A hydrogen production reactor

Abstract

The application provides a hydrogen production reactor and relates to the technical field of heat exchange, and aims to solve the problem of local heat concentration in the heat exchange reaction process, which causes the internal channel structure of the hydrogen production reactor to be damaged. The hydrogen production reactor comprises a reforming module, a preheating module and a heat recovery module which are sequentially arranged in the reactor shell from bottom to top, a first heat supply channel and a heat absorption channel are vertically arranged in the reforming module, a plurality of first fuel inlets which are in communication with the first heat supply channel are arranged on the outer side wall of the reforming module along the axis direction of the first heat supply channel, and the heat absorption channels are arranged on both sides of the first heat supply channel. The reactor structure of the distributed catalytic oxidation heat supply is adopted, the adding amount of the fuel in different sections in the first heat supply channel is accurately controlled, the dynamic temperature difference of the module area is eliminated, the local cold and hot concentration in the module is eliminated, and then the service life of the reactor is prolonged and the performance of the reactor is improved.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of heat exchange, in particular to a hydrogen production reactor. BACKGROUND

[0002] The adoption of catalytic oxidation fuel to provide heat source for the hydrogen production reactor is to further reduce the reactor volume, reduce auxiliary equipment investment and reduce the structure cost.

[0003] In the process of using and developing the hydrogen production reactor, it is found that the adoption of aluminum and aluminum alloy materials with high thermal conductivity in the channel for providing heat source by catalytic oxidation also has the phenomenon of heat concentration. The heat concentration cannot be reflected in the short term, but after the hydrogen production reactor is operated for about 200-500 hours, the main body weld of the hydrogen production reactor begins to have thermal cracking, and the connecting pipe weld is torn, etc. According to the analysis, the main reason for the above problems is that the temperature difference is large, and due to the difference in thermal expansion, the main body or the connecting part has a thermal cracking phenomenon. The above problem is essentially the appearance of local cold and hot zones.

[0004] The heat absorption and heat supply zones of the reactor are isolated by using metal materials. According to the experimental phenomenon analysis, there is a high temperature source concentration in the heat supply zone, and a low temperature source concentration in the heat absorption zone. Since the thermal conductivity of the metal is determined by the material, and the thermal conductivity does not change too much with temperature, the heat flux of the metal material has an upper limit, so it can be determined that under the premise of meeting the metal strength requirement, the maximum temperature of the metal will also be limited to a maximum value, thereby limiting the maximum temperature difference of the reactor in the use process, and the heat flux per unit area of the metal material also has an upper limit. When the hydrogen production reactor is working, the heat absorption zone requires more heat when switching from low load operation to rated operation. However, the fuel is concentrated at the inlet of the heat supply zone, so most of the catalytic oxidation occurs in a small distance close to the inlet, so as the fuel in the heat supply zone increases, the catalytic oxidation exothermic effect will be more intense due to the temperature rise. Since the heat flux per unit area of the metal material has a maximum value, the heat concentration will occur in the catalytic oxidation exothermic zone at the fuel inlet of the heat supply zone, and then a high temperature will occur in the heat concentration zone, which will weaken the metal strength and make its inherent structure more easily damaged. The inlet of the heat absorption zone is in a strong heat absorption state, and then a local relatively low temperature zone will appear in the heat absorption zone. Under the premise of increasing the heat flux in the heat absorption zone and the heat release zone, the temperature difference between the high temperature zone and the low temperature zone will increase, and in the system with pressure difference, it is easy to cause the structure of the reactor to be damaged, the cracks in the connecting part and the weld, and the structure thermal cracking, etc. The high temperature zone and the low temperature zone are shown in Figure 6

[0005] ​The chemical reaction rate of the heat absorption zone and the heat supply zone is fast and almost completed in an instant. When the raw material gradually increases, the heat absorption of the strong endothermic zone gradually increases, and at the same time, the fuel of the heat supply zone needs to be increased to meet the heat required by the reaction. Such a phenomenon leads to the gradual increase of the temperature of the severe oxidation zone and the gradual decrease of the temperature of the strong endothermic zone. According to the analysis of the basic theory of heat, the hot zone and the cold zone should form a dynamic heat balance of heat transfer, reduce the temperature difference between the strong endothermic zone and the exothermic severe oxidation zone, but this requires the metal material to have sufficient heat conduction capacity under the premise of meeting the strength. Since the thermal conductivity coefficient of the metal has an upper limit and does not change much with the change of temperature, under the same heat flux area, high heat flux means high temperature difference. Based on the above principle, it is easy to form cold and hot temperature zones in the reactor. Such factors can easily cause the weld structure of the reactor to be torn, causing the reactor to lose operating capacity, and in severe cases, the heat exchange reactor may leak and cause a safety accident.

[0006] In addition, it is found through tests that when the reactor structure is operated in the normal reaction temperature range of 240-280 DEG C, the most easily damaged part of the reactor structure is the heat absorption zone. It is speculated that most of the heat absorption has been completed at the front end of the strong endothermic zone, and there is little heat absorption at the rear end, but the heat supply zone releases a large amount of heat at the inlet. Due to the limitation of the heat flux of the metal, there is a lot of residual heat that cannot be consumed, and then it is transferred to the rear end of the channel with the heat supply gas flow, which causes a local high temperature at the rear end of the heat absorption zone, thereby weakening the pressure resistance of the reactor, and further damaging the internal structure of the reactor. The main performance is that the metal wall surface separating the oxidation heat supply zone and the reaction heat absorption zone appears serious deformation or crack. At the same time, due to the high temperature, the strength of the metal is weakened, the corrosion rate of the synthesis gas to the metal material is increased, and the service life of the reactor is reduced. SUMMARY

[0007] The present application provides a hydrogen production reactor, which adopts a distributed catalytic oxidation heat supply reactor structure, accurately controls the addition amount of fuel in different sections, eliminates the temperature difference between the low-temperature heat absorption and the high-temperature heat supply source, and prolongs the service life of the reactor.

[0008] The technical scheme adopted by the present application is:

[0009] A hydrogen production reactor comprises a reforming module, a preheating module and a heat recovery module arranged in the reactor shell from bottom to top.

[0010] The first heat supply channel is vertically arranged in the reforming module, and a plurality of first fuel inlets are arranged on the outer side wall of the reforming module and communicated with the first heat supply channel along the axial direction of the first heat supply channel; heat absorption channels are arranged on both sides of the first heat supply channel, and the heat absorption channels arranged on one side of the first heat supply channel at least include two groups; the heat absorption channels arranged on the same side are connected in a head-to-tail mode, the heat absorption channel arranged on the last group is communicated with the first group of heat absorption channels on the other side, the inlet of the heat absorption channel is arranged on the end of the reforming module close to the preheating module, the outlet of the heat absorption channel is arranged on the bottom side wall of the reforming module, and the flow directions of the heat absorption channels arranged on both sides of the first heat supply channel are opposite.

[0011] The second heat supply channel communicated with the first heat supply channel is arranged in the preheating module, and a raw material preheating channel is arranged in the preheating module and communicated with the heat absorption channel.

[0012] The heat recovery module is provided with a flue gas channel, a discharge channel and a raw material feeding channel, the flue gas channel is communicated with the second heat supply channel, one end of the discharge channel is communicated with the heat absorption channel, the other end of the discharge channel is communicated with the outside, and the raw material feeding channel is communicated with the raw material preheating module.

[0013] Optionally, at least three pipes constitute a group of the heat absorption channels.

[0014] Optionally, the reforming module and the preheating module are provided with a connecting piece, and the connecting piece communicates the first heat supply channel and the second heat supply channel.

[0015] Optionally, the connecting piece is provided with a second fuel inlet.

[0016] Optionally, a mixed fuel inlet is arranged on the bottom side of the reforming module, and the mixed fuel inlet is communicated with the first heat supply channel.

[0017] Optionally, the raw material preheating channels are arranged on both sides of the channel of the heat recovery module.

[0018] Optionally, the heat absorption channels are filled with a catalyst.

[0019] Optionally, the first heat supply channel is filled with a catalytic oxidation catalyst.

[0020] Optionally, a third fuel inlet is arranged in the preheating module, and the third fuel inlet is communicated with the second heat supply channel.

[0021] Optionally, the first heat supply channel and the heat absorption channel are in a wave shape.

[0022] Compared with the prior art, the present application has the following beneficial effects:

[0023] 1. The reforming area adopts top feeding, and then uses single high-temperature pipeline to release heat, so that the raw material in the heat absorption channels arranged on both sides of the high-temperature pipeline is uniformly heated.

[0024] 2. The preheating area is used to supplement heat and increase the preheating temperature, so that the raw material entering the reforming area can react quickly and improve the working efficiency.

[0025] 3. The reforming area is supplemented with mixed gas at the bottom to further ensure the heat exchange heat, and at the same time, the mixed gas just entering the heat exchange area is fully reacted.

[0026] 4. A plurality of groups of heat absorption channels are arranged on both sides of the first heat supply channel in a head-to-tail manner, in order to avoid damage caused by temperature difference during use of the first heat supply channel and the heat absorption channels.

[0027] 5. The reactor structure adopts distributed catalytic oxidation heat supply, the addition amount of fuel in different sections of the first heat supply channel is accurately controlled, the dynamic temperature difference (dynamic temperature difference refers to the temperature difference between the first heat supply channel and the heat absorption channels when the reactor reaches a heat transfer balance state during operation) of the module area is eliminated, the cold and hot concentration in the module is eliminated, and the reactor life is prolonged and the reactor performance is improved. BRIEF DESCRIPTION OF DRAWINGS

[0028] In order to more clearly illustrate the technical solutions in the embodiments of the present application or the prior art, the drawings needed to be used in the embodiments or prior art description will be briefly introduced. Obviously, the drawings in the following description are only some embodiments of the present application, and other drawings can be obtained by those skilled in the art without creative labor.

[0029] Figure 1 It is a schematic diagram of the overall structure of the hydrogen production reactor.

[0030] Figure 2 It is a schematic diagram of the raw material flow structure of the hydrogen production reactor.

[0031] Figure 3 It is a schematic diagram of the sectional structure of the hydrogen production reactor.

[0032] Figure 4 It is a schematic diagram of the top view structure of the reforming module of the hydrogen production reactor.

[0033] Figure 5 It is a schematic diagram of the sectional structure of the reforming module of the hydrogen production reactor.

[0034] Reference signs:

[0035] 1, reforming region; 2, preheating region; 3, regenerative region; 4, reforming module; 41, first heat supply channel; 42, first fuel inlet; 43, endothermic channel; 44, mixed fuel inlet; 5, preheating module; 51, second heat supply channel; 52, raw material preheating channel; 53, third fuel inlet; 6, heat recovery module; 61, flue gas channel; 62, discharge channel; 63, raw material feeding channel; 7, connecting piece; 71, second fuel inlet. DETAILED DESCRIPTION

[0036] Hereinafter, only certain exemplary embodiments are simply described. As those skilled in the art can recognize, the described embodiments can be modified in various different ways without departing from the spirit or scope of the present application. Therefore, the drawings and the description are considered to be exemplary in nature rather than limiting.

[0037] In the description of the present application, it needs to be understood that the terms "upper", "lower", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer" and the like indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, or the orientation or positional relationship commonly understood by those skilled in the art, or the orientation or positional relationship commonly understood by those skilled in the art, or the orientation or positional relationship commonly understood by those skilled in the art, only for the convenience of describing the present application and simplifying the description, and therefore cannot be understood as indicating or implying that the indicated device or element must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as limiting the present application.

[0038] In the present application, unless otherwise explicitly specified and limited, the terms "mounting", "connecting", "connecting", "fixing" and the like should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or it can be integrated; it can be mechanically connected, or it can be electrically connected, or it can be communicated; it can be directly connected, or it can be indirectly connected through an intermediate medium; it can be the communication or interaction relationship between two elements. For those skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances.

[0039] In the present application, unless otherwise explicitly specified and limited, the first feature "on" or "under" the second feature can include that the first and second features are in direct contact, or that the first and second features are not in direct contact but are in contact through another feature between them. Moreover, the first feature "on", "above" and "above" the second feature includes that the first feature is directly above and obliquely above the second feature, or only indicates that the horizontal height of the first feature is higher than that of the second feature. The first feature "below", "below" and "below" the second feature includes that the first feature is directly above and obliquely above the second feature, or only indicates that the horizontal height of the first feature is less than that of the second feature.

[0040] The disclosure provided below provides many different embodiments or examples for implementing different structures of the present application. In order to simplify the disclosure of the present application, the components and arrangements of specific examples are described below. Of course, they are only examples, and the purpose is not to limit the present application. In addition, the present application can repeatedly refer to numbers and / or letters in different examples, and such repetition is for the purpose of simplification and clarity, which does not indicate the relationship between the various embodiments and / or arrangements discussed. In addition, the present application provides examples of various specific processes and materials, but those skilled in the art can realize the application of other processes and / or the use of other materials.

[0041] The embodiments of the present application are described in detail below in conjunction with the accompanying drawings.

[0042] As shown in Figure 1 , Figure 2 , Figure 3 , Figure 4 and Figure 5 , the embodiment of the present application provides a hydrogen production reactor, the inside of which is defined from bottom to top as reforming area 1, preheating area 2 and regenerative area 3. The inside of the reactor is provided with reforming module 4, preheating module 5 and heat recovery module 6. The reforming module 4 is installed in the reforming area 1, which serves as a reaction area. The reforming module 4 is provided with two rows of first heat supply channels 41. A plurality of first fuel inlets 42 are arranged on the side wall of the reforming module 4 along the axis direction of the first heat supply channels 41. Fuel is supplied to the reforming module 4 through the first fuel inlets 42. After the fuel enters the first heat supply channels 41, the reaction is warmed up. After the raw material enters the endothermic channels 43, it exchanges heat with the first heat supply channels 41.

[0043] As shown in Figure 4 and Figure 5 , in order to improve the reforming efficiency and avoid the problem of reactor damage due to high temperature in the present embodiment, the endothermic channels 43 on one side of the first heat supply channels 41 include three groups. The endothermic channels 43 of the adjacent two groups are connected end to end, and the endothermic channels 43 of the last group are in communication with the endothermic channels 43 on the other side. Because the endothermic channels 43 are arranged on both sides of the first heat supply channels 41, the heat absorption of the endothermic channels 43 is more uniform, avoiding the problem that the endothermic channels 43 far from the first heat supply channels 41 absorb too little heat, resulting in slow reaction; the raw material in the endothermic channels 43 close to the first heat supply channels 41 reacts quickly. At the same time, the inlets and outlets of the two groups of endothermic channels 43 arranged on both sides of the first heat supply channels 41 are arranged in reverse, reducing the temperature difference between the inlets and outlets of the endothermic channels 43.

[0044] In the specific implementation process, at least three pipes form a group of the heat absorption channels 43, which facilitates the reaction heat absorption of the raw materials in the corresponding channels, and then the raw materials enter the adjacent heat absorption channels 43 through the other end to perform the reaction heat absorption.

[0045] In other real-time modes, the heat absorption channels 43 can be set as four groups, five groups or six groups according to the use requirements, and the number of the heat absorption channels 43 in each group can also be set according to the specific requirements.

[0046] The fuel entering the first heat supply channel 41 through the first fuel inlet 42 is methanol, and the methanol is reacted in the first heat supply channel 41 to obtain flue gas, which provides high-temperature gas for the preheating module 5.

[0047] According to the specific design, each group of heat absorption channels 43 can be connected in series or in parallel. The first fuel inlet 42 can be set according to the hydrogen production scale. The first fuel inlet 42 is distributed along the axial direction of the first heat supply channel, and the distance between the adjacent two first fuel inlets 42 is not less than 10 cm.

[0048] As shown in Figure 1 , Figure 2 and Figure 3 , the preheating module 5 is provided with a second heat supply channel 51 and a raw material preheating channel 52. The second heat supply channel 51 is connected with the first heat supply channel 41, and the flue gas in the first heat supply channel 41 enters the preheating module 5 to preheat the raw materials in the preheating module 5, thereby improving the utilization rate of waste heat.

[0049] As shown in Figure 1 , Figure 2 and Figure 3 , the heat recovery module 6 is arranged at the top of the preheating module 5. The heat recovery module 6 is provided with a flue gas channel 61, a discharge channel 62 and a raw material feeding channel 63. The flue gas channel 61 is connected with the second heat supply channel 51, and the flue gas in the second heat supply channel 51 preheats the raw materials in the heat recovery module 6. At the same time, the discharge channel 62 is connected with the heat absorption channel 43, and the hydrogen after the reaction is discharged through the heat recovery module 6. The hydrogen exchanges heat with the raw materials entering at the same time when the hydrogen is discharged.

[0050] In use, the raw material is preliminarily preheated in the raw material feeding channel 63 of the heat recovery module 6, and then is secondarily preheated in the preheating module 5, so as to improve the reaction speed of the raw material in the reforming module 4. The preheated raw material enters the endothermic channel 43 of the reforming module 4, and exchanges heat with the first heat supply channel 41 of the reforming module 4, so that the reaction occurs in the process of heat exchange and hydrogen is generated. In the process of reaction, the raw material firstly enters a group of endothermic channels 43 to react, and then, with the supplement of raw material, the raw material sequentially passes through a plurality of groups of endothermic channels 43 connected in series to react, and the hydrogen generated by the reaction is connected to the heat recovery module 6 through a pipeline.

[0051] It should be noted that the fuel is supplemented through the first fuel inlet 42 communicated with the first heat supply channel 41 in the process of reaction. The raw material in the endothermic channels 43 located on both sides of the first heat supply channel 41 flows in opposite directions, which can reduce the temperature difference at the inlet and outlet. In addition, a plurality of groups of first fuel inlets 42 are arranged in the axial direction of the first heat supply channel 41, which facilitates the distributed supply of fuel and further eliminates the temperature difference between the low-temperature endothermic and high-temperature heat supply sources. The reforming module 4, the preheating module 5 and the heat recovery module 6 of the hydrogen production reactor are made of copper or copper alloy, aluminum or aluminum alloy, or iron-aluminum, etc. which have high thermal conductivity.

[0052] In another embodiment, as shown in Figure 1 , Figure 2 and Figure 3 , in order to facilitate the connection between the reforming module 4 and the preheating module 5, a connecting piece 7 is arranged between the reforming module 4 and the preheating module 5, and the connecting piece 7 communicates the first heat supply channel 41 and the second heat supply channel 51. In addition, a second fuel inlet 71 is arranged on the connecting piece 7, and the fuel is supplemented through the second fuel inlet 71 on the connecting piece 7, so as to improve the temperature of the raw material entering the endothermic channel 43.

[0053] The fuel entering the second fuel inlet 71 is combustible gas, such as gas containing part of methane, hydrogen, carbon dioxide, carbon monoxide, etc. which has combustible property. The number of the second fuel inlets 71 is determined according to the scale of hydrogen production.

[0054] In another embodiment, as shown in Figure 1 , Figure 2 and Figure 3 , in order to further improve the temperature in the first heat supply channel 41, a mixed fuel inlet 44 is arranged at one side of the bottom of the reforming module 4, and the mixed fuel inlet 44 is communicated with the first heat supply channel 41. The fuel entering the mixed fuel inlet 44 is methanol and air mixed gas. The air is a combustion-supporting agent. The number of the mixed fuel inlets 44 is determined according to the scale of hydrogen production.

[0055] In other embodiments, in order to conveniently control the entering amount of the first fuel inlet 42 and the mixed fuel inlet 44, flow regulating devices are arranged at the first fuel inlet 42 and the mixed fuel inlet 44. The flow regulating devices can be adjustable valves.

[0056] In another embodiment, the endothermic channel 43 is filled with a catalyst, which is a copper-based catalyst. The raw material enters the endothermic channel 43 and reacts with the catalyst to produce hydrogen.

[0057] In other embodiments, the first heat supply channel 41 is filled with a catalytic oxidation catalyst. The catalytic oxidation catalyst reacts with methanol to increase the temperature in the first heat supply channel 41. The catalytic oxidation catalyst is a palladium-based catalyst, a platinum-based catalyst, or other catalysts that can catalyze the oxidation of the fuel entering the first fuel inlet 42, the second fuel inlet 71, and the third fuel inlet 53 at low temperatures.

[0058] In another embodiment, as shown in Figure 3 , in order to improve the utilization rate of waste heat, raw material preheating channels 52 are arranged on both sides of the second heat supply channel 51 to facilitate the rapid exchange of heat between the raw material and the second heat supply channel 51.

[0059] In another embodiment, as shown in Figure 1 , Figure 2 , Figure 3 , in order to further improve the preheating effect of the preheating module 5, a third fuel inlet 53 is arranged in the preheating module 5, which communicates with the second heat supply channel 51.

[0060] In another embodiment, in order to improve the heat exchange efficiency of the reforming module 4, the first heat supply channel 41 and the endothermic channel 43 are designed in a wave shape.

[0061] In another embodiment, as shown in Figure 1 , Figure 2 , Figure 3 , in order to further improve the preheating effect, the second heat supply channel 51 is vertically arranged in the heat recovery module 6, the raw material preheating channels 52 are horizontally arranged on both sides of the second heat supply channel 51, and the raw material preheating channels 52 on both sides of the second heat supply channel 51 are connected to each other.

[0062] Specific working principle:

[0063] In use, the raw material enters the heat recovery module 6 through the raw material feeding channel 63, and is preliminarily preheated by the hydrogen and the flue gas entering the heat recovery module 6. The preliminarily preheated raw material enters the preheating module 5 for preheating, and the preheating of the preheating module 5 is mainly performed by the flue gas generated by the reforming module 4 and the supplemental fuel. Meanwhile, the preheating module 5 horizontally sets the raw material preheating channel 52 at two sides of the second heat supply channel 51, and the raw material is preheated in the raw material preheating channel 52 along the axial direction of the second heat supply channel 51, which facilitates the heat exchange of the heat in the second heat supply channel 51, and then enters the reforming module 4 for the last reaction after the heat exchange. Since the first heat supply channel 41 and the heat absorption channel 43 in the reforming module 4 are both vertically arranged, and the heat absorption channel 43 is arranged at two sides of the first heat supply channel 41, the raw material flows up and down along one side of the first heat supply channel 41 after entering the heat absorption channel 43, and then flows into the heat absorption channel 43 on the other side of the first heat supply channel 41 for reaction. The flow directions of the two oppositely arranged groups of heat absorption channels 43 are opposite, which avoids the problem of excessive local heat absorption and less local heat absorption in use, and thus avoids the problem of damage of the reactor due to temperature difference.

[0064] Finally, it should be noted that: the above only describes the preferred embodiments of the present application, and is not used to limit the present application, although the present application has been described in detail with reference to the foregoing embodiments, for those skilled in the art, the technical solutions recorded in the foregoing embodiments can still be modified, or some technical features can be replaced. Any modification, equivalent replacement, improvement, etc. within the spirit and principles of the present application shall be included in the protection scope of the present application.

Claims

1. A hydrogen production reactor, comprising, from bottom to top, a reforming module, a preheating module, and a heat recovery module arranged inside the reactor shell; characterized in that, The reforming module is vertically provided with a first heating channel. Multiple first fuel inlets communicating with the first heating channel are provided on the outer wall of the reforming module along the axial direction of the first heating channel. Heat absorption channels are provided on both sides of the first heating channel. The heat absorption channels on one side of the first heating channel include at least two groups. The two adjacent groups of heat absorption channels on the same side are connected end to end. The heat absorption channel in the last group is connected to the first group of heat absorption channels on the other side. The inlet of the heat absorption channel is located at the end of the reforming module near the preheating module, and its outlet is located on the bottom side wall of the reforming module. The flow directions of the heat absorption channels on both sides of the first heating channel are opposite. The preheating module is provided with a second heating channel that is connected to the first heating channel, and the preheating module is provided with a raw material preheating channel that is connected to the heat absorption channel; The heat recovery module is equipped with a flue gas channel, a discharge channel and a raw material feeding channel. The flue gas channel is connected to the second heating channel. One end of the discharge channel is connected to the heat absorption channel and the other end of the discharge channel is connected to the outside. The raw material feeding channel is connected to the raw material preheating module.

2. The hydrogen production reactor according to claim 1, characterized in that, At least three pipes form a group of the heat absorption channels.

3. The hydrogen production reactor according to claim 1, characterized in that, The reforming module and the preheating module are connected by a connector, which connects the first heating channel and the second heating channel.

4. The hydrogen production reactor according to claim 3, characterized in that, The connector is equipped with a second fuel inlet.

5. The hydrogen production reactor according to claim 4, characterized in that, A mixed fuel inlet is located on one side of the bottom of the reforming module, and the mixed fuel inlet is connected to the first heating channel.

6. The hydrogen production reactor according to claim 1, characterized in that, The raw material preheating channel is provided on both sides of the heat recovery module channel.

7. The hydrogen production reactor according to claim 1, characterized in that, The heat absorption channel is filled with a catalyst.

8. The hydrogen production reactor according to claim 5, characterized in that, The first heating channel is filled with a catalytic oxidation catalyst.

9. The hydrogen production reactor according to claim 1, characterized in that, The preheating module is equipped with a third fuel inlet, which is connected to the second heating channel.

10. The hydrogen production reactor according to claim 1, characterized in that, The first heating channel and the heat absorption channel are wavy.

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