Inner smoke tube enhanced heat exchange type reforming hydrogen production reactor and use method thereof

Abstract

The invention provides an inner smoke tube enhanced heat exchange type reforming hydrogen production reactor and a using method thereof.The inner smoke tube enhanced heat exchange type reforming hydrogen production reactor comprises a reactor body, a circular sealing end cover and a supporting end cover are arranged at the upper end and the lower end of the reactor body respectively, and the sealing end cover and the supporting end cover are connected with an ellipsoidal upper seal head and an ellipsoidal lower seal head respectively; a feed gas inlet pipe is arranged at the center of the upper end socket, a reformed gas outlet pipe is arranged at the center of the lower end socket, a feed gas distributor is arranged at the joint of the feed gas inlet pipe and the upper end socket, and a reformed gas converging device is arranged at the joint of the reformed gas outlet pipe and the lower end socket. A flue gas inlet tangentially connected with the chamber of the reactor is formed in the side surface of the bottom of the chamber of the reactor, and a flue gas outlet tangentially connected with the chamber of the reactor is formed in the side surface of the top of the chamber of the reactor. According to the invention, high-temperature flue gas is in direct contact with the outer wall surface of the reaction tube and flows through the inner smoke tube, so that the heat exchange area is further increased, the heat exchange efficiency is improved, the reaction tube is heated more uniformly, and the efficiency of reforming reaction is improved.

Description

Technical Field

[0001] The present invention relates to the technical field of reforming hydrogen production, and in particular to an internally flue tube enhanced heat transfer reforming hydrogen production reactor and a method for using the same. Background Art

[0002] As a highly efficient and pollution-free renewable energy, hydrogen energy will become one of the most important parts of the energy structure in the future and plays an important role in assisting carbon emission reduction and accelerating energy transformation. Existing hydrogen production technologies mainly include coal gasification hydrogen production, electrolytic water hydrogen production, and steam reforming hydrogen production. Coal gasification hydrogen production is to convert organic substances in coal into hydrogen under the action of a gasifying agent at high temperature and high pressure. Coal gasification hydrogen production technology is mature and has low cost, but has a large amount of pollutant emissions and low purity of gas products; electrolytic water hydrogen production is to pass direct current into an electrolytic cell filled with electrolyte, and water molecules undergo an electrochemical reaction on the electrodes to decompose into hydrogen and oxygen. This method has high product purity and few impurities, but the maturity of electrolytic water hydrogen production is low and the energy consumption is high; steam reforming hydrogen production is a hydrogen production technology in which methane, methanol, etc. react with water vapor under the action of a catalyst to produce hydrogen and carbon monoxide. The carbon emission of steam reforming hydrogen production technology is much lower than that of coal gasification hydrogen production, and the cost is lower than that of electrolytic water hydrogen production. It has the advantages of high production efficiency and less water consumption, and is the most potential hydrogen production technology at present.

[0003] Most of the existing reforming hydrogen production reactors have problems such as low heating efficiency, uneven temperature field inside the reactor, and difficult catalyst loading and unloading, which affect the development of reforming hydrogen production technology. Therefore, there is an urgent need to develop an efficient reforming hydrogen production reactor with uniform internal temperature and simple catalyst loading and unloading to give full play to the advantages of reforming hydrogen production technology. Summary of the Invention

[0004] The purpose of the present invention is to provide an internally flue tube enhanced heat transfer reforming hydrogen production reactor and a method for using the same. The reactor has a reasonable structure design, can effectively improve the hydrogen production efficiency, simplify the maintenance and replacement of the catalyst, and has strong industrial application prospects.

[0005] According to an object of the present invention, the present invention provides an internal flue tube enhanced heat transfer reforming hydrogen production reactor, which includes a reactor, a plurality of reaction tubes and a burner. Circular sealing end covers and supporting end covers are respectively provided at the upper and lower ends of the reactor. The reaction tubes are connected to the sealing end covers and the supporting end covers. The sealing end covers and the supporting end covers are respectively connected with an ellipsoidal upper head and a lower head. A raw material gas inlet pipe is provided with an opening at the central position of the upper head, and a reformed gas outlet pipe is provided with an opening at the central position of the lower head. A raw material gas distributor is provided at the interface between the raw material gas inlet pipe and the upper head, and a reformed gas collector is provided at the interface between the reformed gas outlet pipe and the lower head. A flue gas inlet tangentially connected to the chamber of the reactor is provided on the side of the bottom of the chamber of the reactor, and the flue gas inlet is connected to the burner. A flue gas outlet tangentially connected to the chamber of the reactor is provided on the side of the top of the chamber of the reactor.

[0006] Further, the reactor includes a cylindrical chamber surrounded by a housing. A convex expansion groove is provided in the middle of the housing. Aluminum silicate fiber and refractory bricks are sequentially provided inside the housing, and the service temperature of the refractory bricks is ≥1300 °C.

[0007] Further, the raw material gas distributor and the reformed gas collector are frustum-shaped shell structures. The raw material gas distributor and the reformed gas collector respectively cover the raw material gas inlet pipe and the reformed gas outlet pipe. The upper ends of the raw material gas distributor and the reformed gas collector are sealed circular discs, and a plurality of inclined openings are evenly provided on the sides of the raw material gas distributor and the reformed gas collector.

[0008] Further, the included angle between the raw material gas distributor and the central axis of the reactor is 3-5°, and the included angle between the reformed gas collector and the central axis of the reactor is 1-3°.

[0009] Further, a plurality of installation holes are evenly provided on the sealing end covers and the supporting end covers. A plurality of the reaction tubes sequentially pass through the installation holes and are connected to the sealing end covers and the supporting end covers.

[0010] Further, an oppositely installed hole is respectively provided at the upper and lower ends of the reaction tube. An internal flue tube is provided inside the reaction tube, and the internal flue tube is connected to the two oppositely installed holes inside the reaction tube.

[0011] Further, a plurality of catalyst cages are placed inside the reaction tube. The catalyst cages are in a columnar bow structure. The catalyst cages include a bow-shaped cage bottom, a bow-shaped cage top, and a plurality of vertical strip-shaped cage frames for connecting the bow-shaped cage bottom and the bow-shaped cage top. The bow-shaped cage bottom is provided with a grille that is misaligned and does not intersect with the strip-shaped cage frames. Spherical catalysts are filled inside the catalyst cages.

[0012] Furthermore, the diameter of the catalyst is 3-5 mm larger than the gaps of the arcuate cage bottom grille and the strip cage frame.

[0013] According to another object of the present invention, the present invention provides a method for using the above-mentioned internally flue-tube enhanced heat transfer reforming hydrogen production reactor, including the following steps:

[0014] S1. The raw material gas enters the interior of the reactor through the raw material gas inlet pipe.

[0015] S2. Start the burner, and the high-temperature flue gas provided by the burner enters the bottom of the reactor chamber, and the flue gas enters the reactor through the flue gas inlet.

[0016] S3. The flue gas is in direct contact with the outer wall of the reaction tube for heat exchange. The flue gas directly heats the outer wall surface of the reaction tube. Part of the flue gas flows into the internal flue tube, increasing the heat exchange area between the reaction tube and the raw material gas and improving the heat exchange efficiency. The catalyst cage is filled inside the reaction tube, and the catalyst inside the catalyst cage is heated simultaneously to ensure uniform reaction temperature inside the reaction tube, thereby optimizing the reaction process and ensuring stable production of hydrogen.

[0017] S4. After the reforming reaction is completed, hydrogen and other by-products are converged to the reformed gas outlet pipe through the reformed gas manifold and finally discharged from the lower head of the reactor.

[0018] Furthermore, in S1, the raw material gas enters the upper head of the reactor through the raw material gas inlet pipe and is evenly distributed to each reaction tube by the raw material gas distributor.

[0019] The technical solution of the present invention is the structural design of the internal flue tube in the reactor. The high-temperature flue gas is in direct contact with the outer wall surface of the reaction tube, and the heat exchange area is further increased by flowing through the internal flue tube, improving the heat exchange efficiency, making the heating of the reaction tube more uniform, ensuring the same temperature inside the reaction tube, and thus improving the efficiency of the reforming reaction. By setting the raw material gas distributor and the reformed gas manifold, the gas flow direction inside the reactor is more stable, thereby effectively improving the stability of the reactor and reducing the reaction efficiency fluctuation caused by unstable gas flow. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] In order to more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the following will briefly introduce the drawings required for the description of the specific embodiments or the prior art. Obviously, the following drawings are some embodiments of the present invention. For those of ordinary skill in the art, other drawings can be obtained based on these drawings without creative efforts.

[0021] Figure 1 It is a schematic structural diagram of an embodiment of the present invention;

[0022] Figure 2 Structural schematic diagram of the reaction tube according to an embodiment of the present invention;

[0023] Figure 3 Structural schematic diagram of the catalyst cage according to an embodiment of the present invention;

[0024] In the figure: 1. Reactor; 11. Outer shell; 12. Upper head; 13. Lower head; 14. Feed gas inlet pipe; 15. Reformed gas outlet pipe; 16. Sealing end cover; 17. Support end cover; 18. Feed gas distributor; 19. Reformed gas collector; 2. Reaction tube; 21. Inner flue tube; 22. Catalyst cage; 221. Arch-shaped cage bottom; 222. Strip-shaped cage frame; 223. Arch-shaped cage top; 23. Bracket; 3. Burner; 31. Flue gas inlet; 32. Flue gas outlet. Detailed implementation manners

[0025] The technical solutions of the present invention will be clearly and completely described below in conjunction with the embodiments. Obviously, the described embodiments are part of the embodiments of the present invention, rather than all of them. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present invention without creative efforts shall fall within the protection scope of the present invention.

[0026] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "transverse", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc. indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as a limitation to the present invention.

[0027] In addition, the terms "first" and "second" are only used for descriptive purposes, and cannot be construed as indicating or implying relative importance or implicitly indicating the quantity of the indicated technical features. Thus, the features defined with "first" and "second" may explicitly or implicitly include one or more of the described features. In the description of the present invention, "a plurality" means two or more, unless otherwise specifically defined. In addition, the terms "installation", "connection" and "connection" should be understood in a broad sense. For example, it may be a fixed connection, a detachable connection, or an integral connection; it may be a mechanical connection or an electrical connection; it may be directly connected, or indirectly connected through an intermediate medium, and it may be the internal communication of two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0028] Embodiment 1

[0029] As Figures 1 - 3 shown:

[0030] An internal smoke pipe enhanced heat transfer reforming hydrogen production reactor, comprising a reactor 1, a plurality of reaction tubes 2 and a burner 3; wherein:

[0031] The main body part of the reactor 1 is a cylindrical chamber surrounded by a housing 11. A convex expansion groove is provided at the central position of the housing 11 of the reactor 1. Inside the housing 11, aluminum silicate fiber and refractory bricks are sequentially provided, and the service temperature of the refractory bricks is ≥1300 °C. The refractory layer and heat insulation layer provided in the reactor can avoid heat loss and improve the thermal efficiency of the reactor.

[0032] Circular sealing end caps 16 and circular support end caps 17 are respectively provided at the upper and lower ends of the chamber of the reactor 1. Flanges are provided on the circumferences of the sealing end caps 16 and the support end caps 17 and are respectively connected to the ellipsoidal upper head 12 and the lower head 13.

[0033] A raw material gas inlet pipe 14 is provided with an opening at the central position of the upper head 12, and a reformed gas outlet pipe 15 is provided with an opening at the central position of the lower head 13. A raw material gas distributor 18 is provided at the interface between the raw material gas inlet pipe 14 and the upper head 12, and a reformed gas collector 19 is provided at the interface between the reformed gas outlet pipe 15 and the lower head 13.

[0034] In this embodiment, the raw material gas distributor 18 and the reformed gas collector 19 are frustum-shaped shell structures. The raw material gas distributor 18 and the reformed gas collector 19 are respectively connected to the upper head 12 and the lower head 13, and respectively cover the raw material gas inlet pipe 14 and the reformed gas outlet pipe 15. The upper ends of the raw material gas distributor 18 and the reformed gas collector 19 are sealed circular discs, and a plurality of inclined openings are evenly formed on the sides of the raw material gas distributor 18 and the reformed gas collector 19.

[0035] In this embodiment, the included angle between the inclined opening of the raw material gas distributor 18 and the central axis of the reactor 1 is 3-5°, and the included angle between the inclined opening of the reformed gas collector 19 and the central axis of the reactor 1 is 1-3°.

[0036] As Figure 1 shown, a flue gas inlet 31 whose one end is tangentially connected to the chamber bottom side of the reactor 1 is provided on the side of the chamber bottom of the reactor 1. The flue gas inlet 31 is connected to the burner 3, and a flue gas outlet 32 tangentially connected to it is provided on the side of the chamber top of the reactor 1.

[0037] The sealing end cap 16 and the support cover plate 17 are evenly provided with a plurality of mounting holes. A plurality of reaction tubes 2 sequentially pass through the mounting holes and are connected to the sealing end cap 16 and the support cover plate 17. The reaction tubes 2 extend out of the sealing end cap 16 and the support end cap 17 by a certain length. Specifically, in this embodiment, the length of the reaction tubes 2 extending out of the sealing end cap 16 and the support end cap 17 is 1-3 mm.

[0038] As Figure 1 and Figure 2 shown, near the upper and lower ends of the reaction tube 2, one installation hole is respectively opened in opposite directions. An inner smoke tube 21 is arranged inside the reaction tube 2, and the inner smoke tube 21 is connected to the two installation holes in opposite directions inside the reaction tube 2. A number of catalyst cages 22 are also placed in the reaction tube 2. A bracket 23 is arranged near the end of the lower part of the reaction tube 2, and the bracket 23 is used to support the catalyst cage 22.

[0039] As Figure 3 shown, in this embodiment, the catalyst cage 22 has a columnar bow-shaped structure, including a bow-shaped cage bottom 221, a bow-shaped cage top 223, and a number of vertical strip-shaped cage frames 222 for connecting the bow-shaped cage bottom 221 and the bow-shaped cage top 223. The bow-shaped cage bottom 221 is also provided with a grille that is offset and non-intersecting with the strip-shaped cage frames 222. The bow-shaped cage bottom 221 and the bow-shaped cage top 223 have the same shape, and the height of the bow is 3-5 mm less than the inner radius of the reaction tube 2. The catalyst cage 22 is filled with a catalyst, and the catalyst is spherical, and its diameter is 3-5 mm larger than the gap of the grille of the bow-shaped cage bottom 221 and the gap of the strip-shaped cage frames 222.

[0040] The reforming hydrogen production reactor of the present invention uses an inner smoke tube to enhance heat exchange, and the heat exchange method is simple; the high-temperature flue gas directly contacts the outer wall surface of the reaction tube, and the heat exchange method is simple and effective; an inner smoke tube 21 is arranged inside the reaction tube 2. While the flue gas heats the outer wall surface of the reaction tube 2, part of it flows into the inner smoke tube 21, increasing the heat exchange area between the reaction tube 2 and the raw material gas. The catalysts in each part of the catalyst cage 22 are heated simultaneously, and the heated temperature is the same, ensuring that the temperature inside the reaction tube is uniform and the heat transfer rate is fast; at the same time, the arranged raw material gas distributor 18 and reformed gas collector 19 can make the gas flow direction inside the reactor stable and improve the stability of the reactor; a sealing end cover is arranged at the upper end of the reactor and is connected to the reactor shell to isolate the flue gas heating cavity from the raw material gas buffer cavity; in addition, the arranged head and catalyst cage are convenient for disassembly, facilitating the loading and unloading of the catalyst cage.

[0041] In this embodiment, the raw material gas is a mixed gas including at least one of natural gas, biogas, pyrolysis gas, etc. and water vapor. The raw material gas enters the reactor 1 from the raw material gas inlet pipe 14.

[0042] When the present invention is in use:

[0043] The raw material gas enters the chamber of the reactor 1 through the raw material gas inlet pipe 14; the raw material gas needs to maintain a certain flow rate and pressure to ensure that it can smoothly enter the reactor and be evenly distributed.

[0044] Start the burner 3, and the high-temperature flue gas provided by the burner enters the bottom of the chamber of the reactor 1, and the flue gas enters the reactor through the flue gas inlet 31;

[0045] The flue gas is in direct contact with the outer wall of the reaction tube 2 for heat exchange. The temperature of the flue gas generally needs to reach a sufficiently high value (usually within the high-temperature range, such as above 600 °C) to ensure the heating effect.

[0046] Specifically, the raw material gas enters the upper head 12 of the reactor 1 through the raw material gas inlet pipe 14 and is evenly distributed to each reaction tube 2 by the raw material gas distributor 18.

[0047] The reaction tube 2 is filled with a catalyst cage 22 inside. The raw material gas passes through the reaction tube, and the catalyst in the catalyst cage 22 is heated and undergoes a steam reforming reaction to produce hydrogen and other by-products.

[0048] At the same time, the flue gas will enter the inner flue tube 21 to further improve the heat exchange efficiency between the outer wall and the inner wall of the reaction tube 2.

[0049] The flue gas directly heats the outer wall surface of the reaction tube 2, and part of the flue gas flows into the inner flue tube 21, increasing the heat exchange area between the reaction tube 2 and the raw material gas and improving the heat exchange efficiency.

[0050] The catalyst inside the catalyst cage 22 is heated simultaneously to ensure uniform reaction temperature inside the reaction tube, thereby optimizing the reaction process and ensuring stable production of hydrogen.

[0051] After the reforming reaction is completed, hydrogen and other by-products are converged to the reformed gas outlet pipe 15 through the reformed gas collector 19 and finally discharged from the lower head 13 of the reactor.

[0052] During this process, the reformed gas collector 19 ensures smooth gas flow, avoids gas stagnation and uneven distribution, and improves the overall stability and efficiency of the reactor.

[0053] The present invention overcomes the defects of the existing reforming hydrogen production reactor, such as low heating efficiency, uneven internal temperature field, and difficult catalyst loading and unloading. The reactor has a compact structure, is easy to disassemble and assemble, has a uniform internal temperature field, and has a high heat exchange efficiency between the flue gas and the reaction tube, and can effectively realize steam reforming hydrogen production.

[0054] The reforming hydrogen production reactor of the present invention uses high-temperature flue gas to supply heat to each reaction tube. The high-temperature flue gas enters the reactor from the flue gas inlet at the bottom of the reforming hydrogen production reactor and is discharged from the flue gas outlet at the upper part of the reactor. The high-temperature flue gas is in direct contact with the outer wall surface of the reaction tube, and the heat exchange method is simple and effective; an inner flue tube is provided inside the reaction tube. While the flue gas heats the outer wall surface of the reaction tube, part of it flows into the inner flue tube, increasing the heat exchange area between the reaction tube and the raw material gas. The catalysts in each part of the catalyst cage are heated simultaneously and have the same heating temperature, ensuring uniform temperature inside the reaction tube, fast heat transfer rate, and at the same time, it can also increase the strength of the reaction tube, prevent its deformation, and improve the reforming hydrogen production efficiency; a refractory layer and a heat insulation layer are provided on the outer layer of the reactor to avoid heat loss.

[0055] In the reaction tube of the reforming hydrogen production reactor of the present invention, a number of hollow catalyst cages that can be lifted up and down are also provided. A catalyst cage bracket is arranged at the bottom of the reaction tube to carry the catalyst cages in the reaction tube. The catalyst cages are filled with catalysts. After the raw material gas enters the reaction tube through the head, it passes through each catalyst cage in turn;

[0056] At the interface between the raw material gas inlet pipe of the reactor of the present invention and the upper head, a frustum-shaped distributor is provided. The distributor housing is provided with a number of obliquely arranged openings. After the raw material gas enters the distributor, it enters the head through each obliquely arranged opening. The raw material gas is evenly distributed in the head and then evenly flows into the reaction tubes at different positions. The reaction degree inside the reaction tubes is consistent; at the interface between the reformed gas outlet pipe of the reactor and the lower head, a reformed gas collector is provided. After the raw material gas undergoes a reforming reaction in each reaction tube, it enters the lower head. The reformed gas converges to the reformed gas outlet pipe through the obliquely arranged openings of the collector. The distributor and collector provided can make the gas flow direction inside the reactor stable and improve the stability of the reactor; a sealing end cover is arranged at the upper end of the reactor and is connected to the reactor shell to isolate the flue gas heating cavity and the raw material gas buffer cavity. At the same time, the head is arranged to be convenient for disassembly, which is convenient for the loading and unloading of the catalyst cages.

[0057] Finally, it should be noted that: the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, those of ordinary skill in the art should understand that: they can still modify the technical solutions recorded in the foregoing embodiments, or perform equivalent replacements on some or all of the technical features; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. An internal smoke tube enhanced heat exchange reforming hydrogen production reactor, characterized in that: It includes a reactor, a plurality of reaction tubes and a burner, wherein a circular sealing end cover and a supporting end cover are respectively provided at the upper and lower ends of the reactor, the reaction tube is connected to the sealing end cover and the supporting end cover, the sealing end cover and the supporting end cover are respectively connected to an ellipsoidal upper head and a lower head, a hole is opened at the center position of the upper head to set a raw gas inlet pipe, a hole is opened at the center position of the lower head to set a reforming gas outlet pipe, a raw gas distributor is provided at the interface between the raw gas inlet pipe and the upper head, a reforming gas merger is provided at the interface between the reforming gas outlet pipe and the lower head, a flue gas inlet tangentially connected to the chamber of the reactor is provided on the side of the bottom of the chamber of the reactor, the flue gas inlet is connected to the burner, and a flue gas outlet tangentially connected to the chamber of the reactor is provided on the side of the top of the chamber of the reactor.

2. The inner smoke tube enhanced heat exchange reforming hydrogen production reactor according to claim 1, characterized in that: The reactor comprises a cylindrical chamber surrounded by an outer shell, a convex expansion groove is arranged in the middle of the outer shell, aluminum silicate fibers and refractory bricks are arranged in sequence inside the outer shell, and the use temperature of the refractory bricks is ≥1300°C.

3. The inner smoke tube enhanced heat exchange reforming hydrogen production reactor according to claim 1, characterized in that: The raw gas distributor and the reformed gas manifold are truncated cone-shaped shell structures, and the raw gas distributor and the reformed gas manifold respectively cover the raw gas inlet pipe and the reformed gas outlet pipe. The upper ends of the raw gas distributor and the reformed gas manifold are sealing discs, and the sides of the raw gas distributor and the reformed gas manifold are evenly provided with a number of oblique openings.

4. The inner smoke tube enhanced heat exchange reforming hydrogen production reactor according to claim 3, characterized in that: The angle between the raw gas distributor and the central axis of the reactor is 3-5°, and the angle between the reformed gas confluence device and the central axis of the reactor is 1-3°.

5. The internal smoke tube enhanced heat exchange reforming hydrogen production reactor according to claim 1, characterized in that: The sealing end cover and the supporting end cover are evenly provided with a plurality of mounting holes, and a plurality of the reaction tubes pass through the mounting holes in sequence and are connected to the sealing end cover and the supporting end cover.

6. The inner smoke tube enhanced heat exchange reforming hydrogen production reactor according to claim 1, characterized in that: An opposite mounting hole is respectively provided at the upper and lower ends of the reaction tube, an inner smoke pipe is provided inside the reaction tube, and the inner smoke pipe is connected to the two opposite mounting holes in the reaction tube.

7. The internal smoke tube enhanced heat exchange reforming hydrogen production reactor according to claim 1, characterized in that: A plurality of catalyst cages are placed in the reaction tube. The catalyst cages include an arched cage bottom, an arched cage top and a plurality of vertical bar cage frames for connecting the arched cage bottom and the arched cage top. The interior of the catalyst cages is filled with spherical catalysts.

8. The inner smoke tube enhanced heat exchange reforming hydrogen production reactor according to claim 7, characterized in that: The diameter of the spherical catalyst is larger than the grid gap of the arched cage bottom grid and the gap of the bar cage frame.

9. The method for using the inner smoke tube enhanced heat exchange reforming hydrogen production reactor according to claim 1, characterized in that: The steps include: S1, the raw gas enters the reactor through the raw gas inlet pipe; S2, start the burner, and the high-temperature flue gas provided by the burner enters the bottom of the reactor chamber, and the flue gas enters the reactor through the flue gas inlet; S3, the flue gas is in direct contact with the outer wall of the reaction tube for heat exchange, the flue gas directly heats the outer wall of the reaction tube, and part of the flue gas flows into the inner flue tube, increasing the heat exchange area between the reaction tube and the raw gas, and improving the heat exchange efficiency; the reaction tube is filled with a catalyst cage, and the catalyst inside the catalyst cage is heated at the same time, ensuring that the reaction temperature in the reaction tube is uniform, thereby optimizing the reaction process and ensuring the stable production of hydrogen; S4. After the reforming reaction is completed, hydrogen and other by-products are converged to the reforming gas outlet pipe through the reforming gas manifold and finally discharged from the lower head of the reactor.

10. The method for using the inner smoke tube enhanced heat exchange reforming hydrogen production reactor according to claim 9, characterized in that: In S1, the raw gas enters the upper head of the reactor through the raw gas inlet pipe and is evenly distributed to each reaction tube by the raw gas distributor.

Images