Tower type solar thermochemical ammonia production system and ammonia production method

Abstract

The invention discloses a tower type solar thermochemical ammonia production system and an ammonia production method. Sunlight is reflected to a solar heat collection tower by a heliostat field for heat collection; the solar heat collection tower is connected with all the reaction kettles and the CO reactor and is used for providing heat required by reaction; the CO reactor, the catalyst sample tank and the water vapor storage tank are connected with all the reaction kettles; wherein in the reaction kettle, the high-valence metal oxide conveyed by the catalyst sample tank is firstly subjected to a reduction reaction with CO, and then the low-valence metal oxide is subjected to a cracking reaction with water vapor to obtain hydrogen; the nitrogen and the hydrogen enter an ammonia reaction device for ammonia synthesis reaction, and ammonia gas is prepared. According to the invention, solar photo-thermal is used as a heat source, hydrogen is prepared by cracking water through a circulating oxidation-reduction reaction, and ammonia is further synthesized, so that the production energy consumption and the production cost of ammonia synthesis are reduced, and environment-friendly, efficient and recyclable ammonia synthesis is realized.

Description

Technical Field

[0001] The invention relates to the technical field of ammonia synthesis, and in particular to a tower-type solar thermal chemical ammonia production system and an ammonia production method. Background Art

[0002] Ammonia is a multifunctional compound used in the nitrogen fertilizer industry, organic synthesis industry, and as a raw material for the manufacture of nitric acid, ammonium salts, and soda ash. It is also a commonly used refrigerant, and the domestic market has a huge demand for it. In addition, ammonia energy, as a new energy source with environmental protection, high energy density, high safety, and low transportation and storage costs, can be directly used as hydrogen-rich fuel or as an energy carrier for hydrogen, and has broad development prospects in the fields of ammonia-hydrogen and ammonia-electricity.

[0003] At present, the synthesis process of ammonia mainly uses coal as raw material. Hydrogen is produced through coal gas, and then reacts with nitrogen to synthesize ammonia under high temperature (300-500℃) and high pressure (20.26-30.39MPa) environment. However, this process has problems such as high energy consumption, high CO2 emissions, and high production costs. Summary of the invention

[0004] In view of the deficiencies in the prior art, the present invention provides a tower solar thermochemical ammonia production system and an ammonia production method, which utilize solar thermal energy as a heat source and crack water through a cyclic redox reaction to produce hydrogen, and further synthesize ammonia, thereby reducing the production energy consumption and production cost of synthetic ammonia and realizing environmentally friendly, efficient and recyclable ammonia synthesis.

[0005] The present invention discloses a tower solar thermal chemical ammonia production system, comprising: a tower solar heat collection module, a photothermal reaction module and an ammonia production module;

[0006] The tower-type solar thermal collection module comprises a heliostat field and a solar thermal collection tower, wherein the heliostat field reflects sunlight to the solar thermal collection tower and converts the collected solar energy into thermal energy;

[0007] The photothermal reaction module includes at least one reactor, a CO reactor, a catalyst sample tank and a water vapor storage tank. The solar collector tower is connected to all the reactors and the CO reactor to provide the heat required for the reaction; the CO reactor is connected to all the reactors through a No. 1 pressure pump, the catalyst sample tank is connected to all the reactors through a powder particle solid feeder, and the water vapor storage tank is connected to all the reactors through a No. 2 pressure pump; wherein, in the reactor, the high-valent metal oxide transported by the catalyst sample tank is first subjected to a reduction reaction with the CO transported by the CO reactor to obtain a low-valent metal oxide and CO2, and the CO2 is returned to the CO reactor to react with the carbon material to regenerate CO; then, the low-valent metal oxide is subjected to a cracking reaction with the water vapor transported by the water vapor storage tank to obtain a high-valent metal oxide and hydrogen;

[0008] The ammonia production module includes an ammonia reaction device and an ammonia collection device. Nitrogen and hydrogen produced by the photothermal reaction module enter the ammonia reaction device to undergo a synthetic ammonia reaction, and the produced ammonia is transported to the ammonia collection device.

[0009] As a further improvement of the present invention, the number of reactors is 2, namely reactor No. 1 and reactor No. 2, and reactor No. 1 and reactor No. 2 are arranged in parallel.

[0010] As a further improvement of the present invention, the heliostat field is composed of a plurality of heliostats surrounding a solar thermal collector tower. The heliostat field focuses sunlight onto the solar thermal collector tower. The temperature of the solar thermal collector tower is controlled by adjusting the height and angle of the heliostats, thereby controlling the heating temperature of the reactor and the CO reactor. The reactor may be a solid bed reactor or a fluidized bed reactor, and a stirring device is provided inside.

[0011] As a further improvement of the present invention, the high-valent metal oxide is a cage oxide, preferably Fe3O4; the low-valent metal oxide is FeO, and the average particle size of the high-valent metal oxide and the low-valent metal oxide is between 5-100 um.

[0012] As a further improvement of the present invention, in the reactor:

[0013] The reaction temperature of the reduction reaction is 680-710°C, and the chemical reaction equation is:

[0014] Fe3O4+CO=FeO+CO2;

[0015] The reaction temperature of the cracking reaction is 1000-1400°C, and the chemical reaction equation is:

[0016] FeO+H2O(l)=Fe3O4+H2.

[0017] As a further improvement of the present invention, the photothermal reaction module further comprises: a first condenser, a hydrogen membrane separator, an exhaust gas storage tank and a hydrogen storage tank;

[0018] The gas outlet of the reactor is connected to a No. 1 condenser, which is used to remove water vapor in the high-temperature mixed gas containing hydrogen. The removed water vapor is transported to the water vapor storage tank through a No. 3 pressure pump, and the remaining gas after the water vapor is removed enters the hydrogen membrane separator; the purified hydrogen separated by the hydrogen membrane separator is stored in the hydrogen storage tank, and the waste gas after hydrogen separation is stored in the waste gas storage tank; the hydrogen storage tank is connected to the ammonia reaction device.

[0019] As a further improvement of the present invention, the ammonia production module also includes: a No. 2 condenser; the No. 2 condenser is placed between the ammonia reaction device and the ammonia collection device, and is used to reduce the temperature of the generated ammonia to facilitate collection.

[0020] The present invention also discloses a tower-type solar thermal chemical ammonia production method, comprising:

[0021] Step 1: At the beginning, all valves are in a closed state, and a high-valent metal oxide as a catalyst is added to the reactor through a powder particle solid feeder, and evenly stirred to disperse it; the No. 1 pressure pump is turned on, and CO gas is introduced into the reactor by the CO reactor, and the temperature of the reactor is controlled to be 680-710°C, and a reduction reaction occurs. The reaction time is 30-60 minutes. After the reaction is complete, the CO2 generated is collected back to the CO reactor, and the CO2 reacts with the carbon material in the CO reactor to regenerate CO;

[0022] Step 2, turn off the No. 1 pressure pump, turn on the No. 2 pressure pump, introduce water vapor into the reactor, control the temperature of the reactor to 1000-1400° C., and cause a cracking reaction for 30-60 minutes to obtain a high-valent metal oxide and hydrogen;

[0023] Step 3: Add nitrogen and hydrogen obtained by the cracking reaction in step 2 to an ammonia reaction device, control the temperature of the ammonia reaction device to 400-500°C, generate ammonia for 30-60 minutes, and collect ammonia generated by the reaction in an ammonia collection device.

[0024] As a further improvement of the present invention, in step 1,

[0025] CO2 reacts with the carbon material in the CO reactor at 600-800°C to regenerate CO, achieving the recycling of CO.

[0026] As a further improvement of the present invention, in step 2,

[0027] The mixed gas containing hydrogen generated by the cracking reaction is first cooled by the No. 1 condenser to remove excess water vapor, and the removed water vapor is transported to the water vapor storage tank by the No. 3 pressure pump, and the remaining gas after the water vapor is removed enters the hydrogen membrane separator; the purified hydrogen separated by the hydrogen membrane separator is stored in the hydrogen storage tank, and the waste gas after hydrogen separation is stored in the waste gas storage tank, and the hydrogen in the hydrogen storage tank is transported to the ammonia reaction device.

[0028] As a further improvement of the present invention, in step 3,

[0029] The ammonia generated by the reaction is cooled by the No. 2 condenser, and the remaining gas is discharged after treatment and collected by the ammonia collection device.

[0030] Compared with the prior art, the present invention has the following beneficial effects:

[0031] 1. The present invention adopts a chemical cycle heat method, and the metal oxide is continuously recycled in the reactor. The raw materials consumed are only carbon substances, water and nitrogen, and the process cost is low;

[0032] 2. The present invention uses solar energy as a heat source and utilizes a solar collector tower to convert the collected solar energy into thermal energy, providing the required heat for the reactor to perform reduction reaction and cracking reaction and the CO reactor to perform CO preparation, converting thermal energy into chemical energy, thereby reducing the process energy consumption of the entire ammonia production system;

[0033] 3. The present invention collects the CO2 generated by the reduction reaction in the reactor into the CO reactor to further generate CO, and almost no CO2 is emitted;

[0034] 4. The present invention has high energy utilization efficiency, reduces waste of exhaust heat, and obtains higher ammonia production efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0035] Figure 1 The present invention is a schematic structural diagram of a tower-type solar thermal chemical ammonia production system disclosed in the present invention.

[0036] In the figure:

[0037] 1- heliostat field, 2- solar collector tower, 3- reactor No. 1, 4- reactor No. 2, 5- catalyst sample tank, 6- powder particle solid feeder, 7- water vapor storage tank, 8- pressure pump No. 1, 9- pressure pump No. 2, 10- condenser No. 1, 11- hydrogen membrane separator, 12- waste gas storage tank, 13- hydrogen storage tank, 14- ammonia reaction device, 15- condenser No. 2, 16- ammonia collection device, 17- CO reactor, 18- pressure pump No. 3. DETAILED DESCRIPTION

[0038] In order to make the purpose, technical solution and advantages of the embodiments of the present invention clearer, the technical solution in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0039] The present invention is further described in detail below in conjunction with the accompanying drawings:

[0040] like Figure 1 As shown, the present invention provides a tower solar thermal chemical ammonia production system, comprising: a tower solar thermal collection module, a photothermal reaction module and an ammonia production module; wherein,

[0041] The tower solar thermal collector module of the present invention comprises a heliostat field 1 and a solar thermal collector tower 2. The heliostat field 1 is composed of a plurality of heliostats surrounding the solar thermal collector tower 2. The heliostat field 1 focuses sunlight onto the solar thermal collector tower 2. The temperature of the solar thermal collector tower 2 is controlled by adjusting the height and angle of the heliostats to convert the collected solar energy into thermal energy, thereby controlling the heating temperature of the No. 1 reactor 3, the No. 2 reactor 4 and the CO reactor 17.

[0042] The photothermal reaction module of the present invention comprises a No. 1 reactor 3, a No. 2 reactor 4, a catalyst sample tank 5, a powder particle solid feeder 6, a water vapor storage tank 7, a No. 1 pressure pump 8, a No. 2 pressure pump 9, a No. 1 condenser 10, a hydrogen membrane separator 11, an exhaust gas storage tank 12, a hydrogen storage tank 13, a CO reactor 17 and a No. 3 pressure pump 18; the solar heat collection tower 2 is connected to the No. 1 reactor 3, the No. 2 reactor 4, and the CO reactor 17 to provide the temperature required for the reduction, cracking and other reactions; the CO reactor 17 is connected to the No. 1 reactor 3, the No. 2 pressure pump 8 and the No. 1 pressure pump 8. The catalyst sample tank 5 is connected to the reactor 3 and the reactor 4 through the powder particle solid feeder 6, and is used to transport CO to the reactor 3 and the reactor 4 for reduction reaction; the catalyst sample tank 5 is connected to the reactor 3 and the reactor 4 through the powder particle solid feeder 6, and is used to transport high-valent metal oxides for reduction reaction to the reactor 3 and the reactor 4, and the high-valent metal oxides are cage oxides, preferably Fe3O4; the water vapor storage tank 7 is connected to the reactor 3 and the reactor 4 through the pressure pump 9, and is used to transport water vapor for cracking reaction to the reactor 3 and the reactor 4. Specifically, in the reactor 3 and the reactor 4, the high-valent metal oxide first undergoes a reduction reaction with CO to obtain low-valent metal oxide FeO and CO2, and CO2 returns to the CO reactor to react with the carbon material at 600-800°C to regenerate CO, so as to realize the recycling of CO; then, the low-valent metal oxide FeO undergoes a cracking reaction with water vapor to obtain high-valent metal oxides and hydrogen. A No. 1 condenser 10 is connected to the gas outlet of the No. 1 reactor 3 and the No. 2 reactor 4. The No. 1 condenser 10 is used to remove water vapor in the high-temperature mixed gas containing hydrogen. The removed water vapor is transported to the water vapor storage tank 7 through the No. 3 pressure pump 18, and the remaining gas after the water vapor is removed enters the hydrogen membrane separator 11; the purified hydrogen separated by the hydrogen membrane separator 11 is stored in the hydrogen storage tank 13, and the waste gas after the hydrogen is separated is stored in the waste gas storage tank 12.

[0043] The reaction temperature of the reduction reaction is 680-710°C, and the chemical reaction equation is:

[0044] Fe3O4+CO=FeO+CO2;

[0045] The reaction temperature of the cracking reaction is 1000-1400°C, and the chemical reaction equation is:

[0046] FeO+H2O(l)=Fe3O4+H2.

[0047] Furthermore, the No. 1 reactor 3 and the No. 2 reactor 4 can be solid bed reactors or fluidized bed reactors, and a stirring device is provided inside; the average particle size of the high-valent metal oxide and the low-valent metal oxide is between 5-100 um.

[0048] The ammonia production module of the present invention includes an ammonia reaction device 14, a second condenser 15 and an ammonia collection device 16 which are arranged in sequence. The hydrogen storage tank 13 is connected to the ammonia reaction device 14. Nitrogen and hydrogen from the hydrogen storage tank 13 enter the ammonia reaction device 14 to perform a synthetic ammonia reaction. The ammonia generated by the reaction is cooled by the second condenser 15, and the remaining gas is discharged after treatment. The ammonia is collected by the ammonia collection device 16.

[0049] The present invention provides a tower-type solar thermal chemical ammonia production method, comprising:

[0050] Step 1, at the beginning, all valves are in a closed state, and Fe3O4 as a catalyst in the catalyst sample tank 5 is added to the No. 1 reactor 3 and the No. 2 reactor 4 through the powder particle solid feeder 6, and is evenly stirred to disperse; the No. 1 pressure pump 8 is turned on, and CO gas is introduced into the No. 1 reactor 3 and the No. 2 reactor 4 by the CO reactor 17, and the temperature of the No. 1 reactor 3 and the No. 2 reactor 4 is controlled to be 680-710°C through the solar collector tower 2, and a reduction reaction occurs, and the reaction time is 30-60min, and low-valent metal oxide FeO and CO2 are obtained; CO2 generated after the reaction is complete is collected back to the CO reactor 17, and CO2 reacts with the carbon material in the CO reactor 17 at 600-800°C to regenerate CO, thereby realizing the recycling of CO;

[0051] Step 2, close the No. 1 pressure pump 8, open the No. 2 pressure pump 9, pass the water vapor in the water vapor storage tank 7 into the No. 1 reactor 3 and the No. 2 reactor 4, control the temperature in the No. 1 reactor 3 and the No. 2 reactor 4 to be 1000-1400°C, and the low-valent metal oxide FeO reacts with the water vapor for 30-60 minutes to obtain Fe3O4, hydrogen and other gases; the mixed gas containing hydrogen generated by the cracking reaction is first cooled by the No. 1 condenser 10 to remove excess water vapor, and the removed water vapor is transported to the water vapor storage tank 7 by the No. 3 pressure pump 18, and the remaining gas after the water vapor is removed enters the hydrogen membrane separator 11; the purified hydrogen separated by the hydrogen membrane separator 11 is stored in the hydrogen storage tank 13, and the waste gas after the hydrogen is separated is stored in the waste gas storage tank 12;

[0052] Step 3: Add the hydrogen in the nitrogen and hydrogen storage tanks 13 to the ammonia reaction device 14, control the temperature of the ammonia reaction device to 400-500°C, and produce ammonia synthesis for 30-60 minutes; the ammonia generated by the reaction is cooled by the second condenser 15, and the remaining gas is discharged after treatment, and the ammonia is collected by the ammonia collection device 16 to achieve the purpose of low energy consumption, low cost and high yield ammonia production.

[0053] Embodiment 1:

[0054] A tower solar thermal chemical ammonia production system and ammonia production method, wherein a metal oxide is used as a catalyst, and a reduction reaction is performed between the metal oxide and CO to generate a low-valent metal oxide, the reaction temperature is 680°C, and the reaction time is 30 minutes. The low-valent metal oxide and water vapor undergo a cracking reaction to regenerate a high-valent metal oxide and hydrogen, the reaction temperature is 1000°C, and the reaction time is 30 minutes. The hydrogen reacts with nitrogen in an ammonia reaction device to synthesize ammonia to generate ammonia, the reaction temperature is 400°C, and the reaction time is 30 minutes.

[0055] Embodiment 2:

[0056] A tower solar thermal chemical ammonia production system and ammonia production method, wherein a metal oxide is used as a catalyst, and a reduction reaction is performed between the metal oxide and CO to generate a low-valent metal oxide, the reaction temperature is 690°C, and the reaction time is 40 minutes. The low-valent metal oxide and water vapor undergo a cracking reaction to regenerate a high-valent metal oxide and hydrogen, the reaction temperature is 1100°C, and the reaction time is 40 minutes. The hydrogen reacts with nitrogen in an ammonia reaction device to synthesize ammonia to generate ammonia, the reaction temperature is 430°C, and the reaction time is 40 minutes.

[0057] Embodiment 3:

[0058] A tower solar thermal chemical ammonia production system and ammonia production method, wherein a metal oxide is used as a catalyst, and a reduction reaction is performed between the metal oxide and CO to generate a low-valent metal oxide, the reaction temperature is 700°C, and the reaction time is 50 minutes. The low-valent metal oxide and water vapor undergo a cracking reaction to regenerate a high-valent metal oxide and hydrogen, the reaction temperature is 1200°C, and the reaction time is 50 minutes. The hydrogen reacts with nitrogen in an ammonia reaction device to synthesize ammonia to generate ammonia, the reaction temperature is 470°C, and the reaction time is 50 minutes.

[0059] Embodiment 4:

[0060] A tower solar thermal chemical ammonia production system and ammonia production method, wherein a metal oxide is used as a catalyst, and a reduction reaction is performed between the metal oxide and CO to generate a low-valent metal oxide, the reaction temperature is 710°C, and the reaction time is 60 minutes. The low-valent metal oxide and water vapor undergo a cracking reaction to regenerate a high-valent metal oxide and hydrogen, the reaction temperature is 1400°C, and the reaction time is 60 minutes. The hydrogen reacts with nitrogen in an ammonia reaction device to synthesize ammonia to generate ammonia, the reaction temperature is 500°C, and the reaction time is 60 minutes.

[0061] The advantages of the present invention are:

[0062] 1. The present invention adopts a chemical cycle heat method, and the metal oxide is continuously recycled in the reactor. The raw materials consumed are only carbon substances, water and nitrogen. The process cost is low. Through industrial application, its process cost is only 18% of the traditional ammonia production process of coal-to-hydrogen production;

[0063] 2. The present invention uses solar energy as a heat source and utilizes a solar collector tower to convert the collected solar energy into thermal energy, providing the required heat for the reactor to perform reduction reaction and cracking reaction and the CO reactor to perform CO preparation, converting thermal energy into chemical energy, thereby reducing the process energy consumption of the entire ammonia production system;

[0064] 3. The present invention collects the CO2 generated by the reduction reaction in the reactor into the CO reactor to further generate CO, and almost no CO2 is emitted;

[0065] 4. The present invention has high energy utilization efficiency, reduces waste of exhaust heat, and obtains higher ammonia production efficiency.

[0066] The above are only preferred embodiments of the present invention and are not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A tower solar thermochemical ammonia production system, characterized in that: include: Tower solar thermal collection module, photothermal reaction module and ammonia production module; The tower-type solar thermal collection module comprises a heliostat field and a solar thermal collection tower, wherein the heliostat field reflects sunlight to the solar thermal collection tower and converts the collected solar energy into thermal energy; The photothermal reaction module includes at least one reactor, a CO reactor, a catalyst sample tank and a water vapor storage tank. The solar collector tower is connected to all the reactors and the CO reactor to provide the heat required for the reaction; the CO reactor is connected to all the reactors through a No. 1 pressure pump, the catalyst sample tank is connected to all the reactors through a powder particle solid feeder, and the water vapor storage tank is connected to all the reactors through a No. 2 pressure pump; wherein, in the reactor, the high-valent metal oxide transported by the catalyst sample tank is first subjected to a reduction reaction with the CO transported by the CO reactor to obtain a low-valent metal oxide and CO2, and the CO2 is returned to the CO reactor to react with the carbon material to regenerate CO; then, the low-valent metal oxide is subjected to a cracking reaction with the water vapor transported by the water vapor storage tank to obtain a high-valent metal oxide and hydrogen; The ammonia production module includes an ammonia reaction device and an ammonia collection device. Nitrogen and hydrogen produced by the photothermal reaction module enter the ammonia reaction device to undergo a synthetic ammonia reaction, and the produced ammonia is transported to the ammonia collection device. As a further improvement of the present invention, the number of reactors is 2, namely reactor No. 1 and reactor No. 2, and reactor No. 1 and reactor No. 2 are arranged in parallel.

2. The tower solar thermal chemical ammonia production system according to claim 1, characterized in that: The heliostat field is composed of a plurality of heliostats surrounding a solar collector tower. The heliostat field focuses sunlight onto the solar collector tower. The temperature of the solar collector tower is controlled by adjusting the height and angle of the heliostats, thereby controlling the heating temperature of the reactor and the CO reactor. The reactor is a solid bed reactor or a fluidized bed reactor, and a stirring device is arranged inside.

3. The tower solar thermal chemical ammonia production system according to claim 1, characterized in that: The high-valent metal oxide is Fe3O4; the low-valent metal oxide is FeO, and the average particle sizes of the high-valent metal oxide and the low-valent metal oxide are between 5-100 um.

4. The tower solar thermal chemical ammonia production system according to claim 3, characterized in that: In the reactor: The reaction temperature of the reduction reaction is 680-710°C, and the chemical reaction equation is: Fe3O4+CO=FeO+CO2; The reaction temperature of the cracking reaction is 1000-1400°C, and the chemical reaction equation is: FeO+H2O(l)=Fe3O4+H2.

5. The tower solar thermal chemical ammonia production system according to claim 1, characterized in that: The photothermal reaction module also includes: a No. 1 condenser, a hydrogen membrane separator, an exhaust gas storage tank and a hydrogen storage tank; The gas outlet of the reactor is connected to a No. 1 condenser, which is used to remove water vapor in the high-temperature mixed gas containing hydrogen. The removed water vapor is transported to the water vapor storage tank through a No. 3 pressure pump, and the remaining gas after the water vapor is removed enters the hydrogen membrane separator; the purified hydrogen separated by the hydrogen membrane separator is stored in the hydrogen storage tank, and the waste gas after hydrogen separation is stored in the waste gas storage tank; the hydrogen storage tank is connected to the ammonia reaction device.

6. The tower solar thermal chemical ammonia production system according to claim 1, characterized in that: The ammonia production module also includes: a second condenser; the second condenser is placed between the ammonia reaction device and the ammonia collection device, and is used to reduce the temperature of generated ammonia to facilitate collection.

7. A method for producing ammonia based on the tower solar thermochemical ammonia production system according to any one of claims 1 to 6, characterized in that: include: Step 1, adding a high-valent metal oxide as a catalyst into a reaction kettle through a powder particle solid feeder, and stirring evenly to disperse it; Turn on the No. 1 pressure pump, and the CO reactor introduces CO gas into the reactor. The temperature of the reactor is controlled at 680-710°C, and a reduction reaction occurs. The reaction time is 30-60 minutes. After the reaction is complete, the CO2 produced is collected back into the CO reactor; Step 2, turn off the No. 1 pressure pump, turn on the No. 2 pressure pump, introduce water vapor into the reactor, control the temperature of the reactor to 1000-1400° C., and cause a cracking reaction for 30-60 minutes to obtain a high-valent metal oxide and hydrogen; Step 3: Add nitrogen and hydrogen obtained by the cracking reaction in step 2 to an ammonia reaction device, control the temperature of the ammonia reaction device to 400-500°C, generate ammonia for 30-60 minutes, and collect ammonia generated by the reaction in an ammonia collection device.

8. The tower solar thermochemical ammonia production method according to claim 7, characterized in that: In step 1, CO2 reacts with the carbon material in the CO reactor at 600-800°C to regenerate CO, achieving the recycling of CO.

9. The tower solar thermochemical ammonia production method according to claim 7, characterized in that: In step 2, The mixed gas containing hydrogen generated by the cracking reaction is first cooled by the No. 1 condenser to remove excess water vapor, and the removed water vapor is transported to the water vapor storage tank by the No. 3 pressure pump, and the remaining gas after the water vapor is removed enters the hydrogen membrane separator; the purified hydrogen separated by the hydrogen membrane separator is stored in the hydrogen storage tank, and the waste gas after hydrogen separation is stored in the waste gas storage tank, and the hydrogen in the hydrogen storage tank is transported to the ammonia reaction device.

10. The tower solar thermochemical ammonia production method according to claim 9, characterized in that: In step 3, The ammonia generated by the reaction is cooled by the No. 2 condenser, and the remaining gas is discharged after treatment and collected by the ammonia collection device.

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