Green hydrogen synthesis ammonia reaction system
By introducing renewable energy hydrogen production and solar thermal ammonia synthesis systems, the problem of insufficient heat in the green hydrogen ammonia synthesis reaction has been solved, stable and continuous ammonia production has been achieved, and energy consumption and production costs have been reduced.
Patent Information
- Application Number
- CN202510603935.7
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-05-12
- Publication Date
- 2025-09-23
AI Technical Summary
In the existing green hydrogen ammonia synthesis process, the heat released by the reaction is not enough to maintain the self-heating balance of the system, resulting in a large amount of electricity consumption, resulting in low energy utilization and economic feasibility.
A green hydrogen synthesis ammonia reaction system is adopted, including a renewable energy hydrogen production subsystem, a solar thermal synthesis ammonia subsystem and an ammonia separation and collection subsystem. Solar energy is used as a heat source to reduce dependence on fossil energy. Ammonia is separated and stored through the ammonia separation and collection subsystem to achieve stable and continuous operation of the reaction.
It reduces the consumption of fossil energy, lowers production costs, and realizes the stable and continuous operation of the green hydrogen synthesis ammonia reaction.
Smart Images
Figure CN120679451A_ABST
Abstract
Description
Technical Field
[0001] The present application belongs to the technical field of solar ammonia production, and specifically relates to a green hydrogen ammonia synthesis reaction system. Background Art
[0002] In recent years, the process of synthesizing ammonia using green hydrogen has gradually become a hot topic in research and application. From the perspective of the chemical reaction itself, although the reaction of nitrogen and green hydrogen to produce ammonia is an exothermic reaction, in the entire process flow, an external heat source, such as an electric heater or heat exchanger, is still required in the initial stage to preheat the gas to the catalyst activity temperature (above approximately 236°C). During the reaction, due to heat loss and other reasons, if the heat released by the reaction is not enough to maintain the self-heating balance of the system, additional heat will be required, which will consume a large amount of electricity, not only increasing energy costs, but also to a certain extent reducing the energy utilization and economic feasibility of the green hydrogen synthesis of ammonia process. Summary of the Invention
[0003] Therefore, the purpose of this application is to provide a green hydrogen ammonia synthesis reaction system to at least solve the problem of large-scale electricity consumption.
[0004] In order to solve the above problems, the present application provides a green hydrogen synthesis ammonia reaction system, including a renewable energy hydrogen production subsystem, a solar thermal ammonia synthesis subsystem and an ammonia separation and collection subsystem; the solar thermal ammonia synthesis subsystem is connected to the renewable energy hydrogen production subsystem; the ammonia separation and collection subsystem is respectively connected to the solar thermal ammonia synthesis subsystem and the renewable energy hydrogen production subsystem;
[0005] The renewable energy hydrogen production subsystem is used to transport the mixed and pressurized hydrogen and nitrogen mixture to the solar thermal ammonia synthesis subsystem, the solar thermal ammonia synthesis subsystem is used to prepare ammonia and transport it to the ammonia separation and collection subsystem, the ammonia separation and collection subsystem is used to separate the ammonia and transport the unreacted hydrogen and nitrogen mixture back to the renewable energy hydrogen production subsystem.
[0006] Optionally, the renewable energy hydrogen production subsystem includes a power generation device, an electrolyzer, a nitrogen source and a compressor, wherein the power generation device is electrically connected to the electrolyzer and the compressor for supplying power to the electrolyzer and the compressor; the electrolyzer and the nitrogen source are both connected to a collection part, and the collection part is connected to the compressor.
[0007] Optionally, the renewable hydrogen production subsystem further includes a hydrogen storage tank, the inlet of the hydrogen storage tank is connected to the electrolyzer so that excess hydrogen in the electrolyzer is transported to the hydrogen storage tank and stored in the form of high-pressure gas, and the outlet of the hydrogen storage tank is connected to the collecting part.
[0008] Optionally, the power generation equipment includes a wind turbine and a photovoltaic array.
[0009] Optionally, the solar thermal ammonia synthesis subsystem includes a heat collection device, an endothermic reactor, a low-temperature oil tank, and a high-temperature oil tank. The heat collection device is used to reflect and converge sunlight to the endothermic reactor to heat the endothermic reactor. The air inlet of the endothermic reactor is connected to the renewable energy hydrogen production subsystem, the oil inlet of the endothermic reactor is connected to the low-temperature oil tank, and the oil outlet of the endothermic reactor is connected to the high-temperature oil tank.
[0010] Optionally, the high-temperature oil tank is connected to the oil inlet of the endothermic reactor, and the low-temperature oil tank is connected to the oil outlet of the endothermic reactor.
[0011] Optionally, the thermal energy collection device includes a heliostat and a trough concentrator; the endothermic reactor includes a square chamber endothermic reactor and a cylindrical chamber endothermic reactor. When the square chamber endothermic reactor is used, the heliostat reflects and converges sunlight onto the square chamber endothermic reactor; when the cylindrical chamber endothermic reactor is used, the cylindrical chamber endothermic reactor is arranged on the trough concentrator, and the trough concentrator reflects and converges sunlight onto the cylindrical chamber endothermic reactor.
[0012] Optionally, the square chamber endothermic reactor includes a reactor shell and a partition, the reactor shell includes a reaction chamber, a plurality of partitions are arranged in the reaction chamber to divide the reaction chamber into a plurality of separated chambers, a first catalyst is arranged in each of the separated chambers, a gas inlet and a gas outlet are arranged on the reactor shell, the reaction gas enters the reaction chamber from the gas inlet, flows through the plurality of separated chambers to undergo catalytic reaction, and then flows out from the gas outlet; the reactor shell and the partition are both hollow structures, the reactor shell and the partition are connected to form an oil chamber, and the oil chamber is used to pass heat transfer oil to heat the reaction chamber.
[0013] Optionally, the cylindrical chamber endothermic reactor includes a hollow tube body, the internal space of the hollow tube body forms a reaction chamber, a second catalyst is arranged in the reaction chamber, a glass shell is coaxially mounted on the outer side of the hollow tube body, a vacuum annular space is formed between the glass shell and the outer peripheral surface of the hollow tube body, and the hollow chamber of the hollow tube body is used to pass heat transfer oil to heat the reaction chamber.
[0014] Optionally, the ammonia separation and collection subsystem includes a cooling tower, a liquid ammonia storage tank and an ammonia separator; the cooling tower is connected to the solar thermal ammonia synthesis subsystem, the ammonia separator is connected to the renewable energy hydrogen production subsystem, the cooling tower is connected to the ammonia separator, and the ammonia separator is connected to the liquid ammonia storage tank.
[0015] By means of the above technical solution, the present invention has at least the following beneficial effects:
[0016] An embodiment of the present application provides a green hydrogen synthesis ammonia reaction system, which produces hydrogen through a renewable energy hydrogen production subsystem, and then introduces nitrogen and the produced hydrogen into a solar thermal synthesis ammonia subsystem; hydrogen and nitrogen react in the solar thermal synthesis ammonia subsystem to produce ammonia; ammonia in the mixed gas is separated and stored by an ammonia separation and collection subsystem; solar energy is collected to provide heat for the solar thermal synthesis ammonia subsystem, thereby changing the previous dependence on fossil energy in the reaction and reducing the consumption of fossil energy; the solar thermal synthesis ammonia subsystem stores the heated high-temperature heat transfer oil and provides heat for the reaction when there is no solar radiation, thereby achieving stable and continuous operation of the reaction. BRIEF DESCRIPTION OF THE DRAWINGS
[0017] Figure 1 This is a flow chart of the green hydrogen ammonia synthesis reaction system of Example 1 of the present application;
[0018] Figure 2 This is a schematic diagram of a square chamber endothermic reactor according to Example 1 of the present application;
[0019] Figure 3 This is a flow chart of the green hydrogen ammonia synthesis reaction system of Example 2 of the present application;
[0020] Figure 4 Schematic diagram of the cylindrical chamber endothermic reactor of Example 2 of the present application.
[0021] The reference numerals indicate:
[0022] 1. Wind turbine; 2. Photovoltaic array; 3. Electrolyzer; 4. Hydrogen storage tank; 5. Compressor; 6. Heliostat; 7. Nitrogen source; 8. Square chamber endothermic reactor; 801. Reactor shell; 802. Partition; 803. First catalyst; 9. Cylindrical chamber endothermic reactor; 901. Hollow tube; 902. Glass shell; 903. Second catalyst; 904. Reaction chamber; 905. Vacuum annular space; 10. Low-temperature oil tank; 11. High-temperature oil tank; 12. Cooling tower; 13. Ammonia separator; 14. Liquid ammonia storage tank; 15. Trough concentrator; 16. Thermal oil. DETAILED DESCRIPTION
[0023] In the description of this application, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", "counterclockwise" and the like to indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as limiting the present invention.
[0024] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of the technical features being referred to. Thus, a feature identified as "first" or "second" may explicitly or implicitly include one or more of the features. In the description of the present invention, "plurality" means two or more, unless otherwise specifically defined.
[0025] In this application, unless otherwise specified or limited, the terms "mounted," "connected," "connect," "fixed," etc. should be understood broadly. For example, they may refer to fixed connection, detachable connection, or integral connection; mechanical connection or electrical connection; direct connection or indirect connection through an intermediate medium; or internal communication between two components. Those skilled in the art will understand the specific meanings of the above terms in this application based on specific circumstances.
[0026] The preferred embodiments of the present invention are described below with reference to the accompanying drawings. It should be understood that the preferred embodiments described herein are only used to illustrate and explain the present invention, and are not used to limit the present invention.
[0027] See also Figures 1 to 4 As shown, according to an embodiment of the present application, a green hydrogen synthesis ammonia reaction system is provided, comprising a renewable energy hydrogen production subsystem, a solar thermal ammonia synthesis subsystem, and an ammonia separation and collection subsystem, wherein the solar thermal ammonia synthesis subsystem is connected to the renewable energy hydrogen production subsystem; the ammonia separation and collection subsystem is respectively connected to the solar thermal ammonia synthesis subsystem and the renewable energy hydrogen production subsystem;
[0028] The renewable energy hydrogen production subsystem is used to transport the mixed and pressurized hydrogen and nitrogen mixture to the solar thermal ammonia synthesis subsystem, the solar thermal ammonia synthesis subsystem is used to prepare ammonia and transport it to the ammonia separation and collection subsystem, the ammonia separation and collection subsystem is used to separate the ammonia and transport the unreacted hydrogen and nitrogen mixture back to the renewable energy hydrogen production subsystem.
[0029] Hydrogen is produced by a renewable energy hydrogen production subsystem, and then nitrogen and the produced hydrogen are introduced into a solar thermal ammonia synthesis subsystem; hydrogen and nitrogen react in the solar thermal ammonia synthesis subsystem to produce ammonia; ammonia is separated from the mixed gas by an ammonia separation and collection subsystem and stored; heat is provided to the solar thermal ammonia synthesis subsystem by collecting solar energy, thereby changing the previous dependence on fossil energy in the reaction and reducing the consumption of fossil energy; the solar thermal ammonia synthesis subsystem stores the heated high-temperature heat transfer oil 16 and provides heat for the reaction when there is no solar radiation, thereby achieving stable and continuous operation of the reaction.
[0030] In another embodiment, the renewable energy hydrogen production subsystem includes a power generation device, an electrolyzer 3, a nitrogen source 7 and a compressor 5. The power generation device is electrically connected to the electrolyzer 3 and the compressor 5 to supply power to the electrolyzer 3 and the compressor 5; the electrolyzer 3 and the nitrogen source 7 are both connected to a collection part, and the collection part is connected to the compressor 5.
[0031] Specifically, the power generation equipment comprises a wind turbine 1 and a photovoltaic array 2. The wind turbine 1 is used to convert wind energy into electricity and is a renewable energy source. The photovoltaic array 2 is used to convert solar energy into electricity and is also a renewable energy source. Providing clean energy to the electrolyzer 3 and compressor 5 through the wind turbine 1 or photovoltaic array 2 significantly reduces the production costs of the system.
[0032] A specific working principle of this implementation is:
[0033] The power generation equipment generates electricity and transmits it to the electrolytic cell 3, which is used to drive the electrolytic cell 3 to electrolyze water to produce hydrogen. The prepared hydrogen is transported to the collection part, and the nitrogen source 7 provides nitrogen to be transported to the collection part. Then, the mixture of hydrogen and nitrogen passes through the collection part and enters the compressor 5, where it is mixed and pressurized.
[0034] In another embodiment, the renewable hydrogen production subsystem further includes a hydrogen storage tank 4, the inlet of which is connected to the electrolyzer 3 so that excess hydrogen in the electrolyzer 3 is transported to the hydrogen storage tank 4 and stored in the form of high-pressure gas, and the outlet of the hydrogen storage tank 4 is connected to the collecting part.
[0035] Among them, the hydrogen storage tank 4 is connected to the electrolyzer 3 and is used to transport excess hydrogen to the hydrogen storage tank 4 for storage; when the wind turbine 1 or the photovoltaic array 2 cannot use wind energy or solar energy to generate electricity, the hydrogen storage tank 4 transports the high-pressure gaseous hydrogen stored therein to the compressor 5 to achieve continuous production of ammonia.
[0036] In another embodiment, the solar thermal ammonia synthesis subsystem includes a heat collection device, an endothermic reactor, a low-temperature oil tank 10, and a high-temperature oil tank 11. The heat collection device is used to reflect and concentrate sunlight onto the endothermic reactor to heat the endothermic reactor. The air inlet of the endothermic reactor is connected to the renewable energy hydrogen production subsystem, the oil inlet of the endothermic reactor is connected to the low-temperature oil tank 10, and the oil outlet of the endothermic reactor is connected to the high-temperature oil tank 11.
[0037] Among them, the thermal energy collection device is used to reflect and concentrate sunlight to the endothermic reactor to heat the endothermic reactor, so that nitrogen and hydrogen generate ammonia at a high temperature of 500°C and are transported to the ammonia separation and collection subsystem at the rear end.
[0038] In another embodiment, the high-temperature oil tank 11 is connected to the oil inlet of the endothermic reactor, and the low-temperature oil tank 10 is connected to the oil outlet of the endothermic reactor.
[0039] When heating the endothermic reactor, the low-temperature heat-conducting oil 16 in the low-temperature oil tank 10 is transported to the endothermic reactor to be heated, and then a circulation is formed in the endothermic reactor to heat the reaction chamber of the endothermic reactor, so that nitrogen and hydrogen react to generate ammonia under high temperature conditions, and the heated heat-conducting oil 16 is transported to the high-temperature oil tank 11 for storage. When there is no sunlight, the high-temperature heat-conducting oil 16 in the high-temperature oil tank 10 is transported to the endothermic reactor to heat the reaction chamber of the endothermic reactor, so that nitrogen and hydrogen react to generate ammonia under high temperature conditions, and the high-temperature heat-conducting oil 16 after releasing heat is transported to the low-temperature oil tank for storage.
[0040] In another embodiment, the thermal energy collection device includes a heliostat 6 and a trough concentrator 15; the endothermic reactor includes a square chamber endothermic reactor 8 and a cylindrical chamber endothermic reactor 9. When the square chamber endothermic reactor 8 is used, the heliostat 6 reflects and converges sunlight onto the square chamber endothermic reactor 8; when the cylindrical chamber endothermic reactor 9 is used, the cylindrical chamber endothermic reactor 9 is arranged on the trough concentrator 15, and the trough concentrator 15 reflects and converges sunlight onto the cylindrical chamber endothermic reactor 9.
[0041] Heliostat 6 is based on the reflection and focusing of sunlight. Its core function is to track the sun's motion and adjust the mirror angle in real time, ensuring that sunlight is consistently reflected into the fixed square chamber endothermic reactor 8. Specifically, heliostat 6 is equipped with mutually perpendicular elevation and azimuth axes. The coordinated control of the elevation and azimuth motors achieves precise sunlight reflection.
[0042] Among them, the reflector of the trough concentrator 15 is usually parabolic in shape, which can focus the parallel incident sunlight onto a line; at this time, the cylindrical chamber endothermic reactor 9 is arranged on the focal line of the reflector of the trough concentrator 15 to receive the sunlight focused by the reflector.
[0043] The sunlight is reflected and collected by the heliostat 6 or the trough concentrator 15, and the heat of the sunlight is used to heat the endothermic reactor; thus, the heat supplementation method using electric energy is eliminated, and the energy cost is reduced.
[0044] In another embodiment, the square chamber endothermic reactor 8 includes a reactor shell 801 and a partition 802. The reactor shell 801 includes a reaction chamber. A plurality of partitions 802 are provided in the reaction chamber to divide the reaction chamber into a plurality of separated chambers. A first catalyst 803 is provided in each of the separated chambers. A gas inlet and a gas outlet are provided on the reactor shell 801. The reaction gas enters the reaction chamber from the gas inlet, flows through a plurality of separated chambers to undergo catalytic reaction, and then flows out from the gas outlet. The reactor shell 801 and the partition 802 are both hollow structures. The reactor shell 801 and the partition 802 are connected to form an oil chamber, and the oil chamber is used to pass heat transfer oil 16 to heat the reaction chamber.
[0045] Among them, the reactor shell 801 includes a reaction chamber, and a plurality of partitions 802 are arranged in the reaction chamber to divide the reaction chamber into a plurality of separated chambers. A first catalyst 803 is arranged in each of the separated chambers. That is to say, the reaction chamber is divided by the plurality of partitions 802, so that the mixture of hydrogen and nitrogen can reduce the flow rate in the reaction chamber, and fully undergo a catalytic reaction to generate ammonia.
[0046] Specifically, in this embodiment, the reaction gas refers to a mixture of nitrogen and hydrogen.
[0047] Among them, the reactor shell 801 and the partition 802 are both hollow structures. The reactor shell 801 and the partition 802 are connected to form an oil chamber, and the oil chamber is used to pass heat transfer oil 16 to heat the reaction chamber; that is, the reactor shell 801 and the partition 802 are through-connected, and can form a heat transfer oil 16 circulation loop, so that the heat transfer oil 16 passed into the endothermic reactor is heated by the reflected and focused sunlight, so as to fully heat the reaction chamber.
[0048] In another embodiment, the cylindrical chamber endothermic reactor 9 includes a hollow tube body 901, the internal space of the hollow tube body 901 forms a reaction chamber 904, a second catalyst 903 is arranged in the reaction chamber 904, a glass shell 902 is coaxially mounted on the outer side of the hollow tube body 901, and a vacuum annular space 905 is formed between the glass shell 902 and the outer peripheral surface of the hollow tube body 901. The hollow chamber of the hollow tube body 901 is used to introduce heat transfer oil 16 to heat the reaction chamber 904.
[0049] A vacuum annular space 905 is formed between the glass shell 902 and the outer circumference of the hollow tube 901. This vacuum annular space 905 significantly reduces heat conduction losses between the working medium within the cylindrical chamber endothermic reactor and the external environment. This means that more heat can be retained within the reaction chamber 904 to heat the working medium, thereby improving heat collection efficiency.
[0050] In another embodiment, the ammonia separation and collection subsystem includes a cooling tower 12, a liquid ammonia storage tank 14 and an ammonia separator 13; the cooling tower 12 is connected to the solar thermal ammonia synthesis subsystem, the ammonia separator 13 is connected to the renewable energy hydrogen production subsystem, the cooling tower 12 is connected to the ammonia separator 13, and the ammonia separator 13 is connected to the liquid ammonia storage tank 14.
[0051] Among them, the cooling tower 12 is connected to the solar thermal ammonia synthesis subsystem, that is, the gas outlet of the endothermic reactor is connected to the gas inlet of the cooling tower 12, so that the ammonia and the mixture of unreacted nitrogen and hydrogen are transported to the cooling tower 12 for cooling; at this time, the oil outlet of the low-temperature oil tank 10 is also connected to the oil inlet of the cooling tower 12, and the low-temperature heat-conducting oil 16 is introduced to cool the mixture of ammonia, nitrogen and hydrogen in the cooling tower 12; the low-temperature heat-conducting oil 16 that absorbs heat becomes high-temperature heat-conducting oil 16, which comes out of the oil outlet of the cooling tower 12 and is transported to the high-temperature oil tank 11 for storage.
[0052] The cooling tower 12 is connected to the ammonia separator 13. After cooling in the cooling tower 12, the ammonia, unreacted nitrogen, and hydrogen mixture is separated in the ammonia separator 13. The separated liquid ammonia is transported to the liquid ammonia storage tank 14 for storage; the separated unreacted nitrogen and hydrogen mixture is transported to the compressor 5.
[0053] Example 1
[0054] like Figures 1 to 2 As shown, in this embodiment, the endothermic reactor is a square chamber endothermic reactor.
[0055] The specific working principle is as follows:
[0056] The wind turbine 1 or photovoltaic array 2 generates electricity and transmits it to the electrolyzer 3, which drives the electrolyzer 3 to electrolyze water to produce hydrogen. Hydrogen and nitrogen are transported to the compressor 5 in proportion for mixing and pressurization. When the hydrogen production is too high, the excess hydrogen is transported to the hydrogen storage tank 4 for storage in the form of high-pressure gas. The heliostat 6 adopts a flat mirror structure. By tracking the position of the sun, it reflects and converges sunlight to the position of the heat absorber 8. The low-temperature heat transfer oil 16 in the low-temperature oil tank 10 is transported to the square chamber heat absorption reactor 8 for heating, thereby indirectly heating the reaction chamber in the square chamber heat absorption reactor 8. The catalyst is evenly placed in the reaction chamber. Nitrogen and hydrogen generate ammonia at a high temperature of 500°C and are transported to the rear ammonia separation and collection sub-unit. In the system, the heated thermal oil 16 is transported to the high-temperature oil tank 11 for storage; the cooling tower 12 receives the ammonia generated in the reaction chamber and the mixture of the unreacted nitrogen and hydrogen, and is cooled to a liquid ammonia state here. The mixture of the unreacted nitrogen and hydrogen is transported to the separator 13, and the liquid ammonia is separated from the unreacted hydrogen and nitrogen in the separator 13. The separated liquid ammonia is stored in the liquid ammonia storage tank 14, and the unreacted hydrogen and nitrogen are returned to the compressor 5; the cold end working fluid in the cooling tower 12 is provided by the low-temperature oil tank 10, and heat exchange occurs in the cooling tower 12. The generated high-temperature working fluid is transported to the high-temperature oil tank 11 for storage to achieve heat recovery. In windless and solar-free conditions, hydrogen is supplied by hydrogen storage tank 4 and transported proportionally with nitrogen to compressor 5 for high-pressure delivery to ammonia synthesis tower 7. High-temperature thermal oil 16 in high-temperature oil tank 11 is transported to square chamber endothermic reactor 8, providing heat to the reaction chamber and meeting the required temperature for the ammonia synthesis reaction between high-pressure nitrogen and hydrogen. The resulting ammonia is then passed into the ammonia separation subsystem for storage. This reaction system enables continuous ammonia production.
[0057] Example 2
[0058] like Figure 3 and Figure 4 As shown, in this embodiment, the endothermic reactor is a cylindrical chamber endothermic reactor.
[0059] The wind turbine 1 or photovoltaic array 2 generates electricity and transmits it to the electrolyzer 3, which drives the electrolyzer 3 to electrolyze water to produce hydrogen. Hydrogen and nitrogen are transported to the compressor 5 in proportion for mixing and pressurization. When the hydrogen production is too high, the excess hydrogen is transported to the hydrogen storage tank 4 for storage in the form of high-pressure gas; the trough concentrator 15 adopts a parabolic structure to reflect and converge sunlight onto the cylindrical chamber endothermic reactor 9 at the focus. The low-temperature heat-conducting oil 16 in the low-temperature oil tank 10 is transported to the cylindrical chamber endothermic reactor 9. The sunlight shines through the glass shell to the surface of the cylindrical chamber endothermic reactor 9, and is absorbed by the heat-conducting oil 16 in the cylindrical chamber endothermic reactor 9 and converted into heat, indirectly heating the reaction chamber 904. The reaction chamber 904 is equipped with a catalyst for full contact with high-pressure hydrogen and nitrogen. Nitrogen and hydrogen generate ammonia at a high temperature of 500°C and are transported to the rear-end ammonia separation and collection subsystem; the heated thermal oil 16 is transported to the high-temperature oil tank 11 for storage; the cooling tower 12 receives the ammonia generated in the reaction chamber and a mixture of the unreacted nitrogen and hydrogen, and is cooled to a liquid ammonia state here. The mixture of the unreacted nitrogen and hydrogen is transported to the separator 13, where the liquid ammonia is separated from the unreacted hydrogen and nitrogen. The separated liquid ammonia is stored in the liquid ammonia storage tank 14, and the unreacted hydrogen and nitrogen are returned to the compressor 5; the cold end working fluid in the cooling tower 12 is provided by the low-temperature oil tank 10, and heat exchange occurs in the cooling tower 12. The generated high-temperature working fluid is transported to the high-temperature oil tank 11 for storage to achieve heat recovery. In windless and solar-free operating conditions, hydrogen is supplied by hydrogen storage tank 4 and transported proportionally with nitrogen to compressor 5 for high-pressure delivery to ammonia synthesis tower 7. High-temperature thermal oil 16 in high-temperature oil tank 11 is transported to cylindrical chamber endothermic reactor 9, providing heat to the reaction chamber and meeting the required temperature for the ammonia synthesis reaction between high-pressure nitrogen and hydrogen. The resulting ammonia is then passed into the ammonia separation subsystem for storage. A vacuum annular space 905 is created between hollow tube 901 and glass shell 902, minimizing heat convection on the surface of the tubular endothermic absorber and reducing heat loss within the cylindrical chamber endothermic reactor. The trough-type concentrated solar collector structure employed in this reaction system facilitates the expansion of ammonia synthesis and reduces costs.
[0060] It is easy for those skilled in the art to understand that, under the premise of no conflict, the above-mentioned advantageous methods can be freely combined and superimposed.
[0061] The above are merely preferred embodiments of the present application and are not intended to limit the present application. Any modifications, equivalent replacements, and improvements made within the spirit and principles of the present application shall be included within the scope of protection of the present application. The above are merely preferred embodiments of the present application. It should be noted that those skilled in the art may make various improvements and variations without departing from the technical principles of the present application, and such improvements and variations shall also be considered within the scope of protection of the present application.
Claims
1. A green hydrogen synthesis ammonia reaction system, characterized in that: include: Renewable energy hydrogen production subsystem; A solar thermal ammonia synthesis subsystem, wherein the solar thermal ammonia synthesis subsystem is connected to the renewable energy hydrogen production subsystem; an ammonia separation and collection subsystem, wherein the ammonia separation and collection subsystem is connected to the solar thermal ammonia synthesis subsystem and the renewable energy hydrogen production subsystem respectively; The renewable energy hydrogen production subsystem is used to transport the mixed and pressurized hydrogen and nitrogen mixture to the solar thermal ammonia synthesis subsystem, the solar thermal ammonia synthesis subsystem is used to prepare ammonia and transport it to the ammonia separation and collection subsystem, the ammonia separation and collection subsystem is used to separate the ammonia and transport the unreacted hydrogen and nitrogen mixture back to the renewable energy hydrogen production subsystem.
2. A green hydrogen ammonia synthesis reaction system according to claim 1, characterized in that: The renewable energy hydrogen production subsystem comprises a power generation device, an electrolyzer (3), a nitrogen source (7) and a compressor (5), wherein the power generation device is electrically connected to the electrolyzer (3) and the compressor (5) for supplying power to the electrolyzer (3) and the compressor (5); the electrolyzer (3) and the nitrogen source (7) are both connected to a collection part, and the collection part is connected to the compressor (5).
3. A green hydrogen ammonia synthesis reaction system according to claim 2, characterized in that: The renewable hydrogen production subsystem further comprises a hydrogen storage tank (4), the inlet of the hydrogen storage tank (4) being connected to the electrolyzer (3) so that excess hydrogen in the electrolyzer (3) is transported to the hydrogen storage tank (4) for storage in the form of high-pressure gas, and the outlet of the hydrogen storage tank (4) is connected to the collecting portion.
4. A green hydrogen ammonia synthesis reaction system according to claim 2, characterized in that: The power generation equipment comprises a wind turbine (1) and a photovoltaic array (2).
5. The green hydrogen synthesis ammonia reaction system according to claim 1, characterized in that: The solar thermal ammonia synthesis subsystem comprises a heat collection device, an endothermic reactor, a low-temperature oil tank (10), and a high-temperature oil tank (11). The heat collection device is used to reflect and converge sunlight to the endothermic reactor to heat the endothermic reactor. The air inlet of the endothermic reactor is connected to the renewable energy hydrogen production subsystem, the oil inlet of the endothermic reactor is connected to the low-temperature oil tank (10), and the oil outlet of the endothermic reactor is connected to the high-temperature oil tank (11).
6. A green hydrogen synthesis ammonia reaction system according to claim 5, characterized in that: The high-temperature oil tank (11) is connected to the oil inlet of the endothermic reactor, and the low-temperature oil tank (10) is connected to the oil outlet of the endothermic reactor.
7. The green hydrogen synthesis ammonia reaction system according to claim 5, characterized in that: The heat energy collection device comprises a heliostat (6) and a trough concentrator (15); the endothermic reactor comprises a square chamber endothermic reactor (8) and a cylindrical chamber endothermic reactor (9); when the square chamber endothermic reactor (8) is used, the heliostat (6) reflects and converges sunlight onto the square chamber endothermic reactor (8); when the cylindrical chamber endothermic reactor (9) is used, the cylindrical chamber endothermic reactor (9) is arranged on the trough concentrator (15), and the trough concentrator (15) reflects and converges sunlight onto the cylindrical chamber endothermic reactor (9).
8. The green hydrogen ammonia synthesis reaction system according to claim 7, characterized in that: The square chamber endothermic reactor (8) comprises a reactor shell (801) and a partition (802), wherein the reactor shell (801) comprises a reaction chamber, wherein a plurality of partitions (802) are provided in the reaction chamber to divide the reaction chamber into a plurality of separated chambers, wherein a first catalyst (803) is provided in each of the separated chambers, and a gas inlet and a gas outlet are provided on the reactor shell (801), wherein the reaction gas enters the reaction chamber from the gas inlet, flows through the plurality of separated chambers to undergo a catalytic reaction, and then flows out from the gas outlet; the reactor shell (801) and the partition (802) are both hollow structures, and the reactor shell (801) and the partition (802) are connected to form an oil chamber, wherein the oil chamber is used to introduce heat transfer oil (16) to heat the reaction chamber.
9. The green hydrogen synthesis ammonia reaction system according to claim 7, characterized in that: The cylindrical chamber endothermic reactor (9) comprises a hollow tube (901), the interior space of the hollow tube (901) forms a reaction chamber (904), a second catalyst (903) is arranged in the reaction chamber (904), a glass shell (902) is coaxially sleeved on the outer side of the hollow tube (901), a vacuum annular space (905) is formed between the glass shell (902) and the outer peripheral surface of the hollow tube (901), and the hollow chamber of the hollow tube (901) is used to pass heat transfer oil (16) to heat the reaction chamber (904).
10. The green hydrogen synthesis ammonia reaction system according to claim 1, characterized in that: The ammonia separation and collection subsystem includes a cooling tower (12), a liquid ammonia storage tank (14) and an ammonia separator (13); the cooling tower (12) is connected to the solar thermal ammonia synthesis subsystem, the ammonia separator (13) is connected to the renewable energy hydrogen production subsystem, the cooling tower (12) is connected to the ammonia separator (13), and the ammonia separator (13) is connected to the liquid ammonia storage tank (14).