Reforming hydrogen production reaction system

Abstract

The invention relates to the technical field of reforming hydrogen production, in particular to a reforming hydrogen production reaction system which comprises a reactor, a catalytic combustion unit, a reforming unit and a recovery unit, the catalytic combustion unit and the reforming unit are arranged in the reactor, the recovery unit is arranged outside the reactor, and the catalytic combustion unit and the reforming unit are oppositely arranged in the first direction. The reactor is provided with at least one gas inlet and at least one gas outlet, the gas inlet is arranged adjacent to the catalytic combustion unit, the gas outlet is arranged adjacent to the reforming unit, and the gas outlet is arranged adjacent to the reforming unit. And the two ends of the recovery unit communicate with the gas outlet and the gas inlet correspondingly, so that the flue gas subjected to heat absorption through the reforming unit flows into the catalytic combustion unit through the recovery unit and is mixed with flue gas generated by catalytic combustion of the catalytic combustion unit, and the reforming hydrogen production reaction system can improve the uniformity of temperature distribution.

Description

Technical Field

[0001] The invention relates to the technical field of reforming hydrogen production, and in particular to a reforming hydrogen production reaction system. Background Art

[0002] Hydrogen energy has attracted great attention from countries around the world due to its advantages such as high efficiency and cleanliness, and is considered to be one of the clean energy sources with the greatest development potential. Due to the difficulty in directly supplying or storing hydrogen, related technologies mostly use reforming hydrogen production reactors to obtain hydrogen. During the reforming hydrogen production process, a catalytic combustion unit is required to continuously provide heat. However, the controllability of the catalytic combustion unit is poor, and the reaction rate of the catalytic combustion unit is much higher than the reforming reaction rate. Direct heat exchange in the same area is prone to local hot spots, resulting in uneven temperature distribution in the reactor. Summary of the invention

[0003] The present invention aims to solve one of the technical problems in the related art at least to a certain extent. To this end, an embodiment of the present invention provides a reforming hydrogen production reaction system, which can improve the uniformity of temperature distribution.

[0004] The reforming hydrogen production reaction system of the embodiment of the present invention includes: a reactor, the reactor having a chamber; a catalytic combustion unit and a reforming unit, the catalytic combustion unit and the reforming unit are installed in the chamber, and the catalytic combustion unit and the reforming unit are arranged relative to each other in a first direction, so that the flue gas generated by catalytic combustion in the catalytic combustion unit is transmitted to the reforming unit, and the reforming unit absorbs the heat of the flue gas to perform a reforming reaction; a recovery unit, the recovery unit is arranged outside the chamber, and the reactor is provided with at least one air inlet and at least one air outlet, the air inlet is located on a side of the catalytic combustion unit away from the reforming unit, and the air outlet is located on a side of the reforming unit away from the catalytic combustion unit, one end of the recovery unit is connected to the air outlet, and the other end of the recovery unit is connected to the air inlet, so that the flue gas after absorbing heat from the reforming unit flows into the catalytic combustion unit through the recovery unit and mixes with the flue gas generated by catalytic combustion in the catalytic combustion unit.

[0005] The reforming hydrogen production reaction system of the embodiment of the present invention can improve the uniformity of temperature distribution.

[0006] In some embodiments, the catalytic combustion unit comprises at least one catalytic combustion tube, one end of the at least one catalytic combustion tube is adapted to be connected to a fuel source, and the at least one catalytic combustion tube is filled with a first catalyst to catalyze the combustion of the fuel.

[0007] In some embodiments, the catalytic combustion tube includes a preheating section and a combustion section, the reactor is provided with a fuel inlet, one end of the preheating section is connected to the fuel inlet tube, and the other end of the preheating section is connected to the combustion section.

[0008] In some embodiments, the reforming hydrogen production reaction system further includes a preheating unit, which is spaced apart from the reforming unit in the first direction, and is located downstream of the reforming unit in the flow direction of the flue gas.

[0009] In some embodiments, the preheating unit has a preheating tube having a feed end and a discharge end. The reactor is provided with a raw material feed port, the raw material feed port is connected to the feed end, and the discharge end is connected to the reforming unit.

[0010] In some embodiments, the reforming unit includes at least one reaction tube, the reactor is provided with a product outlet, one end of at least one reaction tube is connected to the discharge end, the other end of at least one reaction tube is connected to the product outlet, and the reaction tube is filled with a second catalyst.

[0011] In some embodiments, there are multiple catalytic combustion tubes, and the multiple catalytic combustion tubes are arranged at intervals in the circumferential direction of the reactor; and / or, there are multiple reaction tubes, and the multiple reaction tubes are arranged at intervals in the circumferential direction of the reactor.

[0012] In some embodiments, the size of the catalytic combustion tube in the first direction is 10mm-1000mm, and the diameter of the catalytic combustion tube is 10mm-1000mm; and / or, the size of the reaction tube in the first direction is 100mm-1000mm, and the diameter of the reaction tube is 10mm-1000mm.

[0013] In some embodiments, the recovery unit includes a recovery pipe, an exhaust valve and a fan, one end of the recovery pipe is connected to the air outlet, the other end of the recovery pipe is connected to the air inlet, and the exhaust valve and the fan are arranged on the recovery pipe.

[0014] In some embodiments, the reforming hydrogen production reaction system further includes a first mixed flow network, which is arranged between the catalytic combustion unit and the reforming unit; and / or, the reforming hydrogen production reaction system further includes a second mixed flow network, which is arranged between the reforming unit and the preheating unit. BRIEF DESCRIPTION OF THE DRAWINGS

[0015] Figure 1 Schematic diagram of a reforming hydrogen production reaction system according to an embodiment of the present invention.

[0016] Figure 2 It is a schematic diagram of the raw material flow of the reforming hydrogen production reaction system according to an embodiment of the present invention.

[0017] Figure 3 It is a three-dimensional schematic diagram of a reforming hydrogen production reaction system according to an embodiment of the present invention.

[0018] Figure 4 Schematic diagram of a catalytic combustion unit according to an embodiment of the present invention.

[0019] Figure 5 Schematic diagram of a preheating unit according to an embodiment of the present invention.

[0020] Figure 6 is a schematic diagram of a reforming unit according to an embodiment of the present invention.

[0021] Reference numerals:

[0022] Reactor 1, chamber 11, air inlet 12, air outlet 13, fuel inlet 14, raw material feed inlet 15, product outlet 16,

[0023] Catalytic combustion unit 2, catalytic combustion tube 21, preheating section 211, combustion section 212,

[0024] Reforming unit 3, reaction tube 31, recovery unit 4, recovery tube 41, exhaust valve 42, fan 43,

[0025] Preheating unit 5, preheating tube 51, feed end 511, discharge end 512,

[0026] The first mixed flow network 6 and the second mixed flow network 7. DETAILED DESCRIPTION

[0027] Embodiments of the present invention are described in detail below, and examples of the embodiments are shown in the accompanying drawings. The embodiments described below with reference to the accompanying drawings are exemplary and intended to be used to explain the present invention, but should not be understood as limiting the present invention.

[0028] The reforming hydrogen production reaction system of the embodiment of the present invention includes a reactor 1, a catalytic combustion unit 2, a reforming unit 3 and a recovery unit 4. The reactor 1 has a chamber 11. The catalytic combustion unit 2 and the reforming unit 3 are installed in the chamber 11, and the catalytic combustion unit 2 and the reforming unit 3 are arranged relative to each other in the first direction, so that the flue gas generated by the catalytic combustion of the catalytic combustion unit 2 is transmitted to the reforming unit 3, and the reforming unit 3 absorbs the heat of the flue gas to perform a reforming reaction. The recovery unit 4 is arranged outside the chamber 11, and the reactor 1 is provided with at least one air inlet 12 and at least one air outlet 13, the air inlet 12 is located on the side of the catalytic combustion unit 2 away from the reforming unit 3, and the air outlet 13 is located on the side of the reforming unit 3 away from the catalytic combustion unit 2, one end of the recovery unit 4 is connected to the air outlet 13, and the other end of the recovery unit 4 is connected to the air inlet 12, so that the flue gas after absorbing heat by the reforming unit 3 flows into the catalytic combustion unit 2 through the recovery unit 4, and is mixed with the flue gas generated by the catalytic combustion of the catalytic combustion unit 2.

[0029] Specifically, Figure 1-Figure 3 As shown, the catalytic combustion unit 2 is located at the upper end of the chamber 11, and the catalytic combustion unit 2 performs catalytic combustion to generate high-temperature flue gas, and the generated high-temperature flue gas flows downward to the reforming unit 3. The reforming unit 3 is located at the lower end of the chamber 11, and the reforming unit 3 absorbs heat from the high-temperature flue gas to perform a reforming reaction.

[0030] The upper end of the reactor 1 is provided with at least one air inlet 12, and the lower end of the reactor 1 is provided with at least one air outlet 13. The air inlet 12 is located above the catalytic combustion unit 2, and the air outlet 13 is located below the reforming unit 3. The recovery unit 4 is arranged outside the reactor 1, and the upper end of the recovery unit 4 is connected to the air inlet 12, and the lower end of the recovery unit 4 is connected to the air outlet 13. The recovery unit 4 receives the flue gas after the reforming reaction absorbs heat, and transmits it to the catalytic combustion unit 2 through the air inlet 12. The flue gas transmitted to the catalytic combustion unit 2 through the recovery unit 4 is connected to the catalytic combustion unit 3. After the flue gas generated by the catalytic combustion of element 2 is mixed, the mixed flue gas is transmitted to the reforming unit 3, and the reforming unit 3 absorbs the heat in the mixed flue gas. The mixed flue gas after the heat is absorbed by the reforming unit 3 flows to the recovery unit 4 through the outlet 13, and is transmitted to the catalytic combustion unit 2 through the connection between the recovery unit 4 and the air inlet 12. The heat of the flue gas is recycled through the recovery unit 4, which reduces the amount of heat that the catalytic combustion unit 2 needs to provide, that is, the catalytic combustion unit 2 needs to provide less catalytic combustion reaction to achieve the same reforming temperature, thereby achieving energy saving and emission reduction.

[0031] Compared with the arrangement in the related art of arranging the catalytic combustion unit 2 and the reforming unit 3 in the same area, the embodiment of the present invention arranges the catalytic combustion unit 2 and the reforming unit 3 correspondingly in the upper and lower directions. The heat provided by the catalytic combustion unit 2 flows downward to the reforming unit 3, and the flue gas is continuously mixed during the downward flow, thereby reducing the problem of unstable reforming hydrogen production caused by the uncontrollable catalytic combustion temperature and improving the temperature uniformity of the flue gas provided by the catalytic combustion unit 2.

[0032] When the reactor 1 is provided with one air inlet 12 and one air outlet 13, the air inlet 12 is provided at the middle position of the upper end of the reactor 1, and the air outlet 13 is provided at the middle position of the lower end of the reactor 1, so as to facilitate the recovery unit 4 to recycle the flue gas. When the reactor 1 is provided with multiple air inlets 12 and air outlets 13, the multiple air inlets 12 are all provided on the upper end surface of the reactor 1 and are arranged at intervals along the circumference of the reactor 1, and the multiple air outlets 13 are all provided on the lower end surface of the reactor 1 and are arranged at intervals along the circumference of the reactor 1, and the multiple air inlets 12 and the multiple air outlets 13 are arranged one by one, so as to improve the recovery efficiency of the flue gas by the recovery unit 4.

[0033] For example, the flue gas generated by catalytic combustion in the catalytic combustion unit 2 is the first flue gas, and the first flue gas flows to the reforming unit 3 to provide heat for the reforming unit 3. The first flue gas is heat-absorbed by the reforming unit 3 to become the second flue gas, and the temperature of the first flue gas is greater than the temperature of the second flue gas. The second flue gas flows to the recovery unit 4 through the gas outlet 13 to form the recovered flue gas, and the recovered flue gas is transmitted to the catalytic combustion unit 2 through the recovery unit 4 to mix with the first flue gas generated by the catalytic combustion to form the mixed flue gas, and the temperature of the mixed flue gas is greater than the temperature of the recovered flue gas, and the temperature of the mixed flue gas is lower than the temperature of the first flue gas, and the mixed flue gas flows to the reforming unit 3 to provide heat for the reforming unit 3, and the flue gas after heat absorption by the reforming unit 3 is recovered by the recovery unit 4 and the recovered flue gas is transmitted to the catalytic combustion unit 2 for recycling.

[0034] It should be noted that the temperature of the high-temperature flue gas generated by the catalytic combustion of the catalytic combustion unit 2 is about 500°C, while the reaction temperature required by the reforming unit 3 is about 200°C. When the temperature of the catalytic combustion unit 2 is too high, it is easy to accelerate the failure of the first catalyst and the second catalyst, and the reaction rate of the catalytic combustion unit 2 is much higher than the reaction rate of the reforming unit 3. The combustion controllability of the catalytic combustion unit 2 is poor, which makes it difficult to control the heat temperature provided by the catalytic combustion unit 2, and local hot spots are prone to occur, resulting in uneven temperature distribution, which in turn leads to a reduction in the service life of the reactor 1. The embodiment of the present invention sets a recovery unit 4, and the recovery unit 4 recovers the flue gas after absorbing heat from the reforming unit 3 and transmits it to the catalytic combustion unit 2 to cool the catalytic combustion unit 2, thereby ensuring the combustion controllability of the catalytic combustion unit 2, thereby increasing the service life of the catalyst and increasing the service life of the reactor 1.

[0035] When the temperature of the recovered flue gas is greater than or equal to the required temperature of the reforming unit 3, the catalytic combustion unit 2 does not perform catalytic combustion, and the recovered flue gas directly flows downward to the reforming unit 3 to provide heat for the reforming unit 3. When the temperature of the recovered flue gas is lower than the required temperature of the reforming unit 3, the catalytic combustion unit 2 determines the supply of fuel according to the temperature of the recovered flue gas, and the catalytic combustion unit 2 performs catalytic combustion to generate the first flue gas, which is mixed with the recovered flue gas to form a mixed flue gas, and the mixed flue gas flows downward to the reforming unit 3 to provide heat for the reforming unit 3.

[0036] Therefore, the reforming hydrogen production reaction system of the embodiment of the present invention recovers the flue gas after absorbing heat by the reforming unit 3 by setting up a flue gas recovery unit 4, provides the recovered flue gas to the catalytic combustion unit 2 through the recovery unit 4, and determines whether the catalytic combustion unit 2 needs to provide the first flue gas and the flue gas amount of the first flue gas required to be provided by the catalytic combustion unit 2 according to the temperature of the recovered flue gas, and forms a mixed flue gas by mixing the first flue gas and the recovered flue gas, that is, the recovered flue gas is heated by the first flue gas so that the temperature of the mixed flue gas matches the required temperature of the reforming unit 3, forming a heat supply with the recovered flue gas as the main source and the first flue gas provided by the catalytic combustion unit 2 as the auxiliary source, fundamentally changing the heating mode that completely relies on the catalytic combustion unit 2 to provide heat, improving the controllability and stability of the catalytic combustion unit 2, and then improving the uniformity of the temperature distribution in the reactor 1, thereby improving the hydrogen production stability of the reforming unit 3.

[0037] In some embodiments, the catalytic combustion unit 2 includes at least one catalytic combustion tube 21 , one end of the at least one catalytic combustion tube 21 is suitable for being connected to a fuel source, and the at least one catalytic combustion tube 21 is filled with a first catalyst to catalyze the combustion of the fuel.

[0038] Specifically, Figure 4 As shown, the upper end of the catalytic combustion tube 21 is connected to the fuel source, and the first catalyst can be coated on the inside of the catalytic combustion tube 21, or can be filled in the catalytic combustion tube 21. When the number of the catalytic combustion tube 21 is one, the catalytic combustion tube 21 is arranged at the position of the central axis of the reactor 1, so as to facilitate the uniform distribution of the flue gas generated after the fuel combustion in the reactor 1.

[0039] For example, the fuel source may be a mixed fuel formed by mixing methanol and air, a mixed fuel formed by mixing hydrogen and air, or other fuels. The mixed fuel enters the catalytic combustion tube 21 from the fuel inlet 14, reacts with the catalyst and burns to generate flue gas, which flows downward to the reforming unit 3 to provide heat. The first catalyst is a catalyst with metal oxides such as aluminum oxide, zirconium oxide, and yttrium oxide as carriers and precious metals such as platinum and palladium as active ingredients.

[0040] In some embodiments, the catalytic combustion tube 21 includes a preheating section 211 and a combustion section 212 . A fuel inlet 14 is provided on the reactor 1 . One end of the preheating section 211 is connected to the fuel inlet 14 , and the other end of the preheating section 211 is connected to the combustion section 212 .

[0041] Specifically, the combustion section 212 extends in the up-down direction, the upper end of the preheating section 211 is connected to the fuel inlet 14, and the lower end of the preheating section 211 is connected to the combustion section 212 to transfer the preheated fuel to the fuel section. When the number of the catalytic combustion tube 21 is one, the preheating section 211 is a vertical tube extending in the up-down direction, and no catalyst is provided in the preheating section 211, and the fuel is preheated by the preheating section 211.

[0042] In some embodiments, the reforming hydrogen production reaction system further includes a preheating unit 5 , which is spaced apart from the reforming unit 3 in the first direction, and is located downstream of the reforming unit 3 in the flow direction of the flue gas.

[0043] Specifically, Figure 5 As shown, the preheating unit 5 is located in the chamber 11, and the preheating unit 5 is located at the lower end of the reforming unit 3. In the reactor 1, the flue gas generated by the catalytic combustion unit 2 flows downward to the reforming unit 3, and the reforming unit 3 absorbs the heat in the flue gas to perform a reforming reaction. The flue gas after the heat absorption by the reforming unit 3 continues to flow downward to the preheating unit 5. The preheating unit 5 absorbs the flue gas from the reforming unit 3 and the heat in the flue gas to preheat the reforming raw material, that is, the catalytic combustion unit 2 generates flue gas, which flows to the preheating unit 5 after passing through the reforming unit 3, and flows to the recovery unit 4 from the gas outlet 13 after passing through the preheating unit 5.

[0044] In the embodiment of the present invention, the preheating unit 5 is arranged below the reforming unit 3, so that the preheating unit 5 can preheat the reforming raw material by using the temperature of the flue gas after absorbing heat from the reforming unit 3, thereby improving the utilization rate of the flue gas and the reaction efficiency of the reforming unit 3.

[0045] In some embodiments, the preheating unit 5 includes a preheating tube 51, which has a feed end 511 and a discharge end 512. The reactor 1 is provided with a raw material feed port 15, which is connected to the feed end 511, and the discharge end 512 is connected to the reforming unit 3.

[0046] Specifically, Figure 5 As shown, the preheating tube 51 is a serpentine tube. The feed end 511 of the serpentine tube is located on the left side of the preheating tube 51, and the discharge end 512 is located on the right side of the preheating tube 51. The raw material feed port 15 is arranged at the lower left end of the reactor 1. The raw material feed port 15 is connected to the feed end 511 so as to transport the raw material into the preheating unit 5. The discharge end 512 is connected to the lower end of the reforming unit 3.

[0047] The raw material exchanges heat with the flue gas outside the preheating tube 51 while flowing through the serpentine pipe of the preheating unit 5, thereby preheating the raw material. The discharge end 512 is connected to the reforming unit 3 to transfer the preheated raw material to the reforming unit 3 for reforming reaction.

[0048] In some embodiments, the reforming unit 3 includes at least one reaction tube 31, a product outlet 16 is provided on the reactor 1, one end of at least one reaction tube 31 is connected to the discharge end 512, and the other end of at least one reaction tube 31 is connected to the product outlet 16, and the reaction tube 31 is filled with a second catalyst.

[0049] Specifically, Figure 6 As shown, the lower end of the reaction tube 31 is connected to the discharge end 512 of the preheating unit 5 to receive the preheated raw materials, and the upper end of the reaction tube 31 is connected to the product outlet 16 to output the reaction product. The second catalyst can be coated on the inside of the catalytic combustion tube 21, or filled in the catalytic combustion tube 21. When the number of reaction tubes 31 is one, the reaction tube 31 is arranged at the position of the central axis of the reactor 1, so as to facilitate sufficient heat exchange with the flue gas outside the reaction tube 31.

[0050] For example, the second catalyst is a catalyst using copper oxide, zinc oxide, or aluminum oxide as a carrier and a metal such as copper as an active ingredient.

[0051] In some embodiments, there are multiple catalytic combustion tubes 21, and the multiple catalytic combustion tubes 21 are arranged at intervals in the circumferential direction of the reactor 1; and / or, there are multiple reaction tubes 31, and the multiple reaction tubes 31 are arranged at intervals in the circumferential direction of the reactor 1.

[0052] Specifically, when the number of catalytic combustion tubes 21 is multiple, such as two, three, four, five, six, seven, etc., multiple catalytic combustion tubes 21 are evenly spaced in the circumferential direction of the reactor 1, and multiple catalytic combustion tubes 21 are filled with a first catalyst to facilitate catalytic combustion to provide heat. The embodiment of the present invention does not limit the number of catalytic combustion tubes 21, as long as the required reaction temperature can be provided for the reforming unit 3. When the number of reaction tubes 31 is multiple, such as two, three, four, five, six, seven, etc., multiple reaction tubes 31 are evenly spaced in the circumferential direction of the reactor 1, and multiple reaction tubes 31 are filled with a second catalyst to facilitate the reforming reaction. The embodiment of the present invention does not limit the number of reaction tubes 31, as long as the reforming reaction of the reforming unit 3 can be achieved.

[0053] When there are multiple catalytic combustion tubes 21, the multiple catalytic combustion tubes 21 are evenly spaced in the circumferential direction of the reactor 1, and each catalytic combustion tube 21 includes a preheating section 211 and a combustion section 212. Since the fuel inlet 14 is located in the middle of the upper end surface of the reactor 1, the upper ends of the multiple preheating sections 211 are connected to the fuel inlet 14, and the preheating section 211 is an arc-shaped pipe section, that is, the curved pipe of the preheating section 211 facilitates the communication of the multiple preheating sections 211 with the fuel inlet 14 while preheating the fuel. Since the flow path of the fuel in the curved pipe is greater than the flow path of the vertical pipe, the preheating section 211 of the arc-shaped pipe section can achieve a better preheating effect.

[0054] Optionally, the multiple catalytic combustion tubes 21 can also be fixed by one or more brackets, one end of the bracket is connected to the catalytic combustion tube 21, and the other end of the bracket is connected to the side wall of the reactor 1, so as to ensure the stability of the multiple catalytic combustion tubes 21. The reaction tube 31 can also be fixed by one or more brackets, one end of the bracket is connected to the reaction tube 31, and the other end of the bracket is connected to the side wall of the reactor 1, so as to ensure the stability of the multiple reaction tubes 31.

[0055] In some embodiments, the size of the catalytic combustion tube 21 in the first direction is 10mm-1000mm, and the diameter of the catalytic combustion tube 21 is 10mm-1000mm; and / or, the size of the reaction tube 31 in the first direction is 100mm-1000mm, and the diameter of the reaction tube 31 is 10mm-1000mm.

[0056] The size of the catalytic combustion tube 21 in the up and down direction, i.e., the length of the catalytic combustion tube 21 and the setting of the diameter of the catalytic combustion tube 21, can be based on the space velocity performance of the first catalyst placed in the catalytic combustion tube 21 as a reference to ensure the full combustion of the catalytic combustion unit 2. When the diameter of the reaction tube 31 is greater than 1000mm, the heat exchange effect between the second catalyst and the raw material in the reaction tube 31 and the flue gas outside the reaction tube 31 is difficult to ensure. When the diameter of the reaction tube 31 is less than 10mm, the diameter is too small, and the reaction space in the reaction tube 31 is too small, which affects the reaction of the reforming unit 3. Since the raw material enters the reaction tube 31 from the lower end and continuously flows upward to react, when the size of the reaction tube 31 in the up and down direction is greater than 1000mm, the raw material may react in the middle of the reaction tube 31, wasting the second catalyst located in the upper end of the reaction tube 31, which is not conducive to the reaction of the reforming unit 3, and when the size of the reaction tube in the up and down direction is too long, the difficulty of installing the reaction tube will increase.

[0057] The embodiment of the present invention limits the dimensions of the catalytic combustion tube 21 and the reaction tube 31 in the vertical direction and the diameters of the catalytic combustion tube 21 and the reaction tube 31 to ensure sufficient combustion of the fuel in the catalytic combustion tube 21 and sufficient reaction of the raw materials in the reaction tube 31, thereby improving the hydrogen production efficiency.

[0058] In some embodiments, the recovery unit 4 includes a recovery pipe 41 , an exhaust valve 42 and a fan 43 , one end of the recovery pipe 41 is connected to the air outlet 13 , the other end of the recovery pipe 41 is connected to the air inlet 12 , and the exhaust valve 42 and the fan 43 are arranged on the recovery pipe 41 .

[0059] Specifically, the upper end of the recovery pipe 41 is connected to the air inlet 12, and the lower end of the recovery pipe 41 is connected to the air outlet 13. The number of air inlets 12 is the same as the number of recovery pipes 41, that is, when the number of air inlets 12 is one, the number of recovery pipes 41 is one, and when the number of air inlets 12 is multiple, the number of recovery pipes 41 is also set to multiple, and multiple recovery pipes 41 are arranged one by one with the air inlet 12. Each recovery pipe 41 is provided with an exhaust valve 42 and a fan 43, and the fan 43 accelerates the recovery speed of the flue gas. Since the catalytic combustion unit 2 continuously burns to provide flue gas, and the flue gas recovered by the recovery pipe 41 is continuously transmitted to the catalytic combustion unit 2 to provide recovered flue gas, the volume of the chamber 11 of the reactor 1 is fixed, and the pressure in the reactor 1 is ensured by setting the exhaust valve 42.

[0060] In some embodiments, the reforming hydrogen production reaction system also includes a first mixed flow network 6, which is arranged between the catalytic combustion unit 2 and the reforming unit 3; and / or, the reforming hydrogen production reaction system also includes a second mixed flow network 7, which is arranged between the reforming unit 3 and the preheating unit 5.

[0061] Specifically, the recovered flue gas is mixed with the flue gas after combustion in the catalytic combustion unit 2 and flows downward to the reforming unit 3 through the first mixed flow net 6. The first mixed flow net 6 is set to make the temperature of the flue gas entering the reforming unit 3 uniform, thereby improving the stability of the reforming reaction in the reforming unit 3. The flue gas after absorbing heat in the reforming unit 3 flows downward to the preheating unit 5 through the second mixed flow net 7. The second mixed flow net 7 is set to make the temperature of the flue gas entering the preheating unit 5 uniform, thereby improving the uniformity of preheating the raw materials by the preheating unit 5.

[0062] In the description of the present invention, it is to 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”, “axial”, “radial”, “circumferential”, etc., indicating orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as limiting the present invention.

[0063] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of the features. In the description of the present invention, the meaning of "plurality" is at least two, such as two, three, etc., unless otherwise clearly and specifically defined.

[0064] In the present invention, unless otherwise clearly specified and limited, the terms "installed", "connected", "connected", "fixed" and the like should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral one; it can be a mechanical connection, an electrical connection, or communication with each other; it can be a direct connection, or an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements, unless otherwise clearly defined. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0065] In the present invention, unless otherwise clearly specified and limited, a first feature being "above" or "below" a second feature may mean that the first and second features are in direct contact, or that the first and second features are in indirect contact through an intermediate medium. Moreover, a first feature being "above", "above" or "above" a second feature may mean that the first feature is directly above or obliquely above the second feature, or simply means that the first feature is higher in level than the second feature. A first feature being "below", "below" or "below" a second feature may mean that the first feature is directly below or obliquely below the second feature, or simply means that the first feature is lower in level than the second feature.

[0066] In the present invention, the terms "one embodiment", "some embodiments", "examples", "specific examples", or "some examples" etc. mean that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present invention. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the described specific features, structures, materials or characteristics may be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art may combine and combine the different embodiments or examples described in this specification and the features of the different embodiments or examples, without contradiction.

[0067] It is to be understood that the above embodiments are exemplary and are not to be construed as limiting the present invention. A person skilled in the art may change, modify, replace and modify the above embodiments within the scope of the present invention.

Claims

1. A reforming hydrogen production reaction system, characterized in that: include: a reactor having a chamber; A catalytic combustion unit and a reforming unit, wherein the catalytic combustion unit and the reforming unit are installed in the chamber, and the catalytic combustion unit and the reforming unit are arranged opposite to each other in a first direction, so that the flue gas generated by the catalytic combustion of the catalytic combustion unit is transmitted to the reforming unit, and the reforming unit absorbs the heat of the flue gas to perform a reforming reaction; A recovery unit, wherein the recovery unit is arranged outside the chamber, and the reactor is provided with at least one air inlet and at least one air outlet, wherein the air inlet is located on a side of the catalytic combustion unit away from the reforming unit, and the air outlet is located on a side of the reforming unit away from the catalytic combustion unit, one end of the recovery unit is connected to the air outlet, and the other end of the recovery unit is connected to the air inlet, so that the flue gas after absorbing heat in the reforming unit flows into the catalytic combustion unit through the recovery unit and mixes with the flue gas generated by catalytic combustion in the catalytic combustion unit.

2. The reforming hydrogen production reaction system according to claim 1, characterized in that: The catalytic combustion unit comprises at least one catalytic combustion tube, one end of the at least one catalytic combustion tube is suitable for being connected to a fuel source, and the at least one catalytic combustion tube is filled with a first catalyst to catalyze the combustion of the fuel.

3. The reforming hydrogen production reaction system according to claim 2, characterized in that: The catalytic combustion tube comprises a preheating section and a combustion section. A fuel inlet is provided on the reactor. One end of the preheating section is connected to the fuel inlet pipe, and the other end of the preheating section is connected to the combustion section.

4. The reforming hydrogen production reaction system according to claim 2, characterized in that: It also includes a preheating unit, which is arranged at an interval with the reforming unit in the first direction, and the preheating unit is located downstream of the reforming unit in the flow direction of the flue gas.

5. The reforming hydrogen production reaction system according to claim 4, characterized in that: The preheating unit has a preheating tube, which has a feed end and a discharge end. The reactor is provided with a raw material feed port, which is connected to the feed end, and the discharge end is connected to the reforming unit.

6. The reforming hydrogen production reaction system according to claim 5, characterized in that: The reforming unit comprises at least one reaction tube, the reactor is provided with a product outlet, one end of at least one reaction tube is connected to the discharge end, the other end of at least one reaction tube is connected to the product outlet, and the reaction tube is filled with a second catalyst.

7. The reforming hydrogen production reaction system according to claim 6, characterized in that: There are multiple catalytic combustion tubes, and the multiple catalytic combustion tubes are arranged at intervals in the circumferential direction of the reactor; and / or, There are multiple reaction tubes, and the multiple reaction tubes are arranged at intervals in the circumferential direction of the reactor.

8. The reforming hydrogen production reaction system according to claim 6, characterized in that: The size of the catalytic combustion tube in the first direction is 10 mm-1000 mm, and the diameter of the catalytic combustion tube is 10 mm-1000 mm; and / or, The size of the reaction tube in the first direction is 100 mm-1000 mm, and the diameter of the reaction tube is 10 mm-1000 mm.

9. The reforming hydrogen production reaction system according to claim 1, characterized in that: The recovery unit comprises a recovery pipe, an exhaust valve and a fan, one end of the recovery pipe is connected to the air outlet, the other end of the recovery pipe is connected to the air inlet, and the exhaust valve and the fan are arranged on the recovery pipe.

10. The reforming hydrogen production reaction system according to claim 4, characterized in that: It also includes a first mixed flow network, wherein the first mixed flow network is arranged between the catalytic combustion unit and the reforming unit; and / or, It also includes a second mixed flow network, which is arranged between the reforming unit and the preheating unit.

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