Carbon cycle ammonia production system and method based on chemical-looping water splitting

Abstract

According to the carbon cycle ammonia production system and method based on chemical-looping water splitting, in the carbon cycle ammonia production system based on chemical-looping water splitting, a chemical-looping carbon cycle nitrogen-hydrogen cogeneration module combines a fuel reactor and a high-temperature solid carbon dioxide electrolytic cell in a chemical-looping process, and hydrogen-nitrogen cogeneration with zero carbon emission is achieved. According to the Harbin process ammonia preparation module, multi-stage compression and intermediate cooling are carried out on raw material gas, the system energy consumption is reduced, and moisture used for a steam reactor is preheated. Then, a multi-stage reactor is adopted in the ammonia production process, heat recovery and raw material recovery are implemented, and a chemical chain product is efficiently converted into ammonia gas. The concentrating solar thermoelectric steam co-production module adopts molten salt as a working medium and is combined with a reheat return Rankine cycle containing a heat regenerator to meet the heat and electricity requirements of the system. The system utilizes a chemical-looping water splitting technology to prepare high-purity ammonia gas under a zero-carbon condition, and has the advantages of high efficiency, low emission, high resource utilization and the like.

Description

Technical Field

[0001] The present invention relates to the field of energy chemical technology, and in particular to a carbon cycle ammonia production system and method based on chemical chain water splitting. Background Art

[0002] Ammonia (NH3) is a crucial chemical in modern society, playing a vital role in the fertilizer industry, energy and chemical industry, and other fields. In the fertilizer sector, ammonia can be used to make ammonia fertilizer, which is crucial for agricultural production and has driven the rapid growth of the global population. In the energy and chemical industry, ammonia, due to its high hydrogen content, is a highly efficient energy carrier with high storage and transport stability, making it one of the most promising liquid energy carriers. The Haber process is a traditional ammonia production method. It uses a catalyst to synthesize nitrogen and hydrogen under high temperature and pressure to produce ammonia. Its technological maturity is widely recognized.

[0003] Traditional ammonia production processes rely on fossil energy for both raw materials (such as natural gas, heavy oil, or coal) and the necessary electricity consumption. Currently, every ton of ammonia produced generates approximately 2.9 tons of carbon dioxide equivalent emissions, roughly twice that of crude steel and four times that of cement. The ammonia synthesis industry accounts for 1%-2% of global energy consumption and contributes 1.2% of global carbon emissions. According to the International Energy Agency (IEA), ammonia production is expected to increase by a further 40% by 2050, maintaining its crucial position in the energy and chemical sectors. Therefore, developing green ammonia production processes utilizing renewable energy is crucial for reducing global carbon dioxide emissions, mitigating climate change, and achieving my country's dual carbon goals.

[0004] The information disclosed in this Background section is only for enhancement of understanding of the background of the invention and therefore it may contain information that does not form the prior art that is already known to a person of ordinary skill in the art. Summary of the Invention

[0005] In response to the shortcomings or defects of the above-mentioned existing technologies, a carbon cycle ammonia production system and method based on chemical chain water splitting is provided, which adopts high-temperature CO2 electrolyzer and concentrated solar energy technology to achieve new energy consumption and zero-carbon production, and solve the problems of high dependence on fossil fuels, high greenhouse gas emissions, and poor matching of new energy in conventional ammonia production processes.

[0006] The purpose of the present invention is achieved through the following technical solutions.

[0007] A carbon cycle ammonia production system based on chemical chain water splitting includes:

[0008] Chemical chain carbon cycle nitrogen and hydrogen co-generation module, which includes:

[0009] The water is pumped into the downstream water-cooled heat exchanger and the waste heat boiler in series for preheating.

[0010] Regenerator: air is pressurized by the air compressor and enters the regenerator for preheating.

[0011] The first mixer is connected to the waste heat boiler and the first separator to mix the preheated water with the high-pressure steam of the concentrated solar thermal power steam cogeneration module.

[0012] a steam reactor connected to the first mixer via a molten salt heat exchanger for reducing and generating hydrogen,

[0013] A dryer connected to the steam reactor and the waste heat boiler to dry the impurity-removed hydrogen,

[0014] The second mixer is connected to the oxygen storage tank and the regenerator via the oxygen flow control valve to mix the preheated air and oxygen.

[0015] An air reactor is connected to the second mixer to produce oxygen-depleted air, namely, crude nitrogen.

[0016] A fuel reactor connected to a carbon monoxide storage tank via a carbon monoxide flow control valve and to an air reactor for producing carbon dioxide,

[0017] A carbon dioxide storage tank is connected to the fuel reactor via a carbon dioxide compressor to temporarily compress and store carbon dioxide during low power generation.

[0018] a high-temperature solid oxide carbon dioxide electrolyzer connected to the carbon dioxide storage tank via a carbon dioxide flow control valve to reduce carbon dioxide to carbon monoxide when there is surplus power generation;

[0019] a carbon monoxide storage tank, one end of which is connected to the high-temperature solid oxide carbon dioxide electrolyzer, and the other end of which is connected to the fuel reactor via a carbon monoxide flow control valve, so as to temporarily store carbon monoxide. When the carbon monoxide flow control valve is limiting the flow, part of the carbon monoxide is stored during peak power generation, and when the carbon monoxide flow control valve is opened, the carbon monoxide is consumed during low power generation;

[0020] The Haber process ammonia module comprises:

[0021] A pressure swing adsorption device is connected to an air reactor via a waste heat boiler and a regenerator to treat the crude nitrogen,

[0022] A second separator is connected to the dryer via a waste heat boiler to separate part of the hydrogen.

[0023] A first mixer is connected to the pressure swing adsorption device and the second separator to mix the crude nitrogen and hydrogen in a stoichiometric ratio of 2.8 to 2.9 to form a production raw material.

[0024] a second mixer connected to the first mixer and the ammonia separator to mix the production raw materials and unreacted production raw materials;

[0025] The first multi-stage axial flow compressor, the second multi-stage axial flow compressor and the third multi-stage axial flow compressor are connected in series, which are connected to the second mixer and the downstream water-cooled heat exchanger to cool the production raw materials in the middle of the stage compression.

[0026] The first ammonia synthesis tower is connected to the third multi-stage axial flow compressor via the first regenerator to synthesize ammonia.

[0027] The second ammonia synthesis tower is connected to the first ammonia synthesis tower via a second regenerator to synthesize ammonia.

[0028] An ammonia separator is connected to the second ammonia synthesis tower to separate ammonia and unreacted production raw materials.

[0029] The carbon cycle ammonia production system based on chemical chain water splitting also includes a concentrated solar thermal power and steam cogeneration module, which includes:

[0030] The third mixer is connected to the water pump and the regenerator to mix the water input by the water pump and the high-temperature and high-pressure steam from the regenerator.

[0031] A first heat exchanger, which is connected to a third mixer for further heating,

[0032] a first steam turbine connected to the first heat exchanger for generating electricity,

[0033] a second heat exchanger connected to the first steam turbine to reheat the steam to form high-temperature and high-pressure steam;

[0034] The first separator has one end connected to the second heat exchanger and the other end connected to the first mixer and the second steam turbine to respectively feed high-temperature and high-pressure steam. The high-temperature and high-pressure steam entering the second steam turbine is input to the regenerator for heat recovery.

[0035] Cold molten salt storage tank, which stores molten salt and is pumped into the central receiving tower via molten salt pumps,

[0036] The Fresnel lens concentrates the light field towards the central receiving tower to produce hot molten salt,

[0037] A molten salt storage tank is connected to the central receiving tower via a pressure reducing valve to store molten salt. One end of the molten salt heat exchanger is connected between the pressure reducing valve and the molten salt storage tank via a molten salt flow control valve, and the other end is connected to the end of the molten salt storage tank away from the pressure reducing valve.

[0038] The fourth separator has one end connected to the hot molten salt storage tank, and the other end connected to the fourth mixer via the first heat exchanger and the second heat exchanger respectively, and the other end of the fourth mixer is connected to the cold molten salt storage tank.

[0039] In the carbon cycle ammonia production system based on chemical chain water splitting, the concentrated solar thermal power and steam cogeneration module further includes:

[0040] A power conversion hub connecting the first steam turbine and the second steam turbine for power supply

[0041] The power monitoring and control center is connected to the power conversion center to adjust flow and monitor power.

[0042] In the carbon cycle ammonia production system based on chemical chain water splitting, the power monitoring and control center connects and controls the carbon dioxide flow control valve, the carbon monoxide flow control valve, the oxygen flow control valve and the molten salt flow control valve.

[0043] In the carbon cycle ammonia production system based on chemical chain water splitting, the high-temperature carbon dioxide at the outlet of the fuel reactor is used as raw material, and the carbon cycle process is implemented by relying on a high-temperature solid oxide carbon dioxide electrolyzer.

[0044] In the carbon cycle ammonia production system based on chemical chain water splitting, the circulating carbon source is 1.5 to 2 times the carbon consumption in the carbon cycle process, and part of the carbon source is always temporarily stored in the carbon dioxide storage tank and the carbon monoxide storage tank in the form of carbon monoxide or carbon dioxide.

[0045] In the carbon cycle ammonia production system based on chemical chain water splitting, the hot molten salt-driven reheat returns to the Rankine cycle, and part of the reheated high-pressure steam and the steam from the waste heat boiler are introduced into the steam reactor.

[0046] In the carbon cycle ammonia production system based on chemical chain water splitting, the operating temperature of the fuel reactor is 850~1050℃, the operating temperature of the steam reactor is 600~900℃, the operating temperature of the air reactor is 1050~1250℃, and the reaction pressure is 1~30atm.

[0047] In the carbon cycle ammonia production system based on chemical chain water splitting, the electrolyte of the high-temperature solid oxide carbon dioxide electrolyzer is zirconium oxide, and the operating temperature is between 700 and 900°C.

[0048] The process method of the carbon cycle ammonia production system based on chemical chain water splitting includes the following steps:

[0049] Step 1: Based on the chemical chaining carbon cycle nitrogen and hydrogen co-production module, a chemical chaining water splitting process is used to convert preheated CO, H2O, and air into CO2, H2, and crude nitrogen, respectively, in a fuel reactor, a steam reactor, and an air reactor under the catalysis of an oxygen carrier. The H2 and crude nitrogen are then pretreated and ammonia produced in subsequent modules after heat recovery in a waste heat boiler.

[0050] In step 2, H2 and crude nitrogen are fed into the Haber process ammonia production module, where they are first subjected to a drying device and a pressure swing adsorption device to remove excess moisture and oxygen, ensuring that the purity of the pretreated raw gas meets the process requirements for ammonia synthesis. The raw gas, consisting of a mixture of H2 and nitrogen in a certain proportion, undergoes multi-stage compression and intermediate cooling in a water-cooling module. Ammonia is then produced in a multi-stage synthesis tower under the action of a catalyst. The reacted mixed gas containing nitrogen, hydrogen, and ammonia passes through a heat exchanger and leaves the synthesis tower. The generated ammonia is separated from the unreacted hydrogen and nitrogen by condensation, and the unreacted gas is recycled back to the reactor to continue the reaction.

[0051] In step 3, under the action of concentrated solar energy, molten salt is used as the heat transfer fluid medium in the cogeneration process. The cold molten salt is pumped into the solar receiving tower to form high-temperature hot molten salt. Part of the hot molten salt enters the hot salt tank to store heat to ensure the supply of thermal electricity at night, and the other part generates electricity in a reheat Rankine cycle containing a heat regenerator to meet the power consumption required by the compressor and electrolyzer.

[0052] Compared with the prior art, the present invention has the following beneficial effects:

[0053] (1) The chemical chaining carbon cycle nitrogen-hydrogen co-production module uses chemical chaining technology to produce nitrogen and hydrogen, which to a certain extent replaces the functions of the natural gas reforming process and air separation unit in the traditional ammonia production process, and effectively separates and collects CO2. Chemical chaining water splitting technology is an innovative production technology for clean hydrogen / low-carbon hydrogen. It can directly split water molecules into hydrogen through highly selective chemical reactions on metal oxide carriers, thereby avoiding direct fuel combustion and complex hydrogen purification steps, and improving energy efficiency. This technology divides fuel combustion, hydrogen production and heat energy release into three independent reactors: fuel reactor, steam reactor and air reactor in space through the oxygen gain and loss of oxygen by oxygen carriers in the cycle process, which can improve the selectivity of hydrogen production while reducing carbon emissions. The three-step cycle can independently generate hydrogen, carbon dioxide and oxygen-depleted air in different reactors. Among them, hydrogen and crude nitrogen can be used as raw materials for ammonia production after cleaning, and have a good material basis for integration with the ammonia production process.

[0054] (2) The chemical looping process and high-temperature solid oxide carbon dioxide electrolyzer have the advantage of integration, which can provide the latter with a stable carbon source of ideal temperature, pressure and purity, and achieve sustainable energy conversion with zero carbon emissions.

[0055] (3) The oxygen in the high-temperature carbon dioxide electrolysis cell can be sent to the air reactor (AR) after simple treatment, reducing the energy consumption of the air compression and preheating process. High-temperature solid oxide carbon dioxide electrolysis technology uses solid oxide as an electrolyte. Under high temperature conditions of 800~1000℃, CO2 molecules are first adsorbed on the cathode surface to form carbonate intermediates, and then the carbonate intermediates accept electrons and dissociate into CO and O at the three-phase boundary. 2- , then CO is output on the cathode surface, O 2- O₂ is transferred to the anode through the electrolyte, where it is generated through the oxygen evolution reaction. This technology offers advantages such as high selectivity, low overpotential, high efficiency, and low cost. When combined with renewable energy sources such as wind power and photovoltaics, high-temperature CO₂ electrolyzers can fully utilize waste heat from the chemical industry, enabling large-scale storage of renewable energy and resource utilization of CO₂. This provides an important path for storing intermittent renewable energy, helping to promote the transformation and upgrading of the energy structure.

[0056] (4) The nitrogen and hydrogen at the outlet reach the high pressure required for ammonia synthesis in a downstream heat exchanger with multi-stage compression and intermediate cooling without the need for residual pressure recovery. This reduces the mechanical energy consumption of high-pressure conditions and preheats the high-temperature steam required by the system. In addition, the preheated high-temperature steam can be connected in series with nitrogen and hydrogen of higher thermal quality, further increasing the heat and improving the energy utilization rate of the system.

[0057] (5) The dual-mode energy storage of high-temperature molten salt thermal storage and carbon monoxide chemical energy storage is adopted, combined with concentrated solar energy technology, to achieve the effect of "peak shaving and valley filling" under dual working conditions (day and night), ensuring the continuous and stable operation of the system's zero-carbon production.

[0058] (6) While achieving zero carbon emissions, the system combines carbon dioxide resource utilization technology, greatly reducing the storage period of carbon dioxide and the burden on auxiliary equipment, and avoiding the space consumption and capital consumption caused by the long-term storage of carbon dioxide.

[0059] (7) Solar energy is the light and heat energy radiated by the sun to the earth. It is a large-scale clean energy source. Concentrating solar energy technology can concentrate sunlight from a certain area into a small area under the action of a concentrating system, and receive and utilize the energy through a receiver or solar panel. Molten salt composed of sodium nitrate and potassium nitrate is a common heat transfer fluid medium in thermal power generation systems, with good energy storage and fluidity. By storing energy during power surpluses and releasing energy during peak power demand, molten salt energy storage can play a role in peak load shifting to a certain extent, thereby balancing the supply and demand relationship of the power grid, improving energy utilization, enhancing power grid stability and promoting the consumption of new energy. Real-time monitoring of the scale of green power output ensures the energy distribution and resources of the system under fluctuating conditions.

[0060] The above description is only an overview of the technical solution of the present invention. In order to make the technical means of the present invention clearer and easier to understand, so that those skilled in the art can implement it according to the contents of the description, and in order to make the above and other purposes, features and advantages of the present invention more obvious and easy to understand, the specific embodiments of the present invention are illustrated below. BRIEF DESCRIPTION OF THE DRAWINGS

[0061] Various other advantages and benefits of the present invention will become apparent to those skilled in the art upon reading the detailed description of the preferred embodiments below. The accompanying drawings are intended only to illustrate preferred embodiments and are not to be construed as limiting the present invention. It should be understood that the drawings described below are merely examples of the present invention, and that those skilled in the art will be able to derive other drawings from these drawings without inventive effort. Throughout the drawings, identical reference numerals are used to denote identical components.

[0062] In the attached figure:

[0063] Figure 1 A flow chart of a carbon cycle ammonia production system based on chemical chain water splitting provided by the present invention;

[0064] The chemical chain carbon cycle nitrogen and hydrogen co-production module: 1-01 water pump; 1-02 air compressor; 1-03 regenerator; 1-04 downstream water-cooled heat exchanger; 1-05 waste heat boiler; 1-06 first mixer; 1-07 molten salt heat exchanger; 1-08 steam reactor; 1-09 dryer; 1-10 air reactor; 1-11 fuel reactor; 1-12 carbon dioxide compressor; 1-13 carbon dioxide storage tank; 1-14 carbon dioxide flow control valve; 1-15 high-temperature solid oxide carbon dioxide electrolyzer; 1-16 carbon monoxide storage tank; 1-17 carbon monoxide flow control valve; 1-18 oxygen storage tank; 1-19 oxygen flow control valve; 1-20 second mixer;

[0065] The Haber process ammonia production module: 2-01 pressure swing adsorption device; 2-02 second separator; 2-03 first mixer; 2-04 second mixer; 2-05 first multi-stage axial flow compressor; 2-06 second multi-stage axial flow compressor; 2-07 third multi-stage axial flow compressor; 2-08 first regenerator; 2-09 first ammonia synthesis tower; 2-10 second regenerator; 2-11 second ammonia synthesis tower; 2-12 ammonia separator;

[0066] The concentrated solar thermal power and steam cogeneration module: 3-01 water pump; 3-02 third mixer; 3-03 regenerator; 3-04 first heat exchanger; 3-05 first steam turbine; 3-06 second heat exchanger; 3-07 first separator; 3-08 second steam turbine; 3-09 cold molten salt storage tank; 3-10 molten salt pump; 3-11 Fresnel lens focusing field; 3-12 central receiving tower; 3-13 pressure reducing valve; 3-14 hot molten salt storage tank; 3-15 fourth separator; 3-16 fourth mixer; 3-17 hot molten salt flow control valve; 3-18 power conversion center; 3-19 power monitoring and control center.

[0067] The present invention will be further explained below with reference to the accompanying drawings and embodiments. DETAILED DESCRIPTION

[0068] Specific embodiments of the present invention will be described in more detail below with reference to the accompanying drawings. Although specific embodiments of the present invention are shown in the accompanying drawings, it should be understood that the present invention can be implemented in various forms and should not be limited by the embodiments set forth herein. Rather, these embodiments are provided to enable a more thorough understanding of the present invention and to fully convey the scope of the present invention to those skilled in the art.

[0069] It should be noted that certain words are used in the specification and claims to refer to specific components. Those skilled in the art should understand that technicians may use different nouns to refer to the same component. This specification and claims do not use the difference in nouns as a way to distinguish components, but use the difference in the functions of the components as the criterion for distinction. As mentioned throughout the specification and claims, "including" or "comprising" is an open term, so it should be interpreted as "including but not limited to". The subsequent description of the specification is a preferred embodiment of the present invention, but the description is based on the general principles of the specification and is not intended to limit the scope of the invention. The scope of protection of the present invention shall be as defined in the attached claims.

[0070] To facilitate understanding of the embodiments of the present invention, several specific embodiments will be further explained below with reference to the accompanying drawings. However, the accompanying drawings do not limit the embodiments of the present invention.

[0071] For better understanding, Figure 1 As shown, a carbon cycle ammonia production system based on chemical chain water splitting includes:

[0072] Chemical chain carbon cycle nitrogen and hydrogen co-generation module, which includes:

[0073] The water is pumped into the downstream water-cooled heat exchanger 1-04 and the waste heat boiler 1-05 in series for preheating.

[0074] Regenerator 1-03, air is pressurized by air compressor 1-02 and enters regenerator 1-03 for preheating.

[0075] The first mixer 1-06 is connected to the waste heat boiler 1-05 and the first separator 3-07 to mix the preheated water with the high-pressure steam of the concentrated solar thermal power steam cogeneration module.

[0076] The steam reactor 1-08 is connected to the first mixer 1-06 via a molten salt heat exchanger 1-07 to reduce and generate hydrogen.

[0077] The dryer 1-09 is connected to the steam reactor 1-08 and the waste heat boiler 1-05 to dry the impurity-removing hydrogen.

[0078] The second mixer 1-20 is connected to the oxygen storage tank 1-18 and the regenerator 1-03 via the oxygen flow control valve 1-19 to mix the preheated air and oxygen.

[0079] Air reactor 1-10 is connected to the second mixer 1-20 to produce oxygen-depleted air, i.e., crude nitrogen. Air with an oxygen concentration lower than normal atmospheric levels is oxygen-depleted air, also known as crude nitrogen. Crude ammonia begins to exist in the ammonia synthesis tower and should become crude nitrogen after the chemical chaining water splitting process. The volume fraction of nitrogen in the oxygen-depleted air after the chemical chaining reaction can reach approximately 97.6%, while the remaining portion is 2.4% unreacted oxygen, which needs to be further processed in the pressure swing adsorption unit 2-01. The purity of the treated nitrogen should reach 99.9% to meet the subsequent ammonia production requirements.

[0080] The fuel reactor 1-11 is connected to the carbon monoxide storage tank 1-16 and the air reactor 1-10 via the carbon monoxide flow control valve 1-17 to produce carbon dioxide.

[0081] The carbon dioxide storage tank 1-13 is connected to the fuel reactor 1-11 via the carbon dioxide compressor 1-12 to temporarily store compressed carbon dioxide when power generation is low.

[0082] A high-temperature solid oxide carbon dioxide electrolyzer 1-15 is connected to the carbon dioxide storage tank 1-13 via a carbon dioxide flow control valve 1-14 to reduce carbon dioxide to carbon monoxide when there is a surplus of power generation.

[0083] A carbon monoxide storage tank 1-16, one end of which is connected to the high-temperature solid oxide carbon dioxide electrolyzer 1-15, and the other end is connected to the fuel reactor 1-11 via a carbon monoxide flow control valve 1-17, so as to temporarily store carbon monoxide. When the carbon monoxide flow control valve 1-17 limits the flow, part of the carbon monoxide is stored during peak power generation, and when the carbon monoxide flow control valve 1-17 is opened, the carbon monoxide is consumed during low power generation.

[0084] The Haber process ammonia module comprises:

[0085] The pressure swing adsorption device 2-01 is connected to the air reactor 1-10 via the waste heat boiler 1-05 and the regenerator 1-03 to process the crude nitrogen.

[0086] The second separator 2-02 is connected to the dryer 1-09 via the waste heat boiler 1-05 to separate part of the hydrogen.

[0087] The first mixer 2-03 is connected to the pressure swing adsorption device 2-01 and the second separator 2-02 to mix the crude nitrogen and hydrogen in a stoichiometric ratio of 2.8 to 2.9 to form a production raw material.

[0088] The second mixer 2-04 is connected to the first mixer 2-03 and the ammonia separator 2-12 to mix the production raw materials and the unreacted production raw materials,

[0089] The first multi-stage axial flow compressor 2-05, the second multi-stage axial flow compressor 2-06 and the third multi-stage axial flow compressor 2-07 are connected in series, which are connected to the second mixer 2-04 and the downstream water-cooled heat exchanger 1-04 to perform intermediate cooling of the production raw materials through stage compression.

[0090] The first ammonia synthesis tower 2-09 is connected to the third multi-stage axial flow compressor 2-07 via the first regenerator 2-08 to synthesize ammonia.

[0091] The second ammonia synthesis tower 2-11 is connected to the first ammonia synthesis tower 2-09 via the second regenerator 2-10 to synthesize ammonia.

[0092] The ammonia separator 2-12 is connected to the second ammonia synthesis tower 2-11 to separate ammonia and unreacted production raw materials.

[0093] In a preferred embodiment of the carbon cycle ammonia production system based on chemical chaining water splitting, a concentrated solar thermal power and steam cogeneration module is further included, which includes:

[0094] The third mixer 3-02 is connected to the water pump 3-01 and the regenerator 3-03 to mix the water input from the water pump 3-01 and the high-temperature and high-pressure steam from the regenerator 3-03.

[0095] The first heat exchanger 3-04 is connected to the third mixer 3-02 for further heating,

[0096] A first steam turbine 3-05, which is connected to the first heat exchanger 3-04 to generate electricity,

[0097] The second heat exchanger 3-06 is connected to the first steam turbine 3-05 to reheat and form high-temperature and high-pressure steam.

[0098] The first separator 3-07 has one end connected to the second heat exchanger 3-06 and the other end connected to the first mixer 1-06 and the second steam turbine 3-08 to respectively feed high-temperature and high-pressure steam. The high-temperature and high-pressure steam entering the second steam turbine 3-08 is input to the regenerator 3-03 for reheating.

[0099] Cold molten salt storage tank 3-09, which stores molten salt and is pumped into the central receiving tower 3-12 via molten salt pump 3-10,

[0100] The Fresnel lens focuses the light field 3-11, which is directed toward the central receiving tower 3-12 to produce hot molten salt.

[0101] The hot molten salt storage tank 3-14 is connected to the central receiving tower 3-12 via a pressure reducing valve 3-13 to store hot molten salt. One end of the hot molten salt heat exchanger 1-07 is connected between the pressure reducing valve 3-13 and the hot molten salt storage tank 3-14 via a hot molten salt flow control valve 3-17, and the other end is connected to the end of the hot molten salt storage tank 3-14 away from the pressure reducing valve 3-13.

[0102] The fourth separator 3-15 has one end connected to the hot molten salt storage tank 3-14, and the other end connected to the fourth mixer 3-16 via the first heat exchanger 3-04 and the second heat exchanger 3-06 respectively. The other end of the fourth mixer 3-16 is connected to the cold molten salt storage tank 3-09.

[0103] In a preferred embodiment of the carbon cycle ammonia production system based on chemical chaining water splitting, the concentrated solar thermal power and steam cogeneration module further comprises:

[0104] A power conversion hub 3-18 connects the first steam turbine 3-05 and the second steam turbine 3-08,

[0105] The power monitoring and control hub 3-19 is connected to the power conversion hub 3-18 to adjust flow and monitor power.

[0106] In a preferred embodiment of the carbon cycle ammonia production system based on chemical chain water splitting, the power monitoring and control center 3-19 connects and controls the carbon dioxide flow control valve 1-14, the carbon monoxide flow control valve 1-17, the oxygen flow control valve 1-19 and the molten salt flow control valve 3-17.

[0107] In a preferred embodiment of the carbon cycle ammonia production system based on chemical chaining water splitting, the high-temperature carbon dioxide at the outlet of the fuel reactor 1-11 is used as raw material, and the carbon cycle process is implemented by relying on the high-temperature solid oxide carbon dioxide electrolyzer 1-15.

[0108] In a preferred embodiment of the carbon cycle ammonia production system based on chemical chain water splitting, the circulating carbon source is 1.5 to 2 times the carbon consumption of the carbon cycle process, and part of the carbon source is always temporarily stored in the carbon dioxide storage tank 1-13 and the carbon monoxide storage tank 1-16 in the form of carbon monoxide or carbon dioxide.

[0109] In a preferred embodiment of the carbon cycle ammonia production system based on chemical chaining water splitting, the hot molten salt-driven reheat is returned to the Rankine cycle, and part of the reheated high-pressure steam and the steam from the waste heat boiler are introduced into the steam reactor 1-08.

[0110] In a preferred embodiment of the carbon cycle ammonia production system based on chemical chaining water splitting, the operating temperature of the fuel reactor is 850~1050℃, the operating temperature of the steam reactor is 600~900℃, the operating temperature of the air reactor is 1050~1250℃, and the reaction pressure is 1~30atm.

[0111] In a preferred embodiment of the carbon cycle ammonia production system based on chemical chaining water splitting, the electrolyte of the high-temperature solid oxide carbon dioxide electrolyzer 1-15 is zirconium oxide, and the operating temperature is between 700 and 900°C.

[0112] The process method of the carbon cycle ammonia production system based on chemical chain water splitting includes the following steps:

[0113] Step 1: Based on the chemical chaining carbon cycle nitrogen and hydrogen co-production module, a chemical chaining water splitting process is used to convert preheated CO, H2O, and air into CO2, H2, and crude nitrogen, respectively, in a fuel reactor, a steam reactor, and an air reactor under the catalysis of an oxygen carrier. The H2 and crude nitrogen are then pretreated and ammonia produced in subsequent modules after heat recovery in a waste heat boiler.

[0114] In step 2, H2 and crude nitrogen are fed into the Haber process ammonia production module, where they are first subjected to a drying device and a pressure swing adsorption device to remove excess moisture and oxygen, ensuring that the purity of the pretreated raw gas meets the process requirements for ammonia synthesis. The raw gas, consisting of a mixture of H2 and nitrogen in a certain proportion, undergoes multi-stage compression and intermediate cooling in a water-cooling module. Ammonia is then produced in a multi-stage synthesis tower under the action of a catalyst. The reacted mixed gas containing nitrogen, hydrogen, and ammonia passes through a heat exchanger and leaves the synthesis tower. The generated ammonia is separated from the unreacted hydrogen and nitrogen by condensation, and the unreacted gas is recycled back to the reactor to continue the reaction.

[0115] In step 3, under the action of concentrated solar energy, molten salt is used as the heat transfer fluid medium in the cogeneration process. The cold molten salt is pumped into the solar receiving tower to form high-temperature hot molten salt. Part of the hot molten salt enters the hot salt tank to store heat to ensure the supply of thermal electricity at night, and the other part generates electricity in a reheat Rankine cycle containing a heat regenerator to meet the power consumption required by the compressor and electrolyzer.

[0116] In one embodiment, Figure 1 This is a flow chart of a carbon cycle ammonia production system based on chemical chaining water splitting, provided by the present invention. This invention relates to a zero-carbon ammonia production system adapted to renewable energy sources. By monitoring the scale of green electricity, the system's material flow / energy flow coupling relationship can be adjusted to achieve efficient and flexible product production. The device's operating modes can be divided into power supply surplus conditions and power supply low conditions. The overall control strategy for these two conditions is as follows:

[0117] During sunny days with a surplus of electricity, the CSP module operates at full capacity, providing a large amount of heat and electricity to the system, ensuring high system operating conditions. The system's green electricity supply is monitored by the power monitoring and control center 3-19, and transient control is implemented through actuators such as flow control valves. To ensure system self-sufficiency in both electricity and heat, the CSP module operates with molten salt flow control valve 3-17, limiting flow. A portion of the molten salt flows into the molten salt storage tank 3-14 for thermal insulation, reserving thermal energy for fluctuating operating conditions. In the chemical chaining carbon cycle nitrogen-hydrogen cogeneration module, the carbon dioxide flow control valve 1-14 is open, allowing the high-temperature solid oxide carbon dioxide electrolyzer 1-15 to convert as much carbon dioxide from the carbon dioxide storage tank 1-13 as possible into carbon monoxide. Because the circulating carbon exceeds system consumption, the carbon monoxide flow control valve 1-17 limits flow, allowing a portion of the carbon monoxide to remain in the carbon monoxide storage tank 1-16, providing a chemical energy reserve for fluctuating operating conditions. Furthermore, when fuel reactor 1-11 is fully operational, the system's ammonia production capacity is determined by the output of the chemical chaining carbon cycle nitrogen-hydrogen cogeneration module. When power is sufficient, oxygen flow control valve 1-19 limits flow, increasing the capacity of air compressor 1-02 and the ammonia production capacity of the Haber process ammonia production module, thereby enhancing the integration of new energy sources to meet the needs of high-load conditions.

[0118] During low power supply conditions at night or on cloudy days, the CSP cogeneration module performs poorly, reducing its ability to supply heat and power to the system and causing the system to operate at low operating conditions. This insufficient green power supply is monitored by the power monitoring and control center 3-19, and transient control is implemented through actuators such as flow control valves. In the CSP steam cogeneration module, the molten salt flow control valve 3-17 opens, and the molten salt stored in the molten salt storage tank 3-14 replaces the central receiving tower to supply heat and electricity, maintaining a continuous heat and power supply for system operation even under low operating conditions. In the chemical chaining carbon cycle nitrogen-hydrogen cogeneration module, the carbon dioxide flow control valve 1-14 restricts flow, reducing the operating capacity of the high-temperature solid oxide carbon dioxide electrolyzer 1-15 and reducing carbon monoxide production. At this time, the carbon monoxide flow control valve 1-17 opens, and the carbon monoxide stored in the carbon monoxide storage tank 1-16 is fed into the fuel reactor 1-11 to maintain the normal operation of the chemical chaining reaction. In addition, when power is insufficient, the oxygen flow control valve 1-19 opens the air compressor, and the scale of 1-02 and the ammonia production scale of the Haber process ammonia module are reduced to reduce the consumption rate of the system's reserve energy.

[0119] By coupling a chemical chaining carbon cycle nitrogen-hydrogen cogeneration module, a Haber process ammonia production module, and a concentrated solar thermal power and steam cogeneration module, this invention proposes an ammonia production process that is adaptable to fluctuating green electricity supply conditions. This design effectively utilizes renewable energy to achieve zero carbon emissions, and possesses a high degree of flexibility and adaptability, ensuring continuous and stable ammonia production under conditions of unstable green electricity supply. This design can provide path guidance and technical support for green ammonia industrial production within the context of my country's dual carbon goals, and is of great significance for promoting the optimization and upgrading of the energy structure and achieving green, low-carbon development.

[0120] In one embodiment, the method includes,

[0121] Step 1: A chemical-chaining carbon cycle nitrogen-hydrogen cogeneration module utilizes a chemical-chaining water splitting process. Under oxygen carrier catalysis, preheated CO, H2O, and air are converted into CO2, H2, and crude N2, respectively, in three independent reactors. The H2 and crude N2 recover heat in a waste heat boiler before undergoing pretreatment and ammonia production in subsequent modules. The CO2 is flexibly dispatched based on the system's green electricity supply and demand: when green electricity production is in surplus, such as on sunny days, it is fed into a high-temperature CO2 electrolyzer (SOEC) to produce CO. During periods of low green electricity production, such as cloudy days or at night, the CO2 is temporarily stored to reduce the system's power load. Both treatment methods can be performed simultaneously. The CO generated from the electrolyzer cathode can also be converted to a storage form based on green electricity availability. Surplus electricity can be stored as chemical energy of CO and used in the fuel reactor (FR) during periods of low electricity production, ensuring stable operation of the nitrogen-hydrogen cogeneration system despite fluctuations in electricity demand. The high-temperature O2 generated from the electrolyzer anode can be mixed with preheated air after drying, reducing the energy consumption of the air reactor (AR) for air compression and preheating.

[0122] In step 2, H2 and crude N2 are fed into the Haber process ammonia production module. They first pass through a drying unit and a pressure swing adsorption unit to remove excess moisture and oxygen, ensuring that the purity of the pretreated raw gas meets the process requirements for ammonia synthesis. Subsequently, the raw H2 and N2 gases are mixed in a specific ratio and subjected to multi-stage compression and intermediate cooling in a water-cooled module. Ammonia is then produced in a multi-stage synthesis tower under the action of a catalyst. The resulting mixture of nitrogen, hydrogen, and ammonia exits the synthesis tower through a heat exchanger, where the generated ammonia is separated from the unreacted hydrogen and nitrogen by condensation. The unreacted gases are recycled back to the reactor to continue the reaction, ensuring a high ammonia conversion rate.

[0123] In step 3, the concentrated solar thermal power and steam cogeneration module can provide the electricity and heat consumption required for steps 1 and 2. Under the action of concentrated solar energy, specially prepared molten salt can be used as a heat transfer fluid medium in the cogeneration process. Among them, the cold molten salt is pumped into the solar receiving tower to form high-temperature hot molten salt. Part of the hot molten salt enters the hot salt tank to store heat to ensure the thermal power supply at night, and the other part generates electricity in the reheat Rankine cycle containing a heat regenerator to meet the power consumption required by the compressor and electrolyzer. The two processing methods can be carried out simultaneously, and the distribution ratio is also converted in time according to the green electricity situation. The electricity generated by the system is monitored in the power center to provide transient data support for the flow control of the flow control valve in the system.

[0124] Preferably, the oxygen carrier used in the chemical looping water splitting process is metallic iron oxide, which is classified into high-valent, low-valent, and intermediate-valent states. The high-valent oxygen carrier, Fe2O3, is reduced by CO to the low-valent oxygen carrier, Fe / FeO, in the fuel reactor FR, absorbing heat. The resulting low-valent oxygen carrier is oxidized by water vapor in the steam reactor SR to the intermediate state, Fe3O4, which is simultaneously cracked to produce H2, in a mildly exothermic reaction. The intermediate-valent oxygen carrier is further oxidized by oxygen in the air reactor AR to the highest valent state, releasing a significant amount of heat. This allows for a cyclical process using these three reactors. Process heat from the chemical looping water splitting portion can be recovered from the reactor exhaust, i.e., the waste heat boiler, or, if necessary, through a heat exchanger embedded in the reactor. The amount of process heat can be adjusted by varying the ratio of H2O to O2 at the inlet. Methods for maintaining net process heat generation include introducing substoichiometric amounts of steam into the steam reactor SR or directly transferring a portion of the low-valent oxygen carrier, Fe / FeO, from the fuel reactor FR to the air reactor AR, thereby reducing the heat absorption requirement of the fuel reactor FR. This embodiment can also adjust the ratio of ammonia production, thereby affecting the energy consumption of the entire system. The high-temperature solid oxide CO2 electrolyzer, whose electrolyte is a solid ceramic material commonly used zirconium oxide, operates at a temperature between 700 and 900°C, effectively promoting the adsorption and activation of CO2 during the electrochemical process and improving electrolysis performance.

[0125] Preferably, the ratio of nitrogen to hydrogen in step 2 is 2.8-2.9. Part of the hydrogen produced by the chemical chaining water splitting module is used to produce ammonia, and the remaining hydrogen is used as an output product. The multi-stage compression process in step 2 uses a multi-stage axial flow compressor with a pressure ratio of 1.15-1.35 per blade stage. When the gas is compressed by the first few stages of impellers, the temperature rises significantly. This temperature can be lowered by cooling the gas through an intercooler, thereby reducing energy consumption during the compression process and preheating the steam. When the gas is compressed by the subsequent stages of impellers, the mixed gas at the outlet reaches the pressure required for ammonia production, and its temperature is maintained at 300-400°C, slightly below the operating temperature required for the reaction. The regenerator can reach the required operating temperature for the synthesis tower. The ammonia synthesis tower in step 2 uses an iron catalyst, that is, an iron-based mixed catalyst, to produce ammonia and release heat. The operating temperature of the reaction process is 400-500°C and the operating pressure is 150-300 atm, taking into account both equipment requirements and catalyst activity. The molten salt is composed of NaNO₃ and KNO₃ in a mass ratio of 6:4, with a heat transfer temperature range of 290–565°C. A portion of this is stored during periods of surplus electricity supply, providing energy to the system during periods of low electricity supply. The reheat Rankine cycle with a regenerator utilizes the diverted hot molten salt for regeneration and reheating. Part of the resulting high-temperature steam is used for reactions in the steam reactor (SR), and new liquid water is introduced to lower the system's average heat absorption temperature.

[0126] In one embodiment, the system includes a chemical chain carbon cycle nitrogen and hydrogen cogeneration module, a Haber process ammonia production module and a concentrated solar thermal power steam cogeneration module. The chemical chain carbon cycle nitrogen and hydrogen cogeneration module is as follows: Figure 1As shown, the system includes three independent reactors required for chemical-looping water splitting technology: a steam reactor 1-08, an air reactor 1-10, and a fuel reactor 1-11. Fuel reactor 1-11 is coupled with a high-temperature solid oxide carbon dioxide electrolyzer 1-15 to achieve zero-carbon nitrogen and hydrogen cogeneration. Other auxiliary equipment supports the operation of the core components. Liquid water input to the system is delivered via pump 1-01 to a downstream water-cooled heat exchanger 1-04 and its series-connected waste heat boiler 1-05 for preheating. The resulting stream is mixed with high-temperature, high-pressure steam from the concentrated solar thermal power and steam cogeneration module, further heated in a molten salt heat exchanger 1-07, and then reduced to hydrogen in steam reactor 1-08. The resulting hydrogen stream is then passed through a dryer 1-09 for impurity removal and heat recovery in a waste heat boiler 1-05 before being fed to the Haber process ammonia production module. Air entering the system is pressurized by air compressor 1-02 and preheated by regenerator 1-03. It then mixes with oxygen flowing from oxygen storage tank 1-18 through oxygen flow control valve 1-19. The air reactor 1-10 reacts fully, and the resulting crude nitrogen is fed into the Haber process ammonia production module. Furthermore, fuel reactor 1-11 uses internally recycled carbon monoxide as feedstock to produce carbon dioxide. The resulting carbon dioxide is pressurized and fed into carbon dioxide storage tank 1-13. Carbon dioxide flow control valve 1-14 limits the flow of electricity during periods of low power generation. During periods of surplus power generation, the carbon dioxide is converted to carbon monoxide, which opens the valve 1-14. At this time, part of the surplus electrical energy is converted into the chemical energy of carbon monoxide and temporarily stored in the carbon monoxide storage tank 1-16. Under the action of the carbon monoxide flow control valve 1-17, part of the carbon monoxide is stored during the peak power generation period, and the carbon monoxide flow control valve 1-17 limits the flow; during the low power generation period, carbon monoxide is consumed to ensure the normal production of the system, and the carbon monoxide flow control valve 1-17 is opened to adapt to the needs of fluctuating operating conditions through carbon circulation and carbon conversion.

[0127] The Haber process ammonia production module can produce ammonia with the assistance of a chemical chain. Crude nitrogen provided by the upstream chemical chain carbon cycle nitrogen-hydrogen cogeneration module is treated in a pressure swing adsorption unit 2-01 and then fed into the first mixer 2-03 with a portion of the hydrogen from the outlet of the second separator 2-02 at a stoichiometric ratio of 2.8-2.9. The resulting raw material and unreacted raw material are further mixed in the second mixer 2-04. Multi-stage compression and intermediate cooling are performed using multiple axial flow compressors and a downstream water-cooled heat exchanger 1-04. The resulting high-pressure mixer passes through the first regenerator 2-08 and the second regenerator 2-10, and ammonia is synthesized in the first ammonia synthesis tower 2-09 and the second ammonia synthesis tower 2-11. The resulting ammonia product is separated in the ammonia separator 2-12, while the unreacted product continues to recycle.

[0128] The concentrated solar thermal power and steam cogeneration module utilizes solar energy through molten salt and the Rankine cycle, ensuring and controlling the system's heat and electricity consumption and providing high-temperature steam for the chemical chaining carbon cycle nitrogen-hydrogen cogeneration module. In the Rankine cycle, water input to the system is pressurized by pump 3-01 and fed into the third mixer 3-02 along with the reheated steam. The resulting stream is then reheated in regenerator 3-03. A portion of the hot molten salt is further heated in the first heat exchanger 3-04 and passed through the first steam turbine 3-05 to generate electricity. During the steam expansion process, another portion of the molten salt is reheated through the second heat exchanger 3-06. The reheated high-temperature, high-pressure steam is fed into the first separator 3-07. A portion of the steam is fed into the chemical chaining carbon cycle nitrogen-hydrogen cogeneration module for cracking; the remaining portion continues to generate electricity in the second steam turbine 3-08 and is reheated in the regenerator 3-03. In the molten salt circulation, molten salt from the cold molten salt storage tank 3-09 is transported via a molten salt pump 3-10 to a central receiving tower 3-12, where it is concentrated by a Fresnel lens concentrating field 3-11 to produce hot molten salt. This hot molten salt passes through a pressure reducing valve 3-13 and, under the control of a hot molten salt flow control valve 3-17, is stored as heat in the hot molten salt storage tank 3-14 when power is surplus. The remaining portion is split into two streams by a fourth separator 3-15 to assist in reheating back into the Rankine cycle and then recombined in a fourth mixer 3-16, thus completing the molten salt circulation. Furthermore, the electricity generated by the concentrated solar thermal power and steam cogeneration module is adjusted and distributed in the power conversion hub 3-18. Its power status is transmitted to the power monitoring and control hub 3-19, which adjusts the flow rate of the system's flow control valves, provides real-time monitoring and control of the system's material and energy flows, and ensures stable operation under fluctuating operating conditions.

[0129] Utilizing high-temperature carbon dioxide (CO2) from the outlet of fuel reactor 1-11 as feedstock, a carbon recycling process is implemented within a high-temperature solid oxide CO2 electrolyzer 1-15, achieving zero-carbon co-production of crude nitrogen and hydrogen, ensuring sustainable and full utilization of chemical chaining products. The recycled carbon source is 1.5 to 2 times the carbon consumed in the recycling process, ensuring that a portion of the carbon source is always temporarily stored in the form of CO or CO2 in CO2 storage tanks 1-13 and 1-16. This mitigates the carbon capture and storage pressures imposed by continuous ammonia production on the system. Furthermore, it provides a chemical reserve, adapting to real-time conversion of energy and material flows under fluctuating operating conditions and ensuring stable zero-carbon chemical chaining ammonia-hydrogen production. Utilizing high-temperature, high-pressure oxygen at the electrolyzer anode outlet improves combustion in the FR module; reduces inlet air compression and preheating energy consumption through mixing; and, in conjunction with the steam input to the chemical chain, adjusts the system's ammonia production scale. This improves system production flexibility and resource utilization. For the feed gas used in ammonia synthesis, a co-current water-cooled heat exchanger reduces the additional compression energy required to compress the high-temperature gas while ensuring a suitable outlet temperature for subsequent synthesis processes. For water, a series-connected step-by-step heating process using water cooling equipment and a waste heat boiler recovers waste heat from the system, providing high-temperature steam for steam reactor 1-08 and improving system energy efficiency. The production route eliminates the need for an expander, and the ammonia production process can be conducted at the same temperature and pressure as the chemical looping process, avoiding the storage and transportation costs associated with an uncoupled process. The molten salt reserve in the concentrated solar thermal power and steam cogeneration module provides heat and electricity for a certain period of time at night, compensating for the heat loss of the fuel reactor and maintaining the operating temperature of the high-temperature electrolyzer. This heat reserve method, combined with the chemical reserve method, provides a double guarantee for continuous system operation under fluctuating operating conditions. The molten salt-driven reheating system returns to the Rankine cycle, where a portion of the reheated high-pressure steam can be fed into steam reactor 1-08 along with steam from the waste heat boiler, increasing the reactor's operating pressure and hydrogen production efficiency. It also provides an inlet and outlet for the water cycle in the Rankine cycle, lowering the average heat absorption temperature in the Rankine cycle and improving the Rankine cycle's thermal efficiency and power generation. The power conversion hub 3-18 and the power monitoring and control hub 3-19, the former can convert and distribute electricity based on green power conditions, while the latter can monitor the scale of output power and employ active anti-disturbance control to estimate and compensate for internal and external uncertainties in the system. This allows for real-time, stable, and precise control of the four components: the carbon dioxide flow control valve 1-14, the carbon monoxide flow control valve 1-17, the oxygen flow control valve 1-19, and the molten salt flow control valve 3-17. This achieves nonlinear adjustment for high and low operating conditions and their transitions, as well as robustness to fluctuating renewable energy conditions.

[0130] This invention integrates a fuel reactor with a solid oxide CO2 electrolyzer, utilizing electrolysis technology to achieve a "combustible gas-CO2-combustible gas" cycle. This frees the production of crude nitrogen and hydrogen in the chemical chain from upstream fossil fuel constraints. It also proposes chemical energy storage compatible with renewable energy, improving the stability of the integrated system and enabling the co-production of nitrogen and hydrogen under low-carbon conditions. The raw materials required for ammonia production in the Haber process ammonia production module are all supplied by the upstream chemical chain carbon cycle nitrogen-hydrogen cogeneration module. Compared to traditional water-gas reforming and air separation units, this system offers advantages in that: first, the type of hydrogen produced is transformed from "grey hydrogen" dependent on fossil fuels to "green hydrogen" within the carbon cycle, better meeting the dual carbon goals; second, nitrogen extraction from air is shifted to crude nitrogen, resulting in higher extraction efficiency and lower energy consumption. The concentrated solar thermal power and steam cogeneration module combines solar heat storage with steam from the Rankine cycle and the chemical chaining process in module one. The former can be used to preheat the inlet feedstock of the solid oxide CO2 electrolyzer, while the latter can serve as feedstock for the steam reactor and assist in hydrogen production.

[0131] The basic principles of the present application have been described above in conjunction with specific embodiments. However, it should be noted that the advantages, strengths, and effects mentioned in this application are merely illustrative and not restrictive, and it should not be assumed that these advantages, strengths, and effects are required of each embodiment of this application. In addition, the specific details disclosed above are merely illustrative and facilitating understanding, and are not restrictive. The above details do not limit this application to necessarily being implemented using the above specific details.

[0132] The above description has been provided for the purpose of illustration and description. Furthermore, this description is not intended to limit the embodiments of the present application to the forms disclosed herein. Although a number of example aspects and embodiments have been discussed above, those skilled in the art will recognize certain variations, modifications, alterations, additions, and sub-combinations thereof.

Claims

1. A carbon cycle ammonia production system based on chemical chain water splitting, characterized in that: These include, Chemical chain carbon cycle nitrogen and hydrogen co-generation module, which includes: Regenerator (1-03), air is pressurized by the air compressor (1-02) and enters the regenerator (1-03) for preheating. The first mixer (1-06) is connected to the waste heat boiler (1-05) and the first separator (3-07) to mix the preheated water with the high-pressure steam of the concentrated solar thermal power steam cogeneration module, A steam reactor (1-08) is connected to the first mixer (1-06) via a molten salt heat exchanger (1-07) to reduce and generate hydrogen, A dryer (1-09) is connected to the steam reactor (1-08) and the waste heat boiler (1-05) to dry the impurity-removing hydrogen, The second mixer (1-20) is connected to the oxygen storage tank (1-18) and the regenerator (1-03) via the oxygen flow control valve (1-19) to mix the preheated air and oxygen. an air reactor (1-10) connected to the second mixer (1-20) to produce oxygen-depleted air, i.e., crude nitrogen, A fuel reactor (1-11) is connected to a carbon monoxide storage tank (1-16) via a carbon monoxide flow control valve (1-17) and to an air reactor (1-10) to produce carbon dioxide, A carbon dioxide storage tank (1-13) is connected to the fuel reactor (1-11) via a carbon dioxide compressor (1-12) to compress and store carbon dioxide when power generation is low. A high-temperature solid oxide carbon dioxide electrolyzer (1-15) is connected to the carbon dioxide storage tank (1-13) via a carbon dioxide flow control valve (1-14) to reduce carbon dioxide to carbon monoxide when there is a surplus of power generation. A carbon monoxide storage tank (1-16) stores part of the carbon monoxide during peak power generation when the carbon monoxide flow control valve (1-17) is limiting the flow, and consumes the carbon monoxide during low power generation when the carbon monoxide flow control valve (1-17) is opened; Haber process ammonia module.

2. The carbon cycle ammonia production system based on chemical chaining water splitting according to claim 1, characterized in that: Preferably, Also included is a concentrated solar thermal power and steam cogeneration module, which includes: The third mixer (3-02) is connected to the water pump (3-01) and the regenerator (3-03) to mix the water input from the water pump (3-01) and the high-temperature and high-pressure steam from the regenerator (3-03). The first heat exchanger (3-04), which is connected to the third mixer (3-02) for further heating, A first steam turbine (3-05) connected to the first heat exchanger (3-04) to generate electricity, The second heat exchanger (3-06) is connected to the first steam turbine (3-05) to reheat the steam to form high-temperature and high-pressure steam. The first separator (3-07) has one end connected to the second heat exchanger (3-06) and the other end connected to the first mixer (1-06) and the second steam turbine (3-08) to respectively feed high-temperature and high-pressure steam. The high-temperature and high-pressure steam entering the second steam turbine (3-08) is input to the regenerator (3-03) for heat recovery. Cold molten salt storage tank (3-09), which stores molten salt and pumps it into the central receiving tower (3-12) via molten salt pump (3-10), The Fresnel lens concentrates the light field (3-11) toward the central receiving tower (3-12) to produce hot molten salt, A hot molten salt storage tank (3-14) is connected to the central receiving tower (3-12) via a pressure reducing valve (3-13) to store hot molten salt. One end of the hot molten salt heat exchanger (1-07) is connected between the pressure reducing valve (3-13) and the hot molten salt storage tank (3-14) via a hot molten salt flow control valve (3-17), and the other end is connected to the end of the hot molten salt storage tank (3-14) away from the pressure reducing valve (3-13). The fourth separator (3-15) has one end connected to the hot molten salt storage tank (3-14), and the other end connected to the fourth mixer (3-16) via the first heat exchanger (3-04) and the second heat exchanger (3-06), and the other end of the fourth mixer (3-16) is connected to the cold molten salt storage tank (3-09).

3. The carbon cycle ammonia production system based on chemical chaining water splitting according to claim 2, characterized in that: The concentrated solar thermal power and steam cogeneration module also includes: A power conversion hub (3-18) connecting the first steam turbine (3-05) and the second steam turbine (3-08) for power supply, The power monitoring and control center (3-19) is connected to the power conversion center (3-18) to monitor power information and adjust valve flow.

4. The carbon cycle ammonia production system based on chemical chaining water splitting according to claim 1, characterized in that: The power monitoring and control center (3-19) is connected to and controls the carbon dioxide flow control valve (1-14), the carbon monoxide flow control valve (1-17), the oxygen flow control valve (1-19) and the molten salt flow control valve (3-17).

5. The carbon cycle ammonia production system based on chemical chaining water splitting according to claim 1, characterized in that: The high-temperature carbon dioxide at the outlet of the fuel reactor (1-11) is used as raw material, and the carbon cycle process is implemented by relying on the high-temperature solid oxide carbon dioxide electrolyzer (1-15).

6. The carbon cycle ammonia production system based on chemical chaining water splitting according to claim 5, characterized in that: The circulating carbon source is 1.5 to 2 times the carbon consumption in the carbon cycle process, and part of the carbon source is always temporarily stored in the form of carbon monoxide or carbon dioxide in the carbon dioxide storage tank (1-13) and the carbon monoxide storage tank (1-16).

7. The carbon cycle ammonia production system based on chemical chaining water splitting according to claim 1, characterized in that: In the Rankine cycle driven by hot molten salt, part of the reheated high-pressure steam and the steam from the waste heat boiler are introduced into the steam reactor (1-08).

8. The carbon cycle ammonia production system based on chemical chaining water splitting according to claim 1, characterized in that: The operating temperature of the fuel reactor is 850~1050℃, the operating temperature of the steam reactor is 600~900℃, the operating temperature of the air reactor is 1050~1250℃, and the reaction pressure is 1~30atm.

9. The carbon cycle ammonia production system based on chemical chaining water splitting according to claim 1, characterized in that: The electrolyte of the high-temperature solid oxide carbon dioxide electrolyzer (1-15) is zirconium oxide, and the operating temperature is between 700 and 900°C.

10. The process method of the carbon cycle ammonia production system based on chemical chaining water splitting according to any one of claims 1 to 9.

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