An integrated ammonia fuel supply system

Abstract

The application provides an integrated ammonia fuel supply system, comprising: a liquid ammonia storage and BOG processing unit for storing liquid ammonia and receiving system backflow, the liquid ammonia storage and BOG processing unit recycling the evaporation gas generated by the storage tank through the ejection pressure boosting and self-recuperation liquefaction mode to realize zero energy consumption; a power recovery unit using ammonia as the working medium to absorb the heat of external heat source to generate high-temperature and high-pressure ammonia steam, and converting the heat energy into mechanical work through an expander to drive at least one liquid ammonia booster in the system; a fuel conditioning unit receiving the fuel stream ammonia from the liquid ammonia booster, gasifying the ammonia into ammonia gas through a heat source, and using part of the ammonia gas to crack in a plasma-assisted membrane reactor to produce high-purity hydrogen, and then dispensing the remaining ammonia gas and liquid ammonia according to the demand to supply energy equipment. The application realizes self-balancing of system energy consumption, on-demand conditioning of fuel quality, and safe and reliable operation in all working conditions.

Description

Technical Field

[0001] This invention relates to the field of ammonia fuel supply systems, and more particularly to an integrated ammonia fuel supply system. Background Technology

[0002] Ammonia, as a carbon-free hydrogen-rich fuel, faces several key technological bottlenecks in its large-scale application: incomplete combustion of liquid ammonia leads to high ammonia slip; slow cold start-up necessitates high-power electric heating or plasma, resulting in extremely high energy consumption; BOG (bulk boil-off gas) processing relies on compressors, which consumes a lot of power and has a slow dynamic response; insufficient utilization of system waste heat leads to low overall energy efficiency; and the toxicity, corrosiveness, and hydrogen embrittlement risks of ammonia fuel pose serious challenges to system safety. Current technologies cannot simultaneously solve these problems within a single system. Summary of the Invention

[0003] The purpose of this invention is to provide an integrated ammonia fuel supply system and control method. Through the deep coupling of ejector-type self-regenerating BOG treatment, transcritical ammonia working fluid power recovery, plasma membrane separation hydrogen production, tail gas cascade utilization, and digital twin control, the system achieves self-balancing energy consumption, on-demand fuel quality modulation, and safe and reliable operation under all working conditions.

[0004] To achieve the above objectives, the present invention provides an integrated ammonia fuel supply system, including a liquid ammonia storage and BOG processing unit, a power recovery unit, a fuel modulation unit, a waste heat utilization path for exhaust gas, and a control unit.

[0005] The liquid ammonia storage and BOG processing unit is used to store liquid ammonia and receive system reflux. It re-liquefies and recovers the evaporated gas generated in the storage tank through ejector pressurization and self-heating liquefaction with zero energy consumption.

[0006] The power recovery unit uses ammonia as the working fluid, absorbs heat from an external heat source to generate high-temperature, high-pressure ammonia vapor, and converts the thermal energy into mechanical work through an expander to drive at least one liquid ammonia pressurization device in the system.

[0007] The fuel modulation unit receives fuel ammonia from the liquid ammonia pressurization device, vaporizes it into ammonia gas through a heat source, and uses a portion of the ammonia gas to produce high-purity hydrogen through cracking in a plasma-assisted membrane reactor. The hydrogen gas is then mixed with the remaining ammonia gas and liquid ammonia gas as needed and supplied to the energy-consuming equipment.

[0008] The waste heat utilization path of the exhaust gas uses the exhaust gas discharged from the energy-consuming equipment in descending order of grade as the heat source for the power recovery unit, the plasma-assisted membrane reactor, and the fuel modulation unit.

[0009] The control unit is used to adjust the operating parameters of each unit according to load requirements.

[0010] Furthermore, the liquid ammonia storage and BOG processing unit includes: Liquid ammonia storage tank; The thermostatic buffer tank is connected to the liquid phase outlet of the liquid ammonia storage tank via a pipeline equipped with a replenishment valve; The supersonic gas ejector has its low-pressure ejector port connected to the gas phase outlet of the liquid ammonia storage tank, and its power nozzle connected to the ejector branch of the liquid ammonia pressurization device outlet through a working fluid regulating valve. A multi-stream heat exchanger, the hot-side inlet of which is connected to the ejector outlet, and the hot-side outlet is connected to the gas-liquid inlet of the thermostatic buffer tank via a throttling and pressure-reducing valve; The cold evaporation gas outlet at the top of the constant temperature buffer tank is connected to the cold side inlet of the multi-stream heat exchanger. The cold side outlet of the multi-stream heat exchanger is connected to the atmosphere after passing through the membrane separation ammonia extraction device, and the separated ammonia is returned to the ejector circuit.

[0011] Furthermore, the energy recovery unit includes: The ammonia vapor generator has its cold-side inlet connected to the power flow branch of the liquid ammonia booster outlet via a quick-closing valve and a regulating valve, and its hot-side inlet connected to the high-temperature exhaust gas from the energy-consuming equipment. The turbine expander has its inlet connected to the cold side outlet of the ammonia vapor generator, and its output shaft is mechanically connected to the liquid ammonia pressurization device via direct shaft power drive. The feed ammonia heater / phase change accumulator assembly has its hot-side inlet connected to the turbine expander exhaust port, and a turbine bypass pipeline with a bypass throttle valve is connected in parallel. The hot-side outlet of the feed ammonia heater / phase change accumulator assembly is connected to the ammonia inlet of the multi-mode gas distribution manifold.

[0012] Furthermore, the fuel modulation unit includes: The fuel distribution valve assembly has an inlet connected to the fuel flow branch of the liquid ammonia booster outlet, one outlet branch is a liquid ammonia direct injection branch, which is directly connected to the liquid ammonia nozzle of the multi-mode gas distribution main, and the other outlet branch is a gasification branch. The ammonia evaporator has its cold-side inlet connected to the gasification branch and its hot-side inlet connected to the waste heat from the tail gas. The plasma-membrane reactor has its shell-side inlet connected to the cold-side outlet of the ammonia evaporator via the main ammonia gas pipeline, its tube-side is the pure hydrogen permeation side, and its tube-side outlet is connected to the pure hydrogen inlet of the multi-mode gas distribution main. The ammonia static mixer has its inlet connected to the back pressure valve outlet of the shell-side outlet of the plasma-membrane reactor and the ammonia bypass outlet of the ammonia evaporator, respectively, and its outlet connected to the cold side inlet of the feed ammonia heater / phase change accumulator assembly. The cold-side outlet of the feed ammonia heater / phase change accumulator assembly is connected to the ammonia inlet of the multi-mode gas distribution manifold.

[0013] Furthermore, in the waste heat utilization path of the exhaust gas, the exhaust gas discharged from the energy-consuming equipment flows sequentially through the hot side of the ammonia vapor generator, the heating jacket of the plasma-membrane reactor, the hot side of the ammonia evaporator, and the integrated plasma synergistic catalytic purifier, and finally the clean flue gas is discharged through the chimney.

[0014] Preferably, the plasma-assisted membrane reactor is a coaxial dielectric barrier discharge-membrane integrated reactor, the core of which is a multi-channel palladium-silver alloy hollow fiber membrane tube. The shell side is filled with a core-shell structure Ni-Al2O3@SiO2 catalyst. The plasma excites ammonia gas to generate active groups in the shell side, and the generated hydrogen gas is separated in situ through the membrane tube side to produce hydrogen gas with a purity of 99.99%.

[0015] Preferably, all pipelines in contact with ammonia adopt a double-walled concentric sleeve structure. The inner pipe transports fuel, and the annular gap is filled with slightly positive pressure nitrogen and connected to a centralized ammonia-sensitive spectrometer. When a leak is detected, the upstream and downstream dual redundant solenoid valves are automatically shut off.

[0016] Therefore, the present invention adopts the above-mentioned integrated ammonia fuel supply system, and the technical effects are as follows: Rapid cold start: The plasma-membrane reactor instantly produces hydrogen, and pure hydrogen is used for pilot ignition. The system can complete cold ignition and stabilize to idle speed within 30 seconds.

[0017] BOG Zero Energy Consumption Processing: Utilizing high-pressure liquid ammonia to eject BOG, combined with self-regenerating cryogenic liquefaction, it replaces the traditional compressor, achieving near-zero power consumption in BOG processing and recovering evaporative cooling energy.

[0018] Self-powered: By using the transcritical ammonia working fluid Rankine cycle, the waste heat of high-temperature exhaust gas is efficiently converted into shaft power, which directly drives the liquid ammonia booster pump, reducing the system's own power consumption by more than 90%.

[0019] Deep conditioning of fuel quality: In-situ production of 99.99% high-purity hydrogen, realizing stepless gas distribution of hydrogen-ammonia-liquid ammonia three modes, which can meet the requirements of different loads and fuel quality, and fundamentally solve the problems of incomplete combustion and ammonia escape.

[0020] Optimal energy efficiency under all operating conditions: exhaust gas is utilized in stages according to grade, phase change energy storage devices shave peaks and fill valleys, and digital twin control enables predictive self-evolutionary adjustment, with a total system energy efficiency of ≥85%.

[0021] Intrinsic safety and ultra-low emissions: Double-walled pipe gallery inerting protection and leak-proof design, combined with integrated plasma synergistic catalytic purification technology, achieves ammonia escape ≤2ppm and NO... x Emissions ≤50mg / m³ 3 . Attached Figure Description

[0022] Figure 1This is a schematic diagram of an integrated ammonia fuel supply system according to the present invention. Detailed Implementation

[0023] The technical solution of the present invention will be further described below with reference to the accompanying drawings and embodiments.

[0024] Unless otherwise defined, the technical or scientific terms used in this invention shall have the ordinary meaning as understood by one of ordinary skill in the art to which this invention pertains.

[0025] Example 1 like Figure 1 As shown, an integrated ammonia fuel supply system includes: Route 1: Ejector-type self-regenerating BOG zero-energy liquefaction loop The liquid ammonia storage tank operates at a temperature of -33.4℃ and a pressure of 0.1 MPaA, storing cryogenic liquid ammonia. The continuously generated BOG (boil-off gas) is saturated ammonia vapor at -33.4℃. Its BOG is piped to the low-pressure ejector port of the supersonic ejector (EJ). The high-pressure liquid ammonia pump (PUMP) outputs subcooled liquid ammonia at a pressure of 15-25 MPaA and a temperature of -30℃ to -20℃, providing a high-pressure power source for the ejector. The high-pressure liquid ammonia pump draws and pressurizes liquid ammonia from the thermostatic buffer tank. After passing through a three-way diverter valve assembly, one path serves as the ejector working fluid, which enters the ejector's power nozzle through a working fluid regulating valve. The pressure of the mixture at the ejector outlet is increased to 0.8-1.5 MPaA, with a temperature of approximately -10℃ to 0℃. The pressurized mixed gas from the ejector outlet enters the hot side of the multi-stream heat exchanger (MHEX), where it is pre-cooled by the cold-side medium and cooled to below -25°C, remaining in a gaseous state. It then passes through a throttling and pressure-reducing valve (JTV) into a constant-temperature buffer tank, where the pressure drops to 0.1 MPaA and the temperature correspondingly recovers to -33.4°C. Most of the ammonia is reliquefied, completing a zero-energy closed loop. The liquefied ammonia and non-condensable gas (nitrogen) rise to the top of the tank. The cold evaporated gas from the top of the tank is led out to the cold side of the multi-stream heat exchanger to recover its cooling capacity. After membrane separation and purification, the ammonia returns to the ejector circuit, and the inert gas is discharged in compliance with standards. The purified gas after membrane separation is nitrogen-rich, mainly containing nitrogen and trace amounts of argon. Its ammonia volume concentration is stably controlled below 5 ppm through closed-loop regulation of the membrane separation unit, far below the national odor pollutant emission standard limit, allowing it to be directly released into the atmosphere, forming a zero-ammonia escape closed loop. At the same time, an ammonia concentration sensor needs to be installed at the membrane separation outlet and interlocked with the vent valve. If the concentration exceeds the standard, the discharge will be immediately cut off and the system will be switched back to the storage tank to ensure that nothing goes wrong.

[0026] Route 2: Transcritical ammonia working fluid power recovery and fuel preheating loop The second outlet of the high-pressure liquid ammonia pump serves as the power flow, with a pressure of 15-25 MPaA (higher than the critical pressure of ammonia, 11.3 MPa) and a temperature of -30℃, making it a high-density fluid in a supercritical or transcritical state. Entering the cold side of the ammonia vapor generator (HRSG), it absorbs heat from the approximately 700℃ high-temperature exhaust gas discharged from the energy-consuming equipment (ENGINE), transforming into superheated ammonia vapor. Heated to 500-550℃ by the 700℃ exhaust gas, and maintaining a pressure of 15-25 MPaA, it enters a high-temperature, high-pressure superheated steam state, possessing significant work-capacity. The ammonia vapor then passes through a quick-closing valve and a regulating valve into the turbine expander (TURBINE) for expansion and work. After expansion, the pressure drops to 2-3 MPaA, and the temperature drops to 200-300℃, remaining in a gaseous ammonia state. These parameters match the feed preheating requirements, achieving "quality-based energy use." Its output shaft directly drives the high-pressure liquid ammonia pump, achieving self-sufficiency in pump power. Turbine exhaust (still gaseous ammonia) enters the hot side of the feed ammonia heater / phase change accumulator complex (HEATER). The turbine expander exhaust is cooled to 80-100°C, transferring heat to the cold-side fuel ammonia before being sent to the ammonia inlet of the multi-mode distribution manifold (MIXER). A bypass throttle valve is installed in the turbine bypass to ensure uninterrupted fuel supply in the event of a turbine failure.

[0027] Route 3: Plasma-membrane staged hydrogen production and multimodal gas distribution loop The third stream from the high-pressure liquid ammonia pump outlet serves as fuel, entering the ammonia evaporator (EVAP) for vaporization. The ammonia gas at the EVAP outlet has a pressure of 2-3 MPaA and a temperature of 80-150℃, forming saturated or slightly superheated ammonia gas. The vaporized ammonia gas is then split, with the main stream entering the shell side of the plasma-membrane reactor (MEM_REAC). Under the synergistic effect of plasma activation and catalyst / membrane separation, partial ammonia cracking occurs at 400-500℃ and 2-3 MPaA, utilizing plasma-assisted catalysis to achieve efficient in-situ cracking of ammonia. High-purity hydrogen permeates through the membrane tube from the tube side to the pure hydrogen inlet of the main gas distribution pipe. The high-purity hydrogen produced in the tube side has a pressure of 2-3 MPaA and a temperature of 400-500℃. The lean ammonia nitrogen gas at the shell-side outlet is pressurized to 1-1.5 MPaA by the back pressure valve, and then mixed evenly with the ammonia bypass in the ammonia static mixer (SM). It then enters the cold side of the feed ammonia heater / phase change accumulator (HEATER) to absorb heat and is heated to 150-250℃, becoming superheated ammonia gas. This gas is then sent to the ammonia inlet of the gas distribution manifold, ensuring that the fuel has a good thermodynamic state before entering the energy-consuming equipment, which is conducive to combustion organization.

[0028] Exhaust gas cascade utilization path: High-temperature exhaust gas from energy-consuming equipment (large low-speed two-stroke marine engines, ammonia gas turbines or dedicated ammonia boilers, new-generation dual-fuel engines, etc.) sequentially passes through the hot side of an ammonia vapor generator (HRSG), where the temperature drops to approximately 500°C; then it enters the heating jacket of a plasma-membrane reactor (MEM_REAC) to maintain the reaction temperature; next, it flows through the hot side of an ammonia evaporator (EVAP) to provide heat for liquid ammonia vaporization; finally, it enters an integrated plasma-assisted catalytic converter (ASCR) to simultaneously remove NO at 200°C. x The unburned ammonia is discharged into the air, and the clean flue gas is discharged.

[0029] A control method for an integrated ammonia fuel supply system includes the following steps: I. Global Pressure and Power Balance Control Layer of Route 2 The high-pressure liquid ammonia pump (PUMP) adopts variable frequency speed control. Its speed command is obtained by PID calculation based on the deviation between the outlet pressure set value (SP=20 MPaA) and the measured value.

[0030] The opening of the regulating valve of the turbine expander is dynamically adjusted according to the pump speed requirement. When the load of the energy-consuming equipment (ENGINE) increases and the heat of the exhaust gas increases, the steam production of the ammonia vapor generator (HRSG) increases, and the power of the turbine output shaft increases. At this time, the turbine intake regulating valve is adjusted through the speed closed loop to maintain the pump speed constant, so as to achieve "heat-driven power generation and self-consumption".

[0031] Monitor the pressure before the turbine expander inlet quick-closing valve and the turbine outlet pressure. If the turbine trips due to a fault or the inlet superheat is below the safety threshold (<480℃), the quick-closing valve closes instantly, and the bypass throttle valve opens rapidly and linearly according to the outlet set pressure (2.5 MPaA). High-pressure supercritical ammonia is directly depressurized to 2.5 MPaA via the bypass and enters the feed ammonia heater, ensuring uninterrupted downstream fuel supply while protecting the turbine.

[0032] II. Fuel calorific value and multimodal gas distribution quality control layer of Route 3 Based on the target hydrogen doping ratio (e.g., 0%~20%), set the hydrogen partial pressure at the shell outlet of the membrane reactor or the high hydrogen output flow rate at the tube outlet.

[0033] Cascade control is employed: the main loop controls the setpoint for the hydrogen production flow rate in the tube side, while the secondary loop controls the reactor shell-side temperature (400-500℃). The cracking rate is precisely controlled by adjusting the bypass flow rate of the tail gas entering the reactor jacket and the plasma discharge power. When hydrogen production is insufficient, the plasma power is increased first, followed by increasing the high-temperature tail gas bypass flow rate.

[0034] The lean ammonia nitrogen gas (containing a small amount of uncracked ammonia) at the shell outlet of the membrane reactor is stabilized to 1.2 MPaA by the back pressure valve (PCV).

[0035] The ammonia bypass pressure is adjusted to match that of the lean ammonia nitrogen gas (to overcome the pressure difference). Before both enter the static mixer (SM), a flow ratio controller is set. Based on the total fuel demand (flow rate) and target calorific value, the two regulating valves are cross-limited to prevent backfire or combustion oscillation caused by the interruption of either medium supply.

[0036] The temperature of the superheated ammonia gas before entering the main gas distribution pipe is set to 200℃. Adjust the cold side bypass flow of the feed ammonia heater (HEATER) and use the residual heat of the turbine exhaust (200-300℃) to heat the mixed gas to the target temperature, ensuring that the fuel is completely vaporized and has good ignition characteristics before entering the furnace.

[0037] III. Tank Pressure Maintenance and Zero-Energy BOG Liquefaction Control Layer for Route 1 Monitor the tank pressure (P_TANK). When the pressure rises (BOG production increases), increase the opening of the high-pressure working fluid regulating valve to increase the ejector coefficient of the supersonic injector (EJ) and stabilize the injector outlet mixed gas pressure at 1.2 MPaA.

[0038] The cold-side flow rate (from the cold evaporating gas at the top of the tank) of the multi-flow heat exchanger (MHEX) is used to pre-cool the hot-side mixed gas. The hot-side outlet temperature of the MHEX is controlled (target -28°C) to ensure that the mixed gas, after being throttled by the JTV, is just liquefied when it enters the thermostatic buffer tank (BUFFER). If the BUFFER level is too high, it indicates excessive liquefaction; in this case, the working fluid regulating valve should be closed slightly to reduce the injection rate.

[0039] The isothermal buffer tank is equipped with pressure control and venting flow regulation at the top. Cold evaporated gas (enriched with nitrogen) from the top of the tank is introduced into the MHEX cold side for rewarming.

[0040] The most critical safety interlock: Install dual redundant ammonia concentration sensors (online chromatograph / laser analyzer) in the membrane separation outlet pipeline.

[0041] Under normal operating conditions: ammonia concentration < 5 ppm, the vent valve is opened to release ammonia into the atmosphere.

[0042] Abnormal operating conditions (ammonia concentration ≥ 5ppm or sensor failure): The control system triggers a three-level interlock—① Immediately close the membrane separation outlet vent valve; ② Open the reflux valve to switch all unqualified gas back to the storage tank or injector inlet; ③ Issue an alarm and reduce the load until the membrane separation unit is regenerated or repaired, strictly achieving "zero ammonia escape".

[0043] IV. Exhaust Gas Cascade Utilization and Dynamic Heat Dissipation Control Layer The 700°C exhaust gas from the energy-consuming equipment is first forced through the HRSG to generate superheated ammonia vapor to drive the turbine.

[0044] A high-temperature three-way regulating valve is installed on the pipeline from the HRSG outlet to the MEM_REAC jacket. The flow rate of the exhaust gas entering the jacket is adjusted according to the MEM_REAC reaction temperature (SP=450℃), and the excess high-temperature exhaust gas is directly bypassed to the inlet of the downstream ammonia evaporator (EVAP).

[0045] Monitor the ammonia temperature at the EVAP outlet (target 120℃). If the temperature is too low, prioritize closing the exhaust gas baffle of the ASCR to increase the heat exchange of the EVAP. However, it is essential to ensure that the exhaust gas temperature entering the ASCR is not lower than the denitrification window of 200℃.

[0046] ASCR (Air Purifier) ​​Minimum Continuous Operating Temperature Guarantee: Temperature monitoring is installed at the ASCR inlet. If the load is too low, causing the exhaust gas temperature to drop below 180°C, the control system automatically triggers electric heating assistance or briefly increases the engine idle speed, and adjusts the bypass baffle to ensure that the catalyst in the ASCR is maintained within the 200±20°C activity range, simultaneously removing NO. x With unburned ammonia.

[0047] V. Full-condition start-stop and fault self-healing control logic Cold start sequence: Start the high-pressure liquid ammonia pump (PUMP), open the turbine bypass throttle valve to establish a low-pressure fuel gas path, ignite / start the energy-consuming equipment (ENGINE), gradually close the bypass after the exhaust gas temperature rises, connect to the turbine grid, after the turbine output power reaches the standard, open the injector working valve (start BOG liquefaction), start the plasma power supply after the reactor temperature reaches 400℃, and connect to membrane separation for hydrogen production.

[0048] Emergency Stop (ESD) strategy: Once ESD is triggered, the high-pressure liquid ammonia pump quickly reduces its frequency to the minimum maintenance speed (or stops), and the turbine speed shut-off valve and bypass throttle valve simultaneously return to zero.

[0049] Safety is the top priority: the plasma-membrane reactor (MEM_REAC) is immediately powered off and purged with nitrogen; all ammonia discharge valves are forcibly closed, and all residual ammonia in the system is directed to the safety absorption tank through the emergency pressure relief valve to prevent accidental leakage of high-pressure supercritical ammonia.

[0050] In the above scheme, the system achieves energy self-sufficiency through ammonia working fluid power recovery, achieves flexible fuel modulation through in-situ hydrogen production via membrane reactor, and achieves zero-energy consumption treatment of BOG through ejector self-regeneration. Overall, it constitutes a new generation of ammonia fuel supply system that is "self-producing hydrogen, self-supplying energy, zero-emission, and self-evolving".

[0051] Therefore, the present invention adopts the above-mentioned integrated ammonia fuel supply system, which achieves system energy self-balancing, on-demand fuel quality modulation, and safe and reliable operation under all working conditions through deep coupling of ejector self-regenerating BOG treatment, transcritical ammonia working fluid power recovery, plasma membrane separation hydrogen production, tail gas cascade utilization, and digital twin control.

[0052] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention and not to limit them. Although the present invention has been described in detail with reference to preferred embodiments, those skilled in the art should understand that modifications or equivalent substitutions can still be made to the technical solutions of the present invention, and these modifications or equivalent substitutions cannot cause the modified technical solutions to deviate from the spirit and scope of the technical solutions of the present invention.

Claims

1. An integrated ammonia fuel supply system, characterized in that, include: The liquid ammonia storage and BOG processing unit is used to store liquid ammonia and receive system reflux. The liquid ammonia storage and BOG processing unit uses ejector pressurization and self-heating liquefaction to re-liquefy and recover the evaporated gas generated by the storage tank with zero energy consumption. The power recovery unit uses ammonia as the working fluid to absorb heat from an external heat source to generate high-temperature and high-pressure ammonia vapor, and converts the thermal energy into mechanical work through an expander to drive at least one liquid ammonia pressurization device in the system. The fuel modulation unit receives fuel ammonia from the liquid ammonia pressurization unit, vaporizes it into ammonia gas through a heat source, and uses part of the ammonia gas to produce high-purity hydrogen through cracking in a plasma-assisted membrane reactor. The hydrogen gas is then mixed with the remaining ammonia gas and liquid ammonia gas as needed and supplied to the energy-consuming equipment. The waste heat utilization path of exhaust gas involves using the exhaust gas discharged from the energy-consuming equipment in descending order of quality as the heat source for the power recovery unit, the plasma-assisted membrane reactor, and the fuel modulation unit.

2. The integrated ammonia fuel supply system according to claim 1, characterized in that, The liquid ammonia storage and BOG processing unit includes: Liquid ammonia storage tank; The thermostatic buffer tank is connected to the liquid phase outlet of the liquid ammonia storage tank via a pipeline equipped with a replenishment check valve; The supersonic gas ejector has a low-pressure ejector port connected to the gas phase outlet of the liquid ammonia storage tank, and a power nozzle connected to the ejector branch of the high-pressure liquid ammonia pump outlet via a working fluid regulating valve. The multi-stream heat exchanger has its hot-side inlet connected to the outlet of a supersonic gas ejector, and its hot-side outlet connected to the gas-liquid inlet of a thermostatic buffer tank via a throttling and pressure-reducing valve. The cold evaporation gas outlet at the top of the constant temperature buffer tank is connected to the cold side inlet of the multi-stream heat exchanger. The tail gas from the cold side of the multi-stream heat exchanger is treated and then connected to the atmosphere. The separated ammonia is returned to the ejector circuit.

3. The integrated ammonia fuel supply system according to claim 1, characterized in that, The energy recovery unit includes: The cold side inlet of the ammonia vapor generator is connected to the power flow branch of the outlet of the high-pressure liquid ammonia pump through a quick-closing valve and a regulating valve, while the hot side is connected to the high-temperature exhaust gas of the energy-consuming equipment. The inlet of the turboexpander is connected to the cold side outlet of the ammonia vapor generator, and the output shaft is mechanically connected to the high-pressure liquid ammonia pump via direct shaft drive. The hot-side inlet of the feed ammonia heater / phase change accumulator assembly is connected to the exhaust port of the turbine expander, and a turbine bypass pipeline with a bypass throttle valve is installed in parallel. The hot-side outlet of the feed ammonia heater / phase change accumulator assembly is connected to the ammonia inlet of the multi-mode gas distribution manifold.

4. The integrated ammonia fuel supply system according to claim 1, characterized in that, The fuel modulation unit includes: The inlet of the fuel distribution valve group is connected to the fuel flow branch of the liquid ammonia booster outlet. One of the outlet branches is a liquid ammonia direct injection branch, which is directly connected to the liquid ammonia nozzle of the multi-mode gas distribution main pipe. The other outlet branch is a gasification branch. The cold-side inlet of the ammonia evaporator is connected to the gasification branch of the fuel distribution valve group, and the hot-side outlet of the ammonia evaporator is connected to the waste heat of the tail gas and is diverted through the ammonia gas distributor. The shell-side inlet of the plasma-membrane reactor is connected to one of the outlets of the ammonia splitter, the tube-side is the pure hydrogen permeation side, and the tube-side outlet is connected to the pure hydrogen inlet of the multi-mode gas distribution main. The inlet of the ammonia static mixer is connected to the back pressure valve at the shell-side outlet of the plasma-membrane reactor and the ammonia bypass at the outlet of the ammonia splitter, respectively. The outlet of the ammonia static mixer is connected to the cold side inlet of the feed ammonia heater / phase change accumulator assembly. The cold-side outlet of the feed ammonia heater / phase change accumulator assembly is connected to the ammonia inlet of the multi-mode gas distribution manifold.

5. An integrated ammonia fuel supply system according to claim 1, characterized in that, In the aforementioned waste heat utilization path, the exhaust gas discharged from the energy-consuming equipment flows sequentially through: the hot side of the ammonia vapor generator, the heating jacket of the plasma-membrane reactor, the hot side of the ammonia evaporator, and the integrated plasma synergistic catalytic purifier, ultimately resulting in clean flue gas emission.

6. An integrated ammonia fuel supply system according to claim 1, characterized in that, The plasma-assisted membrane reactor is a coaxial dielectric barrier discharge-membrane integrated reactor. Its core is a multi-channel palladium-silver alloy hollow fiber membrane tube. The shell side is filled with a core-shell structure Ni-Al2O3@SiO2 catalyst. The plasma excites ammonia gas to generate active groups in the shell side, and the generated hydrogen gas is separated in situ through the membrane tube side to produce hydrogen gas with a purity of 99.99%.

7. An integrated ammonia fuel supply system according to claim 1, characterized in that, The working medium ammonia used in the power recovery unit expands and does work before entering the fuel modulation unit, where it is supplied to the energy-consuming equipment as part of the fuel, forming an open cycle.

8. An integrated ammonia fuel supply system according to claim 1, characterized in that, All pipelines in contact with ammonia adopt a double-walled concentric sleeve structure. The inner tube transports fuel, and the annular gap is filled with slightly positive pressure nitrogen and connected to a centralized ammonia-sensitive spectrometer. When a leak is detected, the upstream and downstream dual redundant solenoid valves are automatically shut off.

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