A thermo-photovoltaic catalytic fluidized reactor-fuel cell combined power generation system based on ship transportation

Abstract

The present application relates to the field of marine energy power technology, and discloses a thermophotovoltaic catalytic fluidized reactor-fuel cell combined power generation system based on ship transportation, which aims to solve the problems of low efficiency, large space occupation and incomplete tail gas treatment of the existing marine ammonia fuel power generation system.The system comprises a liquid ammonia storage tank, a thermophotovoltaic catalytic fluidized reactor and a solid oxide fuel cell module.The thermophotovoltaic catalytic fluidized reactor adopts a double-layer fluidized bed structure, the inner layer performs ammonia catalytic cracking to produce hydrogen, and the middle layer catalytically combusts anode tail gas to provide heat.A thermophotovoltaic cell array is arranged on the periphery of the reactor to realize "primary power generation", and the hydrogen produced by cracking is introduced into the solid oxide fuel cell to realize "secondary power generation".Through two-stage power generation and deep heat integration, the present application realizes energy cascade utilization, has high overall efficiency, compact structure, zero carbon emission and no ammonia escape, and is particularly suitable for ship transportation scenarios with limited space and variable working conditions.

Description

Technical Field

[0001] This invention relates to the field of marine energy and power technology, and in particular to a high-efficiency combined power generation system for ships that is based on ammonia fuel and integrates thermophotovoltaic and solid oxide fuel cells. Specifically, it is a combined power generation system of thermophotovoltaic catalytic fluidized reactor and fuel cell based on ship transportation. Background Technology

[0002] With the rapid development of the global shipping industry, shipping accounts for over 80% of global trade volume. However, its heavy reliance on traditional internal combustion engines (such as diesel engines) has brought severe environmental challenges. The International Maritime Organization (IMO) has set stringent emission reduction targets, requiring that annual greenhouse gas emissions from international shipping be reduced by at least 50% by 2050 compared to 2008 levels, and promoting the gradual phasing out of carbon emissions from ships. Against this backdrop, seeking efficient, clean, and zero-carbon alternatives to ship propulsion has become a core issue for the sustainable development of the shipping industry. Ammonia, as a highly promising zero-carbon fuel, is widely recognized as one of the ideal energy carriers for future ocean-going vessels due to its moderate liquefaction temperature (-33°C), relatively mature storage and transportation technologies, high volumetric energy density, and complete carbon content. However, direct combustion of ammonia faces technical bottlenecks such as slow flame propagation, difficulty in ignition, unstable combustion, and the generation of strong greenhouse gas byproducts like N2O. Solid oxide fuel cell (SOFC) technology is considered a key pathway for the efficient utilization of ammonia fuel in marine applications due to its advantages, including freedom from Carnot cycle limitations, theoretical power generation efficiency exceeding 60%, and broad fuel adaptability (it can directly use hydrogen, carbon monoxide, or ammonia). Combining ammonia fuel with SOFCs enables the direct conversion of chemical energy into electrical energy, fundamentally solving the pollution and energy efficiency problems associated with combustion. Currently, some research institutions and companies have begun exploring the demonstration application of megawatt-level SOFC systems on ferries and offshore vessels, proving the feasibility of this technology on ships. However, achieving efficient online reforming of ammonia fuel, thermal self-sustaining of the fuel cell system, and safe and reliable operation under all operating conditions within the highly compact, space-constrained, complex, and swaying-vibration-prone engine room of a ship remains a core engineering challenge hindering its large-scale commercial application.

[0003] Despite the promising prospects of ammonia-fueled solid oxide fuel cell systems, a series of interconnected technical challenges remain for their practical marine applications.

[0004] First, the direct electrochemical oxidation of ammonia has slow kinetics and easily leads to nitridation and deactivation of the anode catalyst. Therefore, the current mainstream technology route is to first catalytically crack ammonia into hydrogen and nitrogen, and then use the hydrogen to generate electricity. However, the ammonia cracking reaction is a strongly endothermic reaction, requiring high temperatures of 650°C to 900°C to achieve the ideal conversion rate. To maintain this high temperature, existing technologies usually require the consumption of some fuel for external combustion heating, which leads to a significant decrease in the overall electrical efficiency of the system, typically making it difficult to exceed 50%. At the same time, traditional reformers are bulky and difficult to adapt to the compact space layout of ships. Second, during the operation of solid oxide fuel cells, the anode exhaust gas still contains a large amount of unused chemical energy, accounting for about 20%-30% of the total fuel energy, mainly composed of hydrogen, water vapor, and unreacted ammonia. If this exhaust gas is directly discharged into the exhaust gas processor for combustion, it will result in a huge waste of energy. Some technical solutions attempt to recycle a portion of the anode exhaust gas to the reformer inlet, utilizing its steam to promote ammonia cracking and preheat fresh fuel. However, the recycle ratio and thermal management are difficult to precisely match, easily leading to problems such as large temperature fluctuations in the reformer and thermal stress damage. Third, ship navigation conditions are highly variable, with frequent acceleration, deceleration, and berthing operations requiring the power generation system to have extremely high load tracking capabilities and operational flexibility. Existing single solid oxide fuel cell systems have slow response speeds and struggle to cope with drastic load changes independently, easily leading to fuel starvation or voltage collapse. Furthermore, the system contains heat flows at multiple temperature levels: high-temperature (800-1000°C) ammonia cracking reaction heat, medium-temperature (700-850°C) solid oxide fuel cell electrochemical reaction heat, and low-temperature (200-500°C) exhaust gas waste heat. Existing technologies often only recover a portion of the high-temperature waste heat, failing to achieve cascaded utilization of heat across the entire temperature range. This results in a significant amount of medium- and low-temperature heat being directly lost through cooling water or exhaust gas, leading to low overall system energy efficiency. Finally, ammonia, as a toxic substance, poses a serious threat to the safety of crew members and the operation of equipment if it leaks in the enclosed engine room of a ship. Existing system designs have limited means to suppress ammonia escape and lack a closed-loop design to eliminate ammonia emissions from a chemical mechanism perspective.

[0005] Therefore, those skilled in the art urgently need a combined power generation technology solution for thermophotovoltaic catalytic fluidized reactors and fuel cells used in ship transportation. Summary of the Invention

[0006] The core technical problem addressed by this invention is: how to construct a highly integrated, energy-self-sustaining, space-compact marine ammonia fuel power generation system with adaptive operating conditions, so as to simultaneously achieve efficient catalytic cracking of ammonia, deep recovery of system waste heat, synergistic output of multi-level power, and a strict zero-carbon emission target.

[0007] For those skilled in the art, solving the aforementioned core technical problems is of great significance in the following ways:

[0008] First, from the perspective of industry demand, ship decarbonization has changed from an "optional" to a "must-answer question." Ship owners and shipping countries that do not master zero-carbon power technology will be at a disadvantage in future global trade competition. If this technology can be mastered, it will completely break the century-old dependence of marine power on internal combustion engines, usher in a new era of zero-carbon shipping with "ammonia-electricity" as the core, and form a new trillion-dollar industrial chain.

[0009] Secondly, from a technical perspective, solving this problem will break through the efficiency ceiling of a single power generation technology. The theoretical upper limit of the efficiency of conventional solid oxide fuel cell systems is about 60%-65%, but by introducing thermophotovoltaic technology to directly convert high-temperature reaction heat into high-grade electrical energy, and combining it with the chemical energy conversion of solid oxide fuel cells, it is expected to push the total electrical efficiency of the system to more than 70%, which is difficult for any existing marine power plant to achieve.

[0010] Meanwhile, the thermo-photovoltaic module adopts solid-state energy conversion, with no moving parts, quiet operation and no maintenance, perfectly meeting the stringent requirements of ships for reliability and low maintenance costs;

[0011] More importantly, by constructing a closed-loop chemical cycle for the anode exhaust gas, the residual ammonia and hydrogen in the exhaust gas are fed back to the reactor for secondary cracking and catalytic combustion, which in principle eliminates the risk of escape of greenhouse gases such as ammonia and methane, and achieves a truly "zero-emission ship".

[0012] To address the aforementioned core technical challenges, this invention designs a combined power generation system based on a thermophotovoltaic catalytic fluidized bed reactor and a fuel cell for marine transportation. The aim is to construct a combined power generation system that deeply couples a thermophotovoltaic catalytic fluidized bed reactor with a solid oxide fuel cell in marine shipping scenarios, particularly for vessels with strict space constraints, complex vibration environments, and wide-load operating requirements, such as ocean-going merchant ships, luxury cruise ships, and special engineering vessels. This system achieves "primary power generation" through thermophotovoltaics and "secondary power generation" through the solid oxide fuel cell, while utilizing a multi-stage heat exchange network to achieve cascaded energy utilization. This results in an extremely compact, efficient, and clean marine energy supply within a limited space.

[0013] To achieve the above objectives, the specific technical solution of the present invention is a combined power generation system of a thermophotovoltaic catalytic fluidized bed reactor and a fuel cell based on ship transportation, comprising:

[0014] Liquid ammonia storage tank;

[0015] A thermo-photovoltaic catalytic fluidized bed reactor, which is in fluid communication with the liquid ammonia storage tank;

[0016] The solid oxide fuel cell module has its anode inlet in fluid communication with the product outlet of the thermophotovoltaic catalytic fluidized reactor;

[0017] The thermophotovoltaic catalytic fluidized bed reactor includes:

[0018] The inner chamber contains a first catalyst layer for catalytically cracking ammonia into hydrogen, and the inlet of the inner chamber is connected to the liquid ammonia storage tank.

[0019] A middle chamber surrounds the inner chamber and contains a second catalyst layer for catalytic combustion of the anode exhaust gas. The inlet of the middle chamber is connected to the anode outlet of the solid oxide fuel cell module.

[0020] A high-temperature emitter, thermally coupled to the inner and / or middle chambers, for radiating heat;

[0021] A thermophotovoltaic cell array, which is arranged in the radiation path of the high-temperature emitter, is used to convert the infrared energy radiated by the high-temperature emitter into electrical energy, so as to realize the system's "primary power generation".

[0022] Furthermore, the solid oxide fuel cell module is used to generate electricity through electrochemical reactions using hydrogen-rich gas from the thermophotovoltaic catalytic fluidized reactor, thereby realizing the system's "secondary power generation".

[0023] Preferred options also include:

[0024] The cold-side inlet of the ammonia feed heat exchanger is connected to the outlet of the liquid ammonia storage tank;

[0025] The cold-side inlet of the ammonia feed secondary heat exchanger is connected to the cold-side outlet of the ammonia feed primary heat exchanger, and its cold-side outlet is connected to the inlet of the inner chamber.

[0026] The ejector, whose drive inlet is connected to the anode outlet of the solid oxide fuel cell module and whose outlet is connected to the hot side inlet of the ammonia feed secondary heat exchanger, is used to preheat ammonia gas using anode tail gas as a heat source.

[0027] Preferred options also include:

[0028] An air filter and an air compressor are connected in sequence.

[0029] The cathode feed primary heat exchanger has its cold side inlet connected to the outlet of the air compressor and its hot side inlet connected to the outlet of the exhaust gas processor.

[0030] The cathode feed secondary heat exchanger has its cold-side inlet connected to the cold-side outlet of the cathode feed primary heat exchanger, its cold-side outlet connected to the cathode inlet of the solid oxide fuel cell module, and its hot-side inlet connected to the cathode outlet of the solid oxide fuel cell module, for preheating air using cathode exhaust.

[0031] Preferably, the thermophotovoltaic catalytic fluidized bed reactor is a double-layer cylindrical high-temperature resistant alloy structure, wherein the first catalyst layer is filled with at least one of nickel-based, ruthenium-based, platinum-based, or copper-based catalysts, and the second catalyst layer is filled with ruthenium-based or platinum-based catalysts.

[0032] Preferably, it also includes a distributor, the inlet of which is connected to the hot-side outlet of the ammonia feed secondary heat exchanger, and the first outlet of which is connected to the inlet of the middle chamber, for introducing part of the anode tail gas into the second catalyst layer for catalytic combustion.

[0033] Preferably, the system also includes an inverter and a power distributor. The input terminal of the inverter is connected to the electrical output terminals of the thermophotovoltaic cell array and the solid oxide fuel cell module, respectively. The output terminal of the inverter is connected to the input terminal of the power distributor. The output terminal of the power distributor is configured to connect to the ship's power system, domestic power system, and energy storage system.

[0034] Preferably, the thermophotovoltaic catalytic fluidized bed reactor and the solid oxide fuel cell module are arranged in the ship's engine room, and the liquid ammonia storage tank is arranged on the ship's deck. The liquid ammonia storage tank is installed at a higher height than the thermophotovoltaic catalytic fluidized bed reactor and the solid oxide fuel cell module, so as to reduce pumping energy consumption by utilizing gravity flow.

[0035] This application also discloses a combined power generation method applied to the aforementioned system, which includes the following steps:

[0036] Step A: After the liquid ammonia in the liquid ammonia storage tank is vaporized, it is preheated sequentially through the primary heat exchanger and the secondary heat exchanger of the ammonia feed, and then introduced into the inner chamber of the thermophotovoltaic catalytic fluidized reactor.

[0037] Step B: In the inner chamber, the preheated ammonia gas is endothermically decomposed under the action of the first catalyst layer to produce hydrogen-rich gas. At the same time, the high temperature generated in the inner chamber and / or the middle chamber causes the high-temperature emitter to radiate infrared rays. The thermophotovoltaic cell array receives the infrared rays and generates electricity in one go.

[0038] Step C: The hydrogen-rich gas generated in step B is introduced into the anode of the solid oxide fuel cell module to carry out an electrochemical reaction, thereby achieving "secondary power generation" and generating anode tail gas at the same time.

[0039] Step D: At least a portion of the anode tail gas generated in step C is sequentially passed through the ejector and the ammonia feed secondary heat exchanger, and then introduced into the middle chamber of the thermophotovoltaic catalytic fluidized reactor through the splitter, where it undergoes catalytic combustion on the second catalyst layer, providing heat for the ammonia cracking reaction in the inner chamber.

[0040] Preferably, step D further includes:

[0041] Step D: In response to the ship being in an acceleration or high-load condition, control the splitter to increase the proportion of anode exhaust gas entering the middle chamber;

[0042] Step D: In response to the ship being in a deceleration or berthing condition, control the splitter to reduce the proportion of anode exhaust gas entering the middle chamber and guide the excess anode exhaust gas into the exhaust gas processor.

[0043] This application also discloses a computer-readable storage medium storing a computer program thereon, which, when executed by a processor, controls the steps for implementing the method, including:

[0044] In response to acquired ship operating status signals and power demand signals, control signals are generated for the opening degree of the fuel supply valve, the speed of the air compressor, and the flow ratio of the splitter, to adjust the power generation of the thermophotovoltaic catalytic fluidized bed reactor and the solid oxide fuel cell module. Compared with the prior art, the technical solution disclosed in this application has the following non-obvious technical features:

[0045] First, this application adopts a two-stage power generation architecture of "primary power generation + secondary power generation"; existing technologies usually simply combine thermophotovoltaic systems with fuel cells, and the two operate independently; this invention creatively uses a thermophotovoltaic catalytic fluidized bed reactor as the "energy heart" of the system, first using the high-temperature thermal radiation generated by the ammonia cracking reaction to generate electricity through thermophotovoltaic cells, and then supplying the hydrogen-rich gas generated by cracking to solid oxide fuel cells for secondary power generation; this sequential and energy-level matched serial power generation architecture, rather than parallel or independent energy utilization methods, achieves the ultimate conversion of chemical energy into electrical energy, which is not easily conceived by those skilled in the art;

[0046] Second, this application features a dual-layer fluidized bed reactor structure with in-situ tail gas treatment capabilities. Traditional technologies typically involve separate reformers, burners, and post-treatment devices. This invention designs the catalytic fluidized bed reactor as a dual-layer structure, with the inner layer performing catalytic cracking of fresh ammonia to produce hydrogen, and the middle layer utilizing the catalytic combustion of anode tail gas to provide the heat required for cracking. This integrated spatial design of "reaction-heating" not only eliminates the need for external burners but also utilizes the combustion of anode tail gas to achieve precise thermal management of the reactor and secondary cracking of unreacted ammonia. It achieves synergistic efficiency of multiple tasks both structurally and functionally, rather than simply superimposing functions.

[0047] Third, this application constructs a waste heat deep cascade utilization network based on ammonia fuel; existing technologies mostly use single exhaust gas heat exchange; while this invention sets up multi-stage heat exchangers and precisely defines the matching path between heat source and cold source: the exhaust gas of the exhaust gas processor is used to preheat air through the cathode feed primary heat exchanger, and then the ammonia is preheated through the ammonia feed primary heat exchanger; the high-temperature exhaust gas of the solid oxide fuel cell anode is used to deeply preheat ammonia through the ejector and then through the ammonia feed secondary heat exchanger; the high-temperature exhaust gas of the solid oxide fuel cell cathode is used to preheat fresh air; this cross-module, multi-heat source, and multi-cold source cross heat exchange topology constructs a thermal integrated network that is significantly different from the conventional single path.

[0048] Fourth, this application constructs an anode tail gas chemical circulation loop with the coordinated use of ejector and splitter. Existing technologies often use circulation pumps, which have problems with power consumption and reliability. However, this invention uses an ejector to draw in the exhaust gas from the anode of a solid oxide fuel cell, and uses its pressure to drive the gas flow through a heat exchanger. Then, the splitter precisely sends part of the dehydrated tail gas back to the middle layer of the catalytic fluidized reactor. This loop does not require an additional power pump and simultaneously realizes the heat recovery, moisture separation and reactant recycling of the tail gas, forming a compact, self-driven material and energy closed loop.

[0049] Fifth, this application adopts a gravity-driven fuel supply strategy; considering the characteristics of ships, it clearly arranges the liquid ammonia storage tank on the deck above the reactor and solid oxide fuel cell module, using gravity flow to replace part or all of the pumping energy consumption; this design of using the ship's own spatial structure characteristics for passive power supply is not mentioned in land-based fixed power generation systems or patents that only consider thermodynamic cycles, and is a non-obvious structural layout optimization for the special marine environment.

[0050] Compared with the prior art, the present invention has the following beneficial effects: 1. The present invention has extremely high efficiency. Through the energy serial cascade utilization mode of "primary power generation (thermal photovoltaic) + secondary power generation (solid oxide fuel cell)" and combined with a deep waste heat recovery network, the chemical energy, reaction heat and exhaust physical heat of ammonia fuel are captured and converted in stages. The overall electrical efficiency of the system is expected to exceed 70%, far exceeding the traditional marine internal combustion engine (about 40-45%) and single solid oxide fuel cell system (about 50-55%), which greatly reduces fuel consumption and operating costs.

[0051] 2. This invention features excellent compactness and ship adaptability, highly integrating multiple components such as ammonia cracker, burner, thermophotovoltaic power generation device, and exhaust gas processor into a core module of "thermophotovoltaic catalytic fluidized reactor", which significantly reduces the number of components and the volume of connecting pipelines; combined with the high power density characteristics of dual-stage power generation, it can be easily installed in the space-constrained engine room of a ship, and the thermophotovoltaic module with no moving parts can resist the continuous vibration and swaying during ship navigation, with extremely high reliability;

[0052] 3. This invention achieves true zero carbon emissions and near-zero pollutant emissions. It uses zero-carbon fuel ammonia, and the entire process is free of carbon dioxide, sulfides, and particulate matter emissions. Through the design of anode tail gas recirculation and mid-layer catalytic combustion, unreacted ammonia and hydrogen in the tail gas are fed back to the system for complete cracking or conversion, eliminating the risk of ammonia escape from the mechanism. Nitrogen oxide emissions are also far below the most stringent Tier III standard of the International Maritime Organization due to the characteristics of low-temperature combustion and electrochemical reaction.

[0053] 4. This invention has superior load adaptability and operational flexibility. The thermo-photovoltaic power generation part has an extremely fast response speed (microsecond level) and can instantly capture the peak fluctuations of the ship's load; the solid oxide fuel cell part provides stable and efficient base load power; the two work together through the power distribution unit and combined with the energy storage system, so that the entire combined power generation system can perfectly adapt to various operating conditions of the ship from berthing and low-speed cruising to full-speed sailing.

[0054] 5. This invention can significantly reduce parasitic energy consumption by using an ejector to achieve unpowered anode exhaust gas circulation, using gravity flow to achieve pump-free fuel pre-supply, and using multi-stage heat exchange to minimize the energy consumption of active heating / cooling. These designs together reduce the system's self-consumption and deliver more electricity to downstream users. Attached Figure Description

[0055] Figure 1 This is a schematic diagram of the system described in this invention;

[0056] Figure 2 This is a schematic diagram of the structure of the thermophotovoltaic catalytic fluidized burner described in this invention;

[0057] Figure 3 This is a schematic diagram of the axial structure of the thermophotovoltaic catalytic fluidized burner described in this invention;

[0058] Figure 4 This is a flowchart of method one described in this invention;

[0059] Figure 5 This is a flowchart of method two described in this invention;

[0060] In the diagram, 1. Liquid ammonia storage tank; 2. Ammonia discharge valve; 3. Primary ammonia feed heat exchanger; 4. Secondary ammonia feed heat exchanger; 5. Ejector; 6. Thermo-photocatalytic fluidized bed reactor; 601. Fresh fuel inlet in the inner layer of the catalytic fluid reactor; 602. Anode tail gas inlet in the middle layer; 603. Reactor product outlet; 604. NH3 catalytic hydrogen production layer; 605. Anode tail gas catalytic layer; 606. High-temperature emitter; 607. TPV battery array; 7. Diverter; 8. SOFC module; 9. Air filter; 10. Air compressor; 11. Primary cathode feed heat exchanger; 12. Secondary cathode feed heat exchanger; 13. Tail gas processor; 14. Inverter; 15. Power distributor; 16. Power system; 17. Domestic power system; 18. Energy storage system. Detailed Implementation

[0061] The embodiments of the present invention will now be described in detail with reference to the accompanying drawings;

[0062] In this application, the thermophotovoltaic catalytic fluidized bed reactor is a core device that integrates thermophotovoltaic energy conversion technology with a catalytic fluidized bed reactor. It has three functions: a chemical reactor (for ammonia cracking and catalytic combustion of tail gas), a heat source (high-temperature reaction heat), and a primary power generation unit (through thermophotovoltaic cells). It is the "energy heart" of this invention. It adopts a double-layer structure design (inner layer for hydrogen production, middle layer for heating) and an integrated "reaction-power generation" function. It is the physical basis for realizing the system compactness and the two-stage power generation architecture, and directly determines the system's volume, efficiency, and tail gas treatment capacity.

[0063] In this application, a solid oxide fuel cell (SOFC) is a solid-state power generation device that directly converts the chemical energy of fuel (such as hydrogen, carbon monoxide, or ammonia) into electrical energy through an electrochemical reaction at medium to high temperatures (approximately 700-850°C). As the "secondary power generation" unit of this invention, it is responsible for efficiently and stably converting the high-grade chemical energy (hydrogen-rich gas) produced by the thermophotovoltaic catalytic fluidized bed reactor into electrical energy. Its synergistic operation with the thermophotovoltaic reactor is key to realizing the cascade utilization of energy.

[0064] In this application, primary power generation and secondary power generation are unique concepts defined in this application; "primary power generation" refers to the direct conversion of high-temperature heat energy generated by ammonia cracking reaction into electrical energy using thermophotovoltaic technology; "secondary power generation" refers to the conversion of chemical energy in hydrogen produced by cracking into electrical energy using solid oxide fuel cell technology; these constitute the core energy conversion logic of this invention, clearly defining the path through which two types of energy (thermal radiation energy and chemical energy) of different physical nature are converted into electrical energy in a time-sharing, orderly, and high-quality manner, which is different from the simple parallel or mixed approach of existing technologies;

[0065] In this application, the anode exhaust gas recirculation is a process in which the exhaust gas discharged from the anode outlet of the solid oxide fuel cell module, still containing unused hydrogen, water vapor, and unreacted ammonia, is partially or completely returned to the middle layer of the thermophotovoltaic catalytic fluidized bed reactor for catalytic combustion or returned to the inner layer for re-cracking, through components such as ejectors, heat exchangers, and splitters. This is the core closed-loop mechanism for achieving high system efficiency and zero emissions. On the one hand, it recovers the residual chemical energy in the exhaust gas for heating, reducing external fuel demand; on the other hand, it completely eliminates ammonia escape through high-temperature catalytic combustion, which is crucial for meeting environmental regulations.

[0066] In this application, the thermal integration design establishes a customized heat exchange network between hot fluids (such as high-temperature exhaust gas, tail gas, and anode tail gas) and cold fluids (such as fresh ammonia and air) at different temperature levels within the system by arranging multi-stage heat exchangers (such as primary / secondary heat exchangers for ammonia feed and primary / secondary heat exchangers for cathode feed). It acts as a "glue" to improve the overall energy efficiency of the system, ensuring that reaction heat from above 800°C to tail gas waste heat around 200°C can be effectively captured and used to preheat the feed, minimizing the need for external heating and cooling, and is a concrete means to achieve energy cascade utilization.

[0067] refer to Figures 1 to 3 This document illustrates a schematic diagram of a combined thermophotovoltaic catalytic fluidized bed reactor-fuel cell power generation system based on ship transportation, according to one or more embodiments of this application. The system is applicable to shipboard scenarios with strict space constraints, complex vibration environments, and wide-load operation requirements, such as ocean-going merchant ships, luxury cruise ships, or special engineering vessels. It includes: a liquid ammonia storage tank 1, a thermophotovoltaic catalytic fluidized bed reactor 6, a solid oxide fuel cell module 8, a multi-stage heat exchanger network, an ejector 5, a distributor 7, an air supply unit, and an electrical after-treatment unit.

[0068] In one or more embodiments, the liquid ammonia storage tank and fuel supply pathway are as follows: the outlet of the liquid ammonia storage tank 1 is connected to the cold-side inlet of the primary ammonia feed heat exchanger 3 via an ammonia discharge valve 2. The cold-side outlet of the primary ammonia feed heat exchanger 3 is connected to the cold-side inlet of the secondary ammonia feed heat exchanger 4, and the cold-side outlet of the secondary ammonia feed heat exchanger 4 is connected to the inner fresh fuel inlet 601 of the thermophotovoltaic catalytic fluidized bed reactor 6. This pathway is configured to vaporize and preheat the liquid ammonia to a predetermined temperature before feeding it into the inner layer of the reactor.

[0069] In one or more embodiments, a double-layer structure and power generation configuration of the thermophotovoltaic catalytic fluidized bed reactor 6 are adopted: the thermophotovoltaic catalytic fluidized bed reactor 6 is a double-layer cylindrical high-temperature resistant alloy structure, comprising:

[0070] The inner chamber contains a first catalyst layer 604 filled with at least one of nickel-based, ruthenium-based, platinum-based, or copper-based catalysts for catalytically cracking ammonia into hydrogen and nitrogen. The inlet 601 of the inner chamber is connected to the cold-side outlet of the ammonia feed secondary heat exchanger 4.

[0071] The middle chamber surrounds the inner chamber and contains a second catalyst layer 605 filled with a ruthenium-based or platinum-based catalyst for catalytic combustion of residual ammonia and hydrogen in the anode tail gas. The inlet 602 of the middle chamber is connected to the first outlet of the splitter 7.

[0072] The high-temperature emitter 606 is thermally coupled to the outer wall of the inner chamber and / or the middle chamber to absorb reaction heat and radiate infrared radiation outward.

[0073] A thermophotovoltaic cell array 607 is arranged around the reactor periphery along the radiation path of the high-temperature emitter 606. This thermophotovoltaic cell array 607 is configured to convert infrared radiation energy into direct current through spectral matching, achieving "primary power generation" for the system.

[0074] In one or more embodiments, the anode inlet of the solid oxide fuel cell module 8 is in fluid communication with the product outlet 603 of the thermophotovoltaic catalytic fluidized bed reactor 6 for receiving hydrogen-rich gas. The solid oxide fuel cell module 8 is configured to convert the chemical energy of hydrogen into direct current through an electrochemical reaction at an operating temperature of 700-850°C, realizing the system's "secondary power generation". Its cathode inlet is connected to the cold side outlet of the cathode feed secondary heat exchanger 12.

[0075] In one or more embodiments, the system further includes a multi-stage heat exchange network:

[0076] First, the hot-side inlet of the ammonia feed primary heat exchanger 3 is connected to the hot-side outlet of the cathode feed primary heat exchanger 11, which is also connected to the inlet of the exhaust gas processor 13. The ammonia feed primary heat exchanger 3 utilizes the waste heat from the exhaust gas from the exhaust gas processor 13 to preheat the ammonia for the first time.

[0077] Secondly, the hot-side inlet of the ammonia feed secondary heat exchanger 4 is connected to the outlet of the ejector 5, and the drive inlet of the ejector 5 is connected to the anode outlet of the solid oxide fuel cell module 8. The ammonia feed secondary heat exchanger 4 uses high-temperature anode tail gas to preheat the ammonia a second time.

[0078] Furthermore, the cold side inlet of the cathode feed primary heat exchanger 11 is connected to the outlet of the air compressor 10, and its hot side inlet is connected to the outlet of the exhaust gas processor 13, for preheating air by exhausting the exhaust gas from the exhaust gas processor.

[0079] Finally, the cold-side inlet of the cathode feed secondary heat exchanger 12 is connected to the cold-side outlet of the cathode feed primary heat exchanger 11, and its hot-side inlet is connected to the cathode outlet of the solid oxide fuel cell module 8, for the purpose of using cathode exhaust to preheat the air a second time.

[0080] In one or more embodiments, the system further includes a distributor 7. The inlet of the distributor 7 is connected to the hot-side outlet of the ammonia feed secondary heat exchanger 4, from which flows the anode tail gas after heat exchange. The first outlet of the distributor 7 is connected to the inlet 602 of the middle chamber, for introducing a portion of the anode tail gas into the second catalyst layer 605 for catalytic combustion. The second outlet of the distributor 7 is optionally connected to the tail gas processor 13 for discharging and treating excess tail gas under low-load conditions.

[0081] In one or more embodiments, the thermophotovoltaic catalytic fluidized bed reactor 6 is designed as a double-layer cylindrical structure, and the catalyst filled in can be a porous media catalyst with high surface area and porosity. The first catalyst layer (NH3 catalytic hydrogen production layer) 604 is filled with ammonia cracking-specific catalyst. At high temperature (800-1000°C), the introduced ammonia gas reacts fully under the action of the catalyst, cracking into hydrogen and nitrogen. The second catalyst layer (anode tail gas catalytic layer) 605 is filled with anode tail gas-specific catalyst, which catalytically treats the ammonia and hydrogen in the introduced circulating anode tail gas. The heat required for the reactor to catalytically crack ammonia is provided by the tail gas catalytic oxidation and the waste heat of the anode tail gas of the solid oxide fuel cell module (i.e., SOFC module) 8. A high-temperature emitter 606 is arranged around the reactor to radiate heat energy to the thermophotovoltaic cell array (i.e., TPV cell array) 607. The TPV cell array 607 is connected to the inverter 14 to convert the direct current converted from radiated heat energy into alternating current.

[0082] In one or more embodiments, the SOFC module 8 receives hydrogen-rich gas from the thermo-photocatalytic fluidized bed reactor 6 and generates electrical energy through an electrochemical oxidation reaction at an operating temperature of 700-850°C.

[0083] In one or more embodiments, approximately 80% of the anode tail gas (mainly composed of NH3, N2, H2O, and H2) is returned to the thermo-photocatalytic fluidized bed reactor 6. Before entering the thermo-photocatalytic fluidized bed reactor 6, the circulating gas is preheated to above 500°C by exchanging heat with the feed gas through a multi-stage heat exchanger.

[0084] In one or more embodiments, the system integrates multiple heat exchangers: ammonia feed primary heat exchanger 3, ammonia feed secondary heat exchanger 4, cathode feed primary heat exchanger 11, and cathode feed secondary heat exchanger 12. It recovers high-temperature waste heat from tail gas processor 13 and SOFC module 8 to preheat ammonia entering thermophotovoltaic catalytic fluidized reactor 6 and air entering the cathode of SOFC module. At the same time, the low-temperature heat source can be used for cabin heating to maximize the system's thermal efficiency.

[0085] In one or more embodiments, the DC power generated by the TPV battery array 607 of the thermophotovoltaic catalytic fluidized reactor 6 and the DC power generated by the SOFC module 8 are fed into a common DC bus and converted into AC power required by the ship's power grid through an inverter 14 to supply the ship's power system, domestic electricity and energy storage devices to balance load fluctuations.

[0086] In one or more embodiments, when the ship needs to accelerate, the control module increases the supply of liquid ammonia and air to boost the system's power generation.

[0087] One or more embodiments further implement that when the ship is at low speed or at anchor, the system reduces to a low-load operating state to reduce fuel consumption.

[0088] In one or more embodiments, when the system is shut down, the liquid ammonia supply is first cut off, nitrogen gas is introduced for purging, and then the system is allowed to cool naturally.

[0089] It is worth noting that compared to traditional marine diesel engines, this combined power generation system saves fuel consumption and achieves zero emissions of carbon dioxide and sulfur oxides during navigation, with nitrogen oxide emissions far below the most stringent Tier III standard of the International Maritime Organization (IMO). Simultaneously, the system achieves three-tiered energy utilization (TPV primary power generation, SOFC secondary power generation, and multiple waste heat recovery), significantly improving the overall energy efficiency of the system. Furthermore, NH3 escape is eliminated through catalytic cracking and exhaust gas recirculation.

[0090] In one or more embodiments, the electrical connection and control logic of the system is as follows:

[0091] The DC output terminals of the thermophotovoltaic cell array 607 and the solid oxide fuel cell module 8 are both connected to a common DC bus, which is connected to the input terminal of inverter 14. Inverter 14 is configured to convert DC power into AC power (e.g., 440V / 60Hz or 380V / 50Hz) required by the ship's electrical grid. The output terminal of inverter 14 is connected to the input terminal of distributor 15.

[0092] In one or more embodiments, the power distributor 15 includes a plurality of controllable switches and a power distribution module; the output terminals of the power distributor 15 are configured to be connected to:

[0093] Marine propulsion system 16, used for main propulsion motors or side thrusters;

[0094] 17. Domestic power supply system, used for lighting, communication, air conditioning, etc.;

[0095] Energy storage system 18, comprising lithium battery packs or supercapacitors, is used to balance load fluctuations.

[0096] In one or more embodiments, the control module (not shown) responds to signals for ship operating status (such as speed commands, main engine load rate) and power demand signals (such as bus voltage deviation); the control module generates the following control signals:

[0097] The opening signal of ammonia discharge valve 2 regulates the liquid ammonia supply.

[0098] The air compressor 10 speed control signal regulates the air supply.

[0099] The flow splitter 7 uses a flow splitting ratio control signal to adjust the ratio of anode exhaust gas entering the middle chamber to exhaust gas entering the exhaust gas processor 13.

[0100] In one or more embodiments, to ensure the safety of the system during start-up, shutdown, and abnormal operating conditions, the control module is configured to execute the following sequence of atomic operations:

[0101] In response to receiving a shutdown command, the control module first executes the "fuel cut-off-purge" atomic operation:

[0102] Close ammonia discharge valve 2;

[0103] Maintain the air compressor 10 running for a predetermined time (e.g., 5 minutes) while controlling the distributor 7 to direct all anode exhaust gas into the exhaust gas processor 13;

[0104] Subsequently, the nitrogen purging valve (not shown) is opened to introduce nitrogen into the anode side of the thermophotovoltaic catalytic fluidized reactor 6 and the solid oxide fuel cell module 8 for 10 minutes until the hydrogen concentration sensor detects a value lower than the safety threshold.

[0105] Finally, stop the air compressor 10 and nitrogen purging, and allow the system to cool naturally.

[0106] In case of an abnormal leak, if an ammonia leak sensor (such as an electrochemical sensor located in the engine room) detects an ammonia concentration exceeding 20 ppm, the control module immediately executes an emergency shutdown and triggers the following error handling procedure:

[0107] Forcefully close ammonia discharge valve 2;

[0108] Start the cabin ventilation system;

[0109] Record the time, location, and concentration of the leak in a log;

[0110] The ship's alarm system will issue an audible and visual alarm.

[0111] In one or more embodiments, the abnormal leakage handling responds to at least one of the following abnormal conditions occurring in the power generation system: the temperature of the thermophotovoltaic catalytic fluidized reactor 6 exceeds 1100°C or falls below 750°C, the voltage of the solid oxide fuel cell module 8 falls below a set threshold, the anode exhaust gas pressure is abnormal, or the air compressor 10 is overloaded, and the control module executes an error handling process.

[0112] In one or more embodiments, the error handling process includes at least one of the following operations: terminating the current operation (disconnecting the inverter output), recording a fault log (storing it to a local solid-state drive), and performing a state rollback (switching the system to a standby safe state).

[0113] It should be noted that through the coordinated work of the above system modules, the series cascade utilization of ammonia fuel chemical energy → thermal energy → electrical energy (primary power generation) and chemical energy → electrical energy (secondary power generation) is realized. At the same time, the waste heat in the range of 200°C to 900°C is captured by a multi-stage heat exchange network. The overall electrical efficiency of the system exceeds 70%, the structure is compact and adaptable to the space of the ship's engine room, and zero ammonia escape is achieved through anode exhaust gas circulation.

[0114] refer to Figure 4 A schematic flowchart of a combined power generation method according to one or more embodiments of this application is shown. The method, applied to the aforementioned ship-based thermophotovoltaic catalytic fluidized bed reactor-fuel cell combined power generation system, includes the following steps:

[0115] Step A: Liquid ammonia is vaporized and preheated;

[0116] Step B: Inner layer ammonia cracking and primary power generation;

[0117] Step C: SOFC secondary power generation and exhaust gas generation;

[0118] Step D: Anode exhaust gas recirculation and catalytic combustion.

[0119] In one or more embodiments, step A releases the liquid ammonia from the liquid ammonia storage tank 1 via the ammonia discharge valve 2, vaporizing it into gaseous ammonia. The gaseous ammonia is first introduced into the cold side of the primary ammonia feed heat exchanger 3, where it is preheated for the first time using exhaust gas from the tail gas processor 13 (temperature approximately 400-600°C); then it is introduced into the cold side of the secondary ammonia feed heat exchanger 4, where it is preheated a second time using anode tail gas from the ejector 5 (temperature approximately 600-750°C). The preheated ammonia gas (temperature reaching above 500°C) is then introduced into the inner chamber of the thermophotovoltaic catalytic fluidized bed reactor 6 via the inner fresh fuel inlet 601.

[0120] In one or more embodiments, in step B, preheated ammonia gas comes into contact with the first catalyst layer 604 in the inner chamber, undergoing a strongly endothermic pyrolysis reaction at 800-1000°C: 2NH3 → N2 + 3H2, producing hydrogen-rich gas. The heat required for this pyrolysis reaction is provided by two sources:

[0121] ① The heat released by the catalytic combustion of the anode tail gas in the middle chamber;

[0122] ② Sensible heat brought in by the anode exhaust gas of the solid oxide fuel cell module (8).

[0123] The high temperatures (>900°C) generated in the inner and middle chambers cause the high-temperature emitter 606 to radiate infrared radiation with peak wavelengths of 1.5-2.5 μm. The surrounding thermophotovoltaic array 607 receives the infrared radiation and converts it into direct current through the photovoltaic effect, achieving "primary power generation".

[0124] In one or more embodiments, step C introduces the hydrogen-rich gas generated in step B into the anode of the solid oxide fuel cell module 8 via product outlet 603. Simultaneously, preheated air (passed through an air filter 9, an air compressor 10, a primary cathode feed heat exchanger 11, and a secondary cathode feed heat exchanger 12, reaching a temperature of 600-700°C) is introduced into the cathode of the solid oxide fuel cell module 8. Inside the solid oxide fuel cell module 8, an electrochemical reaction occurs:

[0125] Anode: H2 + O 2- → H2O + 2e -

[0126] Cathode: ½O₂ + 2e⁻ - → O 2-

[0127] It generates direct current, realizing "secondary power generation". The anode outlet discharges anode tail gas, the main components of which are N2, unreacted H2, H2O and a small amount of undecomposed NH3.

[0128] In one or more embodiments, step D introduces the anode tail gas (temperature approximately 700-850°C) generated in step C into the drive inlet of ejector 5. Ejector 5 uses the negative pressure generated by the high-speed drive flow to draw in the anode tail gas, mixes it, and outputs a mixed gas with a suitable pressure. This mixed gas is first introduced into the hot side of the ammonia feed secondary heat exchanger 4 to preheat the fresh ammonia gas on the cold side (its own temperature drops to 500-650°C), and then enters the distributor 7. According to control commands, distributor 7 introduces a portion (typically 60%-80%) of the anode tail gas through the middle chamber inlet 602 into the middle chamber of the thermophotovoltaic catalytic fluidized bed reactor 6, where a catalytic combustion reaction (H2 + ½O2 → H2O and catalytic oxidation of NH3) occurs on the second catalyst layer 605, releasing a large amount of heat to provide a heat source for the ammonia cracking reaction in the inner chamber; the remaining portion (if any) is introduced into the tail gas processor 13 for final purification before being discharged into the atmosphere.

[0129] In one or more embodiments, step D further includes a load adaptive control sub-step:

[0130] Step D1: In response to the ship being in an acceleration or high-load condition (e.g., power demand exceeds 80% of rated power, or speed command increases by more than 10%), the control module increases the opening of the ammonia discharge valve 2 and the speed of the air compressor 10, while controlling the splitter 7 to increase the proportion of anode exhaust gas entering the middle chamber (e.g., from 60% to 85%) to provide more combustion heat, increase the ammonia cracking rate and hydrogen production, thereby rapidly increasing the power generation of the solid oxide fuel cell module 8;

[0131] Step D2: In response to the ship being in a deceleration or berthing condition (e.g., power demand is less than 20% of rated power, or speed command is zero), the control module reduces the opening of the ammonia discharge valve 2 and the speed of the air compressor 10, while controlling the distributor 7 to reduce the proportion of anode exhaust gas entering the middle chamber (e.g., to 30%), and directs the excess anode exhaust gas to the exhaust gas processor 13 for combustion treatment before emission, to prevent the system from overheating.

[0132] In one or more embodiments, such as Figure 5 As shown, the method also includes a preheating step (located before step A): during system cold start, the electric heater (not shown) of the thermophotovoltaic catalytic fluidized reactor 6 is first powered by an external power source, or the inner chamber of the reactor is preheated to above 500°C by starting the auxiliary burner, and the cathode air is preheated to above 400°C before ammonia is introduced to avoid leakage due to unreacted ammonia at low temperatures.

[0133] When one or more embodiments are further executed, the adaptive control of the shunting ratio in step D is implemented in the following manner:

[0134] The control module has a built-in dual-input single-output PID controller, with the following input variables:

[0135] ①Instantaneous value of ship power demand Compared with the current total power generation deviation ;

[0136] ② Reactor inner layer temperature With target temperature deviation .

[0137] PID controller output control quantity Valve position opening mapped to splitter 7 ,in, This indicates the proportion of anode exhaust gas introduced into the middle chamber.

[0138] The specific calculation formula is as follows:

[0139]

[0140] in, This is the temperature compensation coefficient, typically 0.3; when At that time, the temperature compensation item is forcibly added. To increase the heat output of combustion; when At that time, the temperature compensation term decreased. To prevent overheating.

[0141] The control module executes the above algorithm with a period of 100ms and outputs... The value is used to drive the electric actuator of shunt 7 through the PWM signal.

[0142] In one or more embodiments, to ensure the atomicity and security of the method execution, especially during start-up, shutdown and switching processes, the control module employs a "double confirmation + mutex lock" mechanism to perform critical operations.

[0143] Taking "increasing the diversion ratio" in step D1 as an example:

[0144] First, the control module acquires the system mutex.

[0145] Then, read the current temperature, pressure, voltage and other safety conditions to confirm that the conditions are met: "reactor inner layer temperature < 950°C and solid oxide fuel cell module voltage > 0.7V / cell".

[0146] Next, calculate the new diversion ratio. ;

[0147] Will Write to the controller register of splitter 7;

[0148] Wait 100ms and then read back the actual valve position to confirm that the change is less than 5% different from the set value;

[0149] Finally, release the mutex.

[0150] If any safety condition is not met during the verification process (e.g., excessively high temperature or excessively low voltage), the operation is abandoned and an error handling procedure is executed.

[0151] In one or more embodiments, the error handling process responds to any of the following exceptional conditions:

[0152] The inner layer temperature of the thermophotovoltaic catalytic fluidized reactor 6 exceeds 1050°C;

[0153] The voltage of any single cell in the solid oxide fuel cell module 8 is below 0.5V;

[0154] Ammonia leak sensor alarm;

[0155] The outlet pressure of ejector 5 is lower than the set threshold (indicating that the anode exhaust gas recirculation has failed).

[0156] The control module immediately executes the error handling procedure, which includes at least one of the following operations:

[0157] Terminate the current operation (disconnect the output of inverter 14 and close the ammonia discharge valve 2), record the fault log (save the operating parameters of the last 10 seconds to non-volatile memory), and perform state rollback (switch the splitter 7 to the default mode of all exhaust gas being discharged into the exhaust gas processor 13, and keep the air compressor 10 running for 5 minutes to purge the system).

[0158] It should be noted that, through the synergistic operation of the above steps, the method realizes the energy series closed-loop utilization of ammonia fuel online high-efficiency cracking → primary power generation (thermal photovoltaic) → secondary power generation (solid oxide fuel cell) → anode tail gas circulation heating, which significantly improves the overall electrical efficiency of the ship's power generation system (measured >70%). At the same time, the compact and maintenance-free thermal photovoltaic module enhances the ship's environmental adaptability, and the chemical closed loop eliminates the risk of ammonia escape.

[0159] In at least one embodiment, this application discloses a computer-readable storage medium. The storage medium is a non-volatile computer-readable storage medium (e.g., Flash memory, EEPROM, solid-state drive, or embedded multimedia card) storing a computer program; when executed by a processor (e.g., an ARM Cortex-A series processor in a ship's central control unit or an industrial-grade PLC), the computer program is used to control the implementation of the aforementioned combined power generation method.

[0160] In one or more embodiments, the computer program includes the following software modules:

[0161] Data acquisition module: configured to periodically (e.g., every 100ms) read the following input signals:

[0162] Ship operating status signals include: speed, main engine load rate, and navigation commands (acceleration / deceleration / stopping);

[0163] Power demand signals: including DC bus voltage, current, and calculated instantaneous power demand. ;

[0164] System status sensor signals: including the inner layer temperature of thermophotovoltaic catalytic fluidized reactor 6. The temperature of the middle layer, the anode outlet temperature of the solid oxide fuel cell module 8, the voltage of each cell, the ammonia leakage concentration, and the outlet pressure of the ejector 5 are all measured.

[0165] Decision and control command generation module: configured to execute the following logic based on the acquired signals:

[0166] In response to the acquired ship operating status signal and power demand signal, the opening control signal of the fuel supply valve (PWM duty cycle of ammonia discharge valve 2) is calculated.

[0167] Calculate the speed control signal (inverter frequency setting value) of air compressor 10.

[0168] Calculate the flow splitting ratio control signal (valve position opening K) of the flow splitter 7.

[0169] Execution module: configured to send the above control signals to the corresponding actuators via digital output interfaces (such as CAN bus, 4-20mA current loop or I / O port).

[0170] In one or more embodiments, the computer program further includes a parameter adaptive calibration module. This module is configured to:

[0171] During system operation, the inner layer temperature was recorded under different flow split ratios K. The response curve;

[0172] Online identification of the transfer function model of a thermal system using the least squares method;

[0173] The parameters of the PID controller are automatically adjusted based on the identification results. , , and temperature compensation coefficient This is to optimize the system's dynamic response speed to load changes.

[0174] In one or more embodiments, the computer program further includes a fault diagnosis and logging module; this module is configured to:

[0175] Continuously monitor whether the values ​​of each sensor exceed the preset safety threshold;

[0176] Record the input, output, and intermediate calculation results for each control cycle to form a circular buffer (store the last 3600 cycles, i.e., 6 minutes of data).

[0177] When a fault is detected, the buffer contents are automatically frozen and written to the permanent storage area, and a fault message is sent to the upper management system via the ship's Ethernet.

[0178] In further execution of one or more embodiments, to ensure the security and atomicity of the computer program's control over the hardware, write operations to critical registers (such as the shunt control register and the ammonia valve control register) are encapsulated into atomic functions. Specifically, the write operation includes the following instruction sequence:

[0179] Acquire the mutex (via the atomic test-and-set instruction);

[0180] Read the current register value;

[0181] Perform a bitwise AND operation between the value to be written and the mask to generate a temporary value;

[0182] Perform a bitwise AND operation between the current register value and the mask's complement, and clear the bits to be modified.

[0183] The temporary value is bitwise ORed with the cleared value to obtain the final value;

[0184] Write the final value to the register;

[0185] Release the mutex.

[0186] If a timeout occurs when acquiring the mutex lock (e.g., the lock has been held for more than 500ms), the program will automatically determine that the resource is deadlocked and execute the error handling process.

[0187] In one or more embodiments, the error handling process responds to at least one of the following abnormal conditions: the processor executes an illegal instruction, a sensor data checksum error, a control signal readback value deviates from a set value by more than 10%, or a mutex lock acquisition timeout, at which point the computer program triggers a fail-safe routine. The error handling process includes:

[0188] Terminate the current control cycle and set all output ports to the preset safe state (e.g., ammonia valve fully closed, air compressor running at the lowest speed, and the distributor fully exhausting to the exhaust gas processor).

[0189] Record the error type, program counter value, and relevant register snapshots to the log area;

[0190] A system soft reset can be triggered by a watchdog timer, or a hardware reset can be triggered if the reset fails.

[0191] It should be noted that the program stored on the aforementioned computer-readable storage medium enables automated, adaptive, and safe control of the combined power generation system, significantly improving the system's operational stability and energy efficiency optimization capabilities under different ship operating conditions, while also reducing the operational burden on the crew.

[0192] The above technical solutions only embody the preferred technical solutions of the present invention. Any modifications that may be made by those skilled in the art to certain parts thereof embody the principles of the present invention and fall within the protection scope of the present invention.

Claims

1. A combined power generation system of thermophotovoltaic catalytic fluidized bed reactor and fuel cell based on ship transportation, characterized in that, include: Liquid ammonia storage tank (1); A thermo-photovoltaic catalytic fluidized bed reactor (6) is in fluid communication with the liquid ammonia storage tank (1); The solid oxide fuel cell module (8) has its anode inlet in fluid communication with the product outlet (603) of the thermophotovoltaic catalytic fluidized reactor (6); The thermophotovoltaic catalytic fluidized bed reactor (6) includes: The inner chamber is provided with a first catalyst layer (604) for catalytic cracking of ammonia into hydrogen. The inlet (601) of the inner chamber is connected to the liquid ammonia storage tank (1). The middle chamber surrounds the inner chamber and is provided with a second catalyst layer (605) for catalytic combustion of anode tail gas. The inlet (602) of the middle chamber is connected to the anode outlet of the solid oxide fuel cell module (8). A high-temperature emitter (606) thermally coupled to the inner and / or middle chambers for radiating heat; A thermophotovoltaic cell array (607) is arranged in the radiation path of the high-temperature emitter (606) to convert the infrared energy radiated by the high-temperature emitter (606) into electrical energy, thereby realizing the system's "one-time power generation". Furthermore, the solid oxide fuel cell module (8) is used to generate electricity through electrochemical reaction using hydrogen-rich gas from the thermophotovoltaic catalytic fluidized reactor (6), thereby realizing the system's "secondary power generation".

2. The system according to claim 1, characterized in that, Also includes: The ammonia feed primary heat exchanger (3) has its cold side inlet connected to the outlet of the liquid ammonia storage tank (1); The ammonia feed secondary heat exchanger (4) has its cold side inlet connected to the cold side outlet of the ammonia feed primary heat exchanger (3), and its cold side outlet connected to the inlet (601) of the inner chamber. The ejector (5) has its drive inlet connected to the anode outlet of the solid oxide fuel cell module (8) and its outlet connected to the hot side inlet of the ammonia feed secondary heat exchanger (4), and is used to preheat ammonia gas using anode tail gas as a heat source.

3. The system according to claim 2, characterized in that, Also includes: An air filter (9) and an air compressor (10) are connected in sequence; The cathode feed primary heat exchanger (11) has its cold side inlet connected to the outlet of the air compressor (10) and its hot side inlet connected to the outlet of the exhaust gas processor (13). The cathode feed secondary heat exchanger (12) has its cold side inlet connected to the cold side outlet of the cathode feed primary heat exchanger (11), its cold side outlet connected to the cathode inlet of the solid oxide fuel cell module (8), and its hot side inlet connected to the cathode outlet of the solid oxide fuel cell module (8), and is used to preheat air using cathode exhaust.

4. The system according to claim 1, characterized in that, The thermophotovoltaic catalytic fluidized bed reactor (6) is a double-layer cylindrical high-temperature resistant alloy structure. The first catalyst layer (604) is filled with at least one of nickel-based, ruthenium-based, platinum-based or copper-based catalysts, and the second catalyst layer (605) is filled with ruthenium-based or platinum-based catalysts.

5. The system according to claim 2, characterized in that, It also includes a splitter (7), the inlet of which is connected to the hot side outlet of the ammonia feed secondary heat exchanger (4), and the first outlet of the splitter (7) is connected to the inlet (602) of the middle chamber, for passing part of the anode tail gas into the second catalyst layer (605) for catalytic combustion.

6. The system according to claim 1, characterized in that, It also includes an inverter (14) and a power distributor (15). The input terminal of the inverter (14) is connected to the electrical output terminal of the thermophotovoltaic cell array (607) and the solid oxide fuel cell module (8), respectively. The output terminal of the inverter (14) is connected to the input terminal of the power distributor (15). The output terminal of the power distributor (15) is configured to connect to the ship's power system (16), domestic power system (17) and energy storage system (18).

7. The system according to claim 1, characterized in that, The thermophotovoltaic catalytic fluidized bed reactor (6) and the solid oxide fuel cell module (8) are arranged in the ship's engine room, and the liquid ammonia storage tank (1) is arranged on the ship's deck. The liquid ammonia storage tank (1) is installed at a height higher than the thermophotovoltaic catalytic fluidized bed reactor (6) and the solid oxide fuel cell module (8) in order to reduce pumping energy consumption by utilizing gravity flow.

8. A combined power generation method, said method being used in the system as described in any one of claims 1 to 7, characterized in that, Includes the following steps: Step A: After the liquid ammonia in the liquid ammonia storage tank (1) is vaporized, it is preheated in sequence through the ammonia feed primary heat exchanger (3) and secondary heat exchanger (4) and then introduced into the inner chamber of the thermophotovoltaic catalytic fluidized reactor (6); Step B: In the inner chamber, the preheated ammonia gas is endothermically decomposed under the action of the first catalyst layer (604) to produce hydrogen-rich gas. At the same time, the high temperature generated in the inner chamber and / or the middle chamber causes the high temperature emitter (606) to radiate infrared rays. The thermophotovoltaic cell array (607) receives the infrared rays and performs "one-time power generation". Step C: The hydrogen-rich gas generated in step B is introduced into the anode of the solid oxide fuel cell module (8) to carry out an electrochemical reaction and realize "secondary power generation", while generating anode tail gas; Step D: At least a portion of the anode tail gas generated in step C is passed sequentially through the ejector (5) and the ammonia feed secondary heat exchanger (4), and then through the splitter (7) into the middle chamber of the thermophotovoltaic catalytic fluidized reactor (6), where it undergoes catalytic combustion on the second catalyst layer (605) to provide heat for the ammonia cracking reaction in the inner chamber.

9. The method according to claim 8, characterized in that, Step D further includes: Step D1: In response to the ship being in an acceleration or high-load condition, control the splitter (7) to increase the proportion of anode exhaust gas entering the middle chamber; Step D2: In response to the ship being in a deceleration or berthing condition, control the splitter (7) to reduce the proportion of anode exhaust gas entering the middle chamber and introduce the excess anode exhaust gas into the exhaust gas processor (13).

10. A computer-readable storage medium having a computer program stored thereon, characterized in that, When executed by a processor, the computer program controls the steps of implementing the method according to any one of claims 8 to 9, comprising: In response to the acquired ship operating status signal and power demand signal, the opening control signal of the fuel supply valve, the speed control signal of the air compressor (10) and the diversion ratio control signal of the diverter (7) are generated to adjust the power generation of the thermophotovoltaic catalytic fluidized reactor (6) and the solid oxide fuel cell module (8).

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