Green high-efficiency hydrogen energy storage and transportation system and method for thermal-hydrogen synergistic-parallel energy storage

Abstract

The invention discloses a green high-efficiency hydrogen energy storage and transportation system and method for thermal hydrogen synergistic-parallel energy storage. The system comprises a carbon dioxide high-temperature heat pump adjusting unit which is connected with a thermal hydrogen reactor; a compressor is arranged in the carbon dioxide high-temperature heat pump adjusting unit and connected with a gas cooler in series, the gas cooler is connected with a heat regenerator in series, the heat regenerator is connected with an electronic expansion valve in series, the electronic expansion valve is connected with a gas heater in series, the gas heater is connected with an electronic adjusting valve in series, and the electronic adjusting valve is connected with a mixing pipe and the low-pressure side of the heat regenerator in parallel. The low-pressure side of the heat regenerator is connected with a mixing pipe in series, the mixing pipe is connected with a compressor in series, and the compressor, the electronic expansion valve and the electronic adjusting valve are all connected with a PID control module. The hot hydrogen reactor is connected with a cold side outlet of the gas cooler and a hot side inlet of the gas heater. The carbon dioxide heat pump is used for assisting in recycling waste heat generated by the reaction, high-temperature carbon dioxide is produced to supply heat to the reaction, hot hydrogen cooperation-parallel energy storage is achieved, and electric energy consumption and waste heat waste in chemical hydrogen storage are reduced.

Description

Technical Field

[0001] The present invention belongs to the field of energy storage, and in particular to a green hydrogen energy efficient storage, transportation and utilization system and method for thermal-hydrogen synergistic-parallel energy storage. Background Art

[0002] With the rapid development of the new energy industry, in order to meet the time-domain matching requirements of new energy power and the energy consumption side, various large-scale and long-duration energy storage technologies have emerged continuously. Among many energy storage technologies, the green hydrogen energy industry has attracted much attention from all walks of life due to its advantages such as high energy density, long energy storage time, long-distance transportability, complete consumption of new energy power output, and adaptability to various energy terminals.

[0003] Currently, chemical hydrogen storage solutions such as solid metal material hydrogen storage and ammonia synthesis hydrogen storage show advantages in small and medium-scale storage and transportation scenarios due to their high energy storage density and stable transportation characteristics. However, hydrogen storage methods based on chemical reactions inevitably involve significant exothermic and endothermic phenomena in the hydrogen absorption and dehydrogenation reactions. At the same time, chemical hydrogen storage solutions generally require a high-temperature thermal environment to achieve the thermal catalysis of chemical reactions, usually using electric heating or direct combustion of fossil energy to supply the high-temperature environment required for the reaction. This process will also cause significant energy consumption or equivalent carbon emissions. For example, for solid-phase metal material hydrogen storage and ammonia synthesis hydrogen storage technologies, the hydrogen absorption reaction is an exothermic process. By consuming electrical energy, an electric heater is used to provide a high-temperature environment. During the reaction, solid-phase hydrides are obtained while a large amount of low-temperature waste heat is released. The dehydrogenation reaction is an endothermic process. By consuming electrical energy, an electric heater is used to provide a high-temperature environment. During the reaction, hydrogen is obtained while a large amount of high-temperature heat energy is absorbed. Since the long-distance transportation of the heat storage module is not economical, a large amount of low-temperature waste heat is generally dissipated during the hydrogen absorption process, and additional heating is generally required during the dehydrogenation process. Both processes result in significant energy losses or energy consumption.

[0004] Considering the scenarios of high-temperature heat supply and low-temperature waste heat dissipation in the above chemical reaction processes, if the coupling of the hydrogen energy storage-release process and the heat pump technology can be realized, absorbing low-temperature waste heat and supplying a high-temperature thermal environment during the hydrogen absorption process; while absorbing air energy and providing a high-temperature thermal environment during the dehydrogenation process, it will greatly reduce the waste heat waste in the hydrogen absorption process and the electrical energy consumption in the hydrogen absorption / dehydrogenation process, which is equivalent to realizing the collaborative storage of heat and hydrogen energy. However, the current heat pump technology is not sufficient to provide a high-temperature thermal environment of about 300°C under the heat source conditions of ambient temperature or 50°C waste heat temperature, which is the main bottleneck restricting the "thermal-hydrogen synergistic and parallel energy storage" technology. Summary of the Invention

[0005] The purpose of the present invention is to provide a green hydrogen energy efficient storage, transportation and utilization system and method for thermal-hydrogen synergistic-parallel energy storage, so as to solve the problem that the existing heat pump technology is not sufficient to provide a high-temperature thermal environment.

[0006] To achieve the above object, the present invention is implemented by the following technical solutions: A green hydrogen energy efficient storage and transportation system with thermal hydrogen synergistic - parallel energy storage, comprising a carbon dioxide high - temperature heat pump regulation unit and a thermal hydrogen reactor, wherein the carbon dioxide high - temperature heat pump regulation unit is connected to the thermal hydrogen reactor; A compressor is provided in the carbon dioxide high - temperature heat pump regulation unit. The high - pressure side outlet of the compressor is connected in series with the hot - side inlet of a gas cooler. The hot - side outlet of the gas cooler is connected in series with the high - pressure side inlet of a regenerator. The high - pressure side outlet of the regenerator is connected in series with the high - pressure side inlet of an electronic expansion valve. The low - pressure side outlet of the electronic expansion valve is connected in series with the cold - side inlet of a gas heater. The cold - side outlet of the gas heater is connected in series with the high - pressure side inlet of an electronic regulating valve. The low - pressure side outlet of the electronic regulating valve is connected in parallel with a mixing pipe and the low - pressure side of the regenerator. The low - pressure side outlet of the electronic regulating valve is connected in series with the inlet of the mixing pipe. The low - pressure side outlet of the electronic regulating valve is connected in series with the low - pressure side inlet of the regenerator. The low - pressure side outlet of the regenerator is connected in series with the inlet of the mixing pipe. The outlet of the mixing pipe is connected in series with the low - pressure side inlet of the compressor. The compressor, the electronic expansion valve, and the electronic regulating valve are all connected to a PID control module; The thermal hydrogen reactor is connected to the cold - side outlet of the gas cooler and the hot - side inlet of the gas heater.

[0007] Furthermore, a compressor suction temperature sensor is provided on the pipeline of the low - pressure side inlet of the compressor, and a compressor discharge temperature sensor and a compressor discharge pressure sensor are provided on the pipeline of the high - pressure side outlet of the compressor.

[0008] Furthermore, a gas cooler hot - side exhaust temperature sensor is provided on the pipeline of the hot - side outlet of the gas cooler.

[0009] Furthermore, a gas heater cold - side exhaust temperature sensor and a gas heater cold - side exhaust pressure sensor are provided on the pipeline of the cold - side outlet of the gas heater.

[0010] Furthermore, the PID control module includes a compressor discharge pressure PID controller, a compressor suction temperature PID controller, a gas heater exhaust pressure PID controller, and a differential method PID controller. The compressor discharge pressure PID controller, the compressor suction temperature PID controller, and the gas heater exhaust pressure PID controller are all connected to the differential method PID controller. The compressor discharge pressure PID controller is connected to the compressor and an adjustable electronic expansion valve. The compressor suction temperature PID controller is connected to an adjustable electronic regulating valve. The gas heater exhaust pressure PID controller is connected to the electronic expansion valve.

[0011] A method for efficient storage and transportation of green hydrogen energy with thermal hydrogen synergistic - parallel energy storage for the above - mentioned system, comprising: According to the requirements of the hot hydrogen reactor, the high-temperature carbon dioxide heat pump regulation unit switches between the waste heat source heating mode and the air source heating mode in real time. By adjusting the rotational speed of the compressor, the opening degree of the electronic expansion valve, and the flow splitting ratio of the electronic regulating valve through the PID control module, the heating temperature of the high-temperature carbon dioxide heat pump regulation unit is dynamically adjusted and optimized to achieve adaptive regulation of the system.

[0012] Furthermore, the waste heat source heating mode corresponds to the supercritical carbon dioxide cycle condition, and the compressor produces high-grade carbon dioxide to feedback high-temperature heat for the hydrogen storage reaction. The air source heating mode corresponds to the transcritical carbon dioxide cycle condition, and the compressor produces high-grade carbon dioxide to provide high-temperature heat for the hydrogen release reaction.

[0013] Furthermore, the adaptive regulation of the system includes: In the waste heat source heating mode, the rotational speed of the compressor is adjusted by the compressor discharge pressure PID controller to make the discharge pressure of the compressor reach the optimized value. The opening degree of the electronic expansion valve is adjusted by the gas heater discharge pressure PID controller to make the discharge pressure of the gas heater reach the optimized value. The flow splitting ratio of the electronic regulating valve is adjusted by the compressor suction temperature PID controller to make the suction temperature of the compressor reach the optimized value. In the air source heating mode, the opening degree of the electronic expansion valve is adjusted by the compressor discharge pressure PID controller to make the discharge pressure of the compressor reach the optimized value. The flow splitting ratio of the electronic regulating valve is adjusted by the compressor suction temperature PID controller to make the suction temperature of the compressor reach the optimized value.

[0014] Furthermore, in the waste heat source heating mode, the compressor discharge pressure PID controller obtains the optimized discharge temperature value and the optimized discharge pressure value according to the set discharge temperature value of the compressor and the actual discharge pressure of the compressor, and makes the discharge pressure of the compressor approach the optimized value by adjusting the rotational speed of the compressor. The gas heater discharge pressure PID controller obtains the optimized discharge temperature value and the optimized discharge pressure value of the gas heater according to the set discharge temperature value of the compressor and the actual discharge pressure of the gas heater, and makes the discharge pressure of the gas heater approach the optimized value by adjusting the opening degree of the electronic expansion valve. The compressor suction temperature PID controller obtains the optimized discharge temperature value and the optimized suction temperature value according to the set discharge temperature value of the compressor and the actual suction temperature of the compressor, and makes the suction temperature of the compressor approach the optimized value by adjusting the flow splitting ratio of the electronic regulating valve.

[0015] Further, in the air source heating mode, the compressor suction temperature PID controller obtains the optimized exhaust temperature value and the optimized suction temperature value according to the set exhaust temperature of the compressor and the actual suction temperature of the compressor, and adjusts the split ratio of the electronic regulating valve to make the suction temperature of the compressor approach the optimized value; The compressor discharge pressure PID controller obtains the optimized exhaust temperature value and the optimized discharge pressure value according to the set exhaust temperature of the compressor and the actual discharge pressure of the compressor, and adjusts the opening degree of the electronic expansion valve to make the discharge pressure of the compressor approach the optimized value.

[0016] Compared with the prior art, the present invention has the following beneficial effects: The present invention provides a green hydrogen energy efficient storage and transportation system with thermal-hydrogen synergistic-parallel energy storage. By connecting a high-temperature carbon dioxide heat pump regulating unit to a thermal-hydrogen reactor, a compressor is arranged in the high-temperature carbon dioxide heat pump regulating unit. The compressor is connected in series with a gas cooler, the gas cooler is connected in series with a regenerator, the regenerator is connected in series with an electronic expansion valve, the electronic expansion valve is connected in series with a gas heater, the gas heater is connected in series with an electronic regulating valve, the electronic regulating valve is connected in parallel with a mixing pipe and the low-pressure side of the regenerator, the low-pressure side of the regenerator is connected in series with the mixing pipe, the mixing pipe is connected in series with the compressor, and both the compressor and the gas heater are connected to a PID control module; the thermal-hydrogen reactor is connected to the cold-side outlet of the gas cooler and the hot-side inlet of the gas heater. In the chemical hydrogen storage scenario of the present invention, the hydrogen storage reaction needs to absorb high-grade heat to promote the efficient progress of the hydrogen absorption reaction. During the reaction, the corresponding hydride is obtained and a large amount of low-temperature waste heat is released. In this process, the high-temperature carbon dioxide heat pump regulating unit is put into operation, and the waste heat is recycled to make the high-temperature carbon dioxide heat pump regulating unit become a waste heat source heat pump, corresponding to the working mode of a supercritical carbon dioxide waste heat source heat pump. At the same time, the heat pump compressor produces high-grade carbon dioxide to feedback high-temperature heat for the hydrogen storage reaction; in the chemical hydrogen release scenario, the hydrogen release reaction needs to absorb high-grade heat to promote the efficient progress of the dehydrogenation reaction. During the reaction, hydrogen and by-products are obtained. In this process, the high-temperature carbon dioxide heat pump regulating unit is put into operation, and air is used to make the high-temperature carbon dioxide heat pump regulating unit become an air source heat pump, corresponding to the working mode of a transcritical carbon dioxide air source heat pump. At the same time, the heat pump compressor produces high-grade carbon dioxide to provide high-temperature heat for the hydrogen release reaction. The present invention can reduce the degree of a large amount of electric energy consumption and waste heat energy waste in the chemical hydrogen storage technology chain, use a carbon dioxide heat pump to assist in recycling the waste heat generated during the hydrogen absorption process, produce high-temperature carbon dioxide for heating chemical reactions, and achieve thermal-hydrogen synergistic-parallel energy storage. Even when put into operation as an air source heat pump, the regulating system can provide carbon dioxide with a temperature of 150 °C or even higher. Compared with high-energy-consuming heating methods such as electric heaters or fuel combustion, the present invention has obvious advantages. The present invention can replace traditional heating methods such as electric heating below 300 °C or primary energy fuel combustion heating in chemical hydrogen storage technology. The present invention flexibly utilizes waste heat energy and air energy to provide heating heat below 300 °C with an electro-thermal conversion efficiency of 1.5 to 3.5, far exceeding the traditional electric heating method, and is expected to bring a continuous, efficient and economical green hydrogen energy efficient storage and transportation solution for the industrial chemical hydrogen storage field.

[0017] The present invention also provides a green hydrogen energy efficient storage and transportation method for thermal hydrogen synergistic - parallel energy storage. First, according to the characteristics and requirements of chemical hydrogen storage technology, the carbon dioxide high - temperature heat pump regulation unit adjusts the rotational speed of the compressor and the opening of the electronic expansion valve, and switches between the two heating modes of waste heat source heating and air source heating in real - time, corresponding to the supercritical carbon dioxide cycle condition and the transcritical carbon dioxide cycle condition respectively, effectively changing the compression ratio of the compressor in the system and realizing the adaptive regulation of the heat recovery amount of the regenerator. Secondly, the present invention realizes the flexible regulation of the heating temperature of the heat pump unit, enabling the system to operate quickly and efficiently in different modes. With the PID control algorithm, according to the real - time working state and environmental conditions of the system, the opening of the electronic expansion valve and the splitting ratio of the electronic regulating valve are adjusted to dynamically adjust the system control parameters, realizing the precise control of the system and optimizing the performance of the system to the greatest extent. In the present invention, under the two different working modes, the compression ratio and exhaust temperature of the compressor change greatly, resulting in unstable heating temperature. By setting the splitting ratio of the electronic regulating valve and assisting with a certain control algorithm to control the heat recovery amount, the stability of the exhaust temperature is ensured, and the stability and heating effect of the system are improved. The regulation system of the present invention adopts an advanced PID control algorithm with a fast response speed. Combining with the real - time monitoring of the working state and environmental conditions of the system, it can achieve a fast response to the system and ensure the efficient operation of the system. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for use in the embodiments will be briefly introduced below. It should be understood that the following drawings only show some embodiments of the present invention and should not be regarded as limiting the scope. For those of ordinary skill in the art, without creative efforts, other related drawings can also be obtained based on these drawings.

[0019] Figure 1 It is a schematic diagram of the system structure under the hydrogen absorption process of the present invention.

[0020] Figure 2 It is a schematic diagram of the system structure under the dehydrogenation process of the present invention.

[0021] Figure 3 It is a schematic diagram of the PID control module under the hydrogen absorption process of the present invention.

[0022] Figure 4 It is a schematic diagram of the PID control module under the dehydrogenation process of the present invention.

[0023] Wherein: a - compressor, b - gas cooler, c - regenerator, d - electronic expansion valve, e - gas heater, f - electronic regulating valve, g - mixing pipe, h - compressor suction temperature sensor, i - compressor discharge temperature sensor, j - compressor discharge pressure sensor, k - hot-side discharge temperature sensor of the gas cooler, l - cold-side discharge temperature sensor of the gas heater, m - cold-side discharge pressure sensor of the gas heater. Specific embodiments

[0024] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are some, but not all, of the embodiments of the present invention. Usually, the components of the embodiments of the present invention described and illustrated in the accompanying drawings here can be arranged and designed in various different configurations.

[0025] Therefore, the following detailed description of the embodiments of the present invention provided in the accompanying drawings is not intended to limit the scope of the claimed present invention, but merely represents selected embodiments of the present invention. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present invention without creative efforts shall fall within the scope of protection of the present invention.

[0026] It should be noted that: like reference numerals and letters denote like items in the following drawings. Therefore, once an item is defined in one drawing, it does not need to be further defined and explained in subsequent drawings.

[0027] In the description of the embodiments of the present invention, it should be noted that if terms such as "upper", "lower", "horizontal", "inner", etc. are used to indicate the orientation or positional relationship, it is based on the orientation or positional relationship shown in the accompanying drawings, or the orientation or positional relationship in which the product of the present invention is usually placed during use. It is only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be construed as a limitation of the present invention. In addition, terms such as "first", "second", etc. are only used for distinguishing descriptions and cannot be construed as indicating or implying relative importance.

[0028] In addition, if the term "horizontal" appears, it does not mean that the component is required to be absolutely horizontal, but it can be slightly inclined. For example, "horizontal" only means that its direction is more horizontal relative to "vertical", and does not mean that the structure must be completely horizontal, but it can be slightly inclined.

[0029] In the description of the embodiments of the present invention, it should also be noted that unless otherwise clearly specified and limited, the terms "set", "installed", "connected", and "coupled" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the communication inside two components. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood according to specific situations.

[0030] The present invention will be further described in detail below with reference to the accompanying drawings: See Figure 1 and Figure 2 , the present invention provides a green hydrogen energy efficient storage and transportation system for thermal hydrogen synergistic - parallel energy storage, including a carbon dioxide high - temperature heat pump regulation unit and a thermal hydrogen reactor, and the carbon dioxide high - temperature heat pump regulation unit is connected to the thermal hydrogen reactor. The thermal hydrogen reactor is based on chemical hydrogen storage technologies such as solid - phase metal material hydrogen storage and ammonia synthesis hydrogen storage, and utilizes the carbon dioxide high - temperature heat pump regulation system to assist in operation.

[0031] The carbon dioxide high - temperature heat pump regulation unit includes a compressor a, a gas cooler b, a regenerator c, an electronic expansion valve d, a gas heater e, an electronic regulating valve f, a mixing pipe g, and a PID control module. The high - pressure side outlet of the compressor a is serially connected to the hot - side inlet of the gas cooler b, the hot - side outlet of the gas cooler b is serially connected to the high - pressure side inlet of the regenerator c, the high - pressure side outlet of the regenerator c is serially connected to the high - pressure side inlet of the electronic expansion valve d, the low - pressure side outlet of the electronic expansion valve d is serially connected to the cold - side inlet of the gas heater e, the cold - side outlet of the gas heater e is serially connected to the high - pressure side inlet of the electronic regulating valve f, the low - pressure side outlet of the electronic regulating valve f is parallelly connected to two pipelines. One of them is directly serially connected to the inlet of the mixing pipe g, and the other is serially connected to the low - pressure side inlet of the regenerator c. The low - pressure side outlet of the regenerator c is serially connected to the inlet of the mixing pipe g, and the outlet of the mixing pipe g is serially connected to the low - pressure side inlet of the compressor.

[0032] The compressor a, the electronic expansion valve d, and the electronic regulating valve f are all connected to the PID control module. The PID control module includes a compressor discharge pressure PID controller, a compressor suction temperature PID controller, a gas heater discharge pressure PID controller, and a differential method PID controller. The compressor discharge pressure PID controller, the compressor suction temperature PID controller, and the gas heater discharge pressure PID controller are all connected to the differential method PID controller. The compressor discharge pressure PID controller is connected to the compressor a and the regulating electronic expansion valve d, the compressor suction temperature PID controller is connected to the regulating electronic regulating valve f, and the gas heater discharge pressure PID controller is connected to the electronic expansion valve d.

[0033] The hot hydrogen reactor connects the cold-side outlet of the gas cooler b and the hot-side inlet of the gas heater e. For the hydrogen absorption process, the waste heat of the chemical reaction in the hot hydrogen reactor is used as the heat source of the heat pump. At this time, the regulating system is a supercritical carbon dioxide heat pump, and the system uses the high-temperature carbon dioxide discharged by the compressor to provide high-grade heat for the hydrogen absorption reaction in the hot hydrogen reactor; for the dehydrogenation process, ambient air is used as the heat source of the heat pump. At this time, the regulating system is a transcritical carbon dioxide heat pump, and the system uses the high-temperature carbon dioxide discharged by the compressor to provide high-grade heat for the dehydrogenation reaction in the hot hydrogen reactor.

[0034] On the pipeline at the high-pressure side outlet of the compressor a, a compressor exhaust temperature sensor i and an exhaust pressure sensor j are respectively connected to monitor the temperature and pressure of the carbon dioxide working medium. Then the working medium enters the gas cooler b. A temperature sensor k is connected to the pipeline at the hot-side outlet of the gas cooler b. Then the working medium passes through the regenerator c, the electronic expansion valve d, and the gas heater e in sequence. A temperature sensor l and a pressure sensor m are connected to the pipeline at the cold-side outlet of the gas heater e. The working medium flows into the electronic regulating valve f for splitting. Part of the working medium directly flows into the mixing pipe g, and the other part of the working medium flows into the low-pressure side inlet of the regenerator c, absorbs the recovered heat, and then enters the mixing pipe g. Finally, the working medium is fully mixed in the mixing pipe g and flows to the inlet of the compressor a to participate in the subsequent cycle.

[0035] During the hydrogen absorption process, corresponding to the supercritical carbon dioxide cycle condition, the rotational speed of the compressor a controls the outlet pressure of the compressor a, that is, the pressure value monitored by the pressure sensor j; the opening degree of the electronic expansion valve d controls the pressure at the cold-side outlet of the gas heater e, that is, the pressure value detected by the pressure sensor m; the splitting ratio of the electronic regulating valve f controls the suction temperature of the compressor a, that is, the temperature value monitored by the temperature sensor h.

[0036] During the dehydrogenation process, corresponding to the transcritical carbon dioxide cycle condition, the opening degree of the electronic expansion valve d controls the outlet pressure of the compressor a, that is, the pressure value monitored by the pressure sensor j; the splitting ratio of the electronic regulating valve f controls the suction temperature of the compressor a, that is, the temperature value monitored by the temperature sensor h.

[0037] See Figure 3 and Figure 4 , the green hydrogen energy efficient storage and transportation method of hot hydrogen synergistic-parallel energy storage of the present invention includes: In the chemical hydrogen storage scenario, the hydrogen storage reaction needs to absorb high-grade heat to promote the efficient progress of the hydrogen absorption reaction. The corresponding hydride is obtained during the reaction and a large amount of low-temperature waste heat is released. During the process, the carbon dioxide heat pump recovers and utilizes the waste heat to make the heat pump become a waste heat source heat pump, corresponding to the supercritical carbon dioxide cycle condition. At the same time, the heat pump compressor produces high-grade carbon dioxide to feedback high-temperature heat to the hydrogen storage reactor; In the chemical hydrogen release scenario, the hydrogen release reaction requires the absorption of high-grade heat to promote the efficient dehydrogenation reaction. Hydrogen and by-products are obtained during the reaction. During this process, the carbon dioxide heat pump system is put into operation, and air is used to make the heat pump an air-source heat pump, corresponding to the working mode of a transcritical carbon dioxide air-source heat pump. At the same time, the heat pump compressor produces high-grade carbon dioxide to provide high-temperature heat for the hydrogen release reactor.

[0038] In the chemical hydrogen storage scenario, when operating in the waste heat source heating mode, the rotational speed of compressor a is adjusted by the compressor discharge pressure PID controller to make the discharge pressure of compressor a reach the optimized value; the opening degree of electronic expansion valve d is adjusted by the gas heater discharge pressure PID controller to make the discharge pressure of gas heater e reach the optimized value; the split ratio of electronic regulating valve f is adjusted by the compressor suction temperature PID controller to make the suction temperature of compressor a reach the optimized value. In the chemical hydrogen release scenario, when operating in the air-source heating mode, the opening degree of electronic expansion valve d is adjusted by the compressor discharge pressure PID controller to make the discharge pressure of compressor a reach the optimized value; the split ratio of electronic regulating valve f is adjusted by the compressor suction temperature PID controller to make the suction temperature of compressor a reach the optimized value. The optimal values of the above compressor discharge pressure, suction temperature, and gas heater discharge pressure are all coupled and optimized with the ultimate goal of the heat pump heating temperature, and the optimized values under the real-time operating state of the system are obtained according to the actual hydrogen storage technology requirements.

[0039] During the operation of the waste heat source heating mode, the compressor discharge pressure PID controller obtains the optimized values of the discharge temperature and discharge pressure based on the set value of the discharge temperature of compressor a and the actual discharge pressure of compressor a, and adjusts the rotational speed of compressor a through the compressor discharge pressure PID controller to make the discharge pressure of compressor a approach the optimized value.

[0040] The compressor discharge pressure PID controller uses differential method PID control, and the calculation formula is:

[0041] where, Δ P is the difference between the current compressor discharge pressure and the optimized value of the discharge pressure, n is the number of operations, K P 、 K I and K D are the proportional adjustment coefficient, integral adjustment coefficient, and differential adjustment coefficient respectively, and their values are K P = 5×10 -4 , K I = 5×10-1 , and K D = 5×10 -1 .

[0042] During the operation of the waste heat source heating mode, the gas heater exhaust pressure PID controller obtains the optimized exhaust temperature value and the optimized exhaust pressure value of the gas heater e based on the set exhaust temperature of the compressor a and the actual exhaust pressure of the gas heater e, and adjusts the opening of the electronic expansion valve d through the gas heater exhaust pressure PID controller to make the exhaust pressure of the gas heater e approach the optimized value.

[0043] The gas heater exhaust pressure PID controller uses differential method PID control, and the calculation formula is:

[0044] where, Δ P is the difference between the current exhaust pressure of the gas heater and the optimized exhaust pressure value, n is the number of operations, K P , K I and K D are the proportional adjustment coefficient, integral adjustment coefficient and differential adjustment coefficient respectively, and their values are K P = 1×10 -12 , K I = 5×10 -2 , and K D = 3×10 -2 .

[0045] During the operation of the waste heat source heating mode or the air source heating mode, the compressor suction temperature PID controller obtains the optimized exhaust temperature value and the optimized suction temperature value based on the set exhaust temperature of the compressor a and the actual suction temperature of the compressor a, and adjusts the split ratio of the electronic control valve f through the compressor suction temperature PID controller to make the suction temperature of the compressor a approach the optimized value.

[0046] The compressor suction temperature PID controller uses differential method PID control, and the calculation formula is

[0047] where, Δ T is the difference between the current suction temperature of the compressor and the optimized suction temperature value, n is the number of operations, K P , K I andK D are the proportional adjustment coefficient, the integral adjustment coefficient, and the differential adjustment coefficient, with values of K P = 1×10 -1 , K I = 1, and K D = 2×10 -1 .

[0048] During the operation of the air source heating mode, the compressor discharge pressure PID controller obtains the optimized discharge temperature value and the optimized discharge pressure value based on the set discharge temperature of compressor a and the actual discharge pressure of compressor a, and adjusts the opening of electronic expansion valve d through the compressor discharge pressure PID controller, so that the discharge pressure of compressor a approaches the optimized value.

[0049] The compressor discharge pressure PID controller adopts differential method PID control, and the calculation formula is:

[0050] where, Δ P is the difference between the current compressor discharge pressure and the optimized discharge pressure value, n is the number of operation times, K P , K I and K D are the proportional adjustment coefficient, the integral adjustment coefficient, and the differential adjustment coefficient, with values of K P = K P = 1×10 -15 , K I = 4×10 -2 , and K D = 3×10 -2 .

[0051] The following further describes the present invention in detail through specific embodiments: Embodiment 1: In this embodiment, the adaptive control method of the green hydrogen energy efficient storage and transportation method with hot hydrogen synergy - parallel energy storage in different working modes includes: During the hydrogen absorption process, the adaptive adjustment of the discharge pressure of compressor a under the supercritical carbon dioxide cycle condition: the discharge pressure of compressor a ( P ) and the waste heat source temperature ( T wt ) and the suction temperature ( T1) etc. Aiming at improving the coefficient of performance ( COP hp ) of the heat pump system, an association formula between the exhaust pressure and these variables is established, P 2 = f ( T 1, T wt ). Taking the rotational speed of compressor a as the input variable, the compressor exhaust pressure PID controller outputs the adjustment value of the compressor exhaust pressure. According to the dynamic characteristics of the system, three parameters of the differential method PID control K P , K I and K D are determined. After the system goes through a cycle, if the difference in exhaust pressure before and after the cycle is greater than the design accuracy, the difference between the two is used as the input parameter and input into the PID controller. The compressor exhaust pressure PID controller calculates the control quantity according to the error of the input parameter and adjusts the exhaust pressure of compressor a to make the system performance reach the best.

[0052] During the hydrogen absorption process, the adaptive adjustment of the exhaust pressure of the gas heater under the supercritical carbon dioxide cycle condition: The cold-side exhaust pressure of gas heater e ( P 7) is related to the waste heat source temperature ( T wt ) and the cold-side suction temperature of gas heater e ( T 6), etc. Aiming at stabilizing the pressure of the working medium at the cold-side outlet of gas heater e, an association formula between the exhaust pressure of gas heater e and these variables is established, P 7 = f ( T 6, T wt ). Taking the opening degree of electronic expansion valve d as the input variable, the gas heater exhaust pressure PID controller outputs the adjustment value of the cold-side exhaust pressure of gas heater e. According to the dynamic characteristics of the system, three parameters of the differential method PID control K P , K I and K D are determined. After the system goes through a cycle, if the difference in exhaust pressure before and after the cycle is greater than the design accuracy, the difference between the two is used as the input parameter and input into the gas heater exhaust pressure PID controller. The gas heater exhaust pressure PID controller calculates the control quantity according to the error of the input parameter and adjusts the exhaust pressure of gas heater e to make the system performance reach stability.

[0053] During the hydrogen absorption or dehydrogenation process, the adaptive regulation of the suction temperature of compressor a under supercritical or transcritical carbon dioxide cycle conditions: The suction temperature of compressor a ( T 1) is related to the temperature of the waste heat source ( T wt ) and the suction pressure ( P 1), etc. With the goal of improving the coefficient of performance ( COP hp ) of the heat pump system, an association formula between the suction temperature and these variables is established, T 1 = f ( P 1, T wt ). Taking the split ratio of electronic control valve f as the input variable, the compressor suction temperature PID controller outputs the adjustment value of the suction temperature of compressor a, and determines the three parameters of differential PID control according to the dynamic characteristics of the system K P , K I and K D . After the system goes through a cycle, if the difference in suction temperature before and after the cycle is greater than the design accuracy, the difference between the two is used as the input parameter and input into the compressor suction temperature PID controller. The compressor suction temperature PID controller calculates the control quantity according to the error of the input parameter and adjusts the suction temperature of compressor a to make the system performance reach the best.

[0054] During the dehydrogenation process, the adaptive regulation of the discharge pressure of compressor a under transcritical carbon dioxide cycle conditions: The discharge pressure of compressor a ( P 2) is related to the evaporation pressure ( P 7) and the suction temperature of compressor a ( T 1), etc. With the goal of improving the coefficient of performance ( COP hp ) of the heat pump system, an association formula between the discharge pressure and these variables is established, P 2 = f ( P 7, T 1). Taking the opening degree of electronic expansion valve d as the input variable, the compressor discharge pressure PID controller outputs the adjustment value of the discharge pressure of compressor a, and determines the three parameters of differential PID control according to the dynamic characteristics of the system K P , K I and K DAfter the system goes through a cycle, if the difference in the exhaust pressure before and after the cycle is greater than the design accuracy, the difference between the two is used as an input parameter and input into the compressor exhaust pressure PID controller. The compressor exhaust pressure PID controller calculates the control quantity based on the error of the input parameter and adjusts the exhaust pressure of compressor a to optimize the system performance.

[0055] The control method for optimizing the compressor exhaust pressure, the exhaust pressure on the cold side of the gas heater, and the compressor suction temperature in this embodiment is an adjustment method based on the PID control module. During operation, the set value of the PID control module is set by calculating the optimal value under the current operating conditions of the system. At the same time, temperature and pressure sensors are used to monitor the compressor exhaust pressure and suction temperature, the exhaust temperature on the hot side of the gas cooler, the exhaust temperature and exhaust pressure on the cold side of the gas heater.

[0056] The above PID control module adjusts the supercritical or transcritical carbon dioxide cycle conditions through 4 PID controllers: Under supercritical carbon dioxide cycle conditions, the compressor exhaust pressure ( P 2) The PID controller, with the input quantity being the waste heat source temperature of compressor a ( T wt ) and the suction temperature ( T 1), etc., and the output quantity being the rotational speed of compressor a; The exhaust pressure of the gas heater ( P 7) The PID controller, with the input quantity being the waste heat source temperature ( T wt ) and the cold side suction temperature of gas heater e ( T 6), etc., and the output quantity being the opening degree of electronic expansion valve d; Under supercritical or transcritical carbon dioxide cycle conditions, the compressor suction temperature ( T 1) The PID controller, with the input quantity being the waste heat source temperature ( T wt ) and the suction pressure ( P 1), etc., and the output quantity being the split ratio of electronic regulating valve f; Under transcritical carbon dioxide cycle conditions, the compressor exhaust pressure ( P 2) The PID controller, with the input quantity being the evaporation pressure ( P 7) and the suction temperature of compressor a ( T 1), etc., and the output quantity being the opening degree of electronic expansion valve d.

[0057] In this embodiment, on the premise of ensuring the heating temperature, with the goal of improving the coefficient of performance ( COP hp ) of the heat pump system, the rotational speed of compressor a, the opening degree of electronic expansion valve d, and the split ratio of electronic regulating valve f are feedback - adjusted through the PID control module, so that the system is in the best operating state and the heating temperature is stable.

[0058] For the above-mentioned green hydrogen energy efficient storage and transportation method of thermal hydrogen synergistic-parallel energy storage, the performance optimization control method provided in this embodiment is as follows: During the hydrogen absorption process, control of the discharge pressure of compressor a under the supercritical carbon dioxide cycle condition: First step, referring to the set value of the heating temperature ( T supply ), according to the set value of the discharge pressure of compressor a, calculate the optimized value of the discharge pressure. When the discharge pressure is less than 30 MPa, the optimization formula for the discharge pressure of compressor a is:

[0059] Among them, P 2 is the discharge pressure, P 1 is the suction pressure, R h is the regeneration rate, n is the compressor speed, T 1 is the suction temperature, T 2 is the discharge temperature.

[0060] Second step, compare the obtained optimized value of the discharge pressure ( P 2,opt ) with the actual discharge pressure ( P 2), and control it by the speed of compressor a. When P 2 > P 2,opt + ε, reduce the speed of compressor a; conversely, when P 2 < P 2,opt - ε, increase the speed of compressor a; when P 2,opt – ε ≤ P 2 ≤ P 2,opt + ε, keep the speed of compressor a unchanged, and ε is the allowable error precision value.

[0061] Third step, use a PID controller to make the discharge pressure of compressor a approach the set value. The PID controller for the compressor discharge pressure is controlled by the differential method PID, and the calculation formula is:

[0062] Among them, Δ P is the difference between the current compressor discharge pressure and the optimized value of the discharge pressure, n is the number of operations, K P , K I and K DThey are the proportional adjustment coefficient, the integral adjustment coefficient, and the differential adjustment coefficient, with values of K P = 5×10 -4 , K I = 5×10 -1 , and K D = 5×10 -1 .

[0063] During the hydrogen absorption process, control of the cold-side exhaust pressure of the gas heater e under the supercritical carbon dioxide cycle condition: First step, referring to the set value of the heating temperature ( T supply ), according to the set value of the cold-side exhaust pressure of the gas heater e, calculate and obtain the optimized value of the exhaust pressure. When the waste heat source temperature is less than or equal to 200 °C, the optimization formula for the cold-side exhaust pressure of the gas heater e is:

[0064] Where, P 2 is the exhaust pressure, P 1 is the suction pressure, R h is the regenerative rate, n is the compressor speed, T 1 is the suction temperature, T wt is the waste heat temperature.

[0065] Second step, compare the obtained optimized value of the exhaust pressure ( P 7,opt ) with the actual exhaust pressure ( P 7), and control it by the opening degree of the electronic expansion valve d. When P 7 > P 7,opt + ε, reduce the opening degree of the electronic expansion valve d; conversely, when P 7 < P 7,opt - ε, increase the opening degree of the electronic expansion valve d; when P 7,opt –ε ≤ P 7 ≤ P 7,opt + ε, keep the opening degree of the electronic expansion valve d unchanged, and ε is the allowable error precision value.

[0066] Third step, use a PID controller to make the exhaust pressure of the gas heater e approach the set value. The PID controller for the exhaust pressure of the gas heater uses differential method PID control, and the calculation formula is:

[0067] wherein, Δ P is the difference between the current exhaust pressure of the gas heater and the optimized exhaust pressure value, n is the number of operations, K P 、 K I and K D are the proportional adjustment coefficient, the integral adjustment coefficient, and the derivative adjustment coefficient respectively, and their values are K P = 1×10 -11 , K I = 5×10 -2 , and K D = 3×10 -2 .

[0068] During the hydrogen absorption or dehydrogenation process, control of the suction temperature of the compressor under supercritical or transcritical carbon dioxide cycle conditions: In the first step, referring to the set value of the heating temperature ( T supply ), according to the set value of the suction temperature of compressor a, the optimized value of the suction temperature is calculated. When the heating temperature is less than 100 °C, the optimization formula for the suction temperature of compressor a is:

[0069] When the heating temperature is greater than or equal to 100 °C, the optimization formula for the suction temperature of compressor a is:

[0070] wherein, η IHX is the recuperator efficiency, T wt is the temperature of the waste heat source, T 6 is the inlet temperature of the cold side of the gas cooler.

[0071] In the second step, compare the obtained optimized suction temperature value ( T 1,opt ) with the actual suction temperature ( T 1), and control it by the split ratio of the electronic control valve f. When T 1 > T 1,opt + ε, increase the split ratio of the electronic control valve f; conversely, when T 1 < T 1,opt - ε, decrease the split ratio of the electronic control valve f; when T 1,opt –ε ≤T When 1 ≤ T 1,opt + ε, keep the split ratio of the electronic control valve f unchanged, where ε is the allowable error precision value.

[0072] Thirdly, use the PID controller to make the suction temperature of the compressor a approach the set value. The PID controller for the compressor suction temperature is controlled by the differential method PID, and the calculation formula is

[0073] where Δ T is the difference between the current compressor suction temperature and the optimized value of the suction temperature, n is the number of operations, K P , K I and K D are the proportional adjustment coefficient, integral adjustment coefficient and differential adjustment coefficient respectively, and their values are K P = 1×10 -1 , K I = 1, and K D = 2×10 -1 .

[0074] During the dehydrogenation process, control of the discharge pressure of the compressor a under the transcritical carbon dioxide cycle condition: First step, referring to the set value of the heating temperature ( T supply ), calculate the optimized value of the discharge pressure according to the set value of the discharge pressure of the compressor a. When the discharge pressure is less than 30 MPa, the optimized formula for the discharge pressure is:

[0075] where P 2 is the discharge pressure, P 1 is the suction pressure, R h is the regeneration rate, x is the opening of the electronic expansion valve, T 1 is the suction temperature, T 2 is the discharge temperature.

[0076] Second step, compare the obtained optimized value of the discharge pressure ( P 2,opt ) with the actual discharge pressure ( P 2), and control it by the speed of the compressor a. When P 2 > P 2,optWhen it is +ε, increase the opening degree of the electronic expansion valve d; conversely, when P 2 < P 2,opt When it is -ε, decrease the opening degree of the electronic expansion valve d; when P 2,opt –ε ≤ P 2 ≤ P 2,opt When it is +ε, keep the opening degree of the electronic expansion valve d unchanged, and ε is the allowable error precision value.

[0077] In the third step, use the PID controller to make the exhaust pressure of the compressor a approach the set value. The PID controller for the compressor exhaust pressure is controlled by the differential method PID, and the calculation formula is:

[0078] Where, Δ P is the difference between the current compressor exhaust pressure and the optimized exhaust pressure value, n is the number of operations, K P , K I and K D are the proportional adjustment coefficient, integral adjustment coefficient and differential adjustment coefficient respectively, and their values are K P = K P = 1×10 -15 , K I = 4×10 -2 , and K D = 3×10 -2 .

[0079] When comprehensive regulation and control are required, connect the PID control module in series to the carbon dioxide high-temperature heat pump regulation unit. When the system process is not shut down, it runs iteratively in sequence. The performance optimization control logic loops continuously until the result converges and the calculation ends.

[0080] The above are only the preferred embodiments of the present invention and are not used to limit the present invention. For those skilled in the art, the present invention can have various changes and modifications. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included within the protection scope of the present invention.

Claims

1. A green hydrogen energy efficient storage and transportation system with thermal hydrogen synergistic-parallel energy storage, characterized in that, It includes a high-temperature carbon dioxide heat pump regulation unit and a hot hydrogen reactor, and the high-temperature carbon dioxide heat pump regulation unit is connected to the hot hydrogen reactor; In the high-temperature carbon dioxide heat pump regulation unit, a compressor (a) is provided. The high-pressure side outlet of the compressor (a) is connected in series with the hot-side inlet of a gas cooler (b). The hot-side outlet of the gas cooler (b) is connected in series with the high-pressure side inlet of a regenerator (c). The high-pressure side outlet of the regenerator (c) is connected in series with the high-pressure side inlet of an electronic expansion valve (d). The low-pressure side outlet of the electronic expansion valve (d) is connected in series with the cold-side inlet of a gas heater (e). The cold-side outlet of the gas heater (e) is connected in series with the high-pressure side inlet of an electronic regulating valve (f). The low-pressure side outlet of the electronic regulating valve (f) is connected in parallel with the low-pressure side of a mixing pipe (g) and the regenerator (c). The low-pressure side outlet of the electronic regulating valve (f) is connected in series with the inlet of the mixing pipe (g). The low-pressure side outlet of the electronic regulating valve (f) is connected in series with the low-pressure side inlet of the regenerator (c). The low-pressure side outlet of the regenerator (c) is connected in series with the inlet of the mixing pipe (g). The outlet of the mixing pipe (g) is connected in series with the low-pressure side inlet of the compressor (a). The compressor (a), the electronic expansion valve (d), and the electronic regulating valve (f) are all connected to a PID control module; The hot hydrogen reactor is connected to the cold-side outlet of the gas cooler (b) and the hot-side inlet of the gas heater (e).

2. The green hydrogen energy efficient storage and transportation system for thermal hydrogen synergistic-parallel energy storage according to claim 1, characterized in that, On the pipeline of the low-pressure side inlet of the compressor (a), a compressor suction temperature sensor (h) is provided. On the pipeline of the high-pressure side outlet of the compressor (a), a compressor discharge temperature sensor (i) and a compressor discharge pressure sensor (j) are provided.

3. The green hydrogen energy efficient storage and transportation system for thermal hydrogen synergistic-parallel energy storage according to claim 1, characterized in that, On the pipeline of the hot-side outlet of the gas cooler (b), a gas cooler hot-side discharge temperature sensor (k) is provided.

4. A green hydrogen energy efficient storage and transportation system for thermal hydrogen synergistic-parallel energy storage according to claim 1, characterized in that, On the pipeline of the cold-side outlet of the gas heater (e), a gas heater cold-side discharge temperature sensor (l) and a gas heater cold-side discharge pressure sensor (m) are provided.

5. A green hydrogen energy efficient storage and transportation system for thermal hydrogen synergistic-parallel energy storage according to claim 1, characterized in that The PID control module includes a compressor discharge pressure PID controller, a compressor suction temperature PID controller, a gas heater discharge pressure PID controller, and a differential method PID controller. The compressor discharge pressure PID controller, the compressor suction temperature PID controller, and the gas heater discharge pressure PID controller are all connected to the differential method PID controller. The compressor discharge pressure PID controller is connected to the compressor (a) and an adjustable electronic expansion valve (d). The compressor suction temperature PID controller is connected to an adjustable electronic regulating valve (f). The gas heater discharge pressure PID controller is connected to the electronic expansion valve (d).

6. A method for efficient storage and transportation of green hydrogen energy with thermal hydrogen synergistic-parallel energy storage for the system according to any one of claims 1 to 5, characterized in that, It includes: According to the requirements of the hot hydrogen reactor, the high-temperature carbon dioxide heat pump regulation unit switches between the surplus heat source heating mode and the air source heating mode in real time, adjusts the rotation speed of the compressor (a), the opening degree of the electronic expansion valve (d), and the flow splitting ratio of the electronic regulating valve (f) through the PID control module, dynamically adjusts and optimizes the heating temperature of the high-temperature carbon dioxide heat pump regulation unit, and realizes the adaptive regulation of the system.

7. The green hydrogen energy efficient storage and transportation method for thermal hydrogen synergistic-parallel energy storage according to claim 6, characterized in that, The waste heat source heating mode corresponds to the supercritical carbon dioxide cycle condition, and the compressor (a) produces high-grade carbon dioxide to feedback high-temperature heat for the hydrogen storage reaction. The air source heating mode corresponds to the transcritical carbon dioxide cycle condition, and the compressor (a) produces high-grade carbon dioxide to provide high-temperature heat for the hydrogen release reaction.

8. The green hydrogen energy efficient storage and transportation method for thermal hydrogen synergistic-parallel energy storage according to claim 6, characterized in that, The adaptive regulation of the system includes: In the waste heat source heating mode, the speed of the compressor (a) is regulated by the compressor discharge pressure PID controller to make the discharge pressure of the compressor (a) reach the optimized value. The opening degree of the electronic expansion valve (d) is regulated by the gas heater discharge pressure PID controller to make the discharge pressure of the gas heater (e) reach the optimized value. The split ratio of the electronic regulating valve (f) is regulated by the compressor suction temperature PID controller to make the suction temperature of the compressor (a) reach the optimized value. In the air source heating mode, the opening degree of the electronic expansion valve (d) is regulated by the compressor discharge pressure PID controller to make the discharge pressure of the compressor (a) reach the optimized value. The split ratio of the electronic regulating valve (f) is regulated by the compressor suction temperature PID controller to make the suction temperature of the compressor (a) reach the optimized value.

9. The green hydrogen energy efficient storage and transportation method for thermal hydrogen synergistic-parallel energy storage according to claim 8, characterized in that, In the waste heat source heating mode, the compressor discharge pressure PID controller obtains the optimized discharge temperature value and the optimized discharge pressure value according to the set discharge temperature of the compressor (a) and the actual discharge pressure of the compressor (a), and makes the discharge pressure of the compressor (a) approach the optimized value by adjusting the speed of the compressor (a). The gas heater discharge pressure PID controller obtains the optimized discharge temperature value and the optimized discharge pressure value of the gas heater (e) according to the set discharge temperature of the compressor (a) and the actual discharge pressure of the gas heater (e), and makes the discharge pressure of the gas heater (e) approach the optimized value by adjusting the opening degree of the electronic expansion valve (d). The compressor suction temperature PID controller obtains the optimized discharge temperature value and the optimized suction temperature value according to the set discharge temperature of the compressor (a) and the actual suction temperature of the compressor (a), and makes the suction temperature of the compressor (a) approach the optimized value by adjusting the split ratio of the electronic regulating valve (f).

10. The green hydrogen energy efficient storage and transportation method of thermal hydrogen synergy - parallel energy storage according to claim 8, characterized in that, In the air source heating mode, the compressor suction temperature PID controller obtains the optimized discharge temperature value and the optimized suction temperature value according to the set discharge temperature of the compressor (a) and the actual suction temperature of the compressor (a), and makes the suction temperature of the compressor (a) approach the optimized value by adjusting the split ratio of the electronic regulating valve (f). The compressor discharge pressure PID controller obtains the optimized discharge temperature value and the optimized discharge pressure value according to the set discharge temperature of the compressor (a) and the actual discharge pressure of the compressor (a), and makes the discharge pressure of the compressor (a) approach the optimized value by adjusting the opening degree of the electronic expansion valve (d).

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