Reforming hydrogen production reactor and fuel cell system

Abstract

The invention relates to a reforming hydrogen production reactor and a fuel cell system. The method is suitable for the technical field of energy conversion and utilization. According to the technical scheme adopted by the invention, the reforming hydrogen production reactor comprises a third shell, a third cavity is formed in the third shell, and an inlet structure for inputting water vapor and diesel oil into the third cavity is arranged at the upper end of the third shell; the second shell is arranged in the third cavity, a second cavity is formed in the second shell, and a third communication channel for communicating the third cavity with the second cavity is formed in the lower part of the second shell; the first shell is arranged in the second cavity, a first cavity is formed in the first shell, and a second communication channel for communicating the second cavity with the first cavity is formed in the upper part of the first shell; the outlet structure is arranged below the first shell and communicates with the first cavity through a first communicating channel; the heating module is arranged in the first chamber; and the reforming hydrogen production catalyst is arranged in a gap between the heating module and the first shell.

Description

Technical Field

[0001] The present invention relates to a reforming hydrogen production reactor and a fuel cell system, which are applicable to the technical field of energy conversion and utilization. Background Art

[0002] A fuel cell is an energy conversion device that can convert the chemical energy of hydrogen into electrical energy. Hydrogen is considered to be an ideal energy carrier in the future. When combined with a fuel cell, it can be widely used in distributed, fixed and portable power sources, and is often used as an auxiliary or backup power source, such as an auxiliary power unit (APU) in a car. A fuel cell APU relies on hydrogen or synthetic gas as a raw material for power generation.

[0003] In recent years, on-board fuel cells have developed rapidly, and the demand for hydrogen has increased significantly. However, the domestic infrastructure for hydrogen production, storage, and refueling is still insufficient, and hydrogen supply has become one of the main obstacles to the commercialization of fuel cell vehicles. Diesel has a high energy density and is liquid at room temperature, which is easy to store and transport. It can be easily obtained at gas stations. Therefore, the use of diesel steam reforming technology for on-board on-site hydrogen production provides an effective solution to the hydrogen supply problem of fuel cell APUs. However, the design of diesel hydrogen reformers is relatively complex, and different reactor designs, reaction conditions, and catalyst selections will have a significant impact on the efficiency of diesel reforming hydrogen production.

[0004] At present, reforming hydrogen production reactors mostly use low-hydrocarbon fuels such as methanol or methane for hydrogen production experiments. However, my country's gas stations are well-equipped, and diesel is more convenient to obtain than methanol fuel, making it an ideal raw material for hydrogen production.

[0005] In addition, most current reformer research adopts the method of applying external heating equipment, such as thermocouples or heating furnaces, which makes the reformer bulky and restricts its integration and miniaturization. In addition, the catalyst used in the reformer is prone to carbon deposition and deactivation under the action of heavy hydrocarbon fuels, which reduces its service life. Summary of the invention

[0006] The technical problem to be solved by the present invention is: in view of the above-mentioned problems, a reforming hydrogen production reactor and a fuel cell system are provided.

[0007] The technical solution adopted by the present invention is: a reforming hydrogen production reactor, comprising: A third shell has a third chamber inside, and an inlet structure for inputting water vapor and diesel into the third chamber is provided at the upper end of the third shell; A second shell is disposed in the third chamber, the second shell has a second chamber inside, and a third connecting passage connecting the third chamber and the second chamber is formed at the lower part of the second shell; A first shell is disposed in the second chamber, the first shell has a first chamber inside, and a second connecting passage connecting the second chamber and the first chamber is formed on the upper portion of the first shell; an outlet structure, disposed below the first shell and connected to the first chamber via a first connecting passage; A heating module is disposed in the first chamber; a reforming hydrogen production catalyst, disposed in the gap between the heating module and the first shell; The reforming hydrogen production catalyst comprises: Inorganic porous carrier; and, γ-Al2O3, NiO, CeO2 and Rh2O3 coated on an inorganic porous support.

[0008] The inlet structure comprises: A diesel pipeline, used for inputting diesel into the third chamber; A water vapor input mechanism, used for inputting water vapor into the third chamber, comprising a water vapor pipeline and two water vapor nozzles, wherein the water vapor pipeline is connected to the two water vapor nozzles via an arc-shaped branch channel; The two water vapor nozzles are symmetrically arranged with respect to the diesel pipeline, and the nozzles of the water vapor nozzles face toward the output end of the diesel pipeline.

[0009] The heating module comprises: A combustion shell, the interior of which is a combustion chamber; A fuel pipeline, connected to the combustion chamber, for providing fuel to the combustion chamber; an air duct connected to the combustion chamber and used to provide air to the combustion chamber; The combustion exhaust gas pipeline is connected to the combustion chamber and is used to discharge the combustion exhaust gas in the combustion chamber.

[0010] The upper end of the third shell is interference-fitted with the upper flange blind plate, the upper portion of the upper flange blind plate is connected to the flange upper cover, and the inlet structure is arranged on the flange upper cover.

[0011] The lower end of the first shell is interference fit with the lower flange blind plate, and the lower flange blind plate is connected to the flange lower cover; The outlet structure includes an outlet channel arranged on the flange lower cover, and an outlet chamber surrounded by the first shell, the lower flange blind plate and the flange lower cover. The first chamber is connected to the outlet chamber through the first connecting channel, and is connected to the outlet channel through the outlet chamber.

[0012] A first coating layer and a second coating layer outside the first coating layer are formed on the inorganic porous support, wherein the first coating layer contains γ-Al2O3, and the second coating layer contains NiO, CeO2 and Rh2O3.

[0013] The inorganic porous carrier is made of cordierite honeycomb ceramics.

[0014] The method for preparing the reforming hydrogen production catalyst comprises: S1, immersing the inorganic porous support in deionized water, and ultrasonically washing it at room temperature, taking it out, drying it, and cooling it to room temperature; S2, immersing the inorganic porous support obtained in step S1 in alumina sol, taking it out and drying it, heating it to 600°C and firing it, cooling it down to room temperature, and repeating the immersion, drying, firing and cooling operations in this step until the γ-Al2O3 coating amount reaches a preset value; S3, immersing the inorganic porous support obtained in step S2 in the mixed solution, taking it out and drying it, heating it to 700°C for calcination, cooling it to room temperature, and repeating the immersion, drying, calcination and cooling operations in this step until the coating amount of NiO, CeO2 and Rh2O3 reaches a preset value; The mixed solution comprises nickel nitrate, nickel acetate, cerium nitrate solution, and rhodium nitrate solution.

[0015] A fuel cell system comprises the reforming hydrogen production reactor.

[0016] The beneficial effect of the present invention is as follows: the present invention forms a third chamber, a second chamber and a first chamber from the outside to the inside through the cooperation of a third shell, a second shell and a first shell, and a heating module is arranged in the first chamber, the heating module transfers heat to the first chamber, the second chamber and the third chamber in turn, and water vapor and diesel are heated layer by layer in the third chamber, the second chamber and the first chamber in turn, and then contact and react with the reforming hydrogen production catalyst in the first chamber, and hydrogen is discharged from the outlet structure. The overall structure is compact and can effectively reduce the overall volume.

[0017] The reforming hydrogen production reactor in the present invention is designed with an integrated burner and a reformer, and the highly coupled flow channel design is conducive to realizing step-by-step preheating of the reaction raw materials, achieving sufficient heat exchange between the heat releasing and heat absorbing components, and improving the overall energy utilization rate.

[0018] The present invention coats γ-Al2O3, NiO, CeO2 and Rh2O3 on an inorganic porous carrier, wherein γ-Al2O3 is a catalyst carrier; NiO is a catalyst; CeO2 is a promoter, which plays a certain role in inhibiting carbon deposition; Rh obtained after sintering Rh2O3 is also a catalyst. The bimetallic catalyst material of the present invention is mainly NiO, and the amount of precious metal Rh is reduced, thereby reducing the cost as much as possible under the premise of ensuring the performance of the reforming hydrogen production catalyst.

[0019] The reforming hydrogen production catalyst of the present invention can be applied to a variety of hydrocarbon fuels, and can reduce carbon deposition while ensuring stable output and high conversion rate of reforming products, thereby greatly improving the single service life of the catalyst and reducing wear and tear caused by multiple disassembly and assembly of the reactor.

[0020] The water vapor input mechanism of the present invention adopts a buffered split-flow air intake design, which can effectively buffer the uneven flow rate caused by the rapid expansion of water vapor, affect the reaction rate, improve the reaction stability and hydrogen production effect, achieve better temperature distribution and uniform distribution of gas production components, thereby achieving a higher hydrocarbon fuel conversion efficiency.

[0021] The reforming hydrogen production reactor in the present invention is of detachable design, which is convenient for timely replacement when the catalyst is deactivated to ensure the hydrogen production effect. The presence of pins fixes the catalyst in the reforming cavity, including but not limited to raw materials such as diesel, and has rich application scenarios.

[0022] In the coupled power generation and heat production system designed by combining the reforming hydrogen production reactor with the solid oxide fuel cell (SOFC) in the present invention, the tail gas of the fuel cell stack can be used as a heat source for the catalytic reaction during stable operation, thereby increasing the system volume energy density and thus improving the energy utilization of the overall system.

[0023] The reforming hydrogen production reactor in the present invention is suitable for the reforming reaction of heavy hydrocarbon fuels, such as diesel and other high energy density liquid fuels, which are widely used in daily life. The raw materials are easy to obtain and have a relatively mature actual supply system and market basis. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] Figure 1 4 is a cross-sectional view of a reforming hydrogen production reactor in an embodiment.

[0025] Figure 2 It is a three-dimensional diagram of the reforming hydrogen production reactor in the embodiment.

[0026] Figure 3 Schematic diagram of the structure of the flange cover in the embodiment.

[0027] Figure 4 Schematic diagram of the structure of the reforming hydrogen production catalyst in the embodiment.

[0028] Figure 5 The figure shows the influence of different catalysts on the conversion rate and gas production of n-hexadecane in the examples.

[0029] Figure 6 The graph shows the changes of gas production components of different catalysts over time in the examples.

[0030] 1. First shell; 110. First chamber; 120. First connecting channel; 2. Second shell; 210. Second chamber; 220. Second connecting channel; 3. Third shell; 310. Third chamber; 320. Third connecting channel; 4. Combustion shell; 410. Combustion chamber; 5. Reforming hydrogen production catalyst; 6. Upper flange blind plate; 7. Flange upper cover; 8. Diesel pipeline; 9. Steam input mechanism; 910. Steam pipeline; 920. Arc-shaped diverter; 930. Steam nozzle; 10. Lower flange blind plate; 11. Flange lower cover; 12. Outlet chamber. DETAILED DESCRIPTION

[0031] In order to better understand the technical solution of the present application, the embodiments of the present application are described in detail below with reference to the accompanying drawings.

[0032] It should be clear that the described embodiments are only part of the embodiments of the present application, not all of the embodiments. Based on the embodiments in the present application, all other embodiments obtained by ordinary technicians in the field without creative work are within the scope of protection of the present application.

[0033] The terms used in the embodiments of the present application are only for the purpose of describing specific embodiments, and are not intended to limit the present application. The singular forms "a", "said" and "the" used in the embodiments of the present application and the appended claims are also intended to include plural forms, unless the context clearly indicates other meanings.

[0034] Example 1: Figure 1 , 2 As shown, this embodiment is a reforming hydrogen production reactor, which includes a reactor body, an inlet structure, an outlet structure, a heating module, and the reforming hydrogen production catalyst 5 in Example 1, etc.

[0035] In this embodiment, the reactor body includes a third shell 3, a second shell 2 and a first shell 1, wherein the third shell 3 has a third chamber 310 inside; the second shell 2 is arranged in the third chamber 310, and has a second chamber 210 inside the second shell 2, and a circle of third connecting passages 320 connecting the third chamber 310 and the second chamber 210 is formed at the lower part of the second shell; the first shell 1 is arranged in the second chamber 210, and has a first chamber 110 inside the first shell 1, and a circle of second connecting passages 220 connecting the second chamber 210 and the first chamber 110 is formed at the upper part of the first shell.

[0036] In this example, the inlet structure includes an upper flange blind plate 6 and a flange upper cover 7, wherein the upper flange blind plate 6 is connected to the upper end opening of the third shell 3 by interference fit; the flange upper cover 7 is installed on the upper flange blind plate 6, and a metal graphite gasket is added between the flange upper cover 7 and the upper flange blind plate 6 and high-temperature sealant is applied, and stud nuts are used for fastening.

[0037] like Figure 3 As shown, in this embodiment, a diesel pipeline 8 and a water vapor input mechanism 9 are provided on the flange cover 7, wherein the diesel pipeline 8 is used to transport diesel to the third chamber below the flange cover; the water vapor input mechanism 9 is used to input water vapor into the third chamber 310.

[0038] In this example, the water vapor input mechanism 9 has a water vapor pipeline 910, an arc-shaped branch channel 920 and a water vapor nozzle 930, wherein there are two water vapor nozzles 930, and both are located below the flange cover 7, the two water vapor nozzles 930 are symmetrically arranged about the diesel pipeline 8, and the water vapor nozzle nozzles face the output end of the diesel pipeline; the arc-shaped branch channel 920 is formed in the flange cover 7, and the two ends of the arc-shaped branch channel are respectively connected to the two water vapor nozzles 930; the lower end of the water vapor pipeline 910 is connected to the middle part of the arc-shaped branch channel 920 in the flange cover 7.

[0039] The reaction raw materials during steam reforming of hydrocarbon fuels usually contain water, and the vaporized volume of water expands rapidly when evaporating, resulting in excessive pipeline pressure and unstable flow delivery. Therefore, this embodiment designs an arc-shaped diversion channel at the lower end of the water vapor pipeline. In this way, the gas transportation impact is reduced and a certain buffering and pressure stabilizing effect is achieved. After the water vapor is diverted, it is ejected from two water vapor nozzles under the flange. The two thin tubes are symmetrically distributed, and the outlet gases impact each other, which can achieve the effect of mixing the diesel gas together.

[0040] In this embodiment, the outlet structure includes a lower flange blind plate 10 and a flange lower cover 11, wherein the lower flange blind plate 10 is connected to the lower end opening of the first shell 1 by interference fit; the flange lower cover 11 is installed below the lower flange blind plate 10, and a metal graphite gasket is added and high-temperature sealant is applied between the flange lower cover 11 and the lower flange blind plate 10, and stud nuts are used for fastening.

[0041] In this example, a partition is provided in the first chamber 110 of the first shell 1 corresponding to the lower end opening of the first shell 1, and the partition, the lower flange blind plate 10 and the flange lower cover 11 form an outlet chamber 12, and the outlet chamber 12 is connected to the first chamber 110 through a first connecting channel 120 opened on the partition; the flange lower cover 11 is provided with an outlet channel connecting the outside and the outlet chamber 12.

[0042] In this embodiment, the heating module includes a combustion shell 4, a fuel pipeline, an air pipeline and a combustion exhaust gas pipeline, wherein the combustion shell 4 is arranged in the first chamber 110, and the interior of the combustion shell is a combustion chamber 410; one end of the fuel pipeline is connected to the combustion chamber, and the other end passes through the first shell 1, the second shell 2 and the third shell 3 and extends to the outside of the reactor body, so as to provide fuel to the combustion chamber; one end of the air pipeline is connected to the combustion chamber 410, and the other end passes through the first shell 1, the second shell 2 and the third shell 3 and extends to the outside of the reactor body, so as to provide air to the combustion chamber; one end of the combustion exhaust gas pipeline is connected to the combustion chamber 410, and the other end passes through the first shell 1, the second shell 2 and the third shell 3 and extends to the outside of the reactor body, so as to discharge the combustion exhaust gas in the combustion chamber.

[0043] like Figure 4 As shown, in this example, the reforming hydrogen production catalyst 5 is an annular structure, which is sleeved outside the combustion shell 4 and located between the combustion shell 4 and the first shell 1. The lower end of the reforming hydrogen production catalyst 5 is supported on four pins, and the pins are fixed on the first shell.

[0044] In this example, the reforming hydrogen production catalyst 5 includes an inorganic porous carrier, and γ-Al2O3, NiO, CeO2 and Rh2O3 coated on the inorganic porous carrier, wherein the coating amount of γ-Al2O3 is The target coating amounts of NiO, CeO2 and Rh2O3 are 20wt.%, 6wt.% and 1wt.% respectively.

[0045] In this example, the high-performance catalyst obtained by the impregnation method is an inorganic porous carrier of cordierite honeycomb ceramics. Since this example is a solid catalyst, it can achieve a good fixation effect in different occasions and ensure the stability of use. The preparation steps of the reforming hydrogen production catalyst 5 in this example are as follows: S1, immerse the cordierite honeycomb ceramic in deionized water, and wash it with ultrasonic water at room temperature for 30 minutes, set the drying oven to 120℃ for 3 hours, take it out and cool it to room temperature, weigh it and record the original data m0; S2, start the magnetic stirrer, slowly and evenly pour the nano-alumina powder at room temperature, and stir for 30 minutes to obtain a 15% alumina sol, let it stand for 12 hours, precipitate and filter; The cordierite honeycomb ceramic was immersed in alumina sol for 2 minutes and then taken out, dried in a muffle furnace at 120℃ for 3 hours, and heated to 600℃ for 2 hours. After cooling to room temperature, the weight of the honeycomb ceramic was weighed and recorded as m1. The coating amount was calculated and the above operation was repeated until the γ-Al2O3 coating amount 15wt.%, of which ; S3. According to the mass of the catalyst active component to be coated, nickel nitrate, nickel acetate and cerium nitrate solutions, as well as a rhodium nitrate solution with a rhodium content of 10% are prepared in proportion, and stirred evenly to form a mixed solution.

[0046] In this embodiment, based on the target coating amounts of NiO, CeO2 and Rh2O3 on the cordierite honeycomb ceramic, the mass ratios of the required nickel nitrate hexahydrate and cerium nitrate hexahydrate are calculated.

[0047] In this example, the honeycomb ceramic is immersed in the prepared mixed solution for 2 minutes, then taken out, dried at 120°C for 3 hours, heated to 700°C and calcined for 4 hours, cooled to room temperature and weighed, and the operation is repeated until the coating amount reaches 27%.

[0048] In order to verify the performance of the rhodium-nickel catalyst in this example, this example uses a common nickel-based catalyst (γ-Al2O3, NiO, and CeO2 coated on an inorganic porous carrier, where the γ-Al2O3 coating amount is The target coating amount of NiO and CeO2 is 15wt.%, and the target coating amount of NiO and CeO2 is 20wt.%, 6wt.%). As a comparative example, a long-term operation test was carried out, with a liquid space velocity WHSV = 3.35 / h, that is, the flow rate of n-hexadecane is 0.5ml / min, and the water-carbon ratio is S / C =3.5, reaction temperature T =800℃ for long-term stability experiment of both, and the reaction duration is up to 50h.

[0049] Comparing the performance of the two, Figure 5 As shown in the figure, the ordinary nickel-based catalyst can maintain a conversion rate of more than 95% in the first 20 hours, and the total gas production is more than 1950ml / min. After 30 hours, it began to fluctuate greatly and showed a downward trend. After 50 hours of the experiment, the conversion rate decayed to 84.3%, and the total gas production decreased to 1651.0ml / min. The performance of the rhodium-nickel catalyst is relatively stable, basically maintained at more than 96.1% in the first 31 hours, and then began to decline significantly. After 50 hours, the conversion rate decreased to 91.8%, and the total gas production remained above 1936.2ml / min. The rhodium-nickel conversion rate increased by 7.5% relative to the nickel-based catalyst.

[0050] like Figure 6As shown, the H2 content of the nickel-based catalyst gradually decreases from 71.2% to 68.9%, and the CH4 content gradually increases, up to 2.15%, indicating that the catalyst has obvious carbon deposition. CO content is between 13.9%-17%, CO2 is between 12.2%-15.0%, CO content is higher than CO2, and as the experiment proceeds, the gap between the two becomes more and more obvious. In the rhodium-nickel catalyst of this embodiment, the H2 content is always maintained at more than 71%, CO and CO2 content are maintained between 13-15%, and no CH4 is detected between 2-28h, indicating that the CH4 content is lower than the detection limit, and the CH4 content is no more than 0.37%, indicating that there is occasional carbon deposition on the catalyst, but it can be well digested, indicating that the rhodium-doped catalyst contributes to the stable operation of the experiment and the good effect of inhibiting carbon deposition.

[0051] After the experiment, the honeycomb ceramics in the reactor were taken out, and both remained intact and uncracked. A 1 cm thick carbon deposit layer accumulated on the upper layer of the common catalyst, while no obvious carbon deposit layer was observed in the catalyst of this embodiment. Carbon blocking micropores was only observed at the circumferential edge of the honeycomb ceramics, while the central part remained basically unobstructed, indicating that the addition of precious metal rhodium has a relatively excellent effect on inhibiting carbon deposition on the catalyst, and at the same time helps to promote the increase of H2 content and improve the stability of the experiment.

[0052] Hexadecane fails to completely react with water vapor to crack. CH4 and CO undergo chemical vapor deposition under the action of Ni at high temperature. The carbon generated by the decomposition reaction of CH4 and the disproportionation reaction of CO dissolves on the surface of the active metal. Carbon has a certain solubility and diffusion rate in the active metal particles. After the solubility reaches saturation, carbon begins to precipitate to form carbon fragments, and continues to diffuse and lengthen to form carbon nanotubes. The reaction efficiency decreases with the increase of carbon deposition, and the unreacted hexadecane increases, and the vicious cycle aggravates carbon deposition. Carbon nanotubes will lift nickel particles away from the carrier, weaken the interaction between the metal and the carrier, and induce Ni particles to sinter. After adding rhodium, the particle size of the active component becomes smaller and the dispersion is high, which effectively reduces the oxidation temperature and solubility of carbon on the catalyst surface, inhibits the nucleation and growth of carbon whiskers. The solubility of carbon on precious metals is low, which is not conducive to the formation of carbon deposition. Therefore, the carbon deposition on the catalyst is easily removed by steam, and the corresponding hydrogen production is increased. This also explains the experimental phenomenon that the hydrogen production concentration of the rhodium-nickel catalyst is higher than that of the nickel-based catalyst.

[0053] The addition of rhodium helps promote the water-gas reaction, increase the H2 content, and lower the concentration of CO and CH4. Rhodium helps to strengthen the interaction between the active metal and the carrier and improve the redox characteristics of the catalyst. The synergistic effect of rhodium and nickel metals helps to refine the crystal particle size, improve the grain dispersion, and increase the contact area of ​​the reaction. Rhodium-nickel alloy is beneficial to improve the activity of the catalyst and inhibit the agglomeration of active ingredients at high temperatures. The particle size of the active ingredients of the rhodium-doped catalyst becomes smaller and the dispersion is high, which can effectively inhibit the nucleation and growth of carbon whiskers and inhibit carbon deposition. The addition of rhodium to the catalyst can significantly improve the anti-carbon deposition effect and increase the service life.

[0054] In this embodiment, the mixed gas formed by the water vapor and diesel input from the inlet structure enters the second chamber 210 through the first gap between the third shell 3 and the second shell 2 and the third connecting channel 320 at the bottom, then enters the first chamber 110 through the second gap between the second shell 2 and the first shell 1 and the second connecting channel 220 at the top, and enters the outlet chamber 12 below through the third gap between the first shell 1 and the combustion shell 4 (with the reforming hydrogen production catalyst 5) and the first connecting channel 120 at the bottom.

[0055] In this example, the heating module is located at the center of the reactor body, so the temperature in the third gap is greater than the temperature in the second gap and greater than the temperature in the first gap. The mixed gas is gradually heated up when flowing from the inlet structure to the outlet structure, making full use of the heat generated by the heating module.

[0056] Embodiment 2: This embodiment is a fuel cell system having the reforming hydrogen production reactor in Embodiment 1.

[0057] This embodiment uses a reforming hydrogen production reactor to produce hydrogen on-site for liquid hydrocarbon fuels, and supplies a system block diagram of solid oxide fuel cells for power generation and heat production. The reaction raw materials produce hydrogen through the reformer, which is passed into the solid oxide fuel cell for power generation. During the startup phase, the heat required for the reforming reaction of the reformer is provided by the external fuel and air passing into the combustion shell to burn and release heat. After the stack is running stably, some unreacted raw materials remain in the tail gas generated by the stack, which can be passed into the combustion shell to replace the external fuel to continue burning and releasing heat, providing the heat required for the reformer to react. The highly integrated design greatly reduces the volume of the entire system, improves the overall volume energy ratio, and improves the utilization efficiency of the fuel.

Claims

1. A reforming hydrogen production reactor, characterized in that: include: A third shell has a third chamber inside, and an inlet structure for inputting water vapor and diesel into the third chamber is provided at the upper end of the third shell; A second shell is disposed in the third chamber, the second shell has a second chamber inside, and a third connecting passage connecting the third chamber and the second chamber is formed at the lower part of the second shell; A first shell is disposed in the second chamber, the first shell has a first chamber inside, and a second connecting passage connecting the second chamber and the first chamber is formed on the upper portion of the first shell; an outlet structure, disposed below the first shell and connected to the first chamber via a first connecting passage; A heating module is disposed in the first chamber; a reforming hydrogen production catalyst, disposed in the gap between the heating module and the first shell; The reforming hydrogen production catalyst comprises: Inorganic porous carrier; and, γ-Al2O3, NiO, CeO2 and Rh2O3 coated on an inorganic porous support.

2. The reforming hydrogen production reactor according to claim 1, characterized in that: The inlet structure comprises: A diesel pipeline, used for inputting diesel into the third chamber; A water vapor input mechanism, used for inputting water vapor into the third chamber, comprising a water vapor pipeline and two water vapor nozzles, wherein the water vapor pipeline is connected to the two water vapor nozzles via an arc-shaped branch channel; The two water vapor nozzles are symmetrically arranged with respect to the diesel pipeline, and the nozzles of the water vapor nozzles face toward the output end of the diesel pipeline.

3. The reforming hydrogen production reactor according to claim 1, characterized in that: The heating module comprises: A combustion shell, the interior of which is a combustion chamber; A fuel pipeline, connected to the combustion chamber, for providing fuel to the combustion chamber; an air duct connected to the combustion chamber and used to provide air to the combustion chamber; The combustion exhaust gas pipeline is connected to the combustion chamber and is used to discharge the combustion exhaust gas in the combustion chamber.

4. The reforming hydrogen production reactor according to claim 1, characterized in that: The upper end of the third shell is interference-fitted with the upper flange blind plate, the upper portion of the upper flange blind plate is connected to the flange upper cover, and the inlet structure is arranged on the flange upper cover.

5. The reforming hydrogen production reactor according to claim 1, characterized in that: The lower end of the first shell is interference fit with the lower flange blind plate, and the lower flange blind plate is connected to the flange lower cover; The outlet structure includes an outlet channel arranged on the flange lower cover, and an outlet chamber surrounded by the first shell, the lower flange blind plate and the flange lower cover. The first chamber is connected to the outlet chamber through the first connecting channel, and is connected to the outlet channel through the outlet chamber.

6. The reforming hydrogen production reactor according to claim 1, characterized in that: A first coating layer and a second coating layer outside the first coating layer are formed on the inorganic porous support, wherein the first coating layer contains γ-Al2O3, and the second coating layer contains NiO, CeO2 and Rh2O3.

7. The reforming hydrogen production reactor according to claim 1, characterized in that: The inorganic porous carrier is made of cordierite honeycomb ceramics.

8. The reforming hydrogen production reactor according to claim 1 or 6, characterized in that: The method for preparing the reforming hydrogen production catalyst comprises: S1, immersing the inorganic porous support in deionized water, and ultrasonically washing it at room temperature, taking it out, drying it, and cooling it to room temperature; S2, immersing the inorganic porous support obtained in step S1 in alumina sol, taking it out and drying it, heating it to 600°C and firing it, cooling it down to room temperature, and repeating the immersion, drying, firing and cooling operations in this step until the γ-Al2O3 coating amount reaches a preset value; S3, immersing the inorganic porous support obtained in step S2 in the mixed solution, taking it out and drying it, heating it to 700°C for calcination, cooling it to room temperature, and repeating the immersion, drying, calcination and cooling operations in this step until the coating amount of NiO, CeO2 and Rh2O3 reaches a preset value; The mixed solution comprises nickel nitrate, nickel acetate, cerium nitrate solution, and rhodium nitrate solution.

9. A fuel cell system, characterized in that: A reforming hydrogen production reactor having the structure described in any one of claims 1 to 8.

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