Efficient ammonia decomposition hydrogen production and power generation system applying combined reactor

Abstract

The invention relates to an efficient ammonia decomposition hydrogen production and power generation system applying a combined reactor. The system comprises a liquid ammonia tank, a preheating mechanism, an evaporator, the combined reactor, an air cooling mechanism, a water cooling mechanism, a combustion mechanism, a purification device and a fuel cell. The liquid ammonia tank is communicated with the combined reactor in series through the preheating mechanism and the evaporator in sequence, and the evaporator is provided with three independent heat exchange sections which are respectively connected with the fuel cell, the water cooler and the combustion mechanism. The combustion mechanism heats ammonia gas by combusting air, and flue gas enters the combined reactor and then is discharged and used for heating the evaporator. The water cooler is communicated with the purification device and the fuel cell, the fuel cell converts purified gas into electric energy, and tail gas is used for heating the evaporator. The system obviously improves the energy utilization efficiency and reduces the energy consumption by optimizing liquid ammonia evaporation and recycling surface heat dissipation of the reactor and heat of high-temperature decomposed gas, is particularly suitable for remote cold regions such as plateau, and has the characteristics of high efficiency, compactness, energy conservation and environmental protection.

Description

Technical Field

[0001] The present invention relates to the technical field of hydrogen energy power generation equipment, and particularly relates to an efficient ammonia decomposition hydrogen production power generation system using a combined reactor. Background Art

[0002] With the transformation of the global energy structure and the promotion of the "dual carbon" goal, hydrogen energy, as a clean, efficient, and renewable energy carrier, has received increasing attention. However, the high costs of hydrogen storage and transportation limit its large-scale application, especially in remote and cold areas such as plateaus. As an efficient hydrogen storage medium, ammonia has advantages such as safe storage and transportation, high energy density, and easy liquefaction, and is considered one of the effective ways to solve the problems of hydrogen energy storage and transportation. Traditional ammonia decomposition hydrogen production technologies mostly use fixed-bed reactors, which have problems such as high reaction temperature, easy deactivation of catalysts, and low system efficiency. At the same time, existing ammonia decomposition hydrogen production systems often focus on hydrogen production, but pay insufficient attention to the efficient utilization of hydrogen energy, especially the deep integration with power generation systems, resulting in low overall energy utilization efficiency.

[0003] Chinese Patent CN118988162A discloses a low-pressure ammonia decomposition hydrogen production power generation system, which includes a liquid ammonia tank, a low-pressure reactor, a first evaporator, a second evaporator, a purifier, a power system, and a fuel cell. The liquid ammonia tank is connected to the ammonia gas inlet of the low-pressure reactor; the low-pressure reactor includes a plurality of flue gas pipes, a plurality of ammonia gas pipes, and a plurality of partitions. The plurality of partitions divide the low-pressure reactor into alternately arranged flue gas intervals and decomposition intervals. The plurality of flue gas pipes are arranged in the decomposition interval, and the ammonia gas pipes are arranged in the flue gas interval. The flue gas pipes are connected to the flue gas interval, and the ammonia gas pipes are connected to the decomposition interval; the ammonia gas pipes and the flue gas pipes are not connected to each other; the first evaporator is connected to the decomposition gas outlet of the low-pressure reactor and the purifier, and the second evaporator is connected to the power system; the purifier is sequentially connected to the power system and the fuel cell. This low-pressure ammonia decomposition hydrogen production system effectively improves the decomposition efficiency of ammonia, reduces energy loss, and improves the overall power generation efficiency of the system; however, the system has a low reuse rate of the energy generated during operation and is difficult to apply to extreme environments, especially the power supply requirements in remote plateau areas with low heat supply. Summary of the Invention

[0004] In view of the defects in the existing ammonia decomposition hydrogen production power generation system, such as low energy reuse rate and difficulty in adapting to power generation operation in an environment with low heat supply, the present invention provides an ammonia decomposition hydrogen production power generation system using a combined reactor, which has low energy consumption, high energy recovery efficiency and reuse rate, and is applicable to power generation in remote and cold environments.

[0005] The technical solution adopted by the present invention to solve its technical problems is: an efficient ammonia decomposition hydrogen production power generation system using a combined reactor, comprising a liquid ammonia tank, a preheating mechanism, an evaporator, a combined reactor, an air cooling mechanism, a water cooling mechanism, a combustion mechanism, a purification device and a fuel cell; the liquid ammonia tank is connected to the preheating mechanism; the preheating mechanism is then connected in series with the evaporator and the combined reactor in turn; the evaporator comprises three heat exchange sections that are not connected to each other and are arranged close to each other; the air cooling mechanism comprises a separately arranged fan and an air cooler, the fan is connected to the combined reactor; the combined reactor is connected to the air cooler; the air cooler is then connected to the combustion mechanism; the water cooling mechanism comprises a separately arranged water tank and a water cooler, the water tank is connected in series with the water cooler, and the water cooler is then connected to one of the heat exchange sections of the evaporator; the combustion mechanism is capable of The air introduced from the air cooler is burned, and the combusted gas enters the flue gas inlet channel of the combined reactor to heat the ammonia, and is then discharged from the flue gas exhaust channel of the combined reactor and enters another heat exchange section of the evaporator; the water cooler is also connected to the purification device, and the purification device is connected to the fuel cell; the fuel cell is used to convert the chemical energy of the gas purified by the purification device into electrical energy; the gas outlet of the fuel cell is connected to the last heat exchange section of the evaporator; during the operation of the system, the gas discharged from the fuel cell is first introduced into the heat exchange section connecting the fuel cell and the evaporator, and then the liquid water discharged from the water cooler is introduced into the heat exchange section connecting the water cooler and the evaporator, and finally the gas burned in the combustion mechanism is introduced into the heat exchange section connecting the combustion mechanism and the evaporator.

[0006] Furthermore, a liquid ammonia inlet is provided at one end of the evaporator, and an ammonia outlet is provided at the other end of the evaporator, and the liquid ammonia inlet and the ammonia outlet are arranged opposite to each other; the interior of the evaporator is a hollow structure, and a first partition plate, a second partition plate, a third partition plate and a fourth partition plate are provided inside the evaporator, and the first partition plate, the second partition plate, the third partition plate and the fourth partition plate are arranged in sequence; the interval between the first partition plate and the second partition plate is the first heat exchange interval, the interval between the second partition plate and the third partition plate is the second heat exchange interval, and the interval between the third partition plate and the fourth partition plate is the third heat exchange interval; multiple Liquid ammonia pipelines, multiple liquid ammonia pipelines are parallel to each other and arranged at intervals, and the liquid ammonia pipelines are fixed on the first partition plate, the second partition plate, the third partition plate and the fourth partition plate in sequence; the liquid ammonia pipelines pass through the first heat exchange interval, the second heat exchange interval and the third heat exchange interval in sequence; the outer wall of the evaporator is provided with a first heat exchange inlet, a first heat exchange outlet, a second heat exchange inlet, a second heat exchange outlet, a third heat exchange inlet and a third heat exchange outlet; the first heat exchange inlet and the first heat exchange outlet are connected to the first heat exchange interval, the second heat exchange inlet and the second heat exchange outlet are connected to the second heat exchange interval, and the third heat exchange inlet and the third heat exchange outlet are connected to the third heat exchange interval.

[0007] Furthermore, the first heat exchange inlet and the first heat exchange outlet are oppositely arranged, the second heat exchange inlet and the second heat exchange outlet are oppositely arranged, and the third heat exchange inlet and the third heat exchange outlet are oppositely arranged; the first heat exchange inlet, the second heat exchange outlet, and the third heat exchange inlet are located on the same side of the evaporator, and the first heat exchange outlet, the second heat exchange inlet, and the third heat exchange outlet are located on the other side of the evaporator; the first heat exchange section, the second heat exchange section, and the third heat exchange section are respectively used for circulating different heat exchange media.

[0008] Furthermore, the flow direction of the heat exchange medium in the first heat exchange section is opposite to the flow direction of the heat exchange medium in the second heat exchange section, the flow direction of the heat exchange medium in the second heat exchange section is opposite to the flow direction of the heat exchange medium in the third heat exchange section, and the volumes of the first heat exchange section, the second heat exchange section, and the third heat exchange section are not equal to each other.

[0009] Furthermore, the combined reactor includes an ammonia introduction pipe, a plurality of ammonia sleeves, and a decomposition gas pipe; a plurality of introduction pipes are provided on the outer wall of the ammonia introduction pipe, each introduction pipe is correspondingly connected to an ammonia sleeve, and the plurality of ammonia sleeves are connected in sequence; the decomposition gas pipe is also connected to the plurality of ammonia sleeves at the same time; when the ammonia in the ammonia introduction pipe enters the connected plurality of ammonia sleeves through the introduction pipes provided on the outer wall, the ammonia continuously flows up and down in the plurality of ammonia pipes along the installation direction of the ammonia sleeves, and finally exits each ammonia pipe and correspondingly enters the decomposition gas pipe.

[0010] Furthermore, the combined reactor further includes a flue gas introduction pipe, a plurality of flue gas pipes, and a flue gas discharge pipe. A plurality of flue gas dispersion channels are connected in parallel to the side wall of the flue gas introduction pipe, each flue gas dispersion channel is connected to a plurality of flue gas pipes at the same time, and the other ends of the plurality of flue gas pipes are also connected to a flue gas concentration channel at the same time; the plurality of flue gas concentration channels are further connected to the flue gas discharge pipe at the same time; each flue gas pipe correspondingly penetrates through the ammonia pipe; the combined reactor is arranged in a cavity of a closed structure, and the cavity is respectively connected to a fan and an air cooler.

[0011] Furthermore, there is a gap between any two ammonia pipes, and each flue gas pipe is formed by two S-shaped flue gas sub-channels wound around each other, and the ends of the two flue gas sub-channels are correspondingly connected and jointly form the end of the flue gas pipe.

[0012] Further, it further includes an air heat exchanger. The water tank is interconnected with the air heat exchanger. The water cooler is connected to the evaporator, and the evaporator is also connected to the water tank. The combustion mechanism includes a separately arranged air preheater and a burner. The purification device is directly connected to the burner, and the burner is further connected to the combined reactor. The gas after combustion of the burner is used for the ammonia decomposition reaction in the combined reactor. The combined reactor is further connected to the air preheater. The air preheater is also respectively connected to the air cooler, the evaporator, and the burner. The air preheater can preheat the air discharged from the air cooler and then introduce it into the burner for continuous combustion. The air preheater can heat the combusted gas discharged from the combined reactor and then introduce it into the evaporator for heating and evaporation of liquid ammonia.

[0013] Further, the evaporator includes a first heat exchange section, a second heat exchange section, and a third heat exchange section that are not interconnected. The volume of the first heat exchange section is smaller than that of the second heat exchange section, and the volume of the second heat exchange section is smaller than that of the third heat exchange section. The first heat exchange section is connected to the fuel cell, the second heat exchange section is connected to the water cooler, and the third heat exchange section is connected to the air preheater.

[0014] Further, there is a first valve between the fuel cell and the first heat exchange section of the evaporator, a second valve is provided between the water cooler and the second heat exchange section of the evaporator, and a third valve is provided between the air preheater and the evaporator. During the operation of the system, first open the first valve to introduce the tail gas of the fuel cell into the evaporator for heating and evaporation of liquid ammonia. Subsequently, open the second valve to introduce the liquid water in the water cooler into the evaporator for heating and evaporation of liquid ammonia. Finally, open the third valve to introduce the preheated combusted gas in the air preheater into the evaporator for heating and vaporization of liquid ammonia.

[0015] In the high-efficiency ammonia decomposition hydrogen production power generation system using a combined reactor according to the present invention, first, an ammonia gas sleeve and a flue gas pipeline with a casing structure are adopted to form the basic unit of the reactor, and then the ammonia gas sleeve and the flue gas pipeline with the casing structure are arranged in an array. Multiple ammonia gas sleeves are simultaneously connected to the decomposition gas pipeline and the ammonia gas introduction pipeline, and multiple flue gas pipelines are simultaneously connected to a flue gas dispersion pipeline; so that ammonia gas can be simultaneously dispersed into multiple ammonia gas sleeves for ammonia decomposition, and flue gas can simultaneously enter multiple flue gas pipelines for heating; while reducing the gas pressure drop, the ammonia decomposition efficiency is improved; the combined matrix structure also enables ammonia gas to be uniformly heated and decomposed into hydrogen and nitrogen in the combined reactor; the overall temperature of the decomposed hydrogen and nitrogen is increased; on this basis, in this power generation system, air cooling and water cooling methods are simultaneously adopted. The air introduced by the fan is used to control the temperature distribution of each part in the combined reactor, and then the discharged heated air is respectively used for cooling the mixed gas and burning in the burner; the cooling of the mixed gas in the water cooler and the evaporation heating in the evaporator are controlled by the flow of liquid water; at the same time, the heat of the external air is effectively utilized to increase the temperature in the water cycle; the energy utilization rate during the operation of the system is greatly improved, and the energy generated in each stage is fully utilized, effectively saving the system energy consumption; finally, an evaporator with three heat exchange intervals is adopted, and the fuel cell tail gas, liquid water, and the tail gas generated during the combustion process are successively introduced into the evaporator for heating; while effectively reducing the system energy consumption and improving the system energy utilization rate, the stable operation of liquid ammonia evaporation, ammonia decomposition, fuel cell power generation, and gas heat exchange in the system is ensured, and the operation conditions of each part, such as combustion, fuel cell power generation, and water tank heating, can be adjusted according to the evaporation effect during the evaporation process; therefore, this system has:

[0016] A: Characteristics such as high efficiency, compactness, and low energy consumption, which are particularly suitable for remote cold areas such as plateaus, making full use of various natural energy sources to achieve the purpose of energy conservation;

[0017] B: The system optimizes the liquid ammonia evaporation system, reduces the energy loss of liquid ammonia evaporation, integrates an efficient liquid ammonia evaporator, and comprehensively utilizes and balances the cold and heat energy of the system,

[0018] C: Improves the energy recovery efficiency. After the outer surface of the reaction is heat-insulated, an air heat-insulated closed interlayer is set up to make full use of the heat dissipated from the surface of the reactor, recover the heat, and recover the heat of the high-temperature decomposed gas and the flue gas, so as to achieve the purpose of increasing the combustion temperature, reducing the fuel consumption, and improving the energy utilization efficiency. Description of the Drawings

[0019] To more clearly illustrate the specific embodiments of the present invention, the following will briefly introduce the drawings required for the specific embodiments. Obviously, the drawings in the following description are some embodiments of the present invention. For those of ordinary skill in the art, without creative efforts, other drawings can also be obtained based on these drawings.

[0020] Figure 1 Structural schematic diagram of a high-efficiency ammonia decomposition hydrogen production power generation system using a combined reactor according to the present invention;

[0021] Figure 2 Structural schematic diagram of the evaporator of a high-efficiency ammonia decomposition hydrogen production power generation system using a combined reactor according to the present invention;

[0022] Figure 3 Internal structural schematic diagram of the evaporator of a high-efficiency ammonia decomposition hydrogen production power generation system using a combined reactor according to the present invention;

[0023] Figure 4 Structural schematic diagram of the combined reactor of a high-efficiency ammonia decomposition hydrogen production power generation system using a combined reactor according to the present invention;

[0024] Figure 5 Assembly schematic diagram of the ammonia pipeline and the flue gas branch of a high-efficiency ammonia decomposition hydrogen production power generation system using a combined reactor according to the present invention;

[0025] Figure 6 Structural schematic diagram of the flue gas branch of a high-efficiency ammonia decomposition hydrogen production power generation system using a combined reactor according to the present invention. Specific embodiments

[0026] The following will clearly and completely describe the technical solutions of the present invention in conjunction with the drawings. Obviously, the described embodiments are some embodiments of the present invention, rather than all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative efforts fall within the protection scope of the present invention.

[0027] As Figures 1 to 6 shown, a high-efficiency ammonia decomposition hydrogen production power generation system using a combined reactor according to the present invention includes a liquid ammonia tank 1, a preheating mechanism 2, an evaporator 3, a combined reactor 4, an air cooling mechanism 5, a water cooling mechanism 6, a combustion mechanism 7, a purification device 8, and a fuel cell 9;

[0028] The liquid ammonia tank 1 is communicated with the preheating mechanism 2; the preheating mechanism 2 is then connected in series with the evaporator 3 and the combined reactor in sequence; the evaporator 3 includes three non-connected and fitting heat exchange intervals;

[0029] The air-cooling mechanism 5 includes a separately arranged fan 51 and an air cooler 52. The fan 51 is connected to the combined reactor 4; the combined reactor 4 is connected to the air cooler 52; the air cooler 52 is then connected to the combustion mechanism 7;

[0030] The water-cooling mechanism 6 includes a separately arranged water tank 61 and a water cooler 62. The water tank 61 and the water cooler 62 are connected in series, and the water cooler 62 is then connected to one of the heat exchange zones of the evaporator 3;

[0031] The combustion mechanism 7 can burn the air introduced from the air cooler 52. The burned gas enters the flue gas inlet channel 44 of the combined reactor 4 to heat ammonia, and then is discharged from the flue gas discharge channel 46 of the combined reactor 4 and enters another heat exchange zone of the evaporator 3;

[0032] The water cooler 62 is also connected to the purification device 8, and the purification device 8 is then connected to the fuel cell 9; the fuel cell 9 is used to convert the chemical energy of the gas purified by the purification device 8 into electrical energy; the gas outlet of the fuel cell 9 is connected to the last heat exchange zone of the evaporator 3;

[0033] During the operation of the system, first, the gas discharged from the fuel cell 9 is introduced into the heat exchange zone where the fuel cell 9 is connected to the evaporator 3. Second, the liquid water discharged from the water cooler 62 is introduced into the heat exchange zone where the water cooler 62 is connected to the evaporator 3. Finally, the burned gas in the combustion mechanism 7 is introduced into the heat exchange zone where the combustion mechanism 7 is connected to the evaporator 3.

[0034] As Figure 1 shown, the preheating mechanism 2 includes a geothermal preheating pipe 21 and a solar heating pipe 22 connected in series. The liquid ammonia tank 1 is connected to the geothermal preheating pipe 21; the geothermal preheating pipe 21 is buried at a certain depth underground to absorb a certain amount of heat for evaporation using geothermal energy. The solar heating pipe 22 heats the liquid ammonia by absorbing solar energy; the liquid ammonia discharged from the liquid ammonia tank 1 passes through the geothermal preheating tank 21 and then passes through the ground and is further heated by the solar heating pipe 22; the solar heating pipe 22 is then connected to the evaporator 3.

[0035] As Figure 2 and Figure 3As shown, the evaporator 3 is of a cylindrical structure. One end of the evaporator 3 is provided with a liquid ammonia inlet 31, and the other end of the evaporator 3 is provided with an ammonia outlet 32. The liquid ammonia inlet 31 and the ammonia outlet 32 are arranged oppositely; the interior of the evaporator 3 is a hollow structure, and a first partition plate 371, a second partition plate 372, a third partition plate 373 and a fourth partition plate 374 are arranged inside the evaporator 3. The first partition plate 371, the second partition plate 372, the third partition plate 373 and the fourth partition plate 374 are arranged at intervals in sequence, wherein the first partition plate 371 is arranged close to the liquid ammonia inlet 31, and the fourth partition plate 374 is arranged close to the ammonia outlet 32; a plurality of openings are evenly formed on the first partition plate 371, the second partition plate 372, the third partition plate 373 and the fourth partition plate 374. The openings on the first partition plate 371, the openings on the second partition plate 372, the openings on the third partition plate 373 and the openings on the fourth partition plate 374 are arranged in one-to-one alignment; a plurality of liquid ammonia pipes 36 are further arranged inside the evaporator 3. The plurality of liquid ammonia pipes 36 are arranged parallel to each other and coincide with the installation direction of the evaporator 3; the plurality of liquid ammonia pipes 36 are arranged at intervals from each other. The liquid ammonia pipes 36 correspondingly pass through the openings on the plurality of partition plates and are fixed between the plurality of partition plates; wherein, there is a gap between the liquid ammonia inlet 31 and the first partition plate 371, and there is a gap between the ammonia outlet 32 and the fourth partition plate 374; the liquid ammonia entering from the liquid ammonia inlet 31 first converges in the gap between the liquid ammonia inlet 31 and the first partition plate 371, and then correspondingly enters the plurality of liquid ammonia pipes 36 through the plurality of openings on the first partition plate 371; the interval between the first partition plate 371 and the second partition plate 372 is a first heat exchange interval, the interval between the second partition plate 372 and the third partition plate 373 is a second heat exchange interval, and the interval between the third partition plate 373 and the fourth partition plate 374 is a third heat exchange interval; the plurality of liquid ammonia pipes 36 sequentially pass through the first heat exchange interval, the second heat exchange interval and the third heat exchange interval; wherein, a first heat exchange inlet 331, a first heat exchange outlet 332, a second heat exchange inlet 341, a second heat exchange outlet 342, a third heat exchange inlet 351 and a third heat exchange outlet 352 are formed on the outer wall of the evaporator 3; the first heat exchange inlet 331, the first heat exchange outlet 332, the second heat exchange inlet 341, the second heat exchange outlet 342, the third heat exchange inlet 351 and the third heat exchange outlet 352 are separately arranged; wherein, the first heat exchange inlet 331 and the first heat exchange outlet 332 are arranged oppositely, the second heat exchange inlet 341 and the second heat exchange outlet 342 are arranged oppositely, and the third heat exchange inlet 351 and the third heat exchange outlet 352 are arranged oppositely;The first heat exchange inlet 331, the second heat exchange outlet 342, and the third heat exchange inlet 351 are located on the same side of the evaporator 3. The first heat exchange outlet 332, the second heat exchange inlet 341, and the third heat exchange outlet 352 are located on the other side of the evaporator 3. The first heat exchange inlet 331 and the first heat exchange outlet 332 are connected to the first heat exchange section. The second heat exchange inlet 341 and the second heat exchange outlet 342 are connected to the second heat exchange section. The third heat exchange inlet 351 and the third heat exchange outlet 352 are connected to the third heat exchange section. The installation directions of the first heat exchange inlet 331, the first heat exchange outlet 332, the second heat exchange inlet 341, the second heat exchange outlet 342, the fourth heat exchange inlet 351, and the third heat exchange outlet 352 are parallel to each other and perpendicular to the extension direction of the evaporator 3. The first heat exchange section, the second heat exchange section, and the third heat exchange section are respectively used to circulate different heat exchange media. When liquid ammonia enters the evaporator 3 through the liquid ammonia inlet 31, the liquid ammonia sequentially enters a plurality of liquid ammonia pipes 36 arranged at intervals and sequentially passes through the first heat exchange section, the second heat exchange section, and the third heat exchange section along the plurality of liquid ammonia pipes 36. During the flow process, the liquid ammonia exchanges heat with the heat exchange media in the first heat exchange section, the second heat exchange section, and the third heat exchange section in sequence, achieving the heating and vaporization of the liquid ammonia. In the first heat exchange section, the second heat exchange section, and the third heat exchange section, since the liquid ammonia pipes are arranged at intervals, the heat exchange media shuttle and flow in the intervals between the plurality of liquid ammonia pipes in their respective heat exchange sections, achieving the heating of the liquid ammonia flowing in the liquid ammonia pipes. Due to the arrangement of the plurality of liquid ammonia pipes at intervals, a flow disturbance effect is exerted on the flow of the heat exchange media. Therefore, the heat exchange time and heat exchange effect between the heat exchange media and the liquid ammonia are improved, and the effective heat exchange between the liquid ammonia and the heat exchange media is promoted, promoting the effective vaporization of the liquid ammonia. Specifically, the flow direction of the heat exchange media in the first heat exchange section is opposite to the flow direction of the heat exchange media in the second heat exchange section. The flow direction of the heat exchange media in the second heat exchange section is opposite to the flow direction of the heat exchange media in the third heat exchange section. The volumes of the first heat exchange section, the second heat exchange section, and the third heat exchange section are not equal to each other to adapt to heat exchange media with different heat quantities and form a staggered flow between different heat exchange media, which is beneficial to the sufficient heat absorption of the liquid ammonia between the plurality of heat exchange media and improves the vaporization effect of the liquid ammonia.;

[0036] Such as Figures 4 to 6As shown in the figure; when liquid ammonia is vaporized through heat exchange, the ammonia gas formed by vaporization directly enters the combined reactor 4. The combined reactor 4 includes an ammonia gas flow channel and a flue gas flow channel. The ammonia gas flow channel includes an ammonia gas introduction pipe 41, a plurality of ammonia gas sleeves 42, and a decomposition gas pipe 43. The ammonia gas introduction pipe 41 is successively connected to the plurality of ammonia gas pipes 42 and the decomposition gas pipe 43. Among them, a plurality of introduction pipes are provided on the outer wall of the ammonia gas introduction pipe 41, and each introduction pipe is correspondingly connected to one of the ammonia gas sleeves 42. The installation direction of the ammonia gas sleeve 42 is perpendicular to the installation direction of the ammonia gas introduction pipe 41. There are intervals between the plurality of ammonia gas pipes 42 and they are arranged parallel to each other. Among them, a first ammonia gas interface 421 and a second ammonia gas interface 422 are respectively provided at positions near both ends of the outer wall of each ammonia gas sleeve 42. The first ammonia gas interface 421 and the second ammonia gas interface 422 are arranged oppositely. The second ammonia gas interfaces 422 between adjacent two ammonia gas sleeves 42 are connected to each other, and the first ammonia gas interfaces 421 of adjacent two ammonia gas sleeves 42 are connected to each other. The first ammonia gas interface 421 of one of the ammonia gas sleeves 42 is connected to the introduction pipe on the ammonia gas introduction pipe 41, and the first ammonia gas interface 421 of one of the ammonia gas sleeves 42 is connected to the decomposition gas pipe 43. The ammonia gas in the ammonia gas introduction pipe 41 enters the connected plurality of ammonia gas sleeves 42 correspondingly through the introduction pipes provided on the outer wall. The ammonia gas flows inside the ammonia gas pipe 42 along the installation direction of the ammonia gas sleeve 42, and enters the adjacent ammonia gas pipe 42 connected thereto through the second ammonia gas interface 422 on the ammonia gas pipe 42, and then continues to flow in the ammonia gas pipe 42 and enters another connected ammonia gas pipe 42 through the first ammonia gas interface 421. In this way, it continuously flows up and down in the plurality of ammonia gas pipes 42, and finally is discharged through the first ammonia gas interface 421 on one of the ammonia gas pipes 42 and correspondingly enters the decomposition gas pipe 43. By arranging the plurality of ammonia gas pipes 42 at intervals, the first ammonia gas interface 421 and the second ammonia gas interface 422 are respectively provided at positions near the ends of the ammonia gas pipe 42, and then the first ammonia gas interfaces 421 and the second ammonia gas interfaces 422 of the plurality of ammonia gas pipes 42 are connected in one-to-one correspondence; so that the ammonia gas can enter the plurality of ammonia gas pipes 42 respectively and flow up and down in the plurality of ammonia gas pipes 42; greatly increasing the flow distance of the ammonia gas, which is beneficial to the full heating of the ammonia gas and the endothermic decomposition of the ammonia gas; similarly, because a plurality of introduction pipes are provided on the ammonia gas introduction pipe 41 and each introduction pipe is correspondingly connected to the ammonia gas pipe 42, the ammonia gas can be dispersed into the plurality of ammonia gas pipes 42 at the same time for decomposition reaction, which also reduces the pressure drop in each ammonia gas pipe 42, reduces the pressure loss during gas flow, and increases the air pressure of the gas discharged after decomposition, which is beneficial to the power generation of the subsequent fuel cell 9;Ammonia decomposes in each corresponding ammonia introduction pipe 41 to generate a mixed gas of hydrogen and nitrogen. The decomposed mixed gas is discharged from the first ammonia interface 421 on each ammonia introduction pipe 41 and enters the decomposition gas pipe 43 for collection, and finally is discharged through the decomposition gas pipe 43. The installation direction of the decomposition gas pipe 43 is perpendicular to that of the ammonia pipe 42 and parallel to that of the ammonia introduction pipe 41.

[0037] The flue gas flow path includes a flue gas inlet pipe 44, a plurality of flue gas pipes 45, and a flue gas outlet pipe 46. The flue gas inlet pipe 44 is connected to the plurality of flue gas pipes 45, and the plurality of flue gas pipes 45 are further connected to the flue gas outlet pipe 46. A plurality of flue gas dispersion channels 441 are connected in parallel to the side wall of the flue gas inlet pipe 44. The plurality of flue gas dispersion channels 441 are spaced from each other and are simultaneously connected to the flue gas inlet pipe 44. The plurality of flue gas dispersion channels 441 are all located in the same plane. Each flue gas dispersion channel 441 is further simultaneously connected to the plurality of flue gas pipes 45. The plurality of flue gas pipes 45 connected to the same flue gas dispersion channel 441 are located in the same plane and have a spacing therebetween. The plurality of flue gas pipes 45 connected to the same flue gas dispersion channel 441 are parallel to each other. Specifically, each flue gas pipe 45 correspondingly extends through the ammonia pipe 42, and after each flue gas pipe 45 passes through the corresponding ammonia pipe 42, it is connected to the flue gas outlet pipe 46. A plurality of flue gas concentration channels 461 are also connected to the flue gas pipe 46. Each flue gas concentration channel 461 is simultaneously connected to the plurality of flue gas pipes 45. The plurality of flue gas concentration channels 461 are parallel to each other and are located in the same plane as the flue gas outlet pipe 46. The plurality of flue gas concentration channels 461 are located on the same side of the flue gas outlet pipe 46. The installation directions of the flue gas outlet pipe 46 and the flue gas concentration channels 461 are both perpendicular to the installation direction of the flue gas pipe 45. When the high-temperature flue gas enters the flue gas inlet pipe 44, the high-temperature flue gas flows along the extension direction of the flue gas inlet pipe 44 and is dispersed into the plurality of flue gas dispersion channels 441, and then simultaneously enters the plurality of flue gas pipes 45 connected to each flue gas dispersion channel 441. At this time, the high-temperature flue gas flows along the corresponding flue gas pipe 45 in the direction close to the flue gas outlet pipe 46. Since the flue gas pipe 45 is disposed through each ammonia pipe 42, when the high-temperature flue gas flows in the corresponding flue gas pipe 45, the high-temperature flue gas in each flue gas pipe 45 can heat the ammonia flowing in the corresponding external ammonia pipe 42. Promote the endothermic decomposition of ammonia to generate hydrogen and nitrogen. The generated hydrogen and nitrogen flow up and down along the plurality of sequentially connected ammonia channels 42 and are collected in the decomposition gas pipe 43, and then are discharged from the decomposition gas pipe 43. The preparation and collection of hydrogen and nitrogen are completed. The high-temperature flue gas that has completed heat exchange is discharged from the corresponding flue gas pipe 45 and enters the connected flue gas concentration channels 461, and then is centrally introduced into the flue gas outlet pipe 46 through the connected flue gas concentration channels 461 and is finally discharged.

[0038] More specifically, each of the flue gas pipelines 45 is formed by two flue gas sub-channels 451 with an S-shaped structure wound around each other. The ends of the two flue gas sub-channels 451 are correspondingly connected and jointly form the end of the flue gas pipeline 45. When high-temperature flue gas enters through one end of the flue gas pipeline 45, the high-temperature flue gas can respectively enter the two wound flue gas sub-channels 451 and flow along the corresponding flue gas sub-channels 451 in a curved manner, and finally be discharged through the other end where the two flue gas sub-channels 451 are connected. By arranging two flue gas sub-channels 451 with an S-shaped structure and winding them around each other, the flow time of the high-temperature flue gas in the flue gas pipeline 45 is extended, and the heat of the high-temperature flue gas in each flue gas sub-channel 451 can be correspondingly distributed between the two flue gas sub-channels 451 with an S-shaped structure. When ammonia outside the flue gas pipeline 45 flows inside the ammonia channel 42, since the flue gas pipeline 45 is formed by two flue gas sub-channels 451 with an S-shaped structure wound around each other, the S-shaped flue gas sub-channel 451 can cause a turbulence effect on the flow of ammonia inside the ammonia channel 42, improve the degree of ammonia turbulence, and is beneficial to the heating and decomposition of ammonia.

[0039] Such as Figure 4As shown, multiple ammonia pipelines 42 are arranged in an array, and the first ammonia interfaces 421 and the second ammonia interfaces 422 between multiple ammonia pipelines 42 on the same column are connected in one-to-one correspondence; the ammonia inlet pipeline 41 is arranged near the top of the combined reactor 4 and on the same side of multiple ammonia pipelines 42; the decomposition gas pipeline 43 is arranged near the top of the combined reactor 4 and on the same side of multiple ammonia pipelines 42; the ammonia inlet pipeline 41 and the decomposition gas pipeline 43 are oppositely arranged and in the same plane, and the ammonia inlet pipeline 41 and the decomposition gas pipeline 43 are parallel to each other; the flue gas inlet pipeline 44 and multiple flue gas dispersion channels 441 communicated therewith are arranged near the top of the combined reactor 4 and above multiple flue gas pipelines 45 arranged in an array, the flue gas inlet pipeline 44 and multiple flue gas dispersion channels 441 are in the same plane and are perpendicularly arranged to the flue gas pipeline 45, and similarly, the flue gas discharge pipeline 46 and multiple flue gas concentration channels 461 communicated therewith are also in the same plane and are arranged parallel to each other, the flue gas discharge pipeline 46 and multiple flue gas concentration channels 461 are arranged near the bottom of the combined reactor 4 and below multiple flue gas pipelines 45 arranged in an array; and each flue gas pipeline 45 correspondingly passes through each ammonia pipeline 42, and two ends of each flue gas pipeline 45 are respectively connected to the flue gas concentration channel 461 and the flue gas dispersion channel 441; the ammonia inlet pipeline 41, multiple ammonia sleeves 42 and the decomposition gas pipeline 43, as well as the flue gas inlet pipeline 44, multiple flue gas pipelines 45 and the flue gas discharge pipeline 46, together with multiple flue gas dispersion channels 441 distributed on the flue gas inlet pipeline 44 and multiple flue gas concentration channels 461 distributed on the flue gas discharge pipeline 46 jointly form a multi-dimensional combined reactor 4 with a matrix structure; by disassembling and installing the ammonia sleeve 42, the flue gas pipeline 45, the flue gas dispersion channel 441 and the flue gas discharge pipeline 461, the assembly design of the reactor volume can be realized. For example, if one flue gas dispersion channel 441 and one flue gas discharge pipeline 451 are added or reduced, one column of the ammonia sleeves 42 and the corresponding flue gas pipelines 45 are correspondingly added or reduced; it better adapts to the ammonia decomposition with different reaction requirements and improves the adaptability and flexibility of the combined reactor 4; more preferably, the combined reactor 4 is arranged in a closed cavity (not shown), and the cavity is filled with air; by arranging a closed cavity outside the combined reactor 4 with an array structure and filling it with air, during the heating process of ammonia, for example, when the high-temperature flue gas flowing in a curved manner in each flue gas pipeline 45 exchanges heat with the ammonia in the ammonia sleeve 42 and promotes the endothermic decomposition of ammonia to generate hydrogen and nitrogen;When the air in the sealed cavity drives the ammonia decomposition process, the heat of the high-temperature flue gas in the flue gas pipeline 45 flows between multiple spaced-apart and arrayed ammonia sleeves 42. Combining the cavity with a sealed structure and the matrix arrangement structure of the multiple ammonia sleeves 42 enables the heat to be transferred to the ammonia in each ammonia sleeve 42, thus better reducing the risk of heat loss, effectively recycling the heat dispersed during the ammonia decomposition process and improving the energy utilization rate of the ammonia decomposition process. At the same time, it can also promote the uniform distribution of heat in the modular reactor 4, especially between multiple ammonia sleeves 42, further avoiding the situation of uneven heating, which is generally beneficial to the better decomposition of ammonia into hydrogen and nitrogen. Among them, the inlet of the cavity with a sealed structure is connected to the fan 51 in the air-cooling mechanism 5; the fan 51 is used to introduce air into the cavity with a sealed structure, thereby driving the heat dissipated during the heating of ammonia by high-temperature flue gas to flow between the multiple ammonia sleeves 42. The outlet of the cavity is connected to the air cooler 52, and the air in the cavity is discharged and then mixed again with the decomposed hydrogen and nitrogen mixed gas with a higher temperature to exchange heat in the air cooler 52; to further increase the temperature of the air discharged from the cavity and at the same time reduce the decomposed mixed gas discharged from the modular reactor 4.;

[0040] In Figure 1In this case, the air cooler 52 is directly connected to the water cooler 62. After heat exchange and cooling, the hydrogen-nitrogen mixed gas is discharged from the air cooler 52 and directly enters the water cooler 62 for further cooling. The water cooler 62 is connected to the water tank 61. Specifically, the water tank 61 is first connected to the water cooler 62, and the water in the water tank 61 directly enters the water cooler 62 to further cool the hydrogen and nitrogen introduced from the air cooler 52. To effectively utilize the water in the system and the heat after heat exchange and cooling, preferably, the water cooler 62 is further connected to the second heat exchange section of the evaporator 3. The liquid water that has exchanged heat with the hydrogen-nitrogen mixed gas in the water cooler 62 re-enters the second heat exchange section of the evaporator 3 and continues to exchange heat with the liquid ammonia in the heat exchanger 3, thereby improving the heating effect on the liquid ammonia in the heat exchanger 3 and reducing the energy consumption of the system at the same time. The liquid water that has been cooled after heat exchange is discharged from the heat exchanger 3 again and enters the water tank 61, forming a circulating flow of the liquid water in the system. To further improve the heat exchange effect of the liquid water in the system and ensure the effective control of the temperature of each component to ensure the stable operation of the system, preferably, the water tank 61 is further connected to the air heat exchanger 63. The liquid water heated in the water tank 61 can re-enter the air heat exchanger 63. The air heat exchanger 63 uses natural air as the heat source and utilizes the residual heat in the natural air to heat the liquid water after heat exchange in the water tank 61, achieving the effective utilization of the ambient temperature and improving the circulating heating efficiency of the liquid water in the water tank 61.

[0041] The water cooler 62 is further connected to the purification device 8. The cooled hydrogen and nitrogen discharged from the water cooler 62 enter the purification device 8 for purification to remove the residual ammonia in the mixed gas. The hydrogen and nitrogen after purification enter the fuel cell 9 again for power generation of the fuel cell 9. The fuel cell 9 converts the chemical energy of hydrogen and nitrogen into electrical energy, realizing the effective power generation of the system. In order to further and more effectively exchange heat with the liquid ammonia in the evaporator 3, preferably, the gas outlet of the fuel cell 9 is connected to the first heat exchange section of the evaporator 3. After the fuel cell 9 completes power generation, the tail gas generated during the power generation process enters the first heat exchange section of the first heat exchanger 3 again to exchange heat with the preheated liquid ammonia and promote the heating of the liquid ammonia. On the basis of connecting the water cooler 62 to the second heat exchange section, a different heat exchange medium is provided to exchange heat with the liquid ammonia, increasing the temperature difference between the liquid ammonia and the heat exchange medium when the liquid ammonia flows in the evaporator 3, which is beneficial to the liquid ammonia absorbing heat and rising in temperature in the evaporator 3. In order to more effectively improve the recycling of the heat exchange medium in the system and further promote the heating of the liquid ammonia in the evaporator 3, preferably, the first heat exchange section of the evaporator 3 is connected to the purification device 8. The tail gas after the fuel cell power generation and heat exchange in the first heat exchanger section of the evaporator 3 enters the purification device 8 again for purification to remove the water vapor in the mixed gas and increase the hydrogen purity in the mixed gas. Among them, the combustion mechanism 7 includes a burner 71 and an air preheater 72 that are separately arranged. The purification device 8 is directly connected to the burner 71 in the combustion mechanism 7. The mixed gas with high hydrogen purity after purification and purification enters the burner 71 again for heating and combustion. Among them, in order to improve the heat circulation in the system and reduce the energy required during the operation of the system, preferably, the burner 71 is connected to the flue gas introduction pipe 44 of the combined reactor 4, the flue gas discharge pipe 46 of the combined reactor 4 is connected to the air preheater 72, and the flue gas after the burner 71 burns enters the combined reactor 4 through the flue gas introduction pipe 44 for heating the ammonia; the heated flue gas is then discharged from the combined reactor 4 through the flue gas discharge pipe 46 and enters the air preheater 72 for preheating; the air preheater 72 is connected to the third heat exchange section of the evaporator 3, and the burned gas preheated by the air preheater 72 directly enters the third heat exchange section to provide heat for the evaporation of the liquid ammonia in the evaporator 3;More preferably, the air preheater 72 is further connected to the air cooler 52. After the mixed gas of hydrogen and nitrogen is cooled and heat-exchanged in the air cooler 52, the air introduced from the blower 51 enters the air preheater 72 again for heating. The heated air is discharged from the air preheater 72 and enters the burner 71 for combustion, achieving the repeated and effective utilization of the purified gas, that is, the hydrogen-containing tail gas generated after the fuel cell 9 generates electricity; the gas after the burner 71 burns enters the combined reactor 4 and the evaporator 3, and is respectively used for ammonia decomposition in the combined reactor 4 and liquid ammonia heating in the evaporator 3.

[0042] In order to achieve heat exchange of different heat transfer media in the evaporator 3, improve the heat exchange efficiency of each heat transfer medium, and ensure the stable operation of liquid ammonia evaporation, ammonia decomposition, fuel cell power generation, burner combustion, etc. in the system, and improve the stable operation efficiency of the overall system; preferably, there is a first valve (not shown) between the fuel cell 9 and the first heat exchange section of the evaporator 3, a second valve (not shown) is provided between the water cooler 62 and the second heat exchange section of the evaporator 3, and a third valve (not shown) is provided between the air preheater 72 and the evaporator 3. By adjusting the first valve, the second valve and the third valve respectively, the flow rate of the gas entering the evaporator 3 from the fuel cell 9, the flow rate of the liquid water entering the evaporator 3 from the water cooler 62, and the flow rate of the combustion gas entering the evaporator 3 from the air preheater 72 are correspondingly controlled; by adjusting the opening and closing sequence of the first valve, the second valve and the third valve, the sequence of the fuel cell tail gas, the liquid water and the combustion gas entering the evaporator 3 is further adjusted; more preferably, during the operation of the system, the first valve is first opened to introduce the tail gas of the fuel cell into the evaporator 3 for evaporating and heating the liquid ammonia, then the second valve is opened to introduce the liquid water in the water cooler 62 into the evaporator 3 for evaporating and heating the liquid ammonia, and finally the third valve is opened to introduce the preheated combustion gas in the air preheater 72 into the evaporator 3 for heating and vaporizing the liquid ammonia; through the above sequence, the heat of the fuel cell tail gas, the liquid water and the combustion gas can be transferred to the liquid ammonia, avoiding the situation that the liquid ammonia is completely evaporated due to the prior introduction of the combustion gas and the full heating of the combustion gas, resulting in the inability to fully utilize the heat of the fuel cell tail gas and the liquid water. In actual operation, the opening degree of the third valve can also be correspondingly adjusted according to the heat exchange conditions of the fuel cell tail gas and the liquid water, so as to control the combustion and heating of the burner 71 and the air preheater 72, achieving the effective and reasonable control of the system energy consumption and avoiding waste caused by overheating.

[0043] Further, the volume of the first heat exchange section in the evaporator 3 is smaller than that of the second heat exchange section, and the volume of the second heat exchange section is smaller than that of the third heat exchange section. Moreover, the flow direction of the heat exchange medium in the first heat exchange section is opposite to that in the second heat exchange section, and the flow direction of the heat exchange medium in the second heat exchange section is opposite to that in the third heat exchange section. Thereby, the heat exchange effect between the heat exchange medium and liquid ammonia is improved. Coupled with the fact that three heat exchange media with different heat transfer coefficients heat liquid ammonia respectively, liquid ammonia can fully absorb heat and evaporate in the evaporator to generate ammonia gas, improving the overall operation efficiency and stability.

[0044] Obviously, the above embodiments are merely examples given for clear illustration and are not limitations on the implementation manners. For those of ordinary skill in the art, other different forms of changes or alterations can be made based on the above description. It is not necessary and impossible to list all the implementation manners here. And the obvious changes or alterations derived therefrom still fall within the protection scope of the present invention.

Claims

1. An efficient hydrogen production and power generation system for ammonia decomposition using a combined reactor, comprising an ammonia tank, a preheating mechanism, an evaporator, a combined reactor, an air-cooling mechanism, a water-cooling mechanism, a combustion mechanism, a purification device, and a fuel cell; The ammonia tank is communicated with the preheating mechanism; the preheating mechanism is then serially communicated with the evaporator and the combined reactor in sequence; the evaporator includes three non-communicating and closely arranged heat exchange zones; The air-cooling mechanism includes a separately arranged fan and an air-cooler, the fan is connected to the combined reactor; the combined reactor is connected to the air-cooler; the air-cooler is then connected to the combustion mechanism; the water-cooling mechanism includes a separately arranged water tank and a water-cooler, the water tank is connected to the water-cooler in series, and the water-cooler is then communicated with one of the heat exchange zones of the evaporator; The combustion mechanism can burn the air introduced from the air-cooler, and the burned gas enters the flue gas introduction channel of the combined reactor to heat ammonia, and then is discharged from the flue gas discharge channel of the combined reactor and enters another heat exchange zone of the evaporator; The water-cooler is also connected to the purification device, and the purification device is then communicated with the fuel cell; the fuel cell is used to convert the chemical energy of the gas purified by the purification device into electrical energy; the gas outlet of the fuel cell is connected to the last heat exchange zone of the evaporator; During the operation of the system, first, the gas discharged from the fuel cell is introduced into the heat exchange zone where the fuel cell is connected to the evaporator, second, the liquid water discharged from the water-cooler is introduced into the heat exchange zone where the water-cooler is connected to the evaporator, and finally, the burned gas in the combustion mechanism is introduced into the heat exchange zone where the combustion mechanism is connected to the evaporator.

2. The high-efficiency ammonia decomposition hydrogen production power generation system using a combined reactor according to claim 1, characterized in that: One end of the evaporator is provided with a liquid ammonia inlet, and the other end of the evaporator is provided with an ammonia gas outlet, and the liquid ammonia inlet and the ammonia gas outlet are oppositely arranged; the interior of the evaporator is a hollow structure, and a first partition plate, a second partition plate, a third partition plate, and a fourth partition plate are arranged inside the evaporator, and the first partition plate, the second partition plate, the third partition plate, and the fourth partition plate are sequentially arranged at intervals; the interval between the first partition plate and the second partition plate is the first heat exchange zone, the interval between the second partition plate and the third partition plate is the second heat exchange zone, and the interval between the third partition plate and the fourth partition plate is the third heat exchange zone; A plurality of liquid ammonia pipes are also arranged inside the evaporator, the plurality of liquid ammonia pipes are parallel and arranged at intervals, and the liquid ammonia pipes are sequentially fixed on the first partition plate, the second partition plate, the third partition plate, and the fourth partition plate; the liquid ammonia pipes sequentially pass through the first heat exchange zone, the second heat exchange zone, and the third heat exchange zone; the outer wall of the evaporator is provided with a first heat exchange inlet, a first heat exchange outlet, a second heat exchange inlet, a second heat exchange outlet, a third heat exchange inlet, and a third heat exchange outlet; The first heat exchange inlet and the first heat exchange outlet are connected to the first heat exchange section, the second heat exchange inlet and the second heat exchange outlet are connected to the second heat exchange section, and the third heat exchange inlet and the third heat exchange outlet are connected to the third heat exchange section.

3. The high-efficiency ammonia decomposition hydrogen production power generation system using a combined reactor according to claim 2, characterized in that: The first heat exchange inlet and the first heat exchange outlet are oppositely arranged, the second heat exchange inlet and the second heat exchange outlet are oppositely arranged, and the third heat exchange inlet and the third heat exchange outlet are oppositely arranged; the first heat exchange inlet, the second heat exchange outlet and the third heat exchange inlet are located on the same side of the evaporator, and the first heat exchange outlet, the second heat exchange inlet and the third heat exchange outlet are located on the other side of the evaporator; the first heat exchange section, the second heat exchange section and the third heat exchange section are respectively used for flowing different heat exchange media.

4. An efficient ammonia decomposition hydrogen production power generation system using a combined reactor according to claim 3, characterized in that: The flow direction of the heat exchange medium in the first heat exchange section is opposite to the flow direction of the heat exchange medium in the second heat exchange section, the flow direction of the heat exchange medium in the second heat exchange section is opposite to the flow direction of the heat exchange medium in the third heat exchange section, and the volumes of the first heat exchange section, the second heat exchange section and the third heat exchange section are not equal to each other.

5. The high-efficiency ammonia decomposition hydrogen production power generation system using a combined reactor according to claim 1, wherein: The combined reactor includes an ammonia introduction pipe, a plurality of ammonia sleeves and a decomposition gas pipe; a plurality of introduction pipes are provided on the outer wall of the ammonia introduction pipe, each of the introduction pipes is correspondingly connected to one of the ammonia sleeves, and the plurality of ammonia sleeves are connected in sequence; the decomposition gas pipe is also connected to a plurality of ammonia sleeves at the same time; when the ammonia in the ammonia introduction pipe enters the connected plurality of ammonia sleeves through the introduction pipes provided on the outer wall, the ammonia continuously flows up and down in the plurality of ammonia pipes along the installation direction of the ammonia sleeves, and finally exits each ammonia pipe and correspondingly enters the decomposition gas pipe.

6. The high-efficiency ammonia decomposition hydrogen production power generation system using a combined reactor according to claim 5, wherein: The combined reactor further includes a flue gas introduction pipe, a plurality of flue gas pipes and a flue gas discharge pipe. A plurality of flue gas dispersion channels are connected in parallel to the side wall of the flue gas introduction pipe, each of the flue gas dispersion channels is connected to a plurality of flue gas pipes at the same time, and the other ends of the plurality of flue gas pipes are also connected to a flue gas concentration channel at the same time; the plurality of flue gas concentration channels are further connected to the flue gas discharge pipe at the same time; each of the flue gas pipes penetrates through the ammonia pipe correspondingly; the combined reactor is arranged in a cavity of a closed structure, and the cavity is connected to the fan and the air cooler respectively.

7. An efficient ammonia decomposition hydrogen production power generation system using a combined reactor according to claim 6, characterized in that: There is a gap between any two of the ammonia pipes, and each of the flue gas pipes is formed by two S-shaped flue gas sub-channels wound around each other, and the ends of the two flue gas sub-channels are correspondingly connected and jointly form the end of the flue gas pipe.

8. An efficient ammonia decomposition hydrogen production power generation system using a combined reactor according to claim 1, characterized in that: It further includes an air heat exchanger. The water tank is communicated with the air heat exchanger, the water cooler is connected to the evaporator, and the evaporator is also connected to the water tank; The combustion mechanism includes a separately arranged air preheater and a burner. The purification device is directly connected to the burner, and the burner is then connected to the combined reactor. The gas after combustion by the burner is used for the ammonia decomposition reaction in the combined reactor. The combined reactor is then connected to the air preheater. The air preheater is also respectively connected to the air cooler, the evaporator, and the burner. The air preheater can preheat the air discharged from the air cooler and then introduce it into the burner for continuous combustion. The air preheater can heat the gas that has undergone combustion and is discharged from the combined reactor and then introduce it into the evaporator for heating and evaporation of liquid ammonia.

9. An efficient ammonia decomposition hydrogen production power generation system using a combined reactor according to claim 8, characterized in that: The evaporator includes a first heat exchange section, a second heat exchange section, and a third heat exchange section that are not connected to each other. The volume of the first heat exchange section is smaller than that of the second heat exchange section, and the volume of the second heat exchange section is smaller than that of the third heat exchange section. The first heat exchange section is connected to the fuel cell, the second heat exchange section is connected to the water cooler, and the third heat exchange section is connected to the air preheater.

10. The high-efficiency ammonia decomposition hydrogen production power generation system using a combined reactor according to claim 9, wherein: There is a first valve between the fuel cell and the first heat exchange section of the evaporator. A second valve is provided between the water cooler and the second heat exchange section of the evaporator. A third valve is provided between the air preheater and the evaporator. During the operation of the system, first open the first valve to introduce the tail gas of the fuel cell into the evaporator for heating and evaporation of liquid ammonia. Subsequently, open the second valve to introduce the liquid water in the water cooler into the evaporator for heating and evaporation of liquid ammonia. Finally, open the third valve to introduce the preheated gas after combustion in the air preheater into the evaporator for heating and vaporization of liquid ammonia.

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