System and method for producing hydrogen by directly cracking liquid ammonia through plasma

Abstract

The invention relates to the technical field of energy application, in particular to a system and method for producing hydrogen by directly cracking liquid ammonia through plasma. The method mainly aims at solving the problems that an ammonia cracking hydrogen production technology is low in response speed and high in energy consumption, the energy consumption loss of liquid ammonia gasification is remarkable, and the system regulation and control accuracy is insufficient. According to the technical scheme, the device comprises a control system, a cracker tank, a plasma power supply, a first plasma electrode plate, a second plasma electrode plate, a catalyst bin, a grounding end, a liquid ammonia supply assembly, a temperature and pressure monitoring assembly, a gas treatment assembly and a flue gas heat exchange assembly. The liquid ammonia supply assembly comprises a liquid ammonia inlet, a liquid ammonia control valve and a liquid ammonia flow guide pipe. According to the invention, the catalytic synergistic cracking of the coupled plasma and the waste heat gasification of the flue gas are matched with multi-parameter closed-loop control, so that zero-carbon and efficient hydrogen production is realized, the requirements of multiple fields are met, and the low-carbon transformation of energy sources is assisted.

Description

Technical Field

[0001] This invention relates to the field of energy application technology, and in particular to a plasma direct pyrolysis liquid ammonia hydrogen production system and method. Background Technology

[0002] With the increasingly severe environmental problems caused by the massive emissions of greenhouse gases such as carbon dioxide, the use of renewable energy sources such as photovoltaic, wind, and tidal power for low-carbon development, while simultaneously abandoning the use of traditional fossil fuels such as coal, oil, and natural gas, has become an inevitable global trend. However, the inherent instability and intermittency of renewable energy severely limit its rapid development. Utilizing energy storage media such as hydrogen, ammonia, and methanol, or thermal energy storage methods, to convert renewable electricity locally and achieve large-scale transportation and storage of renewable energy has become a feasible solution. In particular, ammonia, with its easier long-term storage and transportation and zero carbon emissions, has received more attention and is gaining widespread recognition and support from the industry. As a carrier of hydrogen and energy storage, the production model, industrial chain, and application-end consumption issues of ammonia are also gradually receiving attention and concern. Ammonia is easily liquefied, stored, and transported, and its advantages are fully utilized as an effective means of long-term energy storage. However, as a fuel, ammonia has strong chemical inertness. Ammonia has poor combustion characteristics, low laminar combustion flame velocity, and low calorific value. In practical applications, it is often used as a combustion aid fuel with fast combustion speed and high calorific value, such as coal, gasoline, diesel, or natural gas. To achieve completely zero-carbon combustion, partially or completely decomposing ammonia into hydrogen to improve its combustion performance is a relatively effective method that can form zero-carbon fuel without requiring additional fuel storage. However, traditional ammonia decomposition methods suffer from slow response speed and high energy consumption, limiting their use and development in many application scenarios. For example, the technology of electrically heated catalytic cracking of ammonia to produce hydrogen is relatively mature, but it is very energy-intensive. Utilizing fuel combustion (such as ammonia) reduces the dependence of the cracking system on electricity, but the response speed is slow. Furthermore, ammonia is generally stored in a liquid state, and liquid ammonia has extremely high latent heat of vaporization, requiring a large amount of heat during ammonia vaporization. This poses a significant challenge to the overall utilization efficiency of the system and the practical value of ammonia-to-hydrogen equipment. Therefore, this invention proposes a plasma direct cracking system and method for producing hydrogen from liquid ammonia, which combines low energy consumption, fast response, and high efficiency. Summary of the Invention

[0003] The purpose of this invention is to address the problems of slow response speed, high energy consumption, significant energy loss from liquid ammonia vaporization, and insufficient precision in system control in the prior art of ammonia cracking hydrogen production technology, and to propose a plasma direct cracking liquid ammonia hydrogen production system and method.

[0004] The technical solution of the present invention is a plasma direct pyrolysis liquid ammonia hydrogen production system, comprising a control system, a pyrolysis tank, a plasma power supply, a first plasma electrode plate, a second plasma electrode plate, a catalyst chamber, a grounding terminal, a liquid ammonia supply component, a temperature and pressure monitoring component, a gas processing component, and a flue gas heat exchange component.

[0005] The liquid ammonia supply assembly includes a liquid ammonia inlet, a liquid ammonia control valve, and a liquid ammonia guide pipe. The liquid ammonia inlet is connected to one end of the liquid ammonia guide pipe via the liquid ammonia control valve, and the other end of the liquid ammonia guide pipe extends into the pyrolysis tank.

[0006] The catalyst chamber is encased in an electrical insulator and fixed between the first plasma electrode plate and the second plasma electrode plate; the first plasma electrode plate is connected to the high-voltage end of the plasma power supply via a conductive line, and the second plasma electrode plate is connected to the grounding terminal and the grounding terminal of the plasma power supply via a conductive line.

[0007] The temperature and pressure monitoring component includes a thermometer and a pressure gauge, with the detection ends of the thermometer and pressure gauge extending into the pyrolysis tank.

[0008] The gas processing assembly includes a gas filter end, a gas purification membrane, a pyrolyzer exhaust control valve, and a pyrolyzer gas outlet. The lower end of the gas filter end is welded to the upper end of the pyrolyzer tank, and the upper end is connected to the pyrolyzer gas outlet via the pyrolyzer exhaust control valve. The gas purification membrane is located on the inner side of the top of the gas filter end.

[0009] The flue gas heat exchange assembly includes a heat exchanger tube, a flue gas inlet, a flue gas outlet, and a flue gas control valve. The heat exchanger tube is placed at the bottom of the pyrolysis tank, with one end connected to the flue gas inlet via a pipeline and the other end connected to the flue gas outlet. The flue gas control valve is installed between the flue gas inlet and the external flue gas pipeline.

[0010] The control system is connected to the liquid ammonia control valve, the pyrolyzer exhaust control valve, the flue gas control valve, and the plasma power supply via control lines, and is connected to the thermometer, pressure gauge, and the upper and lower limit liquid level sensors on the inner wall of the pyrolyzer tank via signal lines.

[0011] Optionally, the plasma power source is any one of a DC power source, an AC power source, a microwave power source, or a pulse modulation power source;

[0012] The plasma generated by energizing the first plasma electrode plate and the second plasma electrode plate is any one of the following: arc plasma, microwave plasma, dielectric barrier discharge plasma, radio frequency plasma, sliding arc plasma, corona discharge plasma, and rotating arc plasma.

[0013] Optionally, the catalyst chamber is filled with a catalyst;

[0014] The catalyst is one of Ni-based transition metal catalysts, Fe-based transition metal catalysts, Co-based transition metal catalysts, Ru-based noble metal catalysts, Pt-based noble metal catalysts, Pd-based noble metal catalysts, Rh-based noble metal catalysts, and Ag-based noble metal catalysts, or a mixture of two or more catalysts.

[0015] The catalyst is supported on a carrier, which may be diatomaceous earth, kaolin, silicon dioxide, cerium oxide, activated carbon, silica gel, glass sheet, glass fiber, silicon dioxide, titanium dioxide, or a polymer.

[0016] Optionally, the structure of the pyrolyzer tank can be a tube sheet structure, a shell-and-tube structure, a partition wall structure, a hybrid structure, or a regenerative structure.

[0017] Optionally, in the external high-temperature flue gas supply pipeline connected to the flue gas inlet, the high-temperature flue gas is the exhaust gas of a gas turbine, the exhaust gas of a reciprocating engine, the exhaust gas of an external combustion engine, the exhaust gas of a gas boiler, the exhaust gas of a burner, or the exhaust gas of an aircraft engine.

[0018] Optionally, the gas purification membrane is either a Pd-based noble metal membrane or an Fe-based non-noble metal membrane.

[0019] This invention also proposes a method for direct plasma pyrolysis of liquid ammonia to produce hydrogen, comprising the following steps:

[0020] Step 1, Initial Preparation: After the control system is started, first output a signal to close the pyrolyzer exhaust control valve, and at the same time open the liquid ammonia control valve;

[0021] Step 2, Liquid Ammonia Level Control: Liquid ammonia is introduced into the pyrolysis tank through the liquid ammonia inlet and liquid ammonia guide pipe. When the upper limit level sensor detects that the liquid ammonia level has reached the set upper limit, the control system controls the liquid ammonia control valve to close. If the lower limit level sensor detects that the liquid ammonia level is lower than the set lower limit, the system returns to Step 1, continues to close the pyrolysis exhaust control valve and open the liquid ammonia control valve to replenish liquid ammonia. If the liquid ammonia level is higher than the set lower limit, the system proceeds to the next step.

[0022] Step 3, Plasma Start-up: The control system outputs a signal to turn on the plasma power supply, causing plasma to be generated between the first plasma electrode plate and the second plasma electrode plate;

[0023] Step 4: Flue gas heat exchange starts: After the plasma is started, the control system opens the flue gas control valve. The high-temperature flue gas from the outside enters the heat exchanger tube through the flue gas inlet and exchanges heat with the liquid ammonia in the pyrolyzer tank to realize the vaporization of liquid ammonia and its participation in the pyrolysis reaction. After heat exchange, the flue gas is discharged through the flue gas outlet.

[0024] Step 5: Reaction Parameter Monitoring: Monitor the temperature and pressure inside the pyrolysis tank in real time using thermometers and pressure gauges. If the pressure reaches the set upper limit or the temperature reaches the set upper limit, proceed to the next step; if the pressure does not reach the upper limit or the temperature does not reach the upper limit, proceed to Step 7.

[0025] Step 6, Reaction Control: The control system adjusts the opening of the flue gas control valve and shuts off the plasma power supply. After the temperature and pressure drop to a safe range, return to Step 3.

[0026] Step 7, Gas Output Judgment: If the pressure gauge detects that the pressure inside the tank has reached the set usage threshold, the control system opens the pyrolyzer exhaust control valve. The hydrogen-containing gas generated by pyrolysis is filtered by the gas filter end and purified by the gas purification membrane, and then supplied to the gas user end through the pyrolyzed gas outlet. If the pressure gauge detects that the pressure inside the tank is lower than the set lower pressure limit, then return to Step 3.

[0027] Step 8: Continuous gas supply: Repeat the above steps to continuously supply hydrogen-containing gas or high-purity hydrogen to the gas user.

[0028] In summary, this application includes at least one of the following beneficial technical effects:

[0029] This invention uses ammonia as the core energy storage and hydrogen production carrier, without relying on fossil fuels such as coal and natural gas. It can directly provide hydrogen-containing fuel or high-purity hydrogen for multiple fields such as engines, gas turbines, marine power, chemical production, metal smelting, and cement building materials, achieving carbon dioxide emission reduction or even zero carbon emissions in end-use scenarios and helping the low-carbon transformation of the energy structure.

[0030] Furthermore, by innovating and coupling high-temperature flue gas waste heat gasification technology, the waste heat of exhaust gas from equipment such as gas turbines and engines is used to achieve controllable gasification of liquid ammonia through heat exchanger tubes. This significantly reduces the external energy input required for liquid ammonia due to its high latent heat of vaporization, reduces calorific value loss by 6%-7%, and significantly improves the overall energy utilization efficiency of the system.

[0031] Furthermore, through the synergistic pyrolysis design of plasma and catalyst, compared with traditional electric heating catalytic pyrolysis, the energy consumption for hydrogen production is reduced. The instantaneous start-up characteristics of plasma greatly improve the system response speed. It only takes a few minutes from start-up to stable hydrogen production, which is far better than the tens of minutes of fuel combustion-assisted pyrolysis. It can be flexibly adapted to dynamic load scenarios such as emergency power generation and ship power. Moreover, the proportion of hydrogen in the pyrolysis gas can be adjusted within the range of 0-100% to meet the fuel requirements of different applications.

[0032] The system of this invention adopts a modular design, with simple connections and reasonable layout of each component, which facilitates expansion and upgrading according to actual production capacity requirements; at the same time, through the coordinated closed-loop control of liquid level, temperature and pressure, it can accurately regulate the liquid ammonia supply, flue gas flow and plasma output parameters, effectively avoid reaction imbalance or safety risks, and ensure the stability and safety of long-term operation.

[0033] In summary, this invention combines plasma-coupled catalytic synergistic cracking with flue gas waste heat gasification, along with multi-parameter closed-loop control, to address the pain points of traditional ammonia-to-hydrogen production, such as high energy consumption, slow response, and large gasification losses. This achieves zero-carbon, high-efficiency hydrogen production, adapts to the needs of multiple fields, and contributes to the low-carbon transformation of energy. Attached Figure Description

[0034] Figure 1 This is a schematic diagram of a plasma direct pyrolysis liquid ammonia to hydrogen production system;

[0035] Figure 2 This is a flowchart of the hydrogen-containing gas supply method proposed in this invention;

[0036] Figure label:

[0037] 01. Plasma power supply; 02. First plasma electrode plate; 03. Second plasma electrode plate; 04. Gas filter end; 05. Liquid ammonia; 06. Heat exchanger tube; 07. Flue gas inlet; 08. Flue gas outlet; 09. Cracker exhaust control valve; 10. Cracking gas outlet; 11. Liquid ammonia inlet; 12. Liquid ammonia control valve; 13. Thermometer; 14. Pressure gauge; 15. Catalyst chamber; 16. Grounding terminal; 17. Gas purification membrane; 18. Cracker tank; 19. Flue gas control valve; 20. Upper limit liquid level sensor; 21. Lower limit liquid level sensor; 22. Liquid ammonia guide pipe. Detailed Implementation

[0038] The technical solution of the present invention will now be clearly and completely described with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments.

[0039] The components of the embodiments of the invention described and shown in the accompanying drawings can typically be arranged and designed in a variety of different configurations. Therefore, the following detailed description of the embodiments of the invention provided in the drawings is not intended to limit the scope of the claimed invention, but merely to illustrate selected embodiments of the invention.

[0040] Example: Figure 1As shown, the present invention proposes a plasma direct pyrolysis liquid ammonia hydrogen production system, including a control system, a pyrolysis tank 18, a plasma power supply 01, a plasma first electrode plate 02, a plasma second electrode plate 03, a catalyst chamber 15, a grounding terminal 16, a liquid ammonia supply component, a temperature and pressure monitoring component, a gas processing component, and a flue gas heat exchange component.

[0041] The plasma power supply 01 is a DC power supply, AC power supply, microwave power supply or pulse modulation power supply; the plasma generated by energizing the first plasma electrode plate 02 and the second plasma electrode plate 03 is an arc plasma, microwave plasma, dielectric barrier discharge plasma, radio frequency plasma, sliding arc plasma, corona discharge plasma and rotating arc plasma.

[0042] The liquid ammonia supply assembly includes a liquid ammonia inlet 11, a liquid ammonia control valve 12, and a liquid ammonia guide pipe 22. The liquid ammonia inlet 11 is connected to one end of the liquid ammonia guide pipe 22 via the liquid ammonia control valve 12, and the other end of the liquid ammonia guide pipe 22 extends into the cracker tank 18.

[0043] The catalyst chamber 15 is encased in an electrically insulating material and fixed between the first plasma electrode plate 02 and the second plasma electrode plate 03. The catalyst chamber 15 is filled with a catalyst. The catalyst is a mixture of at least one catalyst selected from Ni-based transition metal catalysts, Fe-based transition metal catalysts, Co-based transition metal catalysts, Ru-based noble metal catalysts, Pt-based noble metal catalysts, Pd-based noble metal catalysts, Rh-based noble metal catalysts, and Ag-based noble metal catalysts. The catalyst is supported on a carrier, which is diatomaceous earth, kaolin, silica, cerium oxide, activated carbon, silica gel, glass sheet, glass fiber, silica, titanium dioxide, or a polymer. The first plasma electrode plate 02 is connected to the high-voltage terminal of the plasma power supply 01 via a conductive line, and the second plasma electrode plate 03 is connected to the grounding terminal and grounding terminal 16 of the plasma power supply 01 via a conductive line.

[0044] The temperature and pressure monitoring assembly includes a thermometer 13 and a pressure gauge 14, with the detection ends of the thermometer 13 and the pressure gauge 14 extending into the interior of the pyrolyzer tank 18; the structure of the pyrolyzer tank 18 is a tube sheet structure, a shell-and-tube structure, a partition wall structure, a hybrid structure, or a regenerative structure.

[0045] The gas processing assembly includes a gas filter end 04, a gas purification membrane 17, a pyrolyzer exhaust control valve 09, and a pyrolyzer gas outlet 10. The lower end of the gas filter end 04 is welded to the upper end of the pyrolyzer tank 18, and the upper end is connected to the pyrolyzer gas outlet 10 via the pyrolyzer exhaust control valve 09. The gas purification membrane 17 is located on the inner side of the top of the gas filter end 04. The gas purification membrane 17 is a Pd-based noble metal membrane or an Fe-based non-noble metal membrane.

[0046] The flue gas heat exchange assembly includes heat exchanger tube 06, flue gas inlet 07, flue gas outlet 08, and flue gas control valve 19. The heat exchanger tube 06 is placed at the bottom of the pyrolysis tank 18, with one end connected to the flue gas inlet 07 and the other end connected to the flue gas outlet 08 via a pipeline. The flue gas control valve 19 is installed between the flue gas inlet 07 and the external flue gas pipeline. The external high-temperature flue gas supply pipeline connected to the flue gas inlet 07 contains exhaust gas from a gas turbine, reciprocating engine, external combustion engine, gas boiler, burner exhaust, or aircraft engine.

[0047] The control system is connected to the liquid ammonia control valve 12, the pyrolyzer exhaust control valve 09, the flue gas control valve 19, and the plasma power supply 01 via control lines. It is also connected to the thermometer 13, the pressure gauge 14, and the upper limit liquid level sensor 20 and the lower limit liquid level sensor 21 on the inner wall of the pyrolyzer tank 18 via signal lines.

[0048] like Figure 2 As shown, this invention also proposes a method for direct plasma pyrolysis of liquid ammonia to produce hydrogen, comprising the following steps:

[0049] Step 1, Initial Preparation: After the control system is started, first output a signal to close the pyrolyzer exhaust control valve 09, and at the same time open the liquid ammonia control valve 12;

[0050] Step 2, Liquid Ammonia Level Control: Liquid ammonia is introduced into the pyrolysis tank 18 through the liquid ammonia inlet 11 and the liquid ammonia guide pipe 22. When the upper limit level sensor 20 detects that the liquid ammonia level has reached the set upper limit, the control system controls the liquid ammonia control valve 12 to close. If the lower limit level sensor 21 detects that the liquid ammonia level is lower than the set lower limit, the system returns to Step 1, continues to close the pyrolysis exhaust control valve 09 and open the liquid ammonia control valve 12 to replenish liquid ammonia. If the liquid ammonia level is higher than the set lower limit, the system proceeds to the next step.

[0051] Step 3, Plasma Start-up: The control system outputs a signal to turn on the plasma power supply 01, causing plasma to be generated between the first plasma electrode plate 02 and the second plasma electrode plate 03.

[0052] Step 4: Flue gas heat exchange starts: After the plasma is started, the control system opens the flue gas control valve 19. The external high-temperature flue gas enters the heat exchanger tube 06 through the flue gas inlet 07 and exchanges heat with the liquid ammonia in the pyrolyzer tank 18 to realize the vaporization of liquid ammonia and participate in the pyrolysis reaction. After heat exchange, the flue gas is discharged through the flue gas outlet 08.

[0053] Step 5: Reaction Parameter Monitoring: Monitor the temperature and pressure inside the pyrolysis tank 18 in real time using thermometer 13 and pressure gauge 14. If the pressure reaches the set upper limit or the temperature reaches the set upper limit, proceed to the next step; if the pressure does not reach the upper limit or the temperature does not reach the upper limit, proceed to step 7.

[0054] Step 6, Reaction Control: The control system adjusts the opening of the flue gas control valve 19 and shuts off the plasma power supply 01. After the temperature and pressure drop to a safe range, return to Step 3.

[0055] Step 7, Gas Output Judgment: If pressure gauge 14 detects that the pressure inside the tank reaches the set usage threshold, the control system opens the pyrolyzer exhaust control valve 09. The hydrogen-containing gas generated by pyrolysis is filtered by gas filter end 04 and purified by gas purification membrane 17, and then supplied to the gas user end through pyrolyzed gas outlet 10. If pressure gauge 14 detects that the pressure inside the tank is lower than the set pressure lower limit, then return to step 3.

[0056] Step 8: Continuous gas supply: Repeat the above steps to continuously supply hydrogen-containing gas or high-purity hydrogen to the gas user.

[0057] The above specific embodiments are merely several optional embodiments of the present invention. Based on the technical solutions of the present invention and the relevant teachings of the above embodiments, those skilled in the art can make various alternative improvements and combinations to the above specific embodiments.

Claims

1. A plasma direct pyrolysis liquid ammonia hydrogen production system, characterized in that, It includes a control system, a pyrolysis tank (18), a plasma power supply (01), a plasma first electrode plate (02), a plasma second electrode plate (03), a catalyst chamber (15), a grounding terminal (16), a liquid ammonia supply assembly, a temperature and pressure monitoring assembly, a gas processing assembly, and a flue gas heat exchange assembly. The liquid ammonia supply assembly includes a liquid ammonia inlet (11), a liquid ammonia control valve (12), and a liquid ammonia guide pipe (22). The liquid ammonia inlet (11) is connected to one end of the liquid ammonia guide pipe (22) via the liquid ammonia control valve (12), and the other end of the liquid ammonia guide pipe (22) extends into the cracker tank (18). The catalyst chamber (15) is encased in an electrical insulator and fixed between the first plasma electrode plate (02) and the second plasma electrode plate (03). The first plasma electrode plate (02) is connected to the high-voltage end of the plasma power supply (01) via a conductive line, and the second plasma electrode plate (03) is connected to the grounding terminal and the grounding terminal (16) of the plasma power supply (01) via a conductive line. The temperature and pressure monitoring assembly includes a thermometer (13) and a pressure gauge (14), with the detection ends of the thermometer (13) and the pressure gauge (14) extending into the interior of the pyrolysis tank (18); The gas processing assembly includes a gas filter end (04), a gas purification membrane (17), a pyrolyzer exhaust control valve (09), and a pyrolyzer gas outlet (10). The lower end of the gas filter end (04) is welded to the upper end of the pyrolyzer tank (18), and the upper end is connected to the pyrolyzer gas outlet (10) via the pyrolyzer exhaust control valve (09). The gas purification membrane (17) is located on the inner side of the top of the gas filter end (04). The flue gas heat exchange assembly includes a heat exchanger tube (06), a flue gas inlet (07), a flue gas outlet (08), and a flue gas control valve (19). The heat exchanger tube (06) is placed at the bottom of the pyrolyzer tank (18), with one end connected to the flue gas inlet (07) via a pipeline and the other end connected to the flue gas outlet (08). The flue gas control valve (19) is installed between the flue gas inlet (07) and the external flue gas pipeline. The control system is connected to the liquid ammonia control valve (12), the pyrolyzer exhaust control valve (09), the flue gas control valve (19), and the plasma power supply (01) via control lines, and is connected to the thermometer (13), the pressure gauge (14), and the upper limit liquid level sensor (20) and the lower limit liquid level sensor (21) on the inner wall of the pyrolyzer tank (18) via signal lines.

2. The plasma direct pyrolysis liquid ammonia hydrogen production system according to claim 1, characterized in that, The plasma power source (01) is any one of a DC power source, an AC power source, a microwave power source, or a pulse modulation power source; The plasma generated by the first plasma electrode plate (02) and the second plasma electrode plate (03) being energized is any one of the following: arc plasma, microwave plasma, dielectric barrier discharge plasma, radio frequency plasma, sliding arc plasma, corona discharge plasma, and rotating arc plasma.

3. The plasma direct pyrolysis liquid ammonia hydrogen production system according to claim 1, characterized in that, The catalyst chamber (15) is filled with catalyst; The catalyst is a mixture of at least one catalyst selected from Ni-based transition metal catalysts, Fe-based transition metal catalysts, Co-based transition metal catalysts, Ru-based noble metal catalysts, Pt-based noble metal catalysts, Pd-based noble metal catalysts, Rh-based noble metal catalysts, and Ag-based noble metal catalysts. The catalyst is supported on a carrier, which may be diatomaceous earth, kaolin, silicon dioxide, cerium oxide, activated carbon, silica gel, glass sheet, glass fiber, silicon dioxide, titanium dioxide, or a polymer.

4. The plasma direct pyrolysis liquid ammonia hydrogen production system according to claim 1, characterized in that, The structure of the pyrolyzer tank (18) is a tube sheet structure, a shell-and-tube structure, a partition wall structure, a hybrid structure, or a regenerative structure.

5. The plasma direct pyrolysis liquid ammonia hydrogen production system according to claim 1, characterized in that, In the external high-temperature flue gas supply pipeline connected to the flue gas inlet (07), the high-temperature flue gas is the exhaust gas of a gas turbine, the exhaust gas of a reciprocating engine, the exhaust gas of an external combustion engine, the exhaust gas of a gas boiler, the exhaust gas of a burner, or the exhaust gas of an aircraft engine.

6. The plasma direct pyrolysis liquid ammonia hydrogen production system according to claim 1, characterized in that, The gas purification membrane (17) is a Pd-based noble metal membrane or an Fe-based non-noble metal membrane.

7. A method for producing hydrogen from liquid ammonia via direct plasma pyrolysis according to any one of claims 1-6, characterized in that, Includes the following steps: Step 1: After the control system is started, first output a signal to close the pyrolyzer exhaust control valve (09), and at the same time open the liquid ammonia control valve (12). Step 2: Liquid ammonia is introduced into the pyrolysis tank (18) through the liquid ammonia inlet (11) and the liquid ammonia guide pipe (22). When the upper limit liquid level sensor (20) detects that the liquid ammonia level has reached the set upper limit, the control system controls the liquid ammonia control valve (12) to close. If the lower limit liquid level sensor (21) detects that the liquid ammonia level is lower than the set lower limit, the system returns to Step 1, continues to close the pyrolysis exhaust control valve (09) and open the liquid ammonia control valve (12) to replenish liquid ammonia. If the liquid ammonia level is higher than the set lower limit, the system proceeds to the next step. Step 3: The control system outputs a signal to turn on the plasma power supply (01), so that plasma is generated between the first plasma electrode plate (02) and the second plasma electrode plate (03); Step 4: After the plasma is started, the control system opens the flue gas control valve (19). The external high-temperature flue gas enters the heat exchanger tube (06) through the flue gas inlet (07) and exchanges heat with the liquid ammonia in the pyrolyzer tank (18) to realize the vaporization of liquid ammonia and participate in the pyrolysis reaction. After heat exchange, the flue gas is discharged through the flue gas outlet (08). Step 5: Monitor the temperature and pressure inside the cracker tank (18) in real time using a thermometer (13) and a pressure gauge (14). If the pressure reaches the set pressure limit or the temperature reaches the set temperature limit, proceed to the next step. If the pressure does not reach the pressure limit or the temperature does not reach the temperature limit, proceed to step 7. Step 6: The control system adjusts the opening of the flue gas control valve (19) and turns off the plasma power supply (01). After the temperature and pressure drop to a safe range, return to step 3. Step 7: If the pressure gauge (14) detects that the pressure inside the tank reaches the set usage threshold, the control system opens the pyrolyzer exhaust control valve (09). The hydrogen-containing gas generated by pyrolysis is filtered by the gas filter end (04) and purified by the gas purification membrane (17), and then supplied to the gas user end through the pyrolyzed gas outlet (10). If the pressure gauge (14) detects that the pressure inside the tank is lower than the set pressure lower limit, then return to step 3. Step 8: Repeat the above steps to continuously supply hydrogen-containing gas or high-purity hydrogen to the gas user.

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