Centripetal fin type reforming hydrogen production reactor

Abstract

The invention provides a centripetal fin type reforming hydrogen production reactor which comprises a reactor main body, the reactor comprises a cylindrical cavity, circular sealing end covers are arranged at the two ends of the cylindrical cavity respectively, reaction tubes are connected with the circular sealing end covers, centripetal fins are arranged in the reaction tubes, and a flue gas inlet is formed in the bottom of the reactor. A flue gas outlet is formed in the top of the reactor, a plurality of catalyst cages are placed at the bottom in the reaction tube, and a spiral guide plate is welded outside the reaction tube. High-temperature flue gas is adopted to supply heat to the reaction tube, enters from the flue gas inlet, is discharged from the upper flue gas outlet under the guidance of the guide plate, and is directly contacted with the wall surface of the reaction tube, so that the heat exchange mode is simple and effective; the centripetal fins on the inner wall surface of the reaction tube increase the heat exchange area of the wall surface of the reaction tube and feed gas, and catalysts in the catalyst cage are heated at the same time, so that uniform temperature in the reaction tube and high heat transfer rate are ensured, the strength of the reaction tube is increased, deformation is prevented, and the reforming hydrogen production efficiency is improved.

Description

Technical Field

[0001] The invention relates to the technical field of reforming hydrogen production, and in particular to a centripetal fin type reforming hydrogen production reactor. Background Art

[0002] At present, most countries rely on fossil fuels such as coal, oil, and natural gas for energy production. The use of these energy sources produces a large amount of carbon dioxide emissions, leading to serious greenhouse effects and climate change. Hydrogen energy, as an efficient and pollution-free energy source, can replace traditional fossil energy and occupy an important position in the future energy structure.

[0003] Existing hydrogen production technologies mainly include coal gasification, water electrolysis and steam reforming. Steam reforming is the most promising hydrogen production method. Although it has lower carbon emissions and lower production costs, the existing reactors have some problems, such as low heating efficiency, uneven temperature inside the reactor, and difficulty in loading and unloading catalysts, which restrict its further application and development. Summary of the invention

[0004] The object of the present invention is to provide a centripetal fin type reforming hydrogen production reactor, which significantly improves the reforming hydrogen production efficiency and reduces energy consumption and operating costs through efficient heat exchange, uniform temperature distribution and optimized catalyst loading and unloading design.

[0005] According to one object of the present invention, the present invention provides a centripetal fin type reforming hydrogen production reactor, including a reactor body, a plurality of reaction tubes and a flue gas heater, the reactor including a cylindrical chamber, circular sealing end covers are respectively provided at both ends of the cylindrical chamber, a plurality of reaction tubes are connected to the circular sealing end covers, centripetal fins are provided inside the reaction tube, a flue gas inlet is provided at the bottom of the reactor, a flue gas outlet is provided at the top of the reactor, a plurality of catalyst cages are placed at the bottom of the reaction tube, and a spiral guide plate is welded to the outside of the reaction tube.

[0006] Furthermore, flanges are provided on the circumferences of the upper and lower circular sealing end covers and respectively connect the upper and lower ellipsoidal heads. A raw gas inlet pipe is provided at the center opening of the top ellipsoidal head, and a reformed gas outlet pipe is provided at the center opening of the bottom ellipsoidal head.

[0007] Furthermore, the other end of the smoke inlet is connected to a smoke heater.

[0008] Furthermore, the reactor includes an insulation layer, a fire-resistant layer is provided on the inner side of the insulation layer, an outer shell is provided on the outer side of the insulation layer, and support cover plates connected to the circular sealing cover plate are respectively provided at the upper and lower ends of the outer shell; a convex expansion groove is provided in the center of the outer shell.

[0009] Furthermore, the circular sealing end cover is 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 circular sealing end cover.

[0010] Furthermore, the reaction tube protrudes from the top of the circular sealing end cover by 1-3 mm.

[0011] Furthermore, a catalyst cage bracket is provided below the reaction tube near the end.

[0012] Furthermore, the catalyst cage includes a catalyst cage wall, a catalyst cage bottom vertically arranged with respect to the catalyst cage wall, a hook located on the upper surface of the catalyst cage wall, and a hook groove located at the catalyst cage bottom corresponding to the hook.

[0013] Furthermore, the catalyst cage is filled with a catalyst, and the catalyst is spherical.

[0014] Furthermore, the catalyst cage wall includes an annular cage wall surface with a notch and a groove connected to the notch.

[0015] The technical solution of the present invention adopts 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 reactor through the flue gas outlet at the upper part of the reactor under the guidance of the guide plate. The high-temperature flue gas directly contacts the wall of the reaction tube, and the heat exchange method is simple and effective. The inner wall of the reaction tube is provided with centripetal fins to increase the heat exchange area between the wall of the reaction tube and the raw gas. The catalysts at various locations in the catalyst cage are heated at the same time, and the heating temperature is consistent, thereby ensuring that the temperature inside the reaction tube is uniform and the heat transfer rate is fast. At the same time, the strength of the reaction tube can be increased to prevent its deformation, thereby improving the reforming hydrogen production efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] In order to more clearly illustrate the specific implementation methods of the present invention or the technical solutions in the prior art, the drawings required for use in the specific implementation methods or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are some implementation methods of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0017] Figure 1 It is a structural schematic diagram of an embodiment of the present invention;

[0018] Figure 2 This is a schematic diagram of the structure of a reaction tube according to an embodiment of the present invention;

[0019] Figure 3 This is a front view of a catalyst cage according to an embodiment of the present invention;

[0020] Figure 4A top view of a catalyst cage according to an embodiment of the present invention;

[0021] Figure 5 It is a bottom view of the catalyst cage according to an embodiment of the present invention.

[0022] In the figure: 1, reactor; 11, ellipsoidal head; 12, raw gas inlet pipe; 13, reformed gas outlet pipe; 14, circular sealing end cover;

[0023] 2-insulation layer; 21, shell; 22, support cover;

[0024] 3-reaction tube; 31, heat transfer fins; 32, catalyst cage; 321, catalyst cage wall; 322, catalyst cage bottom; 323, hook; 324, hook slot; 33, catalyst cage bracket;

[0025] 4. Flue gas heater; 41. Flue gas inlet; 42. Guide plate; 43. Flue gas outlet. DETAILED DESCRIPTION

[0026] The technical solution 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 the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0027] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", "counterclockwise" and the like indicating directions or positional relationships are based on the directions or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific direction, be constructed and operated in a specific direction, and therefore should not be understood as limiting the present invention.

[0028] In addition, the terms "first" and "second" are only used for descriptive purposes and cannot be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Therefore, the features defined as "first" and "second" may explicitly or implicitly include one or more of the features. In the description of the present invention, "multiple" means two or more, unless otherwise clearly and specifically defined. In addition, the terms "installed", "connected" and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal connection of two components. 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.

[0029] Example 1

[0030] like Figure 1-Figure 5 As shown,

[0031] A centripetal fin reforming hydrogen production reactor comprises a reactor 1, the main part of the reactor 1 comprises a cylindrical chamber surrounded by a heat-insulating layer 2, two circular sealing end covers 14 are arranged at the upper and lower ends of the cylindrical chamber of the reactor 1, flanges are arranged on the circumferences of the upper and lower circular sealing end covers 14 and are respectively connected to upper and lower ellipsoidal heads 11, a raw gas inlet pipe 12 is arranged at a hole at the center of the ellipsoidal head 11 at the top, and a reformed gas outlet pipe 13 is arranged at a hole at the center of the ellipsoidal head 11 at the bottom;

[0032] A flue gas inlet 41 is provided on the bottom side of the cylindrical chamber of the reactor 1, one end of which is tangentially connected to the cylindrical chamber, and the other end of the flue gas inlet 41 is connected to the flue gas heater 4; a flue gas outlet 43 is provided on the top side of the cylindrical chamber of the reactor 1, which is tangentially connected to the cylindrical chamber of the reactor 1;

[0033] A fire-resistant layer is provided inside the insulation layer 2, and an outer shell 21 is provided outside the insulation layer 2. The upper and lower ends of the outer shell 21 are respectively provided with support cover plates 22 connected to the circular sealing cover plate 14; a convex expansion groove is provided in the center of the outer shell 21.

[0034] The circular sealing end cover 14 is evenly provided with a plurality of mounting holes, and a plurality of reaction tubes 3 are sequentially passed through the mounting holes and connected to the circular sealing end cover 14. The reaction tubes 3 protrude a certain height from the top of the circular sealing end cover 14. In this embodiment, the height of the reaction tubes 3 protruding from the circular sealing cover plate 14 is 1-3 mm.

[0035] Strip-shaped heat transfer fins 31 are provided inside the reaction tube 3; the heat transfer fins 31 are in the form of centripetal fins, which can increase the heat exchange area with the high-temperature flue gas.

[0036] A spiral guide plate 42 is welded to the outside of the reaction tube 3 ; a plurality of catalyst cages 32 are placed at the bottom of the reaction tube 3 , and a catalyst cage bracket 33 is provided below each reaction tube 3 near the end thereof, and the catalyst cage bracket 33 is used to support the catalyst cage 32 .

[0037] In this embodiment, the flue gas inlet 41 at the bottom of the high-temperature flue gas reactor 1 enters the reactor 1, and is guided by the guide plate 42 to the flue gas outlet 43 at the upper part of the reactor 1 to discharge the reactor 1. The direct contact heat exchange method is simple and efficient.

[0038] The inner wall of the reaction tube 3 is provided with centripetal heat transfer fins 31, which can increase the heat exchange area between the reaction tube wall and the high-temperature flue gas. The catalysts in the catalyst cage 32 are heated at the same time, and the heating temperature is consistent. The temperature inside the reaction tube 3 is uniform, the heat transfer rate is fast, the thermal intensity is high, and the reforming hydrogen production efficiency is high.

[0039] The flue gas heater and heat exchange method of this embodiment: a flue gas inlet 41 is provided at the bottom of the reactor, and high-temperature flue gas is introduced through the flue gas heater 4. The flue gas flows to the upper part of the reactor 1 under the guidance of the guide plate 42, and directly contacts the wall surface of the reaction tube 3 through heat exchange, thereby improving the heat exchange efficiency. The flue gas outlet 43 is provided on the top side of the reactor 1 to facilitate the discharge of the flue gas.

[0040] The outer layer of the reactor 1 is provided with a fire-resistant layer and a heat-insulating layer to prevent heat loss. The heat-insulating layer and the outer shell of this embodiment: The outer layer of the reactor is provided with a fire-resistant layer and a heat-insulating layer to prevent heat loss. A support cover is provided on the outer shell to ensure the stability of the reactor.

[0041] At the same time, a number of catalyst cages 32 that can be pulled up and down are also provided in the reaction tube 3. A catalyst cage bracket 33 is provided at the bottom of the reaction tube 3 to support the catalyst cages 32 in the reaction tube. The catalyst cages 32 are filled with catalysts. After the raw gas enters the reaction tube 3 through the raw gas inlet pipe 12 on the upper ellipsoidal head 11, it passes through each catalyst cage 32 in turn. The bottom surface of the catalyst cage 32 has holes for facilitating the flow of the raw gas in the reaction tube 3. At the same time, the openings are arranged in a ring shape along the center of the catalyst cage 32, thereby improving the dispersion of the raw gas in the reaction tube 3 and stabilizing the raw gas flow.

[0042] The design of the catalyst cage in this embodiment is that the reaction tube is provided with a catalyst cage, and the catalyst is filled inside the catalyst cage. After the raw gas enters the reaction tube through the head, it passes through each catalyst cage in turn to ensure uniform heating of the catalyst. The catalyst cage has the function of being pulled up and down, which is convenient for loading, unloading and replacing the catalyst. In this embodiment, the raw gas is a mixed gas including at least one of natural gas, biogas, pyrolysis gas, etc. and water vapor.

[0043] In this embodiment, the catalyst cage 32 includes a catalyst cage wall 321, a catalyst cage bottom 322 arranged perpendicular to the catalyst cage wall 321, a hook 323 located on the upper surface of the catalyst cage wall 321, and a hook groove 324 located at the catalyst cage bottom 322 corresponding to the hook 323, the length of the hook groove 324 is greater than 1-2 mm of the length of the hook 323, and the width of the hook groove 324 is greater than 1-2 mm of the width of the hook 323.

[0044] The catalyst cage wall 321 includes an annular cage wall surface with a notch and a groove connected to the notch. The diameter of the annular cage wall surface is 1-3 mm smaller than the diameter of the reaction tube 3. The length of the groove of the catalyst cage wall 321 is 1-3 mm greater than the length of the heat transfer fin 31. The width of the groove of the catalyst cage wall 321 is 1-3 mm greater than the width of the heat transfer fin 31.

[0045] The catalyst cage bottom 322 has a plurality of holes with a diameter of 5-10 mm. The catalyst cage 32 is filled with a catalyst in a spherical shape with a diameter larger than the hole diameter of the catalyst cage bottom 322 by 3-5 mm.

[0046] The centripetal fin reforming hydrogen production reactor of the present invention has a simple and efficient heat exchange mode, a uniform temperature inside the reaction tube, a fast heat transfer rate, high thermal strength, and a high reforming hydrogen production efficiency. The design of the catalyst cage makes the raw gas dispersed evenly and flowed stably. The reactor device is compact as a whole and is easy to disassemble and assemble.

[0047] The reforming hydrogen production reactor of the present invention uses high-temperature flue gas to heat 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 guided by the guide plate to the flue gas outlet at the upper part of the reactor to discharge the reactor. The high-temperature flue gas directly contacts the wall of the reaction tube, and the heat exchange method is simple and effective. The inner wall of the reaction tube is provided with centripetal fins to increase the heat exchange area between the wall of the reaction tube and the raw gas. The catalysts at various locations in the catalyst cage are heated at the same time, and the heating temperature is consistent, ensuring that the temperature inside the reaction tube is uniform and the heat transfer rate is fast. At the same time, the strength of the reaction tube can be increased to prevent its deformation, thereby improving the reforming hydrogen production efficiency. The outer layer of the reactor is provided with a refractory layer and a thermal insulation layer to prevent heat loss.

[0048] At the same time, a number of catalyst cages that can be pulled up and down are also arranged in the reaction tube of the reforming hydrogen production reactor. A catalyst cage bracket is arranged at the bottom of the reaction tube to support the catalyst cage in the reaction tube. The catalyst cage is filled with catalyst. After the raw gas enters the reaction tube through the head, it passes through each catalyst cage in turn. The holes on the bottom of the catalyst cage are convenient for the raw gas to flow in the reaction tube. At the same time, the openings are arranged in a ring shape along the center of the catalyst cage to improve the dispersion of the raw gas in the reaction tube and stabilize the raw gas flow. A sealed end cover is arranged at the upper end of the reactor and is connected to the insulation layer cover to isolate the flue gas heating cavity from the raw gas buffer cavity. At the same time, the head is arranged to facilitate disassembly, which is convenient for the loading and unloading of the catalyst cage.

[0049] 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 aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or replace some or all of the technical features therein with equivalents. However, these modifications or replacements do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A centripetal fin reforming hydrogen production reactor, characterized in that: It includes a reactor, a plurality of reaction tubes and a flue gas heater. The reactor includes a cylindrical chamber. Both ends of the cylindrical chamber are respectively provided with circular sealing end covers. A plurality of reaction tubes are connected to the circular sealing end covers. Centripetal fins are provided inside the reaction tube. A flue gas inlet is provided at the bottom of the reactor. A flue gas outlet is provided at the top of the reactor. A plurality of catalyst cages are placed at the bottom of the reaction tube. A spiral guide plate is welded to the outside of the reaction tube.

2. The centripetal fin reforming hydrogen production reactor according to claim 1, characterized in that: The circumference of the upper and lower circular sealing end covers is provided with flanges and respectively connects the upper and lower ellipsoidal heads. The center position of the ellipsoidal head located at the top is opened with a raw gas inlet pipe, and the center position of the ellipsoidal head located at the bottom is opened with a reformed gas outlet pipe.

3. The centripetal fin reforming hydrogen production reactor according to claim 1, characterized in that: The other end of the smoke inlet is connected to a smoke heater.

4. The centripetal fin reforming hydrogen production reactor according to claim 1, characterized in that: The reactor comprises an insulation layer, a fire-resistant layer is arranged on the inner side of the insulation layer, an outer shell is arranged on the outer side of the insulation layer, and support cover plates connected to the circular sealing cover plate are arranged at the upper and lower ends of the outer shell respectively; a convex expansion groove is arranged in the middle of the outer shell.

5. The centripetal fin reforming hydrogen production reactor according to claim 1, characterized in that: The circular sealing end cover is 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 with the circular sealing end cover.

6. The centripetal fin reforming hydrogen production reactor according to claim 5, characterized in that: The top of the reaction tube exceeds the top height of the circular sealing end cover by 1-3 mm.

7. The centripetal fin reforming hydrogen production reactor according to claim 1, characterized in that: A catalyst cage bracket is provided below the reaction tube near the end.

8. The centripetal fin reforming hydrogen production reactor according to claim 1, characterized in that: The catalyst cage includes a catalyst cage wall, a catalyst cage bottom vertically arranged with respect to the catalyst cage wall, a hook located on the upper surface of the catalyst cage wall, and a hook groove located at the catalyst cage bottom and corresponding to the hook.

9. The centripetal fin reforming hydrogen production reactor according to claim 1, characterized in that: The catalyst cage is filled with a catalyst, and the catalyst is spherical.

10. The centripetal fin reforming hydrogen production reactor according to claim 8, characterized in that: The catalyst cage wall comprises an annular cage wall surface with a notch and a groove connected to the notch.

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