling medium can be circulated in the channel on the back of the water-cooled photovoltaic module to absorb the waste heat generated when the photovoltaic cell is working, and control the module temperature below a preset threshold to improve its power generation efficiency. The cooling medium, which absorbs waste heat and then heats up, is used as a low-temperature heat source and delivered to the evaporator side of a DC-type vapor compression heat pump.

[0012] Optionally, the acquired photovoltaic power generation can be compared with the real-time load demand; If the photovoltaic power generation exceeds the real-time load demand, the control system enters the working mode of sufficient photovoltaic ammonia energy storage. The ample ammonia energy storage mode includes: distributing surplus DC power to the ammonia energy subsystem to drive the electrolytic hydrogen production unit to generate hydrogen, and driving the pressure swing adsorption nitrogen production unit to separate nitrogen from the air. The generated hydrogen and nitrogen are mixed in a predetermined volume ratio and then transported to an ammonia synthesis reactor. Under the action of a catalyst, a synthesis reaction is carried out to generate ammonia, thus realizing the conversion and storage of electrical energy into chemical energy. Waste heat recovery and utilization of the high-temperature reaction gas at the outlet of the ammonia synthesis reactor: First, it is introduced into a flue gas hot water type lithium bromide absorption unit as a driving heat source. Then, its sensible heat and latent heat are recovered step by step through at least two stages of gas-liquid plate-shell heat exchangers connected in series to heat the circulating working fluid in the system. Finally, the reaction gas is cooled and liquid ammonia is separated for storage.

[0013] Optional, also includes: If the photovoltaic power generation is not greater than the real-time load demand, the control system enters the working mode of insufficient light and ammonia energy release mode. The light-deficient ammonia energy release mode includes: vaporizing and purifying stored liquid ammonia to generate pure ammonia gas; Ammonia gas is delivered to the anode of a direct ammonia fuel cell, where it undergoes an electrochemical oxidation reaction under the action of an alkaline electrolyte and an anode catalyst, releasing electrons and generating nitrogen and water. Air is delivered to the cathode of the fuel cell, where oxygen undergoes a reduction reaction with electrons flowing in from the external circuit and components in the electrolyte under the action of the cathode catalyst. The electrolyte enables the directional migration of ions to maintain the charge balance inside the battery; at the same time, the electrons released from the anode flow through the external circuit to form a current and output DC power. The system recovers and processes waste heat and incompletely reacted ammonia generated during fuel cell operation, enabling the recycling of materials and energy within the system.

[0014] This invention provides an ammonia multi-energy complementary energy storage and power generation system and its control method, comprising: a photovoltaic-thermal integrated subsystem, an ammonia energy subsystem, a waste heat cascade recovery subsystem, and a control unit; the photovoltaic-thermal integrated subsystem is used to acquire solar energy and thermal energy, and recover thermal energy and waste heat generated by photovoltaic power generation through a heat exchange medium; the ammonia energy subsystem is connected to the DC power output terminal of the photovoltaic-thermal integrated subsystem, and is used to convert electrical energy into ammonia for chemical energy storage when photovoltaic power generation is excessive, and to convert the chemical energy of ammonia back into electrical energy output through electrochemical reaction when photovoltaic power generation is insufficient; the waste heat cascade recovery subsystem is connected to the high-temperature reaction gas outlet of the ammonia energy subsystem, and is used to perform multi-stage recovery and utilization of high-grade reaction heat generated during ammonia synthesis; the control unit is communicatively connected to the photovoltaic-thermal integrated subsystem, the ammonia energy subsystem, and the waste heat cascade recovery subsystem, respectively, and is used to monitor photovoltaic power generation and load demand in real time, and control the ammonia multi-energy complementary energy storage and power generation system to switch working modes according to the matching relationship between the two. Through this application, the photovoltaic-thermal integrated subsystem can simultaneously acquire solar energy and thermal energy and recover waste heat generated by photovoltaic power generation; the ammonia energy subsystem can convert electrical energy into ammonia for chemical energy storage when photovoltaic power generation is excessive, and convert the chemical energy of ammonia back into electrical energy when power is insufficient; the waste heat cascade recovery subsystem can recover and utilize high-grade reaction heat in the ammonia synthesis process in multiple stages; and the control unit can monitor photovoltaic power generation and load demand in real time and switch the system operating mode accordingly. Therefore, it can solve the problems in related technologies where the efficiency of photovoltaic power generation systems needs to be improved, the utilization rate of waste heat from ammonia synthesis is low and there is no cascade recovery system, and the isolated electrical / thermal / chemical energy conversion path lacks unified scheduling, resulting in insufficient stability of terminal supply. It achieves the technical effects of improving photovoltaic power generation efficiency, improving the utilization efficiency of waste heat from ammonia synthesis, realizing the synergistic coupling and unified scheduling of electrical / thermal / chemical energy, enhancing the stability of terminal supply, zero-carbon energy supply, and energy balance across time periods.

[0015] It should be understood that the description in this section is not intended to identify key or essential features of the embodiments of this application, nor is it intended to limit the scope of this application. Other features of this application will become readily apparent from the following description. Attached Figure Description

[0016] To more clearly illustrate the embodiments of this application, the accompanying drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0017] Figure 1 This is a schematic diagram of the structure of an amino-based multi-energy complementary energy storage and power generation system provided in an embodiment of this application; Figure 2This is a schematic diagram of another amino-based multi-energy complementary energy storage and power generation system provided in an embodiment of this application; Figure 3 A schematic flowchart illustrating a control method for an amino-based multi-energy complementary energy storage and power generation system provided in an embodiment of this application; Figure 4 This is a flowchart illustrating another control method for an amino-based multi-energy complementary energy storage power generation system provided in an embodiment of this application.

[0018] In the diagram: 1. Water-cooled photovoltaic module; 2. DC vapor compression heat pump; 3. Electrolytic hydrogen production unit; 4. Pressure swing adsorption nitrogen production unit; 5. Ammonia synthesis reactor; 6. Separator; 7. Liquid ammonia storage tank; 8. Direct ammonia fuel cell; 9. Flue gas hot water type lithium bromide absorption chiller; 10. First-stage gas-liquid plate heat exchanger; 11. Second-stage gas-liquid plate heat exchanger; 12. Heat user; A. DC converter A; B. DC converter B; C. DC converter C; D. DC converter D; E. DC bus E; F. Inverter F; G. Transformer G. Detailed Implementation

[0019] The following description, in conjunction with the accompanying drawings, illustrates exemplary embodiments of this application, including various details to aid understanding. These should be considered merely exemplary. Therefore, those skilled in the art will recognize that various changes and modifications can be made to the embodiments described herein without departing from the scope and spirit of this application. Similarly, for clarity and brevity, descriptions of well-known functions and structures are omitted in the following description.

[0020] The following description, with reference to the accompanying drawings, illustrates an amino-based multi-energy complementary energy storage power generation system and its control method, according to embodiments of this application.

[0021] Figure 1 This is a schematic diagram of the structure of an amino-based multi-energy complementary energy storage and power generation system provided in an embodiment of this application, as shown below. Figure 1 As shown, the system includes: Photovoltaic-thermal integrated subsystem, ammonia energy subsystem, waste heat cascade recovery subsystem, and control unit; The photovoltaic-thermal integrated subsystem is used to acquire the light and heat energy of sunlight and to recover the heat energy and waste heat generated by photovoltaic power generation through a heat exchange medium. The ammonia energy subsystem is connected to the DC power output terminal of the photovoltaic-thermal integrated subsystem. It is used to convert electrical energy into ammonia for chemical energy storage when there is excess photovoltaic power generation, and to convert the chemical energy of ammonia back into electrical energy output through electrochemical reaction when there is insufficient photovoltaic power generation. The waste heat cascade recovery subsystem is connected to the high-temperature reaction gas outlet of the ammonia energy subsystem and is used for multi-stage recovery and utilization of the high-grade reaction heat generated during the ammonia synthesis process. The control unit is connected to the photovoltaic-thermal integrated subsystem, the ammonia energy subsystem, and the waste heat cascade recovery subsystem to monitor the photovoltaic power generation and load demand in real time, and control the ammonia multi-energy complementary energy storage power generation system to switch working modes according to the matching relationship between the two.

[0022] In this embodiment, the ammonia multi-energy complementary energy storage and power generation system integrates a photovoltaic and solar thermal integrated subsystem, an ammonia energy subsystem, a waste heat cascade recovery subsystem, and a control unit to build an efficient and collaborative zero-carbon energy supply system.

[0023] As the core of energy capture, the photovoltaic-thermal integrated subsystem can fully capture the light and heat energy in sunlight. At the same time, it can effectively recover the waste heat generated during the photovoltaic power generation process through heat exchange media (such as circulating water). This not only avoids the direct loss of energy, but also reduces the operating temperature of the photovoltaic modules by removing heat, thus ensuring the stability of power generation efficiency.

[0024] The ammonia energy subsystem is connected to the DC power output terminal of the photovoltaic-thermal integrated subsystem via a line, undertaking the functions of energy storage and flexible release: when there is excess photovoltaic power generation, the surplus DC power is converted into the chemical energy of ammonia for long-term storage; when there is insufficient photovoltaic power generation, the chemical energy stored in ammonia is converted into electrical energy through a specific electrochemical reaction to promptly supplement the terminal power demand.

[0025] The waste heat cascade recovery subsystem is connected to the high-temperature reaction gas outlet of the ammonia energy subsystem. It is specifically designed to recover and utilize the high-grade reaction heat generated during the ammonia synthesis process in multiple stages, allowing the heat energy that would otherwise be wasted to be fully utilized and further improving the overall energy utilization rate of the system.

[0026] The control unit, acting as the system's central scheduling hub, communicates with the photovoltaic-thermal integrated subsystem, the ammonia energy subsystem, and the waste heat cascade recovery subsystem to monitor real-time photovoltaic power generation and terminal load demand data. It accurately determines the matching relationship between the two and automatically controls the system to switch to the corresponding operating mode, ensuring that energy flow always aligns with supply and demand balance. Beneficial effects: It achieves synergistic coupling of light, electricity, heat, and chemical energy, improves photovoltaic power generation efficiency and waste heat recovery utilization rate, enhances energy supply stability, and achieves the goal of zero-carbon clean energy supply.

[0027] This application utilizes a photovoltaic-thermal integrated subsystem to acquire solar energy and thermal energy, and recovers thermal energy and waste heat generated by photovoltaic power generation through a heat exchange medium; an ammonia energy subsystem, connected to the DC power output terminal of the photovoltaic-thermal integrated subsystem, is used to convert electrical energy into ammonia for chemical energy storage when photovoltaic power generation is excessive, and to convert the chemical energy of ammonia back into electrical energy output through electrochemical reaction when photovoltaic power generation is insufficient; a waste heat cascade recovery subsystem, connected to the high-temperature reaction gas outlet of the ammonia energy subsystem, is used for multi-stage recovery and utilization of high-grade reaction heat generated during ammonia synthesis; and a control unit is connected to both the photovoltaic-thermal integrated subsystem and the ammonia energy subsystem. The system includes a communication connection with a waste heat recovery subsystem for real-time monitoring of photovoltaic power generation and load demand. Based on the matching relationship between the two, it controls the switching of the working mode of the ammonia multi-energy complementary energy storage power generation system. This application can solve the problems in related technologies, such as the need to improve the efficiency of photovoltaic power generation systems, the low utilization rate of waste heat from ammonia synthesis reactions and the lack of a cascade recovery system, and the isolated electrical / thermal / chemical energy conversion paths lacking unified scheduling, resulting in insufficient stability of terminal supply. It achieves the technical effects of improving photovoltaic power generation efficiency, improving the utilization efficiency of ammonia synthesis waste heat, realizing the synergistic coupling and unified scheduling of electrical / thermal / chemical energy, enhancing the stability of terminal supply, and achieving zero-carbon energy supply and energy balance across time periods.

[0028] Figure 2 This application further illustrates an amino-based multi-energy complementary energy storage and power generation system provided in its embodiments, such as... Figure 2 As shown: In this embodiment of the application, the photovoltaic-thermal integrated subsystem includes a water-cooled photovoltaic module 1, a DC converter A, a DC converter B, a DC converter C, a DC converter D, a DC bus E, and a DC vapor compression heat pump 2. The back of the water-cooled photovoltaic module 1 is provided with a channel for the flow of cooling medium, which is used to simultaneously cool the photovoltaic cells and recover waste heat; The evaporator side of the DC-type vapor compression heat pump 2 is connected to the circulation loop of the cooling medium to absorb the low-temperature heat energy carried by the cooling medium. The condenser side of the DC vapor compression heat pump 2 is connected to the heating circuit to output high-temperature heat energy to the heat user 12.

[0029] In this embodiment, the photovoltaic-thermal integrated subsystem, as the core unit for energy capture and conversion, is composed of a water-cooled photovoltaic module 1, DC converters A, B, C, and D, a DC bus E, and a DC vapor compression heat pump 2. This achieves efficient capture, conversion, and cascade utilization of light and heat energy. The water-cooled photovoltaic module 1 is an integrated component that combines power generation and heat exchange. Its photovoltaic cell layer is responsible for converting visible light from sunlight into direct current. A circulation channel made of highly thermally conductive metal is specially provided on the back of the module. This channel is connected to a circulation loop of a cooling medium (such as low-temperature circulating water). When the cooling medium continuously circulates within the channel, it can efficiently remove the waste heat generated during the operation of the photovoltaic cells, preventing the cell temperature from rising and causing a decrease in power generation efficiency. It can also fully absorb the remaining energy from sunlight that has not been converted into electrical energy, achieving simultaneous recovery of waste heat. The DC converters (A, B, C, D) and the DC bus E constitute the power transmission and control link. The DC power generated by the water-cooled photovoltaic module 1 is connected to the DC bus E through the photovoltaic controller. The DC converters (A, B, C, D) ensure the stable transmission and efficient utilization of power within the subsystem by precisely regulating the voltage and stabilizing the current, providing suitable power conditions for subsequent energy conversion. The DC vapor compression heat pump 2, as a key device for heat energy enhancement and supply, has its evaporator side tightly connected to the circulation loop of the cooling medium through pipes. When the cooling medium carries the recovered low-temperature heat energy through the evaporator, the refrigerant in the heat pump absorbs this low-temperature heat energy and completes the evaporation process. The condenser side of the heat pump is connected to the heating loop. The refrigerant that has absorbed the low-temperature heat energy releases high-temperature heat energy after compression and condensation, heating the medium (such as air conditioning water) in the heating loop to the temperature required by the heat user 12, ultimately realizing the function of stably outputting high-temperature heat energy to the heat user 12. Active cooling of photovoltaic cells is achieved through the circulation of cooling medium, which effectively improves the efficiency of photovoltaic power generation. At the same time, low-grade waste heat is efficiently recovered and converted into usable high-temperature heat energy, realizing the synergy of power generation and heating, and significantly improving the utilization rate of solar energy.

[0030] In this embodiment, the ammonia energy subsystem includes an electrolytic hydrogen production device 3, a pressure swing adsorption nitrogen production device 4, an ammonia synthesis reactor 5, a separator 6, a liquid ammonia storage tank 7, and a direct ammonia fuel cell 8, which are connected in sequence. The power input terminals of the electrolytic hydrogen production unit 3 and the pressure swing adsorption nitrogen production unit 4 are connected to the DC bus E through DC converters C and D, respectively. Ammonia synthesis reactor 5 is used to synthesize ammonia from hydrogen and nitrogen. The direct ammonia fuel cell 8 is used to convert the chemical energy in liquid ammonia into electrical energy, and its DC output terminal is connected to the DC bus E through a voltage regulation module.

[0031] In this embodiment, the ammonia energy subsystem, serving as the core carrier for energy storage and flexible release, is composed of an electrolytic hydrogen production unit 3, a pressure swing adsorption (PSA) nitrogen production unit 4, an ammonia synthesis reactor 5, a separator 6, a liquid ammonia storage tank 7, and a direct ammonia fuel cell 8, connected sequentially via pipelines or lines to form a complete "electricity-ammonia-electricity" energy conversion chain. The power input terminals of both the electrolytic hydrogen production unit 3 and the PSA nitrogen production unit 4 are connected to the DC bus E via the aforementioned DC converter, enabling them to receive stable DC power precisely regulated by the DC converter. The electrolytic hydrogen production unit 3 uses this DC power to decompose water and produce high-purity green hydrogen, while the PSA nitrogen production unit 4 efficiently separates high-purity nitrogen from the air using PSA technology. The hydrogen and nitrogen produced by both are then transported to the ammonia synthesis reactor 5 in a preset ratio. The ammonia synthesis reactor 5, as the core equipment for ammonia synthesis, is equipped with a dedicated catalyst that provides a suitable high-temperature, high-pressure environment for the synthesis reaction of hydrogen and nitrogen, promoting the chemical reaction between hydrogen and nitrogen to generate ammonia under the action of the catalyst, thus realizing the conversion of electrical energy into ammonia chemical energy. The generated ammonia-containing gas mixture then enters separator 6, where liquid ammonia is separated from the mixture through processes such as cooling and depressurization. The separated liquid ammonia is then transported to liquid ammonia storage tank 7 for sealed storage, ready for use when needed. The direct ammonia fuel cell 8 adopts a direct ammonia fuel cell (DAFC) structure, capable of directly converting the chemical energy stored in liquid ammonia into electrical energy through an electrochemical reaction. Its DC output terminal is connected to a voltage regulation module, which rectifies and boosts the DC power output from the direct ammonia fuel cell 8, ensuring that the voltage and current parameters of the output power are matched with the DC bus E before being connected to the DC bus E, thus achieving stable power feedback. This achieves efficient conversion between electrical energy and ammonia chemical energy, solving the problem of storing surplus photovoltaic power and providing stable power supplementation when photovoltaic power generation is insufficient, thereby improving the flexibility and continuity of energy supply.

[0032] In this embodiment, the waste heat cascade recovery subsystem includes a flue gas hot water type lithium bromide absorption chiller 9, a first-stage gas-liquid plate heat exchanger 10, a second-stage gas-liquid plate heat exchanger 11, and a heat source water circulation loop. The high-temperature heat source input of the flue gas hot water type lithium bromide absorption unit 9 is connected to the high-temperature reaction gas outlet of the ammonia synthesis reactor 5. The primary gas-liquid plate heat exchanger 10 and the secondary gas-liquid plate heat exchanger 11 are connected in series on the cooling path of the high-temperature reaction gas to perform multi-stage cooling and recover its sensible and latent heat. The recovered heat energy is used to heat the working fluid in the heat source water circulation loop. The working fluid is used as a driving heat source or a low-temperature heat source and is returned to the lithium bromide unit and heating loop.

[0033] In this embodiment, the waste heat cascade recovery subsystem, as the core unit for high-grade heat energy recovery and resource utilization, is composed of a flue gas hot water type lithium bromide absorption turbine unit 9, a primary gas-liquid plate-shell heat exchanger 10, a secondary gas-liquid plate-shell heat exchanger 11, and a heat source water circulation loop, forming a complete chain of heat energy recovery system from high temperature to low temperature. Among them, the flue gas hot water type lithium bromide absorption turbine unit 9 operates on the core principle of "heat cascade enhancement." Its high-temperature heat source input end is directly connected to the high-temperature reaction gas outlet of the ammonia synthesis reactor 5 through a dedicated pipeline, which can efficiently receive the high-temperature reaction gas of about 450-500°C generated during the ammonia synthesis process and use it as a driving heat source to provide energy support for the unit operation. The primary gas-liquid plate-and-shell heat exchanger 10 and the secondary gas-liquid plate-and-shell heat exchanger 11 are arranged in series along the cooling path of the high-temperature reaction gas. This type of heat exchanger features a high heat transfer coefficient and a large heat transfer area, enabling targeted multi-stage cooling of the high-temperature reaction gas: the primary heat exchanger receives the high-temperature reaction gas after initial heat release from the lithium bromide unit and further recovers its sensible heat; the secondary heat exchanger lowers the temperature of the reaction gas below the dew point temperature, achieving comprehensive recovery of both sensible and latent heat. A heat source water circulation loop runs through the entire subsystem. The working fluid (such as heat source water and low-temperature circulating water) in the loop fully absorbs the heat energy released by the high-temperature reaction gas as it flows through each stage of the heat exchanger, gradually increasing in temperature to form a usable heat medium. Part of this heated working fluid serves as a driving heat source connected to the low-pressure generator of the flue gas hot water type lithium bromide absorption chiller 9, supplementing the energy for continuous unit operation; the other part serves as a low-temperature heat source connected to the evaporator of the flue gas hot water type lithium bromide absorption chiller 9, releasing heat to circulate and reheat the heat exchanger. Low-temperature air conditioning return water is sequentially connected in series to the condenser and absorber of the flue gas hot water type lithium bromide absorption chiller unit 9. After being heated, it works in parallel with the high-temperature heat energy output by the DC-type vapor compression heat pump 2 to provide stable heating for heat user 12. The entire subsystem achieves waste-free recovery and recycling of high-temperature reaction gas heat energy through a cascade design of "initial heat extraction from the lithium bromide unit + progressive heat extraction from multi-stage heat exchangers". This significantly improves the recovery and utilization rate of waste heat in the ammonia synthesis process, forms a complete cascade utilization system of thermal energy, reduces energy loss, and provides a supplementary heat source for the system's heating, further improving overall energy utilization efficiency.

[0034] In this embodiment, the flue gas hot water type lithium bromide absorption chiller 9 includes a high-pressure generator, a low-pressure generator, a condenser, an evaporator, and an absorber; The driving heat source for the high-pressure generator is high-temperature reaction gas at 450–500°C from ammonia synthesis reactor 5; The driving heat source for the low-pressure generator is high-temperature hot water heated to 95°C by the primary gas-liquid plate-shell heat exchanger 10. The hot side of both the condenser and the absorber is connected to the heating circuit to provide cascade heating for the air conditioning water in the heating circuit.

[0035] In this embodiment, the flue gas hot water type lithium bromide absorption chiller 9, as the core equipment for waste heat recovery and heat energy supply, is composed of a high-pressure generator, a low-pressure generator, a condenser, an evaporator, and an absorber, which work together through internal flow channels and heat exchange circuits. Its core operation revolves around the principle of "heat gradient enhancement" to achieve efficient conversion and utilization of heat energy of different grades. The driving heat source of the high-pressure generator is directly derived from the high-temperature reaction gas of 450-500°C discharged from the ammonia synthesis reactor 5. This high-temperature reaction gas flows through the high-temperature flue gas heat exchange tube bundle built into the unit and passes through the high-pressure generator, efficiently transferring the high-grade heat energy it carries to the dilute lithium bromide solution outside the tube. When the dilute solution absorbs heat and reaches its boiling point, the water (i.e., refrigerant) in it evaporates to form refrigerant vapor, completing the conversion of high-grade heat energy into refrigerant vapor energy. The low-pressure generator uses high-temperature hot water heated to 95°C by the first-stage gas-liquid plate-shell heat exchanger 10 as the driving heat source. This high-temperature hot water carries the recovered medium-grade heat energy into the low-pressure generator, further heating the lithium bromide solution that has been preliminarily concentrated by the high-pressure generator. This causes the remaining refrigerant in the solution to continue to evaporate and generate refrigerant vapor, realizing the secondary recovery and utilization of medium-grade heat energy. This portion of refrigerant vapor merges with the refrigerant vapor generated by the high-pressure generator and enters the condenser. Both the condenser and absorber's hot sides are connected to the heating circuit via pipes. The combined refrigerant vapor exchanges heat with the air conditioning water in the heating circuit within the condenser, releasing condensation heat for the first stage of heating the air conditioning water. Meanwhile, in the absorber, low-temperature refrigerant vapor flowing from the evaporator comes into full contact with the concentrated lithium bromide solution sprayed from the top. Due to the lithium bromide solution's strong hygroscopic properties, it quickly absorbs the refrigerant vapor and forms a dilute solution. The heat released during this absorption process is transferred to the air conditioning water in the heating circuit through the heat exchange tube bundle, achieving the second stage of heating. Ultimately, this raises the temperature of the air conditioning water to meet the needs of heat user 12. The evaporator provides the low-temperature heat extraction basis for the entire cycle, ensuring stable unit operation. The flue gas hot water type lithium bromide absorption chiller unit utilizes heat sources of different grades in nine stages to achieve tiered heating of the air conditioning water, significantly improving the utilization rate of waste heat from ammonia synthesis and heating efficiency, providing stable and reliable high-temperature heat energy to heat user 12.

[0036] In this embodiment of the application, the control unit is configured to execute the following control logic: Real-time data collection of DC bus E voltage, photovoltaic power generation, and real-time demand data of electrical and thermal loads of the photovoltaic-thermal integrated subsystem; The photovoltaic power generation is compared with the electrical load demand, and a mode switching command is sent to the ammonia energy subsystem according to the comparison result: when the photovoltaic power generation is greater than the electrical load demand, the command system enters the energy storage mode and controls the excess electrical energy to flow to the electrolysis hydrogen production and pressure swing adsorption nitrogen production unit 4; when the photovoltaic power generation is less than the electrical load demand, the command system enters the energy release mode and controls the liquid ammonia storage tank 7 to supply fuel to the direct ammonia fuel cell 8. Based on the heat load demand and the operating status of the waste heat cascade recovery subsystem and the DC-type vapor compression heat pump 2, the heat output distribution of each heating device is dynamically adjusted to optimize the overall thermal efficiency of the system. Maintain the stability of the DC bus E voltage, and perform voltage regulation and power matching of the DC power output from the direct ammonia fuel cell 8 before grid connection.

[0037] In this embodiment, the control unit serves as the intelligent scheduling core of the entire energy storage and power generation system. Through preset control logic, it achieves precise coordinated management and control of each subsystem, ensuring stable and efficient operation of the system under different operating conditions. The control unit first uses a dedicated data acquisition module to capture in real time the DC bus E voltage of the photovoltaic-thermal integrated subsystem, the photovoltaic power generation, and the real-time electrical and thermal load demand data of the end user 12. This data serves as the core basis for subsequent control decisions, ensuring the pertinence and accuracy of control commands. Next, the control unit's built-in power comparison algorithm compares the collected photovoltaic power generation with the electrical load demand in real time. Based on the comparison results, it issues a clear mode switching command to the ammonia energy subsystem: when the photovoltaic power generation exceeds the electrical load demand, it determines that the system has surplus electrical energy, and immediately instructs the system to enter energy storage mode. Simultaneously, the circuit control module guides the surplus electrical energy to flow precisely to the electrolysis hydrogen production unit 3 and the pressure swing adsorption nitrogen production unit 4, providing power support for the ammonia synthesis process. When the photovoltaic power generation is less than the electrical load demand, it determines that the terminal power supply is insufficient, and instructs the system to switch to energy release mode, controlling the opening of the output valve of the liquid ammonia storage tank 7 to stably supply liquid ammonia fuel to the direct ammonia fuel cell 8, ensuring timely response to power replenishment. In terms of heat supply management, the control unit combines real-time heat load demand data with the operating parameters (such as heating temperature, heat output power, etc.) of the waste heat cascade recovery subsystem and the DC vapor compression heat pump 2. By rationally allocating the heat output ratio of each heating device, it avoids overload or heat waste of a single device, thereby optimizing the overall thermal efficiency of the system. In addition, the control unit is responsible for ensuring power quality. It monitors and adjusts the DC bus E voltage in real time through a voltage stabilization module to prevent voltage fluctuations from affecting electrical equipment. Simultaneously, for the DC power output from the direct ammonia fuel cell 8, it uses a linked voltage regulation module for rectification and boosting to ensure that the output voltage level and power parameters match the grid or DC load, guaranteeing the stability of grid-connected or direct supply. This enables intelligent switching of system operating modes and dynamic supply-demand balance, optimizes the allocation of electrical and heat resources, ensures power quality and supply / heating stability, and further improves the overall system operating efficiency and reliability.

[0038] Accordingly, embodiments of this application provide a control method for an amino-based multi-energy complementary energy storage and power generation system, such as... Figure 3 As shown, the method includes: Step 101: Receive light and heat energy from sunlight, and absorb the heat energy and waste heat generated by photovoltaic power generation through a cooling medium to achieve active cooling of the photovoltaic module.

[0039] In some embodiments, the upper photovoltaic cell layer of a photovoltaic module first receives solar radiation, precisely capturing the visible light portion and converting it into direct current. During this energy conversion process, the photovoltaic cells generate a certain amount of waste heat. Simultaneously, most of the remaining energy in the sunlight that is not absorbed and converted by the photovoltaic cells (such as infrared energy) also acts as heat on the module surface. If this heat continues to accumulate, it will cause the photovoltaic module temperature to rise, leading to a decrease in power generation efficiency. To achieve active cooling and heat recovery, a closed flow channel made of a highly thermally conductive metal (such as copper or aluminum) is specially provided on the back of the photovoltaic module. A cooling medium (preferably low-temperature circulating water) is pre-circulated in the channel. The cooling medium continuously circulates along a predetermined path within the channel, efficiently absorbing the waste heat generated by the photovoltaic cells and the unconverted heat energy from the sunlight through close contact with the back of the photovoltaic cells. As the cooling medium absorbs heat, its own temperature gradually increases, while the photovoltaic module actively cools down by continuously dissipating heat, preventing the temperature from exceeding the suitable operating range (usually controlled below 40°C). This ensures that the photovoltaic cells maintain stable power generation efficiency and collects a low-grade heat source for further utilization of the heat energy. The photovoltaic modules are cooled by actively circulating the cooling medium, which effectively suppresses the decline in power generation efficiency caused by temperature rise, and simultaneously recovers the heat energy that would otherwise be wasted, providing a foundation for the comprehensive energy utilization of the system and improving the capture efficiency and utilization value of solar energy resources.

[0040] Step 102: Monitor the photovoltaic power generation and real-time load demand of the system in real time.

[0041] In some embodiments, for photovoltaic power generation monitoring, the control unit deploys high-precision power sensors and data acquisition modules at the DC bus E output end of the photovoltaic-thermal integrated subsystem to continuously collect the DC voltage and current signals output by the photovoltaic modules. Combined with a preset algorithm, the photovoltaic power generation is calculated in real time, while simultaneously recording power fluctuation trends to ensure accurate capture of the intermittent and fluctuating characteristics of photovoltaic power generation caused by changes in light intensity and ambient temperature. For real-time load demand monitoring, the monitoring scope covers two core demands: electrical load and heat load. For electrical load, sensing devices installed in the power supply circuits of terminal electrical equipment and on the load side of the DC bus E collect the actual power consumption data of various electrical equipment in real time, summarizing them to form the overall electrical load demand value of the system. For heat load, temperature sensors and flow sensors are deployed at key nodes in the heating circuit (such as the inlet of heat user 12 and the heating medium circulation pipeline) to monitor the temperature and flow changes of the heating medium in real time. Combined with the heating scenarios of heat user 12 (such as building heating and domestic hot water supply), the heat load demand is dynamically calculated to accurately determine the real-time consumption of high-temperature heat energy by heat user 12. The entire monitoring process employs a high-frequency acquisition mechanism (e.g., several data samples per second). The acquired photovoltaic power data and load demand data are filtered and calibrated by the data processing module built into the control unit to remove invalid data caused by electromagnetic interference, sensor errors, and other factors. This ensures that the monitoring data transmitted to the control unit has high accuracy and real-time performance, providing reliable data support for subsequent system operating mode switching and energy distribution regulation. Real-time and accurate monitoring of photovoltaic power generation output and terminal supply and demand provides a data foundation for intelligent system decision-making, avoiding energy waste or insufficient supply due to information lag, and ensuring the targeted and efficient operation of the system.

[0042] Step 103: Based on the matching relationship between photovoltaic power generation and electrical load demand, the control system switches the system operation mode.

[0043] In some embodiments, the control unit incorporates a supply-demand matching algorithm. First, it quantitatively compares the real-time photovoltaic power generation with the electrical load demand to determine the difference range and matching status between the two. When it is determined that the photovoltaic power generation exceeds the electrical load demand and there is surplus electrical energy, the control unit immediately sends an energy storage mode start command to the ammonia energy subsystem and related execution components. Through circuit switching and flow control, the surplus DC power is guided to be stably input into the electrolytic hydrogen production device 3 and the pressure swing adsorption nitrogen production device 4 via a DC converter, driving the two devices to produce high-purity hydrogen and nitrogen respectively. Then, the two gases are controlled to be introduced into the ammonia synthesis reactor 5 at a volume ratio of 3:1. Under preset high temperature, high pressure and catalyst conditions, ammonia is synthesized. The generated ammonia-containing mixed gas is separated by the separator 6, and the liquid ammonia is transported to the liquid ammonia storage tank 7 for storage, completing the energy conversion and storage of "electricity-ammonia". At the same time, the control unit activates the waste heat cascade recovery subsystem to synchronously recover the high-grade waste heat generated during the ammonia synthesis process. When it is determined that the photovoltaic power generation is less than the electrical load demand and there is a power shortage, the control unit sends an energy release mode start command, controlling the opening of the output pipeline valve of the liquid ammonia storage tank 7 to transport the stored liquid ammonia to the ammonia evaporator. After vaporization and purification using the system's waste heat, it stably supplies ammonia fuel to the direct ammonia fuel cell 8. The direct ammonia fuel cell 8 converts the chemical energy of ammonia into direct current through electrochemical reactions such as anodic oxidation and cathodic reduction. After rectification and boosting by the voltage regulation module to parameters compatible with the DC bus E, it is connected to the bus to supplement the electrical load shortage and realize the energy release of "ammonia-electricity". During this process, the control unit monitors the reaction status and electrical output parameters of the direct ammonia fuel cell 8 in real time to ensure stable power supply. In addition, during the mode switching process, the control unit synchronously coordinates the operating parameters of the photovoltaic-thermal integrated subsystem and the waste heat cascade recovery subsystem to avoid energy fluctuations caused by mode switching and ensure the overall stable operation of the system. This embodiment realizes the adaptive switching of the "energy storage-energy release" mode, efficiently consumes surplus photovoltaic power, timely supplements the power shortage, solves the problem of intermittent photovoltaic power generation, and improves the continuity and stability of energy supply.

[0044] This application provides another control method for an amino-based multi-energy complementary energy storage and power generation system, such as... Figure 4 As shown, the method includes: Step 201: The cooling medium circulates in the channel on the back of the water-cooled photovoltaic module 1 to absorb the waste heat generated when the photovoltaic cell is working, and controls the module temperature below a preset threshold to improve its power generation efficiency.

[0045] In some embodiments, the back of the water-cooled photovoltaic module 1 is specially designed with a closed flow channel made of a highly thermally conductive metal (such as copper or aluminum alloy). This channel is seamlessly connected to the cooling medium circulation loop. The cooling medium filled in the loop is preferably low-temperature circulating water at 20°C (which has the advantages of high specific heat capacity, high thermal conductivity, and low cost). Driven by the circulation power device, the cooling medium flows continuously and uniformly along the channel in a turbulent state. During the process of photovoltaic cells converting visible light in sunlight into direct current, a large amount of waste heat is generated. At the same time, the remaining energy in sunlight that is not absorbed and converted by the photovoltaic cells (such as infrared energy) will also accumulate on the surface of the module in the form of heat. If it is not dissipated in time, the module temperature may rise to 60-70°C, resulting in a significant decrease in power generation efficiency. As the cooling medium flows within the channel, it rapidly absorbs waste heat through close heat conduction with the back of the photovoltaic cells, gradually raising its own temperature to around 30°C. Meanwhile, the temperature of the photovoltaic module is stably controlled within a preset threshold (typically below 40°C, determined based on the module's efficiency characteristics to avoid a 0.3%–0.5% efficiency degradation caused by every 1°C increase in temperature). This active cooling method not only suppresses high-temperature degradation of the module through continuous heat exchange, ensuring the photovoltaic cells remain in their high-efficiency operating range, but also allows the cooling medium, which has absorbed heat, to retain usable thermal energy, providing a stable low-grade heat source for subsequent heat recovery and utilization. This achieves the dual goals of ensuring power generation efficiency and initial energy recovery. Precise control of the photovoltaic module's operating temperature effectively avoids power generation efficiency degradation caused by high temperatures, improving the stability and overall conversion efficiency of photovoltaic power generation, while simultaneously achieving initial waste heat capture, creating conditions for comprehensive energy utilization of the system.

[0046] Step 202: The cooling medium that has been heated after absorbing waste heat is used as a low-temperature heat source and transported to the evaporator side of the DC-type vapor compression heat pump 2.

[0047] In some embodiments, after the waste heat absorption in step 201, the original low-temperature circulating water (cooling medium) at 20°C has been heated to 30°C. At this point, the cooling medium not only carries the waste heat generated by the operation of the photovoltaic cells, but also enriches the low-grade heat energy in the sunlight that has not been converted into electrical energy, thus possessing the value of being used as a heat source. To prevent heat loss during transmission, the heated cooling medium is directionally transported to the evaporator side of the DC-type vapor compression heat pump 2 through a closed circulation pipe with an insulation layer. The insulation design of the pipe effectively reduces heat loss along the way, ensuring that the low-grade heat energy is accurately transferred to the heat pump system. On the evaporator side, the cooling medium flows through a specially designed heat exchange tube bundle, forming a highly efficient heat exchange contact with the low-temperature, low-pressure gas-liquid two-phase refrigerant inside the heat pump. The cooling medium, as a low-temperature heat source, provides the heat required for the evaporation of the refrigerant, while its own temperature decreases after releasing heat, preparing it to subsequently flow back to the back channel of the water-cooled photovoltaic module 1 to perform the cooling and waste heat absorption tasks again. This transfer process enables the directional transfer of low-grade waste heat, transforming potentially wasted thermal energy into the driving energy foundation for the heat pump system, perfectly connecting the core processes of photovoltaic cooling and thermal energy enhancement. It achieves efficient transfer and recovery of low-grade waste heat, providing a stable and reliable low-temperature heat source for the DC-type vapor compression heat pump 2, ensuring the efficient start-up of the subsequent thermal energy enhancement process, promoting the synergistic utilization of solar energy in power generation and heating, and further improving the system's energy utilization rate.

[0048] Step 203: Compare the obtained photovoltaic power generation with the real-time load demand.

[0049] In some embodiments, the photovoltaic power generation power used for comparison is a precise value after filtering and calibration by the data processing module. This value comprehensively reflects the current actual power output capacity of the photovoltaic-thermal integrated subsystem, eliminating errors caused by factors such as light fluctuations and equipment operating noise. The real-time power load demand is the sum of the actual power consumption of all terminal electrical equipment (including internal electrical equipment such as the electrolytic hydrogen production unit 3 and the pressure swing adsorption nitrogen production unit 4, as well as external terminal loads). This value is obtained by the control unit after integrating and correcting the data collected from each monitoring node, ensuring that it accurately reflects the current power consumption demand. During the comparison process, the control unit not only calculates the difference between the two values ​​in real time, but also dynamically analyzes the trend of the difference—for example, determining whether the photovoltaic power generation power is a short-term small surplus or a sustained large surplus, a temporary slight power shortage or a long-term severe supply shortage. At the same time, it combines the system's preset energy buffer threshold (to avoid frequent mode switching due to short-term fluctuations) to form a comprehensive supply and demand matching judgment result. Furthermore, the comparison process employs a high-frequency synchronization mechanism, maintaining consistency with the data acquisition frequency. This ensures timely capture of intermittent fluctuations in photovoltaic power generation and dynamic changes in electrical load demand, providing reliable decision support for the precise switching of subsequent system operation modes. This avoids energy waste or insufficient power supply due to comparison lags or judgment errors. Accurately determining the supply and demand relationship between photovoltaic power generation and electrical load provides a scientific basis for the system's "energy storage-release" mode switching, ensuring the timeliness and accuracy of mode switching and laying the foundation for efficient energy utilization.

[0050] Step 204: If the photovoltaic power generation is greater than the real-time load demand, the control system enters the working mode of photovoltaic-sufficient ammonia energy storage.

[0051] In some embodiments, when the control unit determines in real-time that the photovoltaic power generation exceeds the real-time load demand, it immediately activates the photovoltaic-sufficient ammonia energy storage mode. Through the coordinated operation of the entire chain of "power distribution - ammonia synthesis - waste heat recovery," it achieves efficient storage of surplus electrical energy and cascade utilization of high-grade thermal energy. First, the control unit precisely regulates the voltage and current of the DC bus E through a DC converter, stably distributing the surplus DC power to the electrolytic hydrogen production unit 3 and the pressure swing adsorption nitrogen production unit 4 of the ammonia energy subsystem. After the electrolytic hydrogen production unit 3 is connected to the appropriate DC power, it produces high-purity green hydrogen through water electrolysis. This process involves no fossil energy, ensuring the clean properties of the hydrogen. The pressure swing adsorption nitrogen production unit 4, driven by DC power, uses pressure swing adsorption technology to separate and purify air, efficiently screening out high-purity nitrogen to provide high-quality raw materials for subsequent ammonia synthesis.

[0052] Subsequently, the system mixes hydrogen produced by the electrolytic hydrogen production unit 3 and nitrogen separated by the pressure swing adsorption nitrogen production unit 4 at a preset volume ratio of 3:1 using a dedicated mixer. The mixed gas is then directionally transported to the ammonia synthesis reactor 5 via pipeline. The ammonia synthesis reactor 5 is equipped with a pre-designed high-temperature and high-pressure working environment and a built-in high-efficiency synthesis catalyst. Under the catalytic action of the catalyst, the mixed gas undergoes a chemical reaction to generate ammonia, successfully converting surplus electrical energy into the chemical energy of ammonia, achieving long-term energy storage, and laying the foundation for subsequent energy release.

[0053] Simultaneously, for the high-temperature reaction gas (approximately 450-500°C) discharged from the outlet of ammonia synthesis reactor 5, the system initiates a waste heat recovery process to ensure zero waste of thermal energy. First, the high-temperature reaction gas is used as a driving heat source and introduced into the high-pressure generator of the flue gas hot water type lithium bromide absorption chiller 9. Through the heat exchange tube bundle, heat is transferred to the dilute lithium bromide solution within the unit, causing the water in the solution to evaporate and form refrigerant vapor, providing power for the lithium bromide unit's operation. During this process, the temperature of the high-temperature reaction gas drops to 150°C. Second, the cooled 150°C reaction gas flows into the first-stage gas-liquid plate-and-shell heat exchanger 10, where it exchanges heat with the 70°C heat source water flowing through the heat exchanger, heating the heat source water to 95°C. This heated high-temperature hot water then serves as the driving heat source for the low-pressure generator of the lithium bromide unit again. The reaction gas participates in the heating cycle, and the temperature of the reaction gas is further reduced to 70-65℃. In the third step, the reaction gas at 42-45℃ enters the second-stage gas-liquid plate-shell heat exchanger 11, continuously releasing heat and reducing the temperature below the dew point temperature. In this process, not only is the sensible heat of the reaction gas recovered, but all the latent heat is also fully captured, heating the 20℃ low-temperature circulating water flowing through the heat exchanger to 25℃. Finally, the temperature of the reaction gas is reduced to below 30℃. The low-temperature reaction gas after multi-stage cooling enters the separator 6, where gas-liquid separation is achieved through cooling and depressurization processes. The separated liquid ammonia is transported to the liquid ammonia storage tank 7 for sealed storage.

[0054] Throughout the entire operation, the control unit monitors the operating parameters of each device in real time (such as gas mixing ratio, reactor temperature and pressure, heat exchanger heat exchange efficiency, etc.), and dynamically adjusts the power distribution and medium flow rate to ensure stable and efficient ammonia synthesis reaction and complete waste heat recovery.

[0055] It efficiently absorbs surplus photovoltaic power and converts it into easily stored and transportable ammonia chemical energy. At the same time, it makes full use of the high-temperature waste heat in the ammonia synthesis process through multi-level recycling, which greatly improves the comprehensive energy utilization rate. It not only solves the problem of photovoltaic power generation absorption, but also realizes multi-level energy utilization, providing a double guarantee for zero-carbon energy supply of the system.

[0056] Step 205: If the photovoltaic power generation is not greater than the real-time load demand, the control system enters the working mode of insufficient light and ammonia energy release mode.

[0057] In some embodiments, when the control unit determines that the photovoltaic power generation is not greater than the real-time load demand after real-time comparison, it immediately triggers the ammonia energy release mode for insufficient light. Through the complete link of "ammonia gasification - electrochemical reaction - energy output - recycling", the stored ammonia chemical energy is efficiently converted into electrical energy to supplement the terminal power gap. First, the system starts the ammonia gasification and purification process: the liquid ammonia stored in the liquid ammonia storage tank 7 (storage state is -33℃ atmospheric pressure or room temperature 1.0~1.5MPa) is transported to the ammonia evaporator through the heat-insulated pipeline. The waste heat of 80~100℃ generated during the operation of the direct ammonia fuel cell 8 is used as the gasification heat source to rapidly gasify the liquid ammonia into ammonia gas. To prevent liquid ammonia from directly entering the battery and causing electrode immersion failure, the vaporized ammonia gas then flows through a high-precision filter to efficiently remove any trace impurities, ensuring the ammonia purity meets the battery reaction requirements. Subsequently, a flow controller dynamically adjusts the ammonia supply (the supply is precisely matched to the battery load; for example, a 10kW battery requires precise control). Flow rate is between 0.5 and 0.8. Within a certain range, this ensures the stable conduct of subsequent electrochemical reactions. Next, the purified ammonia gas is uniformly distributed on the surface of the nickel-based catalyst in the direct ammonia fuel cell 8 through the anolyte diffusion layer (under alkaline conditions, nickel catalysts exhibit superior catalytic activity for ammonia oxidation compared to platinum, reducing costs and improving reaction efficiency); the nickel-based catalyst reacts with an alkaline electrolyte (containing...) Under the synergistic effect of ), ammonia undergoes an electrochemical oxidation reaction, the core reaction formula being: In the reaction, 2 mol of ammonia gas loses 6 mol of electrons, producing nitrogen and water. The released electrons, unable to pass through the electrolyte, flow to the cathode via an external circuit, forming the initial electron flow. Simultaneously, the air supply unit delivers oxygen-containing air to the cathode of the fuel cell. The oxygen permeates through the cathode gas diffusion layer and contacts the platinum-based catalyst (platinum has extremely high catalytic activity for oxygen reduction). Electrons flowing from the anode in the external circuit, along with electrons from the electrolyte... It undergoes a reduction reaction with oxygen on the catalyst surface, and the core reaction formula is: 1 mol of oxygen gains 4 mol of electrons and combines with water to form 4 mol of oxygen. , generated They migrate directionally to the anode via electrolytes (such as ion migration in KOH solution or oxygen ion conduction in solid oxide electrolytes) to replenish the ions consumed in the anode reaction. This forms a stable "ion cycle." Electrolytes play a crucial role as "ion bridges" throughout the reaction process, facilitating the flow of ions. The directional migration of electrons maintains the internal charge balance of the battery, preventing charge accumulation that could lead to reaction stagnation. In the external circuit, electrons released from the anode do work as they flow through external loads (such as terminal electrical equipment or energy storage batteries), forming an effective current and achieving electrical energy output. The magnitude of the current is determined by the ammonia supply, catalyst activity, and reaction temperature (alkaline DAFCs are typically controlled at 60–80°C). To improve the adaptability of power generation, the system is equipped with a voltage regulation module in the external circuit. This module rectifies and boosts the low-voltage DC power output from the battery (the output voltage of a single battery is typically 0.6–0.8V), ensuring that its voltage and power parameters are matched with the DC bus E before connection, thus accurately supplementing real-time load demands. Finally, the system activates the product processing and waste heat recovery mechanism. A small amount of unreacted ammonia gas (with a conversion rate of approximately 85%-95%) mixed in the nitrogen gas discharged from the anode is liquefied and recovered after cooling by the exhaust condenser, and then recycled back into the ammonia evaporator. The waste heat released during the electrochemical reaction (approximately 15%-20% of the total energy) is recovered through a waste heat exchanger and used to preheat liquid ammonia to assist in vaporization. The water generated in the reaction (the portion integrated into the electrolyte) is periodically discharged, treated in a wastewater collection tank, and used as system makeup water (such as electrolyte replenishment water), achieving a closed-loop cycle of matter and energy. This embodiment enables rapid response to power shortages, efficiently converting ammonia chemical energy into electrical energy, resulting in high power generation efficiency and fast start-up and shutdown speeds. Simultaneously, it achieves the recovery and recycling of waste heat and unreacted ammonia gas, with emissions consisting only of nitrogen and water, resulting in zero carbon emissions and no pollution, ensuring the stability and cleanliness of the final power supply.

[0058] The various numerical designations such as "first," "second," etc., used in this application are merely for ease of description and are not intended to limit the scope of the embodiments of this application, nor do they indicate the order of events.

[0059] At least one in this application can also be described as one or more, and multiple can be two, three, four or more, and this application does not impose any limitation. In the embodiments of this application, for a technical feature, the technical features in that technical feature are distinguished by "first", "second", "third", "A", "B", "C" and "D", and there is no order or size among the technical features described by "first", "second", "third", "A", "B", "C" and "D".

[0060] It should be understood that the various forms of processes shown above can be used to rearrange, add, or delete steps. For example, the steps described in this application can be executed in parallel, sequentially, or in different orders, as long as the desired result of the technical solution disclosed in this application can be achieved, and this is not limited herein.

[0061] The specific embodiments described above do not constitute a limitation on the scope of protection of this application. Those skilled in the art should understand that various modifications, combinations, sub-combinations, and substitutions can be made according to design requirements and other factors. Any modifications, equivalent substitutions, and improvements made within the spirit and principles of this application should be included within the scope of protection of this application.

Claims

1. An amino-based multi-energy complementary energy storage and power generation system, characterized in that, include: Photovoltaic-thermal integrated subsystem, ammonia energy subsystem, waste heat cascade recovery subsystem, and control unit; The photovoltaic-thermal integrated subsystem is used to acquire the light energy and heat energy of sunlight, and to recover the heat energy and waste heat generated by photovoltaic power generation through a heat exchange medium. The ammonia energy subsystem is connected to the DC power output terminal of the photovoltaic-thermal integrated subsystem. It is used to convert electrical energy into ammonia for chemical energy storage when the photovoltaic power generation is excessive, and to convert the chemical energy of ammonia back into electrical energy output through electrochemical reaction when the photovoltaic power generation is insufficient. The waste heat cascade recovery subsystem is connected to the high-temperature reaction gas outlet of the ammonia energy subsystem and is used to recover and utilize the high-grade reaction heat generated during the ammonia synthesis process in multiple stages. The control unit is communicatively connected to the photovoltaic-thermal integrated subsystem, the ammonia energy subsystem, and the waste heat cascade recovery subsystem, respectively, for real-time monitoring of photovoltaic power generation and load demand, and controlling the ammonia multi-energy complementary energy storage power generation system to switch working modes according to the matching relationship between the two.

2. The amino-based multi-energy complementary energy storage and power generation system according to claim 1, characterized in that, The photovoltaic-thermal integrated subsystem includes water-cooled photovoltaic modules, multiple DC converters, a DC bus, and a DC vapor compression heat pump; The water-cooled photovoltaic module has a channel on the back for the flow of cooling medium, which is used to simultaneously cool the photovoltaic cells and recover waste heat. The evaporator side of the DC-type vapor compression heat pump is connected to the circulation loop of the cooling medium to absorb the low-temperature heat energy carried by the cooling medium. The condenser side of the DC-type vapor compression heat pump is connected to the heating circuit to output high-temperature heat energy to heat users.

3. The amino-based multi-energy complementary energy storage and power generation system according to claim 1, characterized in that, The ammonia energy subsystem includes, in sequence, an electrolytic hydrogen production unit, a pressure swing adsorption nitrogen production unit, an ammonia synthesis reactor, a separator, a liquid ammonia storage tank, and a direct ammonia fuel cell. The power input terminals of the electrolytic hydrogen production device and the pressure swing adsorption nitrogen production device are respectively connected to the DC bus via DC converters. The ammonia synthesis reactor is used to synthesize ammonia from hydrogen and nitrogen. The direct ammonia fuel cell is used to convert the chemical energy in liquid ammonia into electrical energy, and its DC output terminal is connected to the DC bus.

4. The amino-based multi-energy complementary energy storage and power generation system according to claim 1, characterized in that, The waste heat recovery subsystem includes a flue gas hot water type lithium bromide absorption chiller, a first-stage gas-liquid plate heat exchanger, a second-stage gas-liquid plate heat exchanger, and a heat source water circulation loop. The high-temperature heat source input of the flue gas hot water type lithium bromide absorption unit is connected to the high-temperature reaction gas outlet of the ammonia synthesis reactor. The primary gas-liquid plate-shell heat exchanger and the secondary gas-liquid plate-shell heat exchanger are connected in series on the cooling path of the high-temperature reaction gas to perform multi-stage cooling and recover its sensible and latent heat. The recovered heat energy is used to heat the working fluid in the heat source water circulation loop. The working fluid is used as a driving heat source or a low-temperature heat source and is reused in the lithium bromide unit and heating loop.

5. The amino-based multi-energy complementary energy storage and power generation system according to claim 4, characterized in that, The flue gas hot water type lithium bromide absorption chiller includes a high-pressure generator, a low-pressure generator, a condenser, an evaporator, and an absorber; The driving heat source for the high-pressure generator is high-temperature reaction gas at 450–500°C from the ammonia synthesis reactor. The driving heat source for the low-pressure generator is high-temperature hot water heated to 95°C by the first-stage gas-liquid plate-shell heat exchanger. The hot side of both the condenser and the absorber is connected to the heating circuit for cascade heating of the air conditioning water in the heating circuit.

6. The amino-based multi-energy complementary energy storage and power generation system according to claim 1, characterized in that, The control unit is configured to execute the following control logic: Real-time data collection is performed on the DC bus voltage, photovoltaic power generation, and real-time demand data of electrical and thermal loads of the photovoltaic-thermal integrated subsystem. The photovoltaic power generation is compared with the electrical load demand, and a mode switching command is sent to the ammonia energy subsystem based on the comparison result: when the photovoltaic power generation is greater than the electrical load demand, the command system enters the energy storage mode and controls the excess electrical energy to flow to the electrolysis hydrogen production and pressure swing adsorption nitrogen production device; when the photovoltaic power generation is less than the electrical load demand, the command system enters the energy release mode and controls the liquid ammonia storage tank to supply fuel to the direct ammonia fuel cell. Based on the heat load demand and the operating status of the waste heat cascade recovery subsystem and the DC vapor compression heat pump, the heat output distribution of each heating device is dynamically adjusted to optimize the overall thermal efficiency of the system. Maintain the stability of the DC bus voltage and perform voltage regulation and power matching of the DC power output from the direct ammonia fuel cell before grid connection.

7. A control method for an amino-based multi-energy complementary energy storage and power generation system, characterized in that, The method is applied to the amino-based multi-energy complementary energy storage power generation system as described in any one of claims 1-6, comprising: It receives light and heat energy from sunlight, and absorbs the heat energy and waste heat generated by photovoltaic power generation through a cooling medium to achieve active cooling of photovoltaic modules; Real-time monitoring of the photovoltaic power generation and real-time load demand of the system; Based on the matching relationship between the photovoltaic power generation and the electrical load demand, the system is controlled to switch operating modes.

8. The control method for the amino-based multi-energy complementary energy storage and power generation system according to claim 7, characterized in that, The absorption of the thermal energy and waste heat generated by photovoltaic power generation through a cooling medium includes: The cooling medium circulates in the channel on the back of the water-cooled photovoltaic module to absorb the waste heat generated when the photovoltaic cell is working, and controls the module temperature below a preset threshold to improve its power generation efficiency. The cooling medium, which absorbs waste heat and then heats up, is used as a low-temperature heat source and delivered to the evaporator side of a DC-type vapor compression heat pump.

9. The control method for the amino-based multi-energy complementary energy storage and power generation system according to claim 7, characterized in that, The step of controlling the system to switch operating modes based on the matching relationship between photovoltaic power generation and electrical load demand includes: The obtained photovoltaic power generation is compared with the real-time load demand; If the photovoltaic power generation exceeds the real-time load demand, the system is controlled to enter the working mode of sufficient photovoltaic ammonia energy storage. The light-sufficient ammonia energy storage mode includes: allocating surplus DC power to the ammonia energy subsystem to drive the electrolytic hydrogen production device to generate hydrogen, and driving the pressure swing adsorption nitrogen production device to separate nitrogen from the air. The generated hydrogen and nitrogen are mixed in a predetermined volume ratio and then transported to an ammonia synthesis reactor. Under the action of a catalyst, a synthesis reaction is carried out to generate ammonia, thus realizing the conversion and storage of electrical energy into chemical energy. The high-temperature reaction gas at the outlet of the ammonia synthesis reactor is subjected to waste heat recovery and utilization in stages: firstly, it is introduced into the flue gas hot water type lithium bromide absorption unit as a driving heat source, and then its sensible heat and latent heat are recovered step by step through at least two stages of gas-liquid plate and shell heat exchangers connected in series to heat the circulating working fluid in the system. Finally, the reaction gas is cooled and liquid ammonia is separated for storage.

10. The control method for the amino-based multi-energy complementary energy storage and power generation system according to claim 9, characterized in that, Also includes: If the photovoltaic power generation is not greater than the real-time load demand, the system is controlled to enter the working mode of insufficient light and ammonia energy release mode. The light-deficient ammonia energy release mode includes: vaporizing and purifying stored liquid ammonia to generate pure ammonia gas; The ammonia gas is delivered to the anode of the direct ammonia fuel cell, where it undergoes an electrochemical oxidation reaction under the action of an alkaline electrolyte and an anode catalyst, releasing electrons and generating nitrogen and water. Air is delivered to the cathode of the fuel cell, where oxygen undergoes a reduction reaction with electrons flowing in from the external circuit and components in the electrolyte under the action of the cathode catalyst. The electrolyte enables the directional migration of ions to maintain the charge balance inside the battery; at the same time, the electrons released from the anode flow through the external circuit to form a current and output DC power. The waste heat and unreacted ammonia generated during the operation of the fuel cell are recovered and processed, realizing the recycling of materials and energy within the system.

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