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

Abstract

The invention discloses a YHL synthesis tower for synthesizing green ammonia through photovoltaic wind power generation hydrogen production, a YHL preparation system and a method for synthesizing green ammonia through YHL. According to the YHL synthesis tower for photovoltaic wind power generation hydrogen production and green ammonia synthesis, through arrangement of the primary cold air inlet and the secondary cold air inlet in the synthesis tower body and improvement of related structures, balanced cooling of the inner cylinder and the catalyst layer is achieved, accurate temperature control is achieved, cooling media do not need to be additionally introduced, the energy utilization rate is increased, and the YHL synthesis tower is simple in structure and convenient to transform. When water electrolysis for hydrogen production through photovoltaic power generation or wind power generation is affected due to weather influence, continuous and stable operation of low materials and heat recovery are achieved by adjusting the opening degrees of the control valve K1, the control valve K2, the control valve K3 and the control valve K8, adjusting the operation frequency of the synthetic cycle compressor and the like, shutdown operation is not needed, the influence of weather on green ammonia production is reduced or avoided, and the production efficiency is improved. The foreseeability of production operation is improved, and the production problem caused by shutdown is reduced or avoided. The structure is ingenious and reasonable, energy is saved, and industrialization can be achieved.

Description

Technical Field

[0001] The 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 is renewable and environmentally friendly, and this advantage has led many countries, including China, to focus on developing solar energy as a new energy industry. Driven by my country's huge and diverse application market, my country's photovoltaic applications are constantly deepening, and various "photovoltaic" applications are emerging one after another.

[0003] Wind power generation is the process of converting wind kinetic energy into mechanical kinetic energy, and then converting mechanical energy into electrical kinetic energy. As a clean and renewable energy source, wind energy has great potential and is increasingly valued by countries around the world. Both at home and abroad, great importance is attached to using wind power to generate electricity and develop new energy. my country is rich in wind energy resources, with a developable wind energy reserve of about 1 billion kW.

[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 to electrolyze ammonia water are: photovoltaic / wind power generation is greatly affected by the weather, power generation is uneven, and hydrogen production by electrolysis of water is uneven, making it difficult to produce continuously and stably. It is often necessary to shut down at night, on rainy days, or in windless weather. However, after the shutdown and cooling, it usually takes about 7 days to restart the equipment to debug and stabilize and resume production, which not only brings huge energy consumption, but also seriously affects efficiency and production capacity, and cannot meet the continuous production needs of the 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 photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia. The YHL synthesis tower can realize continuous and stable operation of green ammonia preparation when hydrogen is produced by electrolyzing water through intermittent power generation such as photovoltaic or wind power generation, without the need to shut down 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 photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia.

[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 intake main pipe, a central heating pipe and a transition pipe;

[0010] The inner tube is located inside the synthesis tower body, and a gap is left between the inner tube and the synthesis tower body to form a sandwich structure, and the top of the sandwich structure is connected with 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. 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 collection 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 collection tube, the first cooling tube and the second cooling tube are arranged alternately, 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 collection 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 collection tube, the top of the equalizing tube is connected to the gas distribution tube, and the bottom is connected to the gas collection 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, the top passes through the porous catalyst layer, and is connected to the top of the inner tube;

[0015] A primary cold air inlet is provided at the top of the synthesis tower body, and the primary cold air inlet 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 refers to optimized controlled continuous production. The preheater is provided with an air inlet and an air outlet. The raw gas enters from the air inlet, is preheated, and then flows out from the air outlet. The preheater uses the temperature of the gas in the inner cylinder to preheat the temperature of the newly-input raw material. Photovoltaic and wind power generation hydrogen production refers to the use of photovoltaic power generation or wind power generation to produce hydrogen.

[0018] When in 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, and then flows out from the top of the central heating tube, and enters the porous catalyst layer for frequent catalytic reaction. The present application is provided with a secondary cold air inlet and a primary cold air inlet at the same time, and 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, so as to form cooling for the inner tube and the porous catalyst layer. 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 from the top of the sandwich structure into the inner tube 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-averaging pipe and the gas collecting pipe, forms cooling for the porous catalyst layer, and flows into the porous catalyst layer through the air vents when flowing through the first cooling pipe and the second cooling pipe. 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 realizes 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 on the periphery of the preheater in 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] For ease of assembly, the length of the temperature equalizing pipe is equal to the spacing between the gas distribution pipe and the gas collecting pipe.

[0024] As one specific implementation scheme, the number of temperature-averaging tubes is 4 to 8, and all temperature-averaging tubes are evenly distributed between the gas distribution tube and the gas collection tube along the circumferential direction; 2 to 10 first cooling tubes and second cooling tubes are arranged alternately between every two temperature-averaging tubes. The aforementioned 2 to 4 refer to the total number of first cooling tubes 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, continuous and stable operation with low material consumption can be achieved without being affected by weather conditions.

[0027] A YHL preparation system for photovoltaic 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 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 is branched 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 a control valve K1 is provided on the first delivery branch pipe A; the first delivery branch pipe B is connected to the secondary cold air inlet at the bottom of the synthesis tower body, and a control valve K2 is provided on the first delivery branch pipe B; the first delivery branch pipe C is connected to the primary cold air inlet at the top of the synthesis tower body, and a control valve K3 is provided on the first delivery branch pipe C;

[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, and a control valve K4 is provided on the second delivery pipe; 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, and a control valve K5 and a control valve K6 are provided on the third delivery pipe; the second cold material inlet is connected to the outlet of the cold medium supply device through the cold medium inlet pipe, and a control valve K8 is provided on the cold medium inlet pipe, and 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 leads 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] The present application is for a system for producing green ammonia by YHL, in which discontinuous renewable electricity is used for hydrogen production and can be controlled by YHL technology to achieve continuous production of green ammonia.

[0036] The above-mentioned ammonia separator adopts the existing ammonia liquid separator, and the ammonia separator is provided with a feed inlet (mixed material enters) and a gas outlet (unreacted gas flows) at the top, and a discharge port (liquid ammonia flows out) at the bottom.

[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 with 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 first heat exchanger is a shell and tube heat exchanger; the second heat exchanger is a row tube heat exchanger; the control valve K5 is arranged on one end of the third delivery pipe connected to the first hot material outlet, and the control valve K6 is arranged on one end of the third delivery pipe connected to the second hot material inlet; the control valve K9 is arranged on one end of the sixth delivery pipe connected to the top gas outlet of the ammonia separator, and the control valve K10 is arranged on one 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 by a delivery pump.

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

[0042] A method for producing ammonia from YHL, using the above-mentioned YHL preparation system for producing hydrogen and synthesizing 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 material 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 intake main pipe in sequence, and then enters the preheater in the synthesis tower body, and then is heated by the central heating pipe, flows out from the top of the central heating pipe, enters the porous catalyst layer, and is catalytically reacted to generate ammonia;

[0045] 3) Ammonia 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 raw material gas (that is, the nitrogen-hydrogen mixed raw material gas is heated by the gas flowing out from the discharge port at the bottom of the synthesis tower body), enters the second heat exchanger through the third delivery pipe for secondary cooling, and then is sent to the ammonia separator through the fourth delivery pipe to separate the unreacted nitrogen and hydrogen, and 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 enter the synthesis tower body for inner cycle reaction after passing through the seventh delivery pipe, the first heat exchanger, the eighth delivery pipe and the air inlet main pipe in sequence;

[0047] 5) During the reaction process, the opening of the control valve K2 and the control valve 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 tube and the porous catalyst layer, so that the temperature of the inner tube and the porous catalyst is maintained at 300-350°C, and the pressure is maintained at 1-7MPa; 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 from the top of the sandwich structure into the inner tube 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, it flows into the porous catalyst layer through the air holes 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 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 in the synthesis tower body is controlled to be maintained at 300-350°C and the pressure is maintained at 1-7MPa by adjusting the opening of the control valve K1, control valve K2, control valve K3, control valve K8 and adjusting the operating frequency of the synthesis cycle compressor to achieve continuous operation.

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

[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, low-material continuous operation and heat recovery can also be achieved.

[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 enters the synthesis tower after being heated by the product, 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 realizing both the cooling of the product and the 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 material is fed from the top and the bottom of the synthesis tower body at the same time, so as to achieve balanced control of the temperature of the inner cylinder and the porous catalyst layer.

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

[0055] In the above step 6), reducing or closing the control valve K2 / K3 / K8 can reduce the heat taken away, thereby reducing the hydrogen and nitrogen materials that need to maintain the temperature reaction in the tower. By adjusting the opening of the control valve 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 parts of the synthesis tower body are all equipped with temperature measuring devices) are maintained at the reaction temperature, thereby achieving continuous operation. When the power supply is restored, it can be operated according to steps 2)-5).

[0056] The synthesis of ammonia through nitrogen and hydrogen is an exothermic reaction. When the unit is started, once the temperature in the synthesis tower reaches the specified temperature, continuous heating is not required. At the same time, materials can be fed in multiple directions 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 mixed gas enters the nitrogen-hydrogen storage tank;

[0058] The raw material components of the porous catalyst include, by mass percentage, 50-70% austenitic iron powder, 15-20% silica gel, and the balance of auxiliary agents, wherein the auxiliary agent 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 preparation method of the catalyst is as follows: the austenitic iron powder, silica gel and auxiliary agents are uniformly mixed, extruded into granules, heated to 800-1000°C at a speed of 6-8°C / min under nitrogen protection, calcined for 8-10 hours, and cooled naturally to obtain the porous catalyst. The porous catalyst has high strength and good stability and can be used continuously for more than 3 years.

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

[0060] The raw materials not specifically described in this application were of analytical grade AR.

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

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

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

[0064] 1) By setting the primary and secondary cold air inlets on the synthesis tower body and improving the related structures, balanced cooling of the inner tube and the catalyst layer is achieved, precise temperature control is achieved, and no additional cooling medium is required, thus improving energy utilization, simple structure and easy 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 low-material continuous and stable operation 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 downtime.

[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 energy saving. BRIEF DESCRIPTION OF THE DRAWINGS

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

[0069] Figure 2 This is a schematic diagram of the gas flow direction of the temperature equalizing tube of the present invention;

[0070] Figure 3 It is a structural schematic diagram of the YHL preparation system for producing hydrogen and synthesizing green ammonia by 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 tube, 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 cold air inlet, 113 is a secondary cold 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. DETAILED DESCRIPTION

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

[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", "counterclockwise", etc. are based on the orientation or position relationship shown in the drawings or in use, and are only for the convenience of describing the application, 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 a limitation on the application.

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

[0076] Example 1

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

[0078] The inner tube is located inside the synthesis tower body, and a gap is left between the inner tube and the synthesis tower body to form a sandwich structure, and the top of the sandwich structure is connected with 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. 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 collection 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 collection tube, the first cooling tube and the second cooling tube are arranged alternately, 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 collection 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 collection tube, the top of the equalizing tube is connected to the gas distribution tube, and the bottom is connected to the gas collection 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, the top passes through the porous catalyst layer, and is connected to the top of the inner tube;

[0083] A primary cold air inlet is provided at the top of the synthesis tower body, and the primary cold air inlet 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] When in 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, and then flows out from the top of the central heating tube, and enters the porous catalyst layer for frequent catalytic reaction. The present application is provided with a secondary cold air inlet and a primary cold air inlet at the same time, and 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, so as to form cooling for the inner tube and the porous catalyst layer. 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 from the top of the sandwich structure into the inner tube 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-averaging 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 permeable hole for reaction. 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 the 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] On the basis of Example 1, the following improvements are made: temperature measuring devices are distributed at the top (T1), middle (T2), and bottom (T3) of the inner tube; a porous catalyst layer is also distributed on the periphery of the preheater in the inner tube, and the porous catalyst layer in the inner tube extends 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 to 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 6 temperature-averaging tubes, all of which are evenly distributed between the gas distribution tube and the gas collection tube along the circumferential direction; 3 first cooling tubes and second cooling tubes are arranged alternately between every two temperature-averaging tubes, and the top of the second cooling tube is higher than the bottom of the first cooling tube. In the case of insufficient power, low-material continuous and stable operation can be achieved without being affected by weather.

[0087] Example 3

[0088] like Figure 3 As shown, a YHL preparation system for photovoltaic 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 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 electric energy 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 is branched 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 a control valve K1 is provided on the first delivery branch pipe A; the first delivery branch pipe B is connected to the secondary cold air inlet at the bottom of the synthesis tower body, and a control valve K2 is provided on the first delivery branch pipe B; the first delivery branch pipe C is connected to the primary cold air inlet at the top of the synthesis tower body, and a control valve K3 is provided on the first delivery branch pipe C;

[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, and a control valve K4 is provided on the second delivery pipe; 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, and a control valve K5 and a control valve K6 are provided on the third delivery pipe; the second cold material inlet is connected to the outlet of the cold medium supply device through the cold medium inlet pipe, and a control valve K8 is provided on the cold medium inlet pipe, and 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 leads 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] 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 intake main pipe at the bottom of the synthesis tower body. The second heat exchanger is provided with a cold source through a cold medium supply device, which is a cooling water circulation machine.

[0097] The present application is for a system for producing green ammonia by YHL, in which discontinuous renewable electricity is used for hydrogen production and can be controlled by YHL technology to achieve continuous production of green ammonia.

[0098] Example 4

[0099] On the basis of Example 3, the following improvements are further made: 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 top gas outlet 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. In this example, the synthesis cycle compressor is a variable frequency device. The liquid ammonia in the liquid ammonia storage tank is transported to the target container by a delivery pump. Pump bodies, 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 enters the high-pressure unit for compression with the nitrogen produced by the nitrogen production device at a ratio of 3:1.2, and the compressed nitrogen-hydrogen mixed gas enters the nitrogen-hydrogen storage tank; the nitrogen-hydrogen mixed raw material 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 intake main pipe in sequence, and then enters the preheater in the synthesis tower body, and then is heated by the central heating pipe, flows out from the top of the central heating pipe, and enters the porous catalyst layer to catalyze the reaction to generate ammonia;

[0103] 3) Ammonia 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 raw material gas (that is, the nitrogen-hydrogen mixed raw material gas is heated by the gas flowing out from the discharge port at the bottom of the synthesis tower body), enters the second heat exchanger through the third delivery pipe for secondary cooling, and then is sent to the ammonia separator through the fourth delivery pipe to separate the unreacted nitrogen and hydrogen, and 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 enter the synthesis tower body for inner cycle reaction after passing through the seventh delivery pipe, the first heat exchanger, the eighth delivery pipe and the air inlet main pipe in sequence;

[0105] 5) During the reaction process, the opening of the control valve K2 and the control valve 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 tube and the porous catalyst layer, so that the temperature of the inner tube 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 tube from bottom to top, and finally flows from the top of the sandwich structure into the inner tube 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, it flows into the porous catalyst layer through the air holes for reaction;

[0106] 6) When the hydrogen production capacity of the electrolytic hydrogen production device has been or will 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 in the synthesis tower body is controlled to be maintained at 300℃ ( Figure 3The temperatures of T1 / T2 / T3 are all 300°C), and the pressure is maintained at 2MPa to achieve continuous operation.

[0107] In this example, the raw material components of the porous catalyst include: 70% 200-mesh austenitic iron powder, 20% organic silica gel (Doher-711, Sains) and 10% additives, the additives are 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 preparation method of the catalyst is: the austenitic iron powder, silica gel and additives are mixed evenly, extruded into granules, heated to 900°C at a rate of 6°C / min under nitrogen protection, calcined for 8 hours, and cooled naturally to obtain a porous catalyst. This catalyst has high strength, no powdering, good stability, and can be used continuously for more than 3 years. In this example, the synthesis rate of ammonia is: 65mmol / (gh), the single conversion rate is more than 37%, and the cycle conversion rate reaches more than 95%.

[0108] The temperature of the nitrogen-hydrogen mixed raw material gas in the nitrogen-hydrogen storage tank is about 25°C. The nitrogen-hydrogen mixed raw material gas first passes through the synthesis cycle compressor to form a stable pressure, and then enters the synthesis tower after being heated by the product, which not only ensures the stability of operation, but also reduces energy consumption. 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 the weather and the hydrogen production is affected, it can operate continuously and stably with low materials.

[0109] Comparative Example 1

[0110] The difference from Example 4 is that 200 mesh reduced iron powder is used, and the rest is the same as Example 4. Ammonia can only be synthesized at 500-600°C and 35MPa. The ammonia synthesis rate is 610μmol / (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 rate of synthetic ammonia 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 rate of synthetic ammonia 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 rate of synthetic ammonia is 2200 μmol / (gh).

Claims

1. A YHL synthesis tower for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia, characterized by: 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 intake main pipe, a central heating pipe and a transition pipe; The inner tube is located inside the synthesis tower body, and a gap is left between the inner tube and the synthesis tower body to form a sandwich structure, and the top of the sandwich structure is connected with 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. 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 collection 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 collection tube, the first cooling tube and the second cooling tube are arranged alternately, 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 collection 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 collection tube, the top of the equalizing tube is connected to the gas distribution tube, and the bottom is connected to the gas collection 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, the top passes through the porous catalyst layer, and is connected to the top of the inner tube; A primary cold air inlet is provided at the top of the synthesis tower body, and the primary cold air inlet 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.

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

3. The YHL synthesis tower for photovoltaic and wind power generation hydrogen production and green ammonia synthesis as claimed in 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 synthesis tower for photovoltaic and wind power generation hydrogen production and green ammonia synthesis as claimed in 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 synthesis tower for photovoltaic and wind power generation hydrogen production and green ammonia synthesis as claimed in 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 between the gas distribution tube and the gas collection tube along the circumferential direction; 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. 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 photovoltaic wind power generation hydrogen production and green ammonia synthesis according to any one of claims 1 to 5, 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; One end of the first delivery pipe is connected to the nitrogen and hydrogen storage tank, and the other end is branched 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 a control valve K1 is provided on the first delivery branch pipe A; the first delivery branch pipe B is connected to the secondary cold air inlet at the bottom of the synthesis tower body, and a control valve K2 is provided on the first delivery branch pipe B; the first delivery branch pipe C is connected to the primary cold air inlet at the top of the synthesis tower body, and a control valve K3 is provided on the first delivery branch pipe C; 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, and a control valve K4 is provided on the second delivery pipe; 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, and a control valve K5 and a control valve K6 are provided on the third delivery pipe; the second cold material inlet is connected to the outlet of the cold medium supply device through the cold medium inlet pipe, and a control valve K8 is provided on the cold medium inlet pipe, and 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 leads 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.

7. The YHL preparation system for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia as claimed in claim 6, 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 with 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 by the electrolytic hydrogen production device is provided by a photovoltaic power generation device and a wind power generation device.

8. The YHL preparation system for photovoltaic and wind power generation to produce hydrogen and synthesize green ammonia as claimed in claim 6 or 7, characterized in that: The first heat exchanger is a shell and tube heat exchanger; the second heat exchanger is a tube-type heat exchanger; the control valve K5 is arranged on one end of the third delivery pipe connected to the first hot material outlet, and the control valve K6 is arranged on one end of the third delivery pipe connected to the second hot material inlet; the control valve K9 is arranged on one end of the sixth delivery pipe connected to the top gas outlet of the ammonia separator, and the control valve K10 is arranged on one end of the sixth delivery pipe connected to the inlet of the synthesis cycle compressor.

9. A method for synthesizing green ammonia by YHL, produced by using the YHL preparation system for synthesizing green ammonia by photovoltaic and wind power generation and hydrogen production as described in any one of claims 6 to 8, 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 material 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 intake main pipe in sequence, and then enters the preheater in the synthesis tower body, and then is heated by the central heating pipe, flows out from the top of the central heating pipe, enters the porous catalyst layer, and is catalytically reacted to generate ammonia; 3) Ammonia 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 raw gas, enters the second heat exchanger through the third delivery pipe for secondary cooling, and then is sent to the ammonia separator through the fourth delivery pipe to separate the unreacted nitrogen and hydrogen, and 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 enter the synthesis tower body for inner cycle reaction after passing through the seventh delivery pipe, the first heat exchanger, the eighth delivery pipe and the air inlet main pipe in sequence; 5) During the reaction process, the opening of the control valve K2 and the control valve K3 is 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 of the inner cylinder and the porous catalyst is maintained at 300-350°C, and the pressure is maintained at 1-7MPa; 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, it flows into the porous catalyst layer through the air holes 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 in the synthesis tower body is controlled to be maintained at 300-350°C and the pressure is maintained at 1-7MPa by adjusting the opening of the control valve K1, control valve K2, control valve K3, control valve K8 and adjusting the operating frequency of the synthesis cycle compressor, so as to achieve low-material continuous operation.

10. The method for synthesizing green ammonia using YHL as claimed in claim 9, characterized in that: 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 mixed gas enters the nitrogen-hydrogen storage tank; The raw material components of the porous catalyst include, by mass percentage, 50-70% austenite iron powder, 15-20% silica gel, and The remaining amount of the auxiliary agent 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 preparation method of the catalyst is as follows: the austenitic iron powder, silica gel and the auxiliary agent are mixed evenly, extruded into granules, heated to 800-1000°C at a speed of 6-8°C / min under nitrogen protection, calcined for 8-10 hours, and cooled naturally to obtain a porous catalyst.

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