A YHL synthesis tower, YHL preparation system and YHL green ammonia synthesis method for photovoltaic and wind power generation hydrogen production and green ammonia synthesis

Abstract

The present invention discloses a YHL synthesis tower, a YHL preparation system, and a YHL green ammonia synthesis method for photovoltaic and wind power generation hydrogen production and green ammonia synthesis. The YHL synthesis tower for photovoltaic and wind power generation hydrogen production and green ammonia synthesis achieves balanced cooling of the inner cylinder and the catalyst layer and precise temperature control by setting the primary and secondary cold air inlets on the synthesis tower body and improving the related structures. It also does not need to introduce additional cooling medium, thereby improving energy utilization, having a simple structure, and being easy to modify. When the production of hydrogen by electrolysis of water using photovoltaic power generation or wind power generation is affected by weather, by adjusting the opening of the control valve K1, the control valve K2, the control valve K3, and the control valve K8 and adjusting the operating frequency of the synthesis cycle compressor, continuous and stable operation with low material consumption is achieved, heat is recovered, and there is no need to stop the operation, thereby reducing or avoiding the impact of weather on green ammonia production, improving the predictability of production operation, and reducing or avoiding production problems caused by downtime. The structure is ingenious and reasonable, energy-saving, and can be industrialized.

Description

Technical Field

[0001] The present invention relates to a YHL synthesis tower, a YHL preparation system and a YHL green ammonia synthesis method for photovoltaic wind power generation hydrogen production, belonging to the technical field of electrolyzing hydrated ammonia using wind energy or solar energy, and belonging to the technical field of wind energy industry or solar energy industry. Background Art

[0002] Solar energy's renewable and environmentally friendly nature has led many countries, including China, to prioritize its development as a new energy industry. Driven by my country's vast and diverse application market, the application of photovoltaics in my country continues to expand, with a growing number of applications emerging.

[0003] Wind power generation converts wind kinetic energy into mechanical energy, and then converts that mechanical energy into electrical energy. As a clean, renewable energy source, wind energy has enormous potential and is gaining increasing attention worldwide. Both domestically and internationally, significant attention is being paid to utilizing wind power for power generation and the development of new energy sources. my country boasts abundant wind energy resources, with approximately 100 gigawatts of exploitable wind energy reserves.

[0004] One of the future trends in energy development is to use green electricity generated by renewable energy (photovoltaic, wind power, etc.) to electrolyze water to produce green hydrogen, produce nitrogen through air separation, and then produce green ammonia through the synthesis reaction of hydrogen and nitrogen. Using green ammonia as fuel to achieve zero carbon emissions is one of the trends in future energy development.

[0005] However, the pain points of using photovoltaic or wind power for electrolytic ammonia production are: solar / wind power generation is significantly affected by weather, resulting in uneven power generation and hydrogen production from water electrolysis, making continuous and stable production difficult. This often requires shutdowns at night, on rainy days, or in windless weather. After cooling down, restarting the equipment typically takes about seven days to stabilize and resume production. This not only results in significant energy consumption but also severely impacts efficiency and production capacity, making it impossible to meet the continuous production needs of industry. Summary of the Invention

[0006] The present invention provides a YHL synthesis tower, a YHL preparation system and a YHL green ammonia synthesis method for synthesizing green ammonia by producing hydrogen through photovoltaic or wind power generation. The YHL synthesis tower can utilize intermittent power generation such as photovoltaic or wind power generation to electrolyze water to produce hydrogen, thereby achieving continuous and stable operation of green ammonia preparation without the need for shutdown due to weather influences.

[0007] In order to solve the above technical problems, the technical solutions adopted by the present invention are as follows:

[0008] A YHL synthesis tower for producing hydrogen and synthesizing green ammonia from photovoltaic and wind power generation.

[0009] It includes a synthesis tower body, an inner tube, an air distribution pipe, an air collecting pipe, a first cooling pipe, a second cooling pipe, a temperature equalizing pipe, a preheater, an air inlet main pipe, a central heating pipe and a transition pipe;

[0010] The inner tube is located inside the synthesis tower body, with a gap between the inner tube and the synthesis tower body to form a sandwich structure, and the top of the sandwich structure is connected to the top of the inner tube;

[0011] The gas distribution pipe, gas collecting pipe, first cooling pipe, second cooling pipe, temperature equalizing pipe, preheater, central heating pipe and transition pipe are all located inside the inner tube;

[0012] The gas distribution pipe and the gas collection pipe are both annular pipes. The gas distribution pipe is located directly above the gas collection pipe, and a porous catalyst layer is arranged between the gas distribution pipe and the gas collection pipe.

[0013] The first cooling tube, the second cooling tube and the equalizing tube are all located in the porous catalyst layer between the gas distribution tube and the gas collecting tube; the lengths of the first cooling tube and the second cooling tube are both less than the interval between the gas distribution tube and the gas collecting tube, the first cooling tube and the second cooling tube are staggered, the top of the first cooling tube is connected to the gas distribution tube, the bottom of the second cooling tube is connected to the gas collecting tube, and air holes are distributed on the side walls of the first cooling tube and the second cooling tube; the length of the equalizing tube is not less than the interval between the gas distribution tube and the gas collecting tube, the top of the equalizing tube is connected to the gas distribution tube, and the bottom is connected to the gas collecting tube;

[0014] The preheater is located at the bottom of the gas collecting pipe. One end of the air inlet main pipe is connected to the air inlet on the preheater, and the other end passes through the bottom of the synthesis tower body. The top of the central heating pipe is connected to the air outlet on the preheater, passes through the porous catalyst layer, and penetrates the top of the inner cylinder.

[0015] A primary cold air inlet is provided at the top of the synthesis tower body, which is connected to the air distribution pipe through a transition pipe; a secondary cold air inlet, a discharge port and a waste discharge port are provided at the bottom of the synthesis tower body, and the secondary cold air inlet is connected to the sandwich structure between the inner tube and the synthesis tower body.

[0016] No air holes are provided on the above-mentioned air distribution pipes, air collecting pipes and temperature equalizing pipes.

[0017] YHL stands for Optimized Controlled Continuous Production. The preheater is equipped with an air inlet and an air outlet. Raw gas enters through the inlet, is preheated, and then flows out through the outlet. The preheater uses the temperature of the gas within the inner cylinder to preheat the incoming raw material. Photovoltaic and wind power generation hydrogen production refers to the production of hydrogen using photovoltaic or wind power.

[0018] During use, the raw mixed gas (a mixture of nitrogen and hydrogen) enters from the air inlet main pipe, is preheated by the preheater, enters the central heating tube for heating, then flows out from the top of the central heating tube, and enters the porous catalyst layer for catalytic reaction. The present application is provided with a secondary cold air inlet and a primary cold air inlet at the same time. The low-temperature reaction raw gas can be input to the secondary cold air inlet and the primary cold air inlet according to the reaction needs, and the inner tube and the porous catalyst layer are cooled. The low-temperature reaction raw gas entering from the secondary cold air inlet cools the side wall of the inner tube from bottom to top, and finally flows into the inner tube from the top of the sandwich structure and enters the porous catalyst layer for reaction. The low-temperature reaction raw gas entering from the primary cold air inlet enters the gas distribution pipe through the transition pipe, circulates between the gas distribution pipe, the temperature equalizing pipe and the gas collecting pipe, forms a cooling for the porous catalyst layer, and when flowing through the first cooling pipe and the second cooling pipe, flows into the porous catalyst layer through the air vents to react. The catalytically synthesized ammonia is discharged from the discharge port at the bottom of the synthesis tower body.

[0019] The above-mentioned arrangement of the primary and secondary cold air inlets not only realizes the cooling of the inner cylinder and the catalyst layer and achieves precise temperature control, but also eliminates the need to introduce additional cooling media, thereby improving energy utilization.

[0020] In order to facilitate temperature testing, improve the balance, stability and conversion rate of the reaction, and improve the uniformity of temperature distribution, temperature measuring devices are distributed at the top, middle and bottom of the inner cylinder to test the temperature (T1 / T2 / T3) at the top, middle and bottom positions of the inner cylinder.

[0021] In order to improve the conversion rate, a porous catalyst layer is also distributed around the preheater inside the inner cylinder.

[0022] The gas distribution pipe and the gas collection pipe are of the same shape and size and are arranged opposite to each other up and down.

[0023] To facilitate assembly, the length of the temperature equalizing pipe is equal to the distance between the gas distribution pipe and the gas collecting pipe.

[0024] In one specific implementation, there are 4 to 8 temperature-averaging tubes, all of which are evenly distributed circumferentially between the gas distribution and collection tubes. Between every two temperature-averaging tubes, there are 2 to 10 first and second cooling tubes, each alternately spaced. The 2 to 4 tubes mentioned above refer to the total number of first and second cooling tubes.

[0025] In order to further improve the balance, the top of the second cooling tube is higher than the bottom of the first cooling tube.

[0026] In the case of insufficient electricity, it can achieve continuous and stable operation with low material consumption and is not affected by weather.

[0027] A YHL preparation system for photovoltaic and wind power generation hydrogen production and green ammonia synthesis, comprising a nitrogen and hydrogen storage tank, a first delivery pipe, a YHL synthesis tower for photovoltaic and wind power generation hydrogen production and green ammonia synthesis, a second delivery pipe, a first heat exchanger, a third delivery pipe, a second heat exchanger, a fourth delivery pipe, an ammonia separator, a fifth delivery pipe, a liquid ammonia storage tank, a sixth delivery pipe and a synthesis cycle compressor, a seventh delivery pipe, and an eighth delivery pipe;

[0028] One end of the first delivery pipe is connected to the nitrogen and hydrogen storage tank, and the other end branches into a first delivery branch pipe A, a first delivery branch pipe B, and a first delivery branch pipe C. The first delivery branch pipe A is connected to the inlet of the synthesis cycle compressor and is provided with a control valve K1. The first delivery branch pipe B is connected to the secondary cooling air inlet at the bottom of the synthesis tower body and is provided with a control valve K2. The first delivery branch pipe C is connected to the primary cooling air inlet at the top of the synthesis tower body and is provided with a control valve K3.

[0029] The first heat exchanger is provided with a first hot material inlet, a first hot material outlet, a first cold material inlet and a first cold material outlet; the second heat exchanger is provided with a second hot material inlet, a second hot material outlet, a second cold material inlet and a second cold material outlet;

[0030] One end of the second delivery pipe is connected to the discharge port at the bottom of the synthesis tower body, and the other end is connected to the first hot material inlet. The second delivery pipe is provided with a control valve K4. One end of the third delivery pipe is connected to the first hot material outlet, and the other end is connected to the second hot material inlet. The third delivery pipe is provided with control valves K5 and K6. The second cold material inlet is connected to the outlet of the cold medium supply device through the cold medium inlet pipe. The cold medium inlet pipe is provided with a control valve K8. The second cold material outlet is connected to the inlet of the cold medium supply device through the cold medium outlet pipe.

[0031] One end of the fourth delivery pipe is connected to the second hot material outlet, and the other end is connected to the top feed port of the ammonia separator. A control valve K7 is provided on the fourth delivery pipe;

[0032] One end of the fifth delivery pipe is connected to the bottom discharge port of the ammonia separator, and the other end is connected to the liquid ammonia storage tank. A control valve K8' is provided on the fifth delivery pipe;

[0033] One end of the sixth delivery pipe is connected to the gas outlet at the top of the ammonia separator, and the other end is connected to the inlet of the synthesis cycle compressor. The sixth delivery pipe is provided with a control valve K9 and a control valve K10;

[0034] One end of the seventh delivery pipe is connected to the outlet of the synthesis cycle compressor and the other end is connected to the first cold material inlet. The seventh delivery pipe is provided with a control valve K11; one end of the eighth delivery pipe is connected to the first cold material outlet and the other end is connected to the air inlet main pipe at the bottom of the synthesis tower body.

[0035] This application is for a system for YHL production of green ammonia. Hydrogen production uses discontinuous renewable electricity and can be controlled by YHL technology to achieve continuous production of green ammonia.

[0036] The ammonia separator adopts the existing ammonia-liquid separator, and the top of the ammonia separator is provided with a feed inlet (for the mixed material to enter) and a gas outlet (for the unreacted gas to flow), and the bottom is provided with a discharge port (for the liquid ammonia to flow out).

[0037] The second heat exchanger is provided with a cold source through a cold medium supply device, and the cold medium supply device may be a cooling water circulation machine.

[0038] The above-mentioned YHL preparation system for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia also includes: an electrolytic hydrogen production device, a hydrogen purification device, a nitrogen production device and a high-pressure unit; the hydrogen outlet of the electrolytic hydrogen production device is connected to the air inlet of the hydrogen purification device through a pipeline, and the air outlet of the hydrogen purification device is connected to the air inlet of the high-pressure unit through a pipeline; the nitrogen outlet of the nitrogen production device is connected to the air inlet of the high-pressure unit through a pipeline; the air outlet of the high-pressure unit is connected to the nitrogen and hydrogen storage tank through a pipeline; the electric energy required for the electrolytic hydrogen production device is provided by the photovoltaic power generation device and the wind power generation device.

[0039] The above-mentioned first heat exchanger is a shell and tube heat exchanger; the second heat exchanger is a tube-and-tube heat exchanger; the control valve K5 is arranged on the end of the third delivery pipe connected to the first hot material outlet, and the control valve K6 is arranged on the end of the third delivery pipe connected to the second hot material inlet; the control valve K9 is arranged on the end of the sixth delivery pipe connected to the gas outlet at the top of the ammonia separator, and the control valve K10 is arranged on the end of the sixth delivery pipe connected to the inlet of the synthesis cycle compressor.

[0040] The liquid ammonia in the liquid ammonia storage tank is transported to the target container through a transfer pump.

[0041] Pumps, instruments and other equipment can be connected to each pipeline as needed.

[0042] A method for producing ammonia from YHL, using the YHL preparation system for producing green ammonia from photovoltaic and wind power generation, comprises the following steps:

[0043] 1) Close all control valves, open the central heating pipe on the synthesis tower body, so that the temperature inside the synthesis tower body reaches 300-350 ° C, and then open the control valves except control valve K2 and control valve K3;

[0044] 2) The nitrogen-hydrogen mixed raw gas in the nitrogen-hydrogen storage tank passes through the first delivery branch pipe A, the synthesis cycle compressor, the seventh delivery pipe, the first heat exchanger, the eighth delivery pipe, and the air inlet main pipe in sequence, and then enters the preheater in the synthesis tower body. After being heated by the central heating pipe, it flows out from the top of the central heating pipe and enters the porous catalyst layer to catalyze the reaction to produce ammonia.

[0045] 3) Ammonia gas flows out of the discharge port at the bottom of the synthesis tower body, enters the first heat exchanger through the second delivery pipe, is cooled by the nitrogen-hydrogen mixed feed gas (i.e., the nitrogen-hydrogen mixed feed gas is heated by the gas flowing out of the discharge port at the bottom of the synthesis tower body), and then enters the second heat exchanger through the third delivery pipe for secondary cooling. Thereafter, it is delivered to the ammonia separator through the fourth delivery pipe to separate the unreacted nitrogen and hydrogen. The liquid ammonia in the ammonia separator enters the liquid ammonia storage tank through the fifth delivery pipe.

[0046] 4) The unreacted nitrogen and hydrogen separated by the ammonia separator enter the synthesis cycle compressor through the sixth delivery pipe to mix with the nitrogen and hydrogen mixed raw material gas, and then pass through the seventh delivery pipe, the first heat exchanger, the eighth delivery pipe and the air inlet main pipe in sequence, and then enter the synthesis tower body for inner cycle reaction;

[0047] 5) During the reaction process, the openings of the control valves K2 and K3 are controlled, and the nitrogen-hydrogen mixed raw material gas directly output from the nitrogen-hydrogen storage tank (delivered by the first delivery branch pipe B and the first delivery branch pipe C) is used to cool the inner cylinder and the porous catalyst layer, so that the temperature of the inner cylinder and the porous catalyst is maintained at 300-350°C, and the pressure is maintained at 1-7 MPa; the low-temperature reaction raw gas entering from the secondary cold air inlet cools the side wall of the inner cylinder from bottom to top, and finally flows from the top of the sandwich structure into the inner cylinder and enters the porous catalyst layer for reaction; the low-temperature reaction raw gas entering from the primary cold air inlet enters the gas distribution pipe through the transition pipe, circulates between the gas distribution pipe, the temperature equalizing pipe and the gas collecting pipe, forms cooling for the porous catalyst layer, and when flowing through the first cooling pipe and the second cooling pipe, flows into the porous catalyst layer through the air vents for reaction;

[0048] 6) When the hydrogen production capacity of the electrolytic hydrogen production device has been or is about to be affected by weather, the opening of the control valve K4 is adjusted to adjust the amount of hydrogen and nitrogen entering the synthesis tower body and the amount of liquid ammonia taken out. By adjusting the opening of the control valve K1, control valve K2, control valve K3, and control valve K8 and adjusting the operating frequency of the synthesis cycle compressor, the temperature in the synthesis tower body is controlled to be maintained at 300-350°C and the pressure is maintained at 1-7MPa to achieve continuous operation.

[0049] When it is known that hydrogen electrolysis will be affected by weather, step 6 can be initiated, significantly improving production predictability.

[0050] The above method can operate continuously, stably and efficiently under the condition that the electrolytic hydrogen production device has sufficient power supply. When the electrolytic hydrogen production device has been or is about to be affected by weather and the hydrogen production is affected, it can also achieve low-material continuous operation and recover heat.

[0051] The temperature of the nitrogen-hydrogen mixed raw gas in the above-mentioned nitrogen-hydrogen storage tank is about 20-30°C. The nitrogen-hydrogen mixed raw gas first passes through the synthesis cycle compressor to form a stable pressure, and then is heated by the product before entering the synthesis tower, which not only ensures the stability of operation but also reduces energy consumption.

[0052] The first heat exchanger of the present application utilizes the product to heat the raw material, thereby achieving both cooling of the product and heating of the raw material, which is ingenious, reasonable, energy-saving and environmentally friendly.

[0053] In the above step 5), by controlling the opening of the control valve K2 and the control valve K3, the materials are fed simultaneously from the top and the bottom of the synthesis tower body, thereby achieving balanced control of the temperature of the inner cylinder and the porous catalyst layer.

[0054] This application provides a frequency conversion control for a synthetic cycle compressor.

[0055] In the above step 6), reducing or closing the control valves K2 / K3 / K8 can reduce the heat taken away, thereby reducing the need to maintain the temperature reaction of the materials hydrogen and nitrogen in the tower. By adjusting the opening of the control valves K4 / K41 and the operating frequency of the synthesis cycle compressor, the amount of hydrogen and nitrogen entering the synthesis tower and the amount of liquid ammonia taken out are adjusted to ensure that the temperature T1 / T2 / T3 (T1 / T2 / T3 refers to the temperature of the upper, middle and lower parts of the synthesis tower body, that is, the upper, middle and lower positions of the synthesis tower body are all provided with temperature measuring devices) are maintained at the reaction temperature, thereby achieving continuous operation. When power is restored, follow steps 2)-5) to operate.

[0056] The synthesis of ammonia through nitrogen and hydrogen is an exothermic reaction. After the machine is started, when the temperature in the synthesis tower reaches the specified temperature, continuous heating is not required. At the same time, multi-directional feeding can be carried out as needed to lower the temperature.

[0057] The hydrogen produced by the electrolytic hydrogen production device is purified by the hydrogen purification device and then enters the high-pressure unit for compression with the nitrogen produced by the nitrogen production device in a ratio of 3:(1-1.2) (i.e., hydrogen:nitrogen=3:(1-1.2)). The compressed nitrogen-hydrogen mixture enters the nitrogen-hydrogen storage tank;

[0058] The raw materials for the porous catalyst, calculated by mass percentage, include: 50-70% austenitic iron powder, 15-20% silica gel, and the balance an additive, which is a mixture of kaolin, calcium carbonate powder, and diatomaceous earth in a mass ratio of 1:(0.2-0.5):(1-1.2). The catalyst is prepared by uniformly mixing the austenitic iron powder, silica gel, and additives, extruding into granules, and heating to 800-1000°C at a rate of 6-8°C / min under nitrogen protection. The catalyst is then calcined at this temperature for 8-10 hours and allowed to cool naturally to obtain the porous catalyst. The catalyst exhibits high strength and excellent stability, and can be used continuously for more than three years.

[0059] The austenitic iron used in this application can be ground from austenitic iron, or directly purchased from the market.

[0060] For raw materials not otherwise specified in this application, analytical grade AR was used.

[0061] The present invention can achieve rapid reactions at low pressure and low temperature. The reaction pressure in the prior art is about 35 MPa and the temperature is 500-600°C. However, the present invention can achieve rapid reactions at a reaction pressure of about 1-7 MPa and a temperature of 300-350°C.

[0062] The technologies not mentioned in this invention are all referred to the prior art.

[0063] The present invention has the following beneficial effects.

[0064] 1) By setting up the primary and secondary cooling air inlets on the synthesis tower body and improving the related structures, balanced cooling of the inner tube and catalyst layer is achieved, precise temperature control is achieved, and no additional cooling medium is required, thereby improving energy utilization, simplifying the structure, and facilitating modification.

[0065] 2) When the production of hydrogen by electrolyzing water using photovoltaic power generation or wind power generation is affected by weather, the opening of control valve K1, control valve K2, control valve K3, control valve K8 and the operating frequency of the synthesis cycle compressor can be adjusted to achieve continuous and stable operation with low material consumption and recover heat without stopping the operation, thereby reducing or avoiding the impact of weather on green ammonia production, improving the predictability of production operation, and reducing or avoiding production problems caused by shutdown.

[0066] 3) The unreacted gas can be recycled repeatedly, which improves the conversion rate and material utilization rate, and the reaction rate is fast, which can be industrialized.

[0067] 4) Using the product to heat the raw materials, killing two birds with one stone, with a clever and reasonable structure and saving energy. BRIEF DESCRIPTION OF THE DRAWINGS

[0068] Figure 1 This is a schematic structural diagram of the YHL synthesis tower used for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia;

[0069] Figure 2 Schematic diagram of gas flow in the temperature equalizing tube of the present invention;

[0070] Figure 3 This is a schematic structural diagram of the YHL preparation system for producing hydrogen and synthesizing green ammonia using photovoltaic and wind power generation according to the present invention;

[0071] In the figure, 1 is a synthesis tower, 101 is a gas distribution pipe, 102 is a gas collecting pipe, 103 is a first cooling pipe, 104 is a second cooling pipe, 105 is a temperature equalizing pipe, 106 is an inner cylinder, 107 is a preheater, 108 is an air inlet main pipe, 109 is a central heating pipe, 110 is a transition pipe; 111 is a temperature measuring device, 112 is a primary cooling air inlet, 113 is a secondary cooling air inlet, 114 is a discharge port, and 115 is a waste discharge port;

[0072] 2 is a nitrogen-hydrogen storage tank, 3 is a first delivery pipe, 4 is a second delivery pipe, 5 is a first heat exchanger, 6 is a third delivery pipe, 7 is a second heat exchanger, 8 is a fourth delivery pipe, 9 is an ammonia separator, 10 is a fifth delivery pipe, 11 is a liquid ammonia storage tank, 12 is a sixth delivery pipe, 13 is a synthesis cycle compressor, 14 is a seventh delivery pipe, 15 is an eighth delivery pipe, 16 is an electrolytic hydrogen production device, 17 is a hydrogen purification device, 18 is a nitrogen production device, 19 is a high-pressure unit, 20 is a delivery pump, and a is a finished liquid ammonia product. DETAILED DESCRIPTION

[0073] In order to better understand the present invention, the content of the present invention is further illustrated below in conjunction with the examples, but the content of the present invention is not limited to the following examples.

[0074] In this application, directional words such as "center", "longitudinal", "lateral", "length", "width", "thickness", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", and "counterclockwise" are based on the orientation or position relationship shown in the drawings or in the use state, and are only for the convenience of describing this application, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operate in a specific orientation. Therefore, they should not be understood as limiting this application.

[0075] Note: In order to better illustrate the internal structure, the porous catalyst layer and other components are omitted in the figure.

[0076] Example 1

[0077] like Figure 1 As shown, a YHL synthesis tower for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia includes a synthesis tower body, an inner cylinder, a gas distribution pipe, a gas collecting pipe, a first cooling pipe, a second cooling pipe, a temperature equalizing pipe, a preheater, an air inlet main pipe, a central heating pipe and a transition pipe;

[0078] The inner tube is located inside the synthesis tower body, with a gap between the inner tube and the synthesis tower body to form a sandwich structure, and the top of the sandwich structure is connected to the top of the inner tube;

[0079] The gas distribution pipe, gas collecting pipe, first cooling pipe, second cooling pipe, temperature equalizing pipe, preheater, central heating pipe and transition pipe are all located inside the inner tube;

[0080] The gas distribution pipe and the gas collection pipe are both annular pipes. The gas distribution pipe is located directly above the gas collection pipe, and a porous catalyst layer is arranged between the gas distribution pipe and the gas collection pipe.

[0081] The first cooling tube, the second cooling tube and the equalizing tube are all located in the porous catalyst layer between the gas distribution tube and the gas collecting tube; the lengths of the first cooling tube and the second cooling tube are both less than the interval between the gas distribution tube and the gas collecting tube, the first cooling tube and the second cooling tube are staggered, the top of the first cooling tube is connected to the gas distribution tube, the bottom of the second cooling tube is connected to the gas collecting tube, and air holes are distributed on the side walls of the first cooling tube and the second cooling tube; the length of the equalizing tube is not less than the interval between the gas distribution tube and the gas collecting tube, the top of the equalizing tube is connected to the gas distribution tube, and the bottom is connected to the gas collecting tube;

[0082] The preheater is located at the bottom of the gas collecting pipe. One end of the air inlet main pipe is connected to the air inlet on the preheater, and the other end passes through the bottom of the synthesis tower body. The top of the central heating pipe is connected to the air outlet on the preheater, passes through the porous catalyst layer, and penetrates the top of the inner cylinder.

[0083] A primary cold air inlet is provided at the top of the synthesis tower body, which is connected to the air distribution pipe through a transition pipe; a secondary cold air inlet, a discharge port and a waste discharge port are provided at the bottom of the synthesis tower body, and the secondary cold air inlet is connected to the sandwich structure between the inner tube and the synthesis tower body.

[0084] During use, the raw mixed gas (a mixture of nitrogen and hydrogen) enters from the air inlet main pipe, is preheated by the preheater, enters the central heating tube for heating, then flows out from the top of the central heating tube, and enters the porous catalyst layer for catalytic reaction. The present application is provided with a secondary cold air inlet and a primary cold air inlet at the same time. The low-temperature reaction raw gas can be input to the secondary cold air inlet and the primary cold air inlet according to the reaction needs, and the inner tube and the porous catalyst layer are cooled. The low-temperature reaction raw gas entering from the secondary cold air inlet cools the side wall of the inner tube from bottom to top, and finally flows into the inner tube from the top of the sandwich structure and enters the porous catalyst layer for reaction. The low-temperature reaction raw gas entering from the primary cold air inlet enters the gas distribution pipe through the transition pipe, circulates between the gas distribution pipe, the temperature equalizing pipe and the gas collecting pipe, forms a cooling for the porous catalyst layer, and when flowing through the first cooling pipe and the second cooling pipe, flows into the porous catalyst layer through the air vents to react. Catalytic synthesis of ammonia is discharged from the discharge port at the bottom of the synthesis tower body. By setting up the primary and secondary cold air inlets, the inner cylinder and catalyst layer can be cooled and precise temperature control can be achieved without the need to introduce additional cooling media, thereby improving energy utilization.

[0085] Example 2

[0086] Based on Example 1, the following improvements were made: temperature measuring devices were distributed on the top (T1), middle (T2), and bottom (T3) of the inner tube; a porous catalyst layer was also distributed on the periphery of the preheater in the inner tube, and the porous catalyst layer in the inner tube extended from the gas distribution pipe to the bottom of the inner tube. The gas distribution pipe and the gas collection pipe have the same shape and size, and are arranged opposite each other up and down; the length of the temperature equalizing pipe is equal to the distance between the gas distribution pipe and the gas collection pipe. Figure 2 As shown, there are six equalizing tubes, all evenly distributed circumferentially between the gas distribution and collection tubes. Three primary and secondary cooling tubes are placed alternately between every two equalizing tubes, with the top of the secondary cooling tube higher than the bottom of the primary cooling tube. This allows for continuous, stable operation at low temperatures, even in the event of power shortages, unaffected by weather.

[0087] Example 3

[0088] like Figure 3 As shown, a YHL preparation system for photovoltaic and wind power generation hydrogen production and green ammonia synthesis includes an electrolytic hydrogen production device, a hydrogen purification device, a nitrogen production device, a high-pressure unit, a nitrogen and hydrogen storage tank, a first delivery pipe, a YHL synthesis tower for photovoltaic and wind power generation hydrogen production and green ammonia synthesis (Example 2), a second delivery pipe, a first heat exchanger, a third delivery pipe, a second heat exchanger, a fourth delivery pipe, an ammonia separator, a fifth delivery pipe, a liquid ammonia storage tank, a sixth delivery pipe and a synthesis cycle compressor, a seventh delivery pipe, and an eighth delivery pipe;

[0089] The hydrogen outlet of the electrolytic hydrogen production device is connected to the air inlet of the hydrogen purification device through a pipeline, and the air outlet of the hydrogen purification device is connected to the air inlet of the high-pressure unit through a pipeline; the nitrogen outlet of the nitrogen production device is connected to the air inlet of the high-pressure unit through a pipeline; the air outlet of the high-pressure unit is connected to the nitrogen and hydrogen storage tank through a pipeline; the electricity required by the electrolytic hydrogen production device is provided by the photovoltaic power generation device and the wind power generation device;

[0090] One end of the first delivery pipe is connected to the nitrogen and hydrogen storage tank, and the other end branches into a first delivery branch pipe A, a first delivery branch pipe B, and a first delivery branch pipe C. The first delivery branch pipe A is connected to the inlet of the synthesis cycle compressor and is provided with a control valve K1. The first delivery branch pipe B is connected to the secondary cooling air inlet at the bottom of the synthesis tower body and is provided with a control valve K2. The first delivery branch pipe C is connected to the primary cooling air inlet at the top of the synthesis tower body and is provided with a control valve K3.

[0091] The first heat exchanger is provided with a first hot material inlet, a first hot material outlet, a first cold material inlet and a first cold material outlet; the second heat exchanger is provided with a second hot material inlet, a second hot material outlet, a second cold material inlet and a second cold material outlet;

[0092] One end of the second delivery pipe is connected to the discharge port at the bottom of the synthesis tower body, and the other end is connected to the first hot material inlet. The second delivery pipe is provided with a control valve K4. One end of the third delivery pipe is connected to the first hot material outlet, and the other end is connected to the second hot material inlet. The third delivery pipe is provided with control valves K5 and K6. The second cold material inlet is connected to the outlet of the cold medium supply device through the cold medium inlet pipe. The cold medium inlet pipe is provided with a control valve K8. The second cold material outlet is connected to the inlet of the cold medium supply device through the cold medium outlet pipe.

[0093] One end of the fourth delivery pipe is connected to the second hot material outlet, and the other end is connected to the top feed port of the ammonia separator. A control valve K7 is provided on the fourth delivery pipe;

[0094] One end of the fifth delivery pipe is connected to the bottom discharge port of the ammonia separator, and the other end is connected to the liquid ammonia storage tank. A control valve K8' is provided on the fifth delivery pipe;

[0095] One end of the sixth delivery pipe is connected to the gas outlet at the top of the ammonia separator, and the other end is connected to the inlet of the synthesis cycle compressor. The sixth delivery pipe is provided with a control valve K9 and a control valve K10;

[0096] The seventh delivery pipe is connected to the outlet of the synthesis cycle compressor at one end and to the first cold material inlet at the other end. A control valve K11 is installed on the seventh delivery pipe. The eighth delivery pipe is connected to the first cold material outlet at one end and to the main air intake pipe at the bottom of the synthesis tower body at the other end. The second heat exchanger is supplied with a cold medium supply device, which is a cooling water circulation unit.

[0097] This application is for a system for YHL production of green ammonia. Hydrogen production uses discontinuous renewable electricity and can be controlled by YHL technology to achieve continuous production of green ammonia.

[0098] Example 4

[0099] Based on Example 3, the following improvements were made: the first heat exchanger is a double-tube heat exchanger; the second heat exchanger is a calandria heat exchanger; control valve K5 is located at the end of the third delivery pipe connected to the first hot material outlet, and control valve K6 is located at the end of the third delivery pipe connected to the second hot material inlet; control valve K9 is located at the end of the sixth delivery pipe connected to the top outlet of the ammonia separator, and control valve K10 is located at the end of the sixth delivery pipe connected to the inlet of the synthesis cycle compressor. In this example, the synthesis cycle compressor is a variable frequency device. Liquid ammonia from the liquid ammonia storage tank is transported to the target container via a delivery pump. Pumps, instruments, and other equipment can be connected to each pipeline as needed.

[0100] The method for producing ammonia using the YHL preparation system for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia comprises the following steps:

[0101] 1) Close all control valves, open the central heating pipe on the synthesis tower body, so that the temperature inside the synthesis tower body reaches 300-350 ° C, and then open the control valves except control valve K2 and control valve K3;

[0102] 2) The hydrogen produced by the electrolytic hydrogen production device is purified by the hydrogen purification device and then compressed with the nitrogen produced by the nitrogen production device in a ratio of 3:1.2 by the high-pressure unit. The compressed nitrogen-hydrogen mixed gas enters the nitrogen-hydrogen storage tank. The nitrogen-hydrogen mixed raw gas in the nitrogen-hydrogen storage tank passes through the first delivery branch pipe A, the synthesis cycle compressor, the seventh delivery pipe, the first heat exchanger, the eighth delivery pipe, and the air inlet main pipe in sequence, and then enters the preheater in the synthesis tower body. After being heated by the central heating pipe, it flows out from the top of the central heating pipe and enters the porous catalyst layer for a catalytic reaction to generate ammonia.

[0103] 3) Ammonia gas flows out of the discharge port at the bottom of the synthesis tower body, enters the first heat exchanger through the second delivery pipe, is cooled by the nitrogen-hydrogen mixed feed gas (i.e., the nitrogen-hydrogen mixed feed gas is heated by the gas flowing out of the discharge port at the bottom of the synthesis tower body), and then enters the second heat exchanger through the third delivery pipe for secondary cooling. Thereafter, it is delivered to the ammonia separator through the fourth delivery pipe to separate the unreacted nitrogen and hydrogen. The liquid ammonia in the ammonia separator enters the liquid ammonia storage tank through the fifth delivery pipe.

[0104] 4) The unreacted nitrogen and hydrogen separated by the ammonia separator enter the synthesis cycle compressor through the sixth delivery pipe to mix with the nitrogen and hydrogen mixed raw material gas, and then pass through the seventh delivery pipe, the first heat exchanger, the eighth delivery pipe and the air inlet main pipe in sequence, and then enter the synthesis tower body for inner cycle reaction;

[0105] 5) During the reaction process, the openings of the control valves K2 and K3 are controlled, and the nitrogen-hydrogen mixed raw material gas directly output from the nitrogen-hydrogen storage tank is used to cool the inner cylinder and the porous catalyst layer, so that the temperature inside the inner cylinder and the porous catalyst is maintained at 300°C and the pressure is maintained at 2MPa; the low-temperature reaction raw gas entering from the secondary cold air inlet cools the side wall of the inner cylinder from bottom to top, and finally flows from the top of the sandwich structure into the inner cylinder and enters the porous catalyst layer for reaction; the low-temperature reaction raw gas entering from the primary cold air inlet enters the gas distribution pipe through the transition pipe, circulates between the gas distribution pipe, the temperature equalizing pipe and the gas collecting pipe, forms a cooling for the porous catalyst layer, and when it flows through the first cooling pipe and the second cooling pipe, it flows into the porous catalyst layer through the air vents for reaction;

[0106] 6) When the hydrogen production capacity of the electrolytic hydrogen production device has been or is about to be affected by weather, the opening of the control valve K4 is adjusted to adjust the amount of hydrogen and nitrogen entering the synthesis tower body and the amount of liquid ammonia taken out, and the opening of the control valves K1, K2, K3 and K8 and the operating frequency of the synthesis cycle compressor are adjusted to control the temperature inside the synthesis tower body to be maintained at 300℃ ( Figure 3The temperature of T1 / T2 / T3 is 300℃, and the pressure is maintained at 2MPa to achieve continuous operation.

[0107] In this example, the porous catalyst's raw materials include 70% 200-mesh austenitic iron powder, 20% organic silica gel (Doher-711, Sains), and 10% additive, a mixture of 325-mesh kaolin, 250-mesh calcium carbonate powder, and 300-mesh diatomaceous earth in a mass ratio of 1:0.3:1. The catalyst is prepared by uniformly mixing the austenitic iron powder, silica gel, and additive, extruding into granules, and heating to 900°C under nitrogen at a rate of 6°C / min, calcining for 8 hours, and cooling naturally to obtain the porous catalyst. This catalyst exhibits high strength, no pulverization, and excellent stability, enabling continuous use for over three years. In this example, the ammonia synthesis rate was 65 mmol / (gh), with a single-pass conversion rate exceeding 37% and a recycle conversion rate exceeding 95%.

[0108] The nitrogen-hydrogen mixed feed gas in the nitrogen-hydrogen storage tank is kept at a temperature of approximately 25°C. The nitrogen-hydrogen mixed feed gas first passes through a synthesis cycle compressor to achieve a stable pressure, and then, after being heated by the product, enters the synthesis tower. This ensures operational stability while reducing energy consumption. This method allows for continuous, stable, and efficient operation when the electrolytic hydrogen production unit is adequately powered. It also allows for continuous, stable, and low-cost operation when the electrolytic hydrogen production unit is or is about to be affected by weather, which could impact hydrogen production.

[0109] Comparative Example 1

[0110] The difference from Example 4 is that 200-mesh reduced iron powder is used. The rest of the process is the same as in Example 4. Ammonia synthesis requires temperatures of 500-600°C and 35 MPa. The ammonia synthesis rate is 610 μmol / (gh).

[0111] Comparative Example 2

[0112] The difference from Example 4 is that all the auxiliary agents are kaolin, and the rest are the same as Example 4. The ammonia synthesis rate is 3020 μmol / (gh).

[0113] Comparative Example 3

[0114] The difference from Example 4 is that all the auxiliary agents are diatomaceous earth, and the rest are the same as Example 4. The ammonia synthesis rate is 4500 μmol / (gh).

[0115] Comparative Example 4

[0116] The difference from Example 4 is that all the auxiliary agents are calcium carbonate powder, and the rest are the same as Example 4. The ammonia synthesis rate is 2200 μmol / (gh).

Claims

1. A YHL preparation system for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia, characterized by: It includes a nitrogen and hydrogen storage tank, a first delivery pipe, a YHL synthesis tower for producing hydrogen and synthesizing green ammonia through photovoltaic and wind power generation, a second delivery pipe, a first heat exchanger, a third delivery pipe, a second heat exchanger, a fourth delivery pipe, an ammonia separator, a fifth delivery pipe, a liquid ammonia storage tank, a sixth delivery pipe and a synthesis cycle compressor, a seventh delivery pipe and an eighth delivery pipe; The YHL synthesis tower used for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia includes a synthesis tower body, an inner cylinder, a gas distribution pipe, a gas collecting pipe, a first cooling pipe, a second cooling pipe, a temperature equalizing pipe, a preheater, an air inlet main pipe, a central heating pipe and a transition pipe; The inner tube is located inside the synthesis tower body, with a gap between the inner tube and the synthesis tower body to form a sandwich structure, and the top of the sandwich structure is connected to the top of the inner tube; The gas distribution pipe, gas collecting pipe, first cooling pipe, second cooling pipe, temperature equalizing pipe, preheater, central heating pipe and transition pipe are all located inside the inner tube; The gas distribution pipe and the gas collection pipe are both annular pipes. The gas distribution pipe is located directly above the gas collection pipe, and a porous catalyst layer is arranged between the gas distribution pipe and the gas collection pipe. The first cooling tube, the second cooling tube and the equalizing tube are all located in the porous catalyst layer between the gas distribution tube and the gas collecting tube; the lengths of the first cooling tube and the second cooling tube are both less than the interval between the gas distribution tube and the gas collecting tube, the first cooling tube and the second cooling tube are staggered, the top of the first cooling tube is connected to the gas distribution tube, the bottom of the second cooling tube is connected to the gas collecting tube, and air holes are distributed on the side walls of the first cooling tube and the second cooling tube; the length of the equalizing tube is not less than the interval between the gas distribution tube and the gas collecting tube, the top of the equalizing tube is connected to the gas distribution tube, and the bottom is connected to the gas collecting tube; The preheater is located at the bottom of the gas collecting pipe. One end of the air inlet main pipe is connected to the air inlet on the preheater, and the other end passes through the bottom of the synthesis tower body. The top of the central heating pipe is connected to the air outlet on the preheater, passes through the porous catalyst layer, and penetrates the top of the inner cylinder. A primary cooling air inlet is provided at the top of the synthesis tower body, which is connected to the air distribution pipe through a transition pipe; a secondary cooling air inlet, a material discharge port and a waste discharge port are provided at the bottom of the synthesis tower body, and the secondary cooling air inlet is connected to the sandwich structure between the inner tube and the synthesis tower body; One end of the first delivery pipe is connected to the nitrogen and hydrogen storage tank, and the other end branches into a first delivery branch pipe A, a first delivery branch pipe B, and a first delivery branch pipe C. The first delivery branch pipe A is connected to the inlet of the synthesis cycle compressor and is provided with a control valve K1. The first delivery branch pipe B is connected to the secondary cooling air inlet at the bottom of the synthesis tower body and is provided with a control valve K2. The first delivery branch pipe C is connected to the primary cooling air inlet at the top of the synthesis tower body and is provided with a control valve K3. The first heat exchanger is provided with a first hot material inlet, a first hot material outlet, a first cold material inlet and a first cold material outlet; the second heat exchanger is provided with a second hot material inlet, a second hot material outlet, a second cold material inlet and a second cold material outlet; One end of the second delivery pipe is connected to the discharge port at the bottom of the synthesis tower body, and the other end is connected to the first hot material inlet. The second delivery pipe is provided with a control valve K4. One end of the third delivery pipe is connected to the first hot material outlet, and the other end is connected to the second hot material inlet. The third delivery pipe is provided with control valves K5 and K6. The second cold material inlet is connected to the outlet of the cold medium supply device through the cold medium inlet pipe. The cold medium inlet pipe is provided with a control valve K8. The second cold material outlet is connected to the inlet of the cold medium supply device through the cold medium outlet pipe. One end of the fourth delivery pipe is connected to the second hot material outlet, and the other end is connected to the top feed port of the ammonia separator. A control valve K7 is provided on the fourth delivery pipe; One end of the fifth delivery pipe is connected to the bottom discharge port of the ammonia separator, and the other end is connected to the liquid ammonia storage tank. A control valve K8' is provided on the fifth delivery pipe; One end of the sixth delivery pipe is connected to the gas outlet at the top of the ammonia separator, and the other end is connected to the inlet of the synthesis cycle compressor. The sixth delivery pipe is provided with a control valve K9 and a control valve K10; One end of the seventh delivery pipe is connected to the outlet of the synthesis cycle compressor and the other end is connected to the first cold material inlet. The seventh delivery pipe is provided with a control valve K11. One end of the eighth delivery pipe is connected to the first cold material outlet and the other end is connected to the air inlet main pipe at the bottom of the synthesis tower body. The raw material components of the porous catalyst layer include, by mass percentage, 50-70% austenitic iron powder, 15-20% silica gel, and the balance an additive, wherein the additive is a mixture of kaolin, calcium carbonate powder and diatomaceous earth in a mass ratio of 1:(0.2-0.5):(1-1.2); the catalyst preparation method comprises the following steps: uniformly mixing the austenitic iron powder, silica gel and the additive, extruding the mixture into granules, heating the mixture to 800-1000°C at a rate of 6-8°C / min under nitrogen protection, calcining the mixture for 8-10 hours, and naturally cooling the mixture to obtain the porous catalyst.

2. The YHL preparation system for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia according to claim 1, characterized in that: Temperature measuring devices are distributed on the top, middle and bottom of the inner tube; a porous catalyst layer is also distributed on the periphery of the preheater in the inner tube.

3. The YHL preparation system for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia according to claim 1 or 2, characterized in that: The gas distribution pipe and the gas collection pipe have the same shape and size and are arranged opposite to each other up and down.

4. The YHL preparation system for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia according to claim 1 or 2, characterized in that: The length of the temperature equalizing pipe is equal to the distance between the gas distribution pipe and the gas collecting pipe.

5. The YHL preparation system for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia according to claim 1 or 2, characterized in that: The number of temperature-averaging tubes is 4 to 8, and all temperature-averaging tubes are evenly distributed circumferentially between the gas distribution tube and the gas collection tube; 2 to 10 first cooling tubes and second cooling tubes are arranged alternately between every two temperature-averaging tubes; the top of the second cooling tube is higher than the bottom of the first cooling tube.

6. The YHL preparation system for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia according to claim 1 or 2, characterized in that: Also includes: An electrolytic hydrogen production device, a hydrogen purification device, a nitrogen production device and a high-pressure unit; the hydrogen outlet of the electrolytic hydrogen production device is connected to the air inlet of the hydrogen purification device through a pipeline, and the air outlet of the hydrogen purification device is connected to the air inlet of the high-pressure unit through a pipeline; the nitrogen outlet of the nitrogen production device is connected to the air inlet of the high-pressure unit through a pipeline; the air outlet of the high-pressure unit is connected to the nitrogen and hydrogen storage tank through a pipeline; the electric energy required for the electrolytic hydrogen production device is provided by a photovoltaic power generation device and a wind power generation device.

7. The YHL preparation system for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia according to claim 1 or 2, characterized in that: The first heat exchanger is a shell and tube heat exchanger; the second heat exchanger is a tube-and-tube heat exchanger; the control valve K5 is arranged on the end of the third delivery pipe connected to the first hot material outlet, and the control valve K6 is arranged on the end of the third delivery pipe connected to the second hot material inlet; the control valve K9 is arranged on the end of the sixth delivery pipe connected to the gas outlet at the top of the ammonia separator, and the control valve K10 is arranged on the end of the sixth delivery pipe connected to the inlet of the synthesis cycle compressor.

8. A method for synthesizing green ammonia using YHL, produced using the YHL preparation system for synthesizing green ammonia using photovoltaic and wind power generation hydrogen production as described in any one of claims 1 to 7, characterized in that: The steps include: 1) Close all control valves, open the central heating pipe on the synthesis tower body, so that the temperature inside the synthesis tower body reaches 300-350 ° C, and then open the control valves except control valve K2 and control valve K3; 2) The nitrogen-hydrogen mixed raw gas in the nitrogen-hydrogen storage tank passes through the first delivery branch pipe A, the synthesis cycle compressor, the seventh delivery pipe, the first heat exchanger, the eighth delivery pipe, and the air inlet main pipe in sequence, and then enters the preheater in the synthesis tower body. After being heated by the central heating pipe, it flows out from the top of the central heating pipe and enters the porous catalyst layer to catalyze the reaction to produce ammonia. 3) Ammonia gas flows out from the discharge port at the bottom of the synthesis tower body, enters the first heat exchanger through the second delivery pipe, is cooled by the nitrogen-hydrogen mixed feed gas, and then enters the second heat exchanger through the third delivery pipe for secondary cooling. Thereafter, it is delivered to the ammonia separator through the fourth delivery pipe to separate the unreacted nitrogen and hydrogen. The liquid ammonia in the ammonia separator enters the liquid ammonia storage tank through the fifth delivery pipe. 4) The unreacted nitrogen and hydrogen separated by the ammonia separator enter the synthesis cycle compressor through the sixth delivery pipe to mix with the nitrogen and hydrogen mixed raw material gas, and then pass through the seventh delivery pipe, the first heat exchanger, the eighth delivery pipe and the air inlet main pipe in sequence, and then enter the synthesis tower body for inner cycle reaction; 5) During the reaction process, the openings of the control valves K2 and K3 are controlled, and the nitrogen-hydrogen mixed raw material gas directly output from the nitrogen-hydrogen storage tank is used to cool the inner cylinder and the porous catalyst layer, so that the temperature inside the inner cylinder and the porous catalyst is maintained at 300-350°C and the pressure is maintained at 1-7 MPa; the low-temperature reaction raw gas entering from the secondary cold air inlet cools the side wall of the inner cylinder from bottom to top, and finally flows from the top of the sandwich structure into the inner cylinder and enters the porous catalyst layer for reaction; the low-temperature reaction raw gas entering from the primary cold air inlet enters the gas distribution pipe through the transition pipe, circulates between the gas distribution pipe, the temperature equalizing pipe and the gas collecting pipe, forms a cooling for the porous catalyst layer, and when it flows through the first cooling pipe and the second cooling pipe, it flows into the porous catalyst layer through the air vents for reaction; 6) When the hydrogen production capacity of the electrolytic hydrogen production device has been or is about to be affected by weather, the amount of hydrogen and nitrogen entering the synthesis tower body and the amount of liquid ammonia taken out are adjusted by adjusting the opening of the control valve K4, and the temperature inside the synthesis tower body is controlled to be maintained at 300-350°C and the pressure is maintained at 1-7 MPa by adjusting the opening of the control valve K1, control valve K2, control valve K3, and control valve K8 and adjusting the operating frequency of the synthesis cycle compressor to achieve low-material continuous operation.

9. The method for synthesizing green ammonia using YHL as claimed in claim 8, wherein: The hydrogen produced by the electrolytic hydrogen production device is purified by the hydrogen purification device and then enters the high-pressure unit for compression with the nitrogen produced by the nitrogen production device in a ratio of 3: (1~1.2). The compressed nitrogen-hydrogen mixture enters the nitrogen-hydrogen storage tank.

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