Heat exchange component, steam reforming hydrogen production conversion tube and steam reforming hydrogen production reforming furnace

Abstract

The present invention provides a heat exchange component for steam reforming hydrogen production, and its heat exchange medium includes a raw material gas and a reformed gas. The heat exchange component includes a first heat exchange part, a second heat exchange part and a gas flow reversal part. The first heat exchange part is configured to include an inner reformed gas cooling channel and an outer raw material gas heating channel; the second heat exchange part is configured to include a reformed gas heat dissipation gas path and a raw material gas heat absorption gas path; the gas flow diversion part is configured to fluidly connect the outer raw material gas heating channel to the raw material gas heat absorption gas path, and fluidly connect the reformed gas heat dissipation gas path to the inner reformed gas cooling channel. In the flow direction of the raw material gas, the second heat exchange part is located downstream of the first heat exchange part. The present invention also provides a steam reforming hydrogen production conversion tube and a reforming furnace. The present invention can reduce the heat loss at the location of the first heat exchange part, improve the heat utilization rate, enable the heat to be more effectively used for heating the raw material gas, and is conducive to the miniaturized design of the device.

Description

Technical Field

[0001] The present invention relates to the technical field of hydrogen production by steam reforming, and particularly to a heat exchange component, a steam reforming hydrogen production conversion tube having the heat exchange component, and a steam reforming hydrogen production reformer furnace. Background Art

[0002] In recent years, the market demand for small-scale hydrogen production has gradually increased, and small-scale natural gas steam reforming hydrogen production reformer furnaces have become increasingly important. In traditional natural gas steam reforming hydrogen production reformer furnaces, the reformed gas and the feed gas only conduct heat exchange through a tubular heat exchanger. The feed gas flows into the furnace tube through the pipeline of the tubular heat exchanger, and the reformed gas flows outside the pipeline of the tubular heat exchanger to conduct heat exchange with the feed gas. Its heat loss is large, the heat exchange efficiency is low, and the temperature rise efficiency of the feed gas is poor. Therefore, it is necessary to design a longer pipeline to continue heating the feed gas in the subsequent process to reach the temperature required for the reforming reaction; and other heat exchange devices also need to be arranged outside the reformer furnace to continue cooling the reformed gas. Therefore, traditional natural gas steam reforming hydrogen production reformer furnaces have long furnace tubes and large volumes. If a natural gas steam reforming hydrogen production reformer furnace is designed and built in the traditional way, the heat utilization rate of the reformed gas is insufficient, and more heat is lost, resulting in waste of resources, which is not conducive to the miniaturized design and construction of the conversion tube and the reformer furnace device. Summary of the Invention

[0003] The present disclosure provides a heat exchange component, a conversion tube having the heat exchange component, and a reformer furnace to solve the problems of the prior art.

[0004] In a first aspect, the present disclosure provides a heat exchange component for hydrogen production by steam reforming. The heat exchange medium of the heat exchange component includes a feed gas and a reformed gas. The heat exchange component includes a first heat exchange part, a second heat exchange part, and a gas flow reversal part. Among them, the first heat exchange part is configured to include an inner reformed gas cooling channel and an outer feed gas heating channel; the second heat exchange part is configured to include a reformed gas heat dissipation gas path and a feed gas heat absorption gas path; the gas flow guiding part is configured to fluidly connect the outer feed gas heating channel to the feed gas heat absorption gas path, and fluidly connect the reformed gas heat dissipation gas path to the inner reformed gas cooling channel; wherein, in the flow direction of the feed gas, the second heat exchange part is located downstream of the first heat exchange part.

[0005] Further, the first heat exchange part includes an inner cylinder and an outer cylinder surrounding the inner cylinder. The inner reformed gas cooling channel is defined by the inner cylinder, and the outer feed gas heating channel is defined by the channel between the outer cylinder and the inner cylinder.

[0006] Specifically, the gas flow diversion part is provided with a first chamber, a second chamber, and a partition located between the first chamber and the second chamber. The partition is provided with a raw material gas flow interface and a reformed gas flow interface. The reformed gas cooling gas path is fluidly connected to the inner reformed gas cooling channel through the second chamber and the raw material gas flow interface; the outer raw material gas heating channel is fluidly connected to the raw material gas heat absorption gas path through the first chamber and the reformed gas flow interface. Preferably, the partition is provided with 2 raw material gas flow interfaces and 1 reformed gas flow interface. The reformed gas flow interface is arranged in the middle of the partition, and the raw material gas flow interfaces are arranged on both sides of the reformed gas flow interface.

[0007] Furthermore, the second heat exchange part is configured as a tubular heat exchanger. Optionally, the tubular heat exchanger can be a shell-and-tube heat exchanger or a coil heat exchanger.

[0008] Specifically, the tubular heat exchanger has a raw material gas inlet and a raw material gas outlet. The heat exchange assembly further includes a core tube. The raw material gas inlet is communicated with the raw material gas flow interface, and the raw material gas outlet is communicated with the inlet of the core tube.

[0009] Particularly, the first chamber and / or the second chamber is in the shape of a bowl with an opening facing downwards.

[0010] Furthermore, a heat preservation packing layer is provided on the outer side of the outer cylinder, and a packing protection tube is provided on the outer side of the heat preservation packing layer. The upper end of the inner cylinder is provided with a reformed gas outlet connection end, and the upper end of the outer cylinder is provided with a raw material gas inlet connection end.

[0011] In a second aspect, the present disclosure provides a steam reforming hydrogen production reforming tube. The reforming tube includes a furnace tube body, a catalyst bed, a porous support plate, and the heat exchange assembly provided with a core tube in the first aspect above. Among them, the porous support plate is arranged at the lower end inside the furnace tube body, and the catalyst bed is arranged in the cavity defined by the furnace tube body and the porous support plate below the second heat exchange part; the core tube extends in the catalyst bed to the bottom end of the core tube and passes through the porous support plate.

[0012] Particularly, the height of the catalyst bed is 1 - 2.5 m, or the length of the reforming tube is 2 - 3 m.

[0013] In a third aspect, the present disclosure provides a steam reforming hydrogen production reforming furnace, and the reforming furnace includes the reforming tube in the second aspect above.

[0014] The features and advantages of the present invention include:

[0015] By providing the first heat exchange part with external cooling and internal heating, with the reformed gas on the inner side and the raw material gas on the outer side, and the flow directions of the raw material gas and the reformed gas being opposite, the present invention can not only improve the heat exchange efficiency between the reformed gas and the raw material gas, but also reduce the heat loss at the position where the first heat exchange part is located, improve the heat utilization rate, and enable the heat to be more effectively used for heating the raw material gas.

[0016] Furthermore, since both the first heat exchange section and the second heat exchange section provide effective heat exchange for the raw material gas respectively, the heat required for the raw material gas thereafter is reduced; therefore, after the second heat exchange section, the design of the heat exchange path or heat exchange device for increasing the temperature of the raw material gas can be simplified, so that the length of the conversion tube can be shortened and the reformer device can be made smaller. Brief Description of the Drawings

[0017] In order to more clearly illustrate the technical solutions in the embodiments of the present disclosure, the drawings required for the description of the embodiments will be briefly introduced below. Obviously, the drawings in the following description are only some embodiments of the present disclosure. For those of ordinary skill in the art, other drawings can be obtained based on these drawings without creative efforts.

[0018] Figure 1 Shows a schematic diagram of a steam reforming hydrogen production reformer according to the present invention;

[0019] Figure 2 Shows a schematic diagram of a steam reforming hydrogen production conversion tube according to the present invention;

[0020] Figure 3A Shows a schematic diagram of an embodiment of a heat exchange assembly according to the present invention;

[0021] Figure 3B Shows a schematic diagram of another embodiment of a heat exchange assembly according to the present invention;

[0022] Figure 3C Shows a schematic diagram of still another embodiment of a heat exchange assembly according to the present invention;

[0023] Figure 3D Shows a schematic diagram of yet another embodiment of a heat exchange assembly according to the present invention;

[0024] Figure 4 Shows a top view structural schematic diagram of an air flow diversion part according to the present invention;

[0025] Figure 5 Shows a schematic diagram of the connection relationship between the second heat exchange section and the upstream and downstream components according to the present invention.

[0026] Description of the Reference Numerals:

[0027] 10 - Hydrogen production reformer, 11 - Burner, 12 - Furnace top area, 13 - Reformer main body;

[0028] 20 - Conversion tube, 210 - Heat exchange assembly, 22 - Porous support plate, 23 - Catalyst bed, 24 - Furnace tube body;

[0029] 211 - First heat exchange section, 211a - Inner cylinder, 211b - Outer cylinder;

[0030] 212 - Gas flow diversion section, 212a - Feed gas flow connection port, 212c - Reformed gas flow connection port, 212d - Partition member, 212e - First chamber, 212f - Second chamber;

[0031] 213 - Second heat exchange section, 2131 - Tube heat exchanger, 2132 - Feed gas inlet, 2133 - Feed gas outlet;

[0032] 214 - Core tube, 215 - Feed gas inlet connection end, 216 - Reformed gas outlet connection end, 217 - Heat insulation packing layer, 218 - Flange cover, 219 - Packing protection tube;

[0033] 25a - Reformed gas flow, 25b - Feed gas flow. Detailed implementation manners

[0034] Next, the technical solutions in the embodiments of the present disclosure will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present disclosure. Obviously, the described embodiments are only a part of the embodiments of the present disclosure, rather than all the embodiments. Based on the embodiments in the present disclosure, all other embodiments obtained by those of ordinary skill in the art without creative efforts shall fall within the protection scope of the present disclosure.

[0035] Refer to Figure 1 , the present invention discloses a steam reforming hydrogen production reformer 10, such as a natural gas reforming hydrogen production reformer, which causes a reforming reaction of a feed gas (a mixture of natural gas and water vapor) to generate a reformed gas (a mixture of methane, hydrogen, CO, CO2, and H2O). The reformer 10 includes a furnace top region 12 and a reformer main body 13. A plurality of burners 11 and reforming tubes 20 are provided in the reformer 10. The burners 11 are arranged in the furnace top region 12, and the reforming tubes 20 extend longitudinally downward from the furnace top region 12 into the reformer main body 13. The high-temperature flue gas generated by the combustion of the burners 11 provides the heat required for the reforming reaction in the reforming tubes 20.

[0036] In some specific implementation manners, refer to Figure 2 , the reforming tube 20 includes a furnace tube body 24, a porous support plate 22, a catalyst bed 23, and a heat exchange assembly 210. Preferably, the length of the reforming tube 20 is 2 - 3 m; or, the height of the catalyst bed is 1 - 2.5 m. The porous support plate 22 is provided at the lower end inside the furnace tube body 24 to provide support for the catalyst bed 23. The heat exchange assembly 210 is used to exchange heat between the feed gas that needs to be heated and the reformed gas that needs to be cooled.

[0037] Refer to Figure 3A, the upper end of the heat exchange component 210 is provided with a raw material gas inlet connection end 215 and a reformed gas outlet connection end 216. The raw material gas stream 25b flows into the reforming tube 20 from the raw material gas inlet connection end 215, is heated to 500 - 700 °C through the heat exchange component 210, and then enters the catalyst bed through the pores on the porous support plate 22 to undergo a reforming reaction to obtain the reformed gas stream 25a; the reformed gas passes through the heat exchange component 210 to reduce the temperature to 300 - 500 °C and then flows out of the reforming tube 20 from the reformed gas outlet connection end 216.

[0038] In some embodiments, the heat exchange component 210 includes a first heat exchange part 211, a second heat exchange part 213, and a gas flow diversion part 212. Among them, the first heat exchange part 211 includes an inner reformed gas cooling channel and an outer raw material gas heating channel; the second heat exchange part 213 includes a raw material gas heat absorption gas path and a reformed gas heat dissipation gas path; the gas flow diversion part 212 fluidly connects the outer raw material gas heating channel of the first heat exchange part 211 to the raw material gas heat absorption gas path of the second heat exchange part 213, and fluidly connects the reformed gas heat dissipation gas path of the second heat exchange part 213 to the inner reformed gas cooling channel of the first heat exchange part 211. The first heat exchange part 211, the second heat exchange part 213, and the gas flow diversion part 212 are arranged in the furnace top area 12 of the reforming furnace. Among them, in the flow direction of the raw material gas, the second heat exchange part 213 is located downstream of the first heat exchange part 211. That is, in the flow direction of the reformed gas, the second heat exchange part 213 is located upstream of the first heat exchange part 211. The gas flow diversion part is arranged between the first heat exchange part and the second heat exchange part.

[0039] By setting the first heat exchange part with external cooling and internal heating in the heat exchange component 210, with the reformed gas on the inside and the raw material gas on the outside, and the flow directions of the raw material gas and the reformed gas being opposite, not only is the heat exchange efficiency between the reformed gas and the raw material gas high, but also the heat loss at the position where the first heat exchange part is located can be reduced, the heat utilization rate can be improved, and the heat can be more effectively used for heating the raw material gas. Further, since the first heat exchange part and the second heat exchange part respectively provide effective heat exchange for the raw material gas, the heat required for the raw material gas after this is reduced; therefore, the design of the heat exchange path or heat exchange device for increasing the temperature of the raw material gas after the second heat exchange part can be simplified, thereby greatly reducing the length of the reforming tube, and the length of the reforming tube can be shortened to about 30%, greatly reducing the volume of the reforming furnace device.

[0040] Further, referring to Figure 3A, the first heat exchange part 211 includes an inner cylinder 211a and an outer cylinder 211b surrounding the inner cylinder 211a. The raw gas inlet connection end 215 is arranged at the upper end of the outer cylinder 211b. Specifically, the raw gas inlet connection end 215 is arranged on the side wall of the outer cylinder 211b; the converted gas outlet connection end is arranged at the upper end of the inner cylinder 211a. The inner cylinder 211a defines an inner side converted gas cooling flow path, so that the converted gas flows out of the conversion tube from the inner cylinder. The flow path between the outer cylinder 211b and the inner cylinder 211a defines a raw gas heating flow path, so that the raw gas flows to the second heat exchange part 213 after passing through the outer cylinder 211b. The converted gas flow 25a flowing through the inner cylinder 211a exchanges heat with the raw gas flow 25b flowing through the outer cylinder 211b, so that the temperature of the raw gas rises and the temperature of the converted gas drops.

[0041] According to several embodiments of the present invention, the second heat exchange part 213 can be a coil-type or shell-and-tube type tubular heat exchanger 2131. The tubular heat exchanger 2131 is provided with a raw gas inlet 2132, a raw gas outlet 2133 and tubes or coils. Optionally, in some embodiments, the tubes or coils therein serve as the raw gas heat absorption gas path of the second heat exchange part 212, and the space outside the tube or coil pipeline serves as the converted gas heat release gas path. Optionally, in other embodiments, the tubes or coils of the tubular heat exchanger 2131 serve as the converted gas heat release gas path of the second heat exchange part 212, and the space outside the tube or coil pipeline serves as the raw gas heat absorption gas path. Refer to Figure 5 , the tubular heat exchanger 2131 is provided with a raw gas inlet 2132 and a raw gas outlet 2133.

[0042] Specifically, refer to Figures 3A to 3D , the gas flow turning part 212 includes a first chamber 212e, a second chamber 212f and a partition 212d located between the first chamber 212e and the second chamber 212f. The partition 212d is provided with a raw gas circulation interface 212a and a converted gas circulation interface 212c. The converted gas heat release gas path of the second heat exchange part 212 is fluidly connected to the inner side converted gas cooling flow path of the first heat exchange part 211 through the second chamber 212f and the converted gas circulation interface 212c; the outer side raw gas heating flow path of the first heat exchange part 211 is fluidly connected to the raw gas heat absorption gas path of the second heat exchange part 212 through the first chamber 212e and the raw gas circulation interface 212a.

[0043] Refer to Figures 3A to 3D , the first chamber 212e can be configured into any suitable shape. Optionally, the first chamber 212e is configured into a bowl shape with an opening facing downwards (refer to Figure 3A and Figure 3B ), and the top of the first chamber 212e can also be configured into a conical top (refer to Figure 3C ) or a flat top (refer to Figure 3D) etc. The second chamber 212f can also be configured in any shape. Optionally, the second chamber 212f is configured as a bowl shape with the opening facing downward (refer to Figure 3A and Figure 3B ), or the separator 212d is configured as a flat plate type (refer to Figure 3C and Figure 3D ), etc. To facilitate the welding process of the gas flow diversion part 212, as a preferred embodiment, the first chamber 212e and the second chamber 212f are configured as bowl shapes with the opening facing downward.

[0044] Optionally, refer to Figure 3A , Figure 4 and Figure 5 , the gas flow diversion part 212 is provided with two raw material gas circulation interfaces 212a. Refer to Figures 3B to 3D , the gas flow diversion part 212 is provided with one raw material gas circulation interface 212a. It is easy for those skilled in the art to understand that three or more raw material gas circulation interfaces 212a can also be set according to actual needs.

[0045] Preferably, refer to Figure 3A and Figure 4 , the separator 212d is provided with two raw material gas circulation interfaces 212a and one converted gas circulation interface 212c. The converted gas circulation interface 212c is arranged in the middle of the separator 212d, and the two raw material gas circulation interfaces 212a are arranged on both sides of the converted gas circulation interface 212c. The bottom end of the inner cylinder 211a is connected to the converted gas circulation interface 212c. The raw material gas circulation interface 212a is communicated with the raw material gas heating flow path of the outer cylinder 211b through the first chamber 212e. The raw material gas circulation interface 212a is in fluid communication with the raw material gas heat absorption gas path of the second heat exchange part 212. Specifically, refer to Figure 5 , the raw material gas circulation interface 212a is communicated with the raw material gas inlet 2132 of the tubular heat exchanger 2131. The raw material gas flow 25b enters the outer cylinder 211b of the first heat exchange part 211 from the raw material gas inlet connection end 215, further travels downward along the outer raw material gas heating flow path in the outer cylinder 211b to the bottom of the outer cylinder 211b, and then flows into the raw material gas inlet 2132 of the tubular heat exchanger 2131 through the first chamber 212e and the raw material gas circulation interface 212a of the gas flow diversion part 212. After the raw material gas flow 25b absorbs heat in the second heat exchange part 213, it flows out of the tubular heat exchanger 2131 from the raw material gas outlet 2133.

[0046] According to some embodiments of the present invention, the heat exchange assembly 210 further includes a core tube 214. The top end of the core tube 214 is connected to the raw material gas outlet 2133 of the tubular heat exchanger 2131; that is, the gas inlet of the core tube 214 is communicated with the raw material gas outlet 2133. Optionally, the core tube 214 is a spiral tube. Preferably, the core tube 214 is a straight tube. Using a straight tube for the core tube 214 facilitates the equipment maintenance personnel to replace the catalyst.

[0047] Further, referring to Figure 2 , the core tube 214 is a straight tube and is disposed in the middle of the furnace tube body 24 below the second heat exchange part 213. The catalyst bed 23 is disposed in the cavity defined by the furnace tube body 24 and the porous support plate 22 below the second heat exchange part 213. The core tube 214 extends downward along the catalyst bed 23 to a lower end exceeding the porous support plate 22. The raw material gas stream 25b enters the core tube 213 from the raw material gas outlet 2133 of the tubular heat exchanger 2131, further reaches below the porous support plate 22 along the downwardly extending core tube 214, and then enters the catalyst bed 23 through the pores on the porous support plate 22 to undergo a reforming conversion reaction. The converted gas stream 25a generated by the reforming reaction flows out from above the catalyst bed and enters the converted gas heat dissipation gas path of the second heat exchange part 213. Further, referring to Figure 3A , after flowing out from the second heat exchange part 213, the converted gas stream 25a enters the inner cylinder 211a through 212f of the gas flow diversion part 212 and the converted gas circulation interface 212c, and flows upward along the inner cylinder 211a to the converted gas outlet connection end 216 and then flows out of the conversion tube 20.

[0048] Optionally, the partition 212d can be disposed at any angle at any position inside the gas flow inversion part 212; preferably, referring to Figures 3A to 3D , the partition 212d is horizontally disposed in the middle of the gas flow inversion part 212 to make the raw material gas 25b enter the raw material gas circulation interface 212a and the converted gas 25a enter the converted gas circulation interface 212c more smoothly.

[0049] Preferably, referring to Figure 2 and Figure 3A , a heat preservation filler layer 217 is disposed on the outer side of the outer cylinder 211b of the first heat exchange part 211, and a filler protection tube 219 is disposed on the outer periphery of the heat preservation filler layer 217. The flange cover 218 fixes the filler protection tube 219 and the heat preservation filler layer 217 therein to the furnace tube body 24. By providing the heat preservation filler layer 217, the heat loss of the outer cylinder 211b is reduced, and the heat exchange effect between the converted gas stream 25a in the inner cylinder 211a and the raw material gas stream 25b in the outer cylinder 211b is improved. Since the first heat exchange part 211 is cold outside and hot inside, therefore, it is not necessary to fill heat insulation materials at the flange cover 218 to ensure that the flange cover 218 will not be deformed by heat, and the flange cover 218 can adopt an ordinary flat-top flange plate, thereby reducing costs.

[0050] By providing the first heat exchange part with cold outside and hot inside, the present invention can reduce the heat loss at the upper end of the conversion tube, improve the heat utilization rate, and make the heat be more effectively used for heating the raw material gas.

[0051] Further, in the present invention, by providing a first heat exchange section, a second heat exchange section, and an air flow diversion section, the air flow diversion section guides the raw material gas outside the first heat exchange section to enter the appropriate second heat exchange section for further heating after being heated in one stage. Since both the first heat exchange section and the second heat exchange section provide effective heat exchange for the raw material gas, the heat required for the raw material gas thereafter is reduced; therefore, the design of the heat exchange path or heat exchange device for increasing the temperature of the raw material gas after the second heat exchange section can be simplified, so that the length of the conversion tube can be shortened and the reformer device can be made smaller.

[0052] The above are only several embodiments of the present disclosure, and those skilled in the art can make various changes or modifications to the embodiments of the present disclosure without departing from the spirit and scope of the present disclosure according to the content disclosed in the application documents.

Claims

1. A heat exchange component for hydrogen production by steam reforming, wherein the heat exchange medium of the heat exchange component comprises a raw material gas and a reformed gas, and is characterized in that The heat exchange component includes a first heat exchange part, a second heat exchange part and an air flow diversion part; The first heat exchange part is configured to include an inner side reformed gas cooling channel and an outer side raw material gas heating channel. The first heat exchange part includes an inner cylinder and an outer cylinder surrounding the inner cylinder. The inner side reformed gas cooling channel is defined by the inner cylinder, and the outer side raw material gas heating channel is defined by the channel between the outer cylinder and the inner cylinder; The second heat exchange part is configured to include a raw material gas inlet, a raw material gas outlet, a reformed gas heat dissipation gas path and a raw material gas heat absorption gas path. The second heat exchange part is a coil type or shell and tube type tubular heat exchanger. The tubes or coils therein serve as the raw material gas heat absorption gas path of the second heat exchange part, and the space outside the tube or coil pipeline serves as the reformed gas heat release gas path; The air flow diversion part is arranged between the first heat exchange part and the second heat exchange part. The air flow diversion part includes a first chamber, a second chamber and a partition located between the first chamber and the second chamber. The partition is provided with a raw material gas circulation interface and a reformed gas circulation interface; Wherein, in the flowing direction of the raw material gas, the second heat exchange part is located downstream of the first heat exchange part; the reformed gas heat dissipation gas path of the second heat exchange part is fluidly connected to the inner side reformed gas cooling channel of the first heat exchange part through the second chamber and the reformed gas circulation interface, and the outer side raw material gas heating channel of the first heat exchange part is fluidly connected to the raw material gas heat absorption gas path of the second heat exchange part through the first chamber and the raw material gas circulation interface.

2. The heat exchange component according to claim 1, wherein The heat exchange component further includes a core tube. The raw material gas inlet is communicated with the raw material gas circulation interface, and the raw material gas outlet is communicated with the air inlet of the core tube.

3. The heat exchange component according to claim 2, wherein The first chamber and / or the second chamber is in a bowl shape with the opening facing downwards.

4. The heat exchange component according to claim 3, wherein The partition is provided with 2 raw material gas circulation interfaces and 1 reformed gas circulation interface; the reformed gas circulation interface is arranged in the middle of the partition, and the raw material gas circulation interfaces are arranged on both sides of the reformed gas circulation interface.

5. The heat exchange component according to any one of claims 2 to 4, characterized in that, A heat preservation filler layer is arranged on the outer side of the outer cylinder, and a filler protection tube is arranged on the outer side of the heat preservation filler layer; a reformed gas outlet connection end is arranged at the upper end of the inner cylinder, and a raw material gas inlet connection end is arranged at the upper end of the outer cylinder.

6. A steam reforming hydrogen production reforming tube, characterized in that, It includes a furnace tube body, a catalyst bed, a porous support plate and the heat exchange component according to claim 5; wherein, The porous support plate is arranged at the lower end inside the furnace tube body, and the catalyst bed is arranged in the cavity defined by the furnace tube body and the porous support plate below the second heat exchange part; The core tube extends in the catalyst bed until the air outlet of the core tube passes through the porous support plate.

7. The steam reforming hydrogen production reforming tube according to claim 6, characterized in that, The height of the catalyst bed is 1 - 2.5 m, or the length of the reforming tube is 2 - 3 m.

8. A steam reforming hydrogen production reformer, characterized in that, It includes the steam reforming hydrogen production reforming tube according to claim 6 or 7.

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