A natural gas hydrogen production device and method

Abstract

The present invention relates to a natural gas hydrogen production device and method, the natural gas hydrogen production device comprises a central transmission unit and a catalytic reaction unit arranged around the central transmission unit; the catalytic reaction unit is provided with a reforming catalytic zone, a cooling zone and a conversion catalytic zone in sequence from bottom to top; the bottom of the natural gas hydrogen production device is provided with a combustion-aiding gas inlet; the top of the central transmission unit is provided with a raw gas inlet; the natural gas hydrogen production device is provided with a baffle; the center line of the baffle coincides with the center line of the natural gas hydrogen production device. In the present invention, through the reasonable design of the structure of the small hydrogen generator, the thermal efficiency of the hydrogen production process is improved, the prepared hydrogen has a high purity, and a self-heating system is adopted to avoid dependence on external heat sources for natural gas reforming.

Description

Technical Field

[0001] The present invention relates to the field of hydrogen production by reforming natural gas, and in particular to a natural gas hydrogen production device and method. Background Art

[0002] Hydrogen energy is a recognized clean energy source, and is emerging as a low-carbon and zero-carbon energy source. Due to its advantages such as high energy density and zero carbon emissions, hydrogen energy is considered to be the most promising alternative to fossil fuels in the future, and has always been regarded as the "ultimate solution" in the field of mobile energy represented by hydrogen fuel cell vehicles.

[0003] At present, the production of hydrogen mainly includes: hydrogen production from fossil energy, hydrogen recovery from industrial by-products and hydrogen production from water electrolysis. Taking into account the production cost, hydrogen is currently mainly obtained by the first two methods. For example, WO2017080207A1 discloses a methanol water reforming hydrogen production machine and a hydrogen production method thereof, wherein the methanol water reforming hydrogen production machine includes a methanol water storage container (1), a delivery pump (2), a frequency converter (3), a heat exchanger (5) and a reformer (4), wherein: the frequency converter (3) is used to convert a low-frequency voltage or a DC voltage into a high-frequency voltage required by the electromagnetic coil (421) of the electromagnetic heater (42), and the frequency converter (3) is provided with a liquid cooling radiator (31), and the methanol water raw material is in the delivery pump ( 2) during the pumping process, the liquid flows through the liquid cooling radiator (31), so that the heat generated by the frequency converter (3) is taken away by the methanol water raw material; the reformer (4) is provided with a reforming chamber (41), an electromagnetic heater (42) and a hydrogen purification device (43), the electromagnetic heater (42) includes an electromagnetic coil (421) and a metal magnet (422), the electromagnetic coil (421) can generate a high-frequency magnetic field after inputting a high-frequency voltage, so that the metal magnet (422) is induced by the magnetic field and generates heat, thereby providing heat energy for the reforming chamber (41). The frequency converter (3) has low noise, good heat dissipation effect, low energy consumption, and the heat generated can be effectively utilized.

[0004] CN105621357A discloses a method for producing hydrogen by reforming methane, which adopts a moving bed radial flow reactor. The reactor is divided into a fluid feed channel, a catalyst fixed bed layer, a catalyst moving bed layer and a fluid discharge channel from the outside to the inside or from the inside to the outside in the radial direction; a fluid feed port and a fluid discharge port are respectively arranged at the top and the bottom of the reactor; the fluid feed port is communicated with the fluid feed channel, and the fluid discharge port is communicated with the fluid discharge channel; a moving bed catalyst inlet is arranged at the top of the catalyst moving bed layer, and a moving bed catalyst outlet is arranged at the bottom; the fluid feed channel, the catalyst fixed bed layer, the catalyst moving bed layer and the fluid discharge channel are separated by a material with pores, and the pore size satisfies that gas can pass through but catalyst particles cannot pass through; the method for producing hydrogen by reforming methane simplifies the device construction and operation process, saves energy consumption, and is conducive to realizing continuous reaction and regeneration in production.

[0005] However, both fossil energy hydrogen production and industrial by-product hydrogen recovery are industrial devices with large-scale hydrogen production and low cost. However, to supply distributed users in the surrounding area, they need to be transported by trailers or tank trucks, which has high transportation costs and limits the scope of hydrogen supply and use. At present, my country's hydrogen energy demonstration applications are mainly arranged around the hydrogen production site (less than 200 kilometers), and hydrogen storage and transportation are mainly in high-pressure gaseous form. Furthermore, for users with small consumption and discontinuous gas consumption, there are still problems such as inconvenient access to hydrogen or poor purity of the produced hydrogen. Summary of the invention

[0006] In view of the problems existing in the prior art, the purpose of the present invention is to provide a natural gas hydrogen production device and method, through the integrated design of the equipment, convenient and efficient preparation of hydrogen can be achieved, which can meet the needs of customers with less usage.

[0007] To achieve this object, the present invention adopts the following technical solutions:

[0008] In a first aspect, the present invention provides a natural gas hydrogen production device, the natural gas hydrogen production device comprising a central transmission unit and a catalytic reaction unit arranged around the central transmission unit;

[0009] The catalytic reaction unit is provided with a reforming catalytic zone, a cooling zone and a shift catalytic zone in sequence from bottom to top;

[0010] The bottom of the natural gas hydrogen production equipment is provided with a fuel gas inlet;

[0011] A raw gas inlet is provided at the top of the central transmission unit;

[0012] The equipment for producing hydrogen from natural gas is provided with a baffle;

[0013] The center line of the baffle coincides with the center line of the natural gas hydrogen production equipment.

[0014] In the present invention, the thermal efficiency of the hydrogen production process is improved through the reasonable design of the structure of the small hydrogen generator, the prepared hydrogen has high purity, and the self-heating system is adopted to avoid dependence on external heat sources for natural gas reforming. The equipment is embedded with waste heat recovery tubes to recover the heat of high-temperature reformed gas and shift reaction for preheating of raw gas, realizing the cascade utilization of energy and high energy utilization rate.

[0015] As a preferred technical solution of the present invention, the cooling zone and the conversion catalytic zone are both shell-and-tube heat exchange structures.

[0016] In the present invention, the embedded waste heat recovery tubes are used to recover the heat of high-temperature reformed gas and shift reaction, which is used for preheating the raw gas, thus realizing the cascade utilization of energy and achieving high energy utilization rate.

[0017] Preferably, at least two baffles are provided, for example, 2, 3, 4, 5, 6 or 7, etc., but are not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0018] Preferably, when two baffles are provided, the first baffle is provided in the conversion catalytic zone, and the second baffle is provided in the cooling zone. When more than two baffles are provided, an appropriate number can be added in each zone according to demand.

[0019] Preferably, the baffle is set up with an area of ​​60-70% of the plane area perpendicular to the center line of the natural gas hydrogen production device, for example, it can be 60%, 61%, 62%, 63%, 64%, 65%, 66%, 67%, 68%, 69% or 70%, etc., but is not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0020] Preferably, the cooling zone and the conversion catalytic zone are connected to the central transmission unit via heat exchange holes.

[0021] Preferably, the combustion-supporting gas inlet is provided with an igniter and a combustion nozzle.

[0022] Preferably, the outer wall of the natural gas hydrogen production equipment is provided with a heat insulation layer.

[0023] In a second aspect, the present invention provides a method for producing hydrogen from natural gas, the method comprising: preheating the raw gas and passing it through a combustion zone of an auxiliary combustion gas, and then obtaining hydrogen through reforming reaction, cooling and conversion catalysis in sequence.

[0024] The hydrogen-rich gas obtained by the present invention can be purified to obtain pure hydrogen.

[0025] As a preferred technical solution of the present invention, the raw gas includes natural gas and water vapor.

[0026] Preferably, the volume ratio of natural gas to water vapor in the raw gas is 1:(1-2.5), for example, it can be 1:1, 1:1.1, 1:1.2, 1:1.3, 1:1.4, 1:1.5, 1:1.6, 1:1.7, 1:1.8, 1:1.9, 1:2, 1:2.1, 1:2.2, 1:2.3, 1:2.4 or 1:2.5, etc., but is not limited to the listed values, and other values ​​not listed in this range are also applicable.

[0027] As a preferred technical solution of the present invention, the catalyst in the reforming reaction includes a nickel-based catalyst and / or a nickel-platinum-based catalyst, which are commonly used catalysts in the art.

[0028] In the present invention, the nickel-based catalyst can be Ni / Al2 O 3 Catalyst, Ni / ZrO catalyst or Ni / MgO catalyst, etc.

[0029] In the present invention, the nickel-platinum-based catalyst may be Ni-Pt / Al 2 O 3 Catalyst, Ni-Pt / ZrO catalyst or Ni-Pt / MgO catalyst, etc.

[0030] As a preferred technical solution of the present invention, the temperature of the reforming reaction is 800-1000°C, for example, it can be 800°C, 820°C, 840°C, 860°C, 880°C, 900°C, 920°C, 940°C, 960°C, 980°C or 1000°C, but is not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0031] As a preferred technical solution of the present invention, the cooling is to cool the reformed material.

[0032] Preferably, the terminal temperature of the cooling is 450-500°C, for example, it can be 450°C, 455°C, 460°C, 465°C, 470°C, 475°C, 480°C, 485°C, 490°C, 495°C or 500°C, but is not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0033] As a preferred technical solution of the present invention, the catalyst in the conversion catalyst is a carbon monoxide conversion catalyst.

[0034] Preferably, the carbon monoxide shift catalyst comprises a medium-shift series low-shift catalyst.

[0035] In the present invention, the carbon monoxide conversion catalyst can be Fe 2 O 3 -Cr 2 O 3 -Al 2 O 3 Catalyst and / or CuO-ZnO-Al 2 O 3 Catalysts, etc.

[0036] As a preferred technical solution of the present invention, the temperature of the conversion catalysis is 200-500°C, for example, it can be 200°C, 220°C, 240°C, 260°C, 280°C, 300°C, 320°C, 340°C, 360°C, 380°C, 400°C, 420°C, 440°C, 460°C, 480°C or 500°C, but is not limited to the listed values, and other unlisted values ​​within the range are also applicable.

[0037] As a preferred technical solution of the present invention, the method comprises: preheating the raw gas and passing it through a combustion zone of an auxiliary gas, and then successively performing a reforming reaction, cooling and a conversion catalysis to obtain hydrogen;

[0038] The volume ratio of natural gas to water vapor in the raw gas is 1:(1-2.5);

[0039] The cooling end point temperature is 450-500°C;

[0040] The temperature of the shift catalysis is 200-500°C.

[0041] Compared with the prior art solutions, the present invention has at least the following beneficial effects:

[0042] In the present invention, the thermal efficiency of the hydrogen production process is improved by the reasonable design of the structure of the small hydrogen generator. The hydrogen production equipment completely adopts a self-heating system to avoid dependence on external heat sources for natural gas reforming. The equipment is embedded with waste heat recovery tubes to recover the heat of high-temperature reformed gas and shift reaction for preheating of raw gas. Through the coupling of the internal structure of a single device, the cascade utilization of energy is achieved, and the energy utilization rate is high. The flow rate of hydrogen in the obtained product can reach more than 2520kmol / L. BRIEF DESCRIPTION OF THE DRAWINGS

[0043] Figure 1 A natural gas hydrogen production device is provided in an embodiment of the present invention.

[0044] In the figure: 1-central transmission unit, 2-conversion catalytic zone, 3-cooling zone, 4-reforming catalytic zone, 5-igniter, A-raw gas, B-product, C-combustion gas.

[0045] The present invention is further described in detail below. However, the following examples are only simplified examples of the present invention and do not represent or limit the scope of protection of the present invention. The scope of protection of the present invention shall be subject to the claims. DETAILED DESCRIPTION

[0046] To better illustrate the present invention and facilitate understanding of the technical solution of the present invention, typical but non-limiting embodiments of the present invention are as follows:

[0047] Example 1

[0048] This embodiment provides a natural gas hydrogen production device, such as Figure 1 As shown, the natural gas hydrogen production equipment includes a central transmission unit 1 and a catalytic reaction unit arranged around it;

[0049] The catalytic reaction unit is provided with a reforming catalytic zone 4, a cooling zone 3 and a shift catalytic zone 2 in sequence from bottom to top;

[0050] The bottom of the natural gas hydrogen production equipment is provided with an auxiliary fuel gas C inlet;

[0051] A raw gas A inlet is provided at the top of the central transmission unit 1;

[0052] The equipment for producing hydrogen from natural gas is provided with a baffle;

[0053] The center line of the baffle coincides with the center line of the natural gas hydrogen production equipment.

[0054] The cooling zone 3 and the conversion catalytic zone 2 are both tube-in-tube heat exchange structures;

[0055] The baffles are provided with two, the first baffle is provided in the conversion catalytic zone 2, and the second baffle is provided in the cooling zone 3;

[0056] The installation area of ​​the baffle is 65% of the plane area perpendicular to the center line of the natural gas hydrogen production device;

[0057] The cooling zone 3 and the shift catalytic zone 2 are connected to the central transmission unit 1 through heat exchange holes;

[0058] The inlet of the combustion-supporting gas C is provided with an igniter 5 and a combustion nozzle;

[0059] The outer wall of the natural gas hydrogen production equipment is provided with a heat insulation layer.

[0060] Example 2

[0061] This embodiment provides a natural gas hydrogen production device, which includes a central transmission unit 1 and a catalytic reaction unit arranged around the central transmission unit 1;

[0062] The catalytic reaction unit is provided with a reforming catalytic zone 4, a cooling zone 3 and a shift catalytic zone 2 in sequence from bottom to top;

[0063] The bottom of the natural gas hydrogen production equipment is provided with an auxiliary fuel gas C inlet;

[0064] A raw gas A inlet is provided at the top of the central transmission unit 1;

[0065] The equipment for producing hydrogen from natural gas is provided with a baffle;

[0066] The center line of the baffle coincides with the center line of the natural gas hydrogen production equipment.

[0067] The cooling zone 3 and the conversion catalytic zone 2 are both tube-in-tube heat exchange structures;

[0068] The baffles are provided with two, the first baffle is provided in the conversion catalytic zone 2, and the second baffle is provided in the cooling zone 3;

[0069] The installation area of ​​the baffle is 70% of the plane area perpendicular to the center line of the natural gas hydrogen production device;

[0070] The cooling zone 3 and the shift catalytic zone 2 are connected to the central transmission unit 1 through heat exchange holes;

[0071] The inlet of the combustion-supporting gas C is provided with an igniter 5 and a combustion nozzle;

[0072] The outer wall of the natural gas hydrogen production equipment is provided with a heat insulation layer.

[0073] Example 3

[0074] This embodiment provides a natural gas hydrogen production device, which includes a central transmission unit 1 and a catalytic reaction unit arranged around the central transmission unit 1;

[0075] The catalytic reaction unit is provided with a reforming catalytic zone 4, a cooling zone 3 and a shift catalytic zone 2 in sequence from bottom to top;

[0076] The bottom of the natural gas hydrogen production equipment is provided with an auxiliary fuel gas C inlet;

[0077] A raw gas A inlet is provided at the top of the central transmission unit 1;

[0078] The equipment for producing hydrogen from natural gas is provided with a baffle;

[0079] The center line of the baffle coincides with the center line of the natural gas hydrogen production equipment.

[0080] The cooling zone 3 and the conversion catalytic zone 2 are both tube-in-tube heat exchange structures;

[0081] The baffles are provided with two, the first baffle is provided in the conversion catalytic zone 2, and the second baffle is provided in the cooling zone 3;

[0082] The installation area of ​​the baffle is 60% of the plane area perpendicular to the center line of the natural gas hydrogen production device;

[0083] The cooling zone 3 and the shift catalytic zone 2 are connected to the central transmission unit 1 through heat exchange holes;

[0084] The inlet of the combustion-supporting gas C is provided with an igniter 5 and a combustion nozzle;

[0085] The outer wall of the natural gas hydrogen production equipment is provided with a heat insulation layer.

[0086] Application Example 1

[0087] The hydrogen production equipment provided in Example 1 is used to produce hydrogen, and the method comprises: preheating the raw gas and passing it through a combustion zone of an auxiliary gas, and then sequentially performing a reforming reaction, cooling, and a conversion catalysis to obtain hydrogen;

[0088] The volume ratio of natural gas to water vapor in the raw gas is 1:2.5; the flow rate of natural gas is 1000 kmol / h, and the flow rate of water vapor is 2500 kmol / h;

[0089] The catalyst in the reforming reaction is Ni / Al 2 O 3 catalyst;

[0090] The temperature of the reforming reaction is 1000°C;

[0091] The cooling is to cool the reformed material;

[0092] The cooling end point temperature is 470°C;

[0093] The catalyst in the shift catalysis is CuO-ZnO-Al 2 O 3 catalyst;

[0094] The temperature of the shift catalyst is 250°C.

[0095] H 2 :2780kmol / h; CO: 80kmol / h; CH 4 :4kmol / h;CO 2 :915kmol / h; H 2 O: 1700kmol / h.

[0096] Application Example 2

[0097] The hydrogen production equipment provided in Example 1 is used to produce hydrogen, and the method comprises: preheating the raw gas and passing it through a combustion zone of an auxiliary gas, and then sequentially performing a reforming reaction, cooling, and a conversion catalysis to obtain hydrogen;

[0098] The volume ratio of natural gas to water vapor in the raw gas is 1:1; the flow rate of natural gas is 1000 kmol / h, and the flow rate of water vapor is 1000 kmol / h;

[0099] The catalyst in the reforming reaction is Ni / Al 2 O 3 catalyst;

[0100] The temperature of the reforming reaction is 800°C;

[0101] The cooling is to cool the reformed material;

[0102] The cooling end point temperature is 450°C;

[0103] The catalyst in the shift catalysis is Fe2 O 3 -Cr 2 O 3 -Al 2 O 3 catalyst;

[0104] The temperature of the shift catalyst is 450°C.

[0105] H 2 :2680kmol / h; CO: 230kmol / h; CH 4 :360kmol / h; CO 2 :410kmol / h; H 2 O: 600kmol / h.

[0106] Application Example 3

[0107] The hydrogen production equipment provided in Example 1 is used to produce hydrogen, and the method comprises: preheating the raw gas and passing it through a combustion zone of an auxiliary gas, and then sequentially performing a reforming reaction, cooling, and a conversion catalysis to obtain hydrogen;

[0108] The volume ratio of natural gas to water vapor in the raw gas is 1:1.5; the flow rate of natural gas is 1000 kmol / h, and the flow rate of water vapor is 1500 kmol / h;

[0109] The catalyst in the reforming reaction is Ni / Al 2 O 3 catalyst;

[0110] The temperature of the reforming reaction is 900°C;

[0111] The cooling is to cool the reformed material;

[0112] The cooling end point temperature is 500°C;

[0113] The catalyst in the shift catalysis is Fe 2 O 3 -Cr 2 O 3 -Al 2 O 3 catalyst;

[0114] The temperature of the shift catalyst is 350°C.

[0115] H 2 :2520kmol / h; CO: 255kmol / h; CH 4 :70kmol / h; CO 2 :675kmol / h; H 2 O: 845kmol / h.

[0116] Comparative Example 1

[0117] The only difference from Example 1 is that the volume ratio of natural gas to water vapor is 1:4, that is, the flow rate of water vapor is 4000 kmol / L, and the H 2 :2540kmol / h; CO: 23kmol / h; CH 4 :0.6kmol / h; CO 2 :976kmol / h; H 2 O: 3494 kmol / h. It can be seen that changing the volume ratio will lead to a decrease in the hydrogen flow rate, while the content of other components will increase significantly, making the quality of the resulting hydrogen-rich gas worse.

[0118] Comparative Example 2

[0119] The only difference from Example 1 is that no cooling zone is provided, and the H 2 :2138kmol / h; CO: 600kmol / h; CH 4 :3kmol / h;CO 2 :397kmol / h; H 2 O: 2355 kmol / h. When no cooling zone is provided, the hydrogen content in the hydrogen-rich gas is significantly reduced, and the carbon monoxide content is significantly increased, resulting in a decrease in the quality of the hydrogen product.

[0120] Comparative Example 3

[0121] The only difference from Example 1 is that the conversion catalytic zone and the central transmission unit are not provided with connecting holes, and the H 2 :2536kmol / h; CO: 61kmol / h; CH 4 :3kmol / h;CO 2 :936kmol / h; H 2 O: 1959 kmol / h. When no heat exchange holes are provided, the carbon dioxide content in the obtained product gas increases, and the hydrogen content decreases, so that the quality of the obtained hydrogen-rich gas decreases.

[0122] It can be seen from the results of the above embodiments and comparative examples that in the present invention, the thermal efficiency of the hydrogen production process is improved by the reasonable design of the structure of the small hydrogen generator, and the hydrogen production equipment completely adopts a self-heating system to avoid dependence on external heat sources for natural gas reforming. The equipment is embedded with waste heat recovery tubes to recover the heat of high-temperature reformed gas and shift reaction for preheating of raw gas. Through the coupling of the internal structure of a single device, the cascade utilization of energy is achieved, and the energy utilization rate is high.

[0123] The applicant declares that the present invention illustrates the detailed structural features of the present invention through the above-mentioned embodiments, but the present invention is not limited to the above-mentioned detailed structural features, that is, it does not mean that the present invention must rely on the above-mentioned detailed structural features to be implemented. Those skilled in the art should understand that any improvement of the present invention, equivalent replacement of the components selected by the present invention, addition of auxiliary components, selection of specific methods, etc., all fall within the protection scope and disclosure scope of the present invention.

[0124] The preferred embodiments of the present invention are described in detail above. However, the present invention is not limited to the specific details in the above embodiments. Within the technical concept of the present invention, a variety of simple modifications can be made to the technical solution of the present invention, and these simple modifications all belong to the protection scope of the present invention.

[0125] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, the present invention will not further describe various possible combinations.

[0126] In addition, various embodiments of the present invention may be arbitrarily combined, and as long as they do not violate the concept of the present invention, they should also be regarded as the contents disclosed by the present invention.

Claims

1. A natural gas hydrogen production equipment, characterized in that: The natural gas hydrogen production equipment includes a central transmission unit and a catalytic reaction unit arranged around the central transmission unit; The catalytic reaction unit is provided with a reforming catalytic zone, a cooling zone and a shift catalytic zone in sequence from bottom to top; The bottom of the natural gas hydrogen production equipment is provided with a fuel gas inlet; A raw gas inlet is provided at the top of the central transmission unit; The equipment for producing hydrogen from natural gas is provided with a baffle; The center line of the baffle coincides with the center line of the natural gas hydrogen production equipment; The baffle is set up with an area of ​​60-70% of the plane area perpendicular to the center line of the natural gas hydrogen production device, and the cooling area and the conversion catalytic area are connected to the central transmission unit through heat exchange holes; The hydrogen production process is as follows: The raw gas is preheated and passed through a combustion zone of a combustion-supporting gas, and then successively undergoes reforming reaction, cooling and conversion catalysis to obtain hydrogen-rich gas; the raw gas includes natural gas and water vapor; the volume ratio of natural gas to water vapor in the raw gas is 1:(1-2.5).

2. The natural gas hydrogen production equipment according to claim 1, characterized in that: The cooling zone and the conversion catalytic zone are both tube-in-tube heat exchange structures.

3. The natural gas hydrogen production equipment according to claim 1, characterized in that: At least two baffles are provided.

4. The natural gas hydrogen production equipment according to claim 3, characterized in that: When two baffles are provided, the first baffle is provided in the conversion catalytic zone, and the second baffle is provided in the cooling zone.

5. The natural gas hydrogen production equipment according to claim 1, characterized in that: The combustion-supporting gas inlet is provided with an igniter and a combustion nozzle.

6. The natural gas hydrogen production equipment according to claim 1, characterized in that: The outer wall of the natural gas hydrogen production equipment is provided with a heat insulation layer.

7. A method for producing hydrogen from natural gas, characterized in that: The method is carried out using the natural gas hydrogen production equipment according to any one of claims 1 to 6, comprising: preheating the raw gas and passing it through a combustion zone of an auxiliary gas, and then successively undergoing reforming reaction, cooling and conversion catalysis to obtain hydrogen-rich gas; The raw gas includes natural gas and water vapor; the volume ratio of natural gas to water vapor in the raw gas is 1:(1-2.5).

8. The method according to claim 7, characterized in that The catalyst in the reforming reaction includes a nickel-based catalyst and / or a nickel-platinum-based catalyst.

9. The method according to claim 7, characterized in that The temperature of the reforming reaction is 800-1000°C.

10. The method according to claim 7, characterized in that The cooling is to cool the reformed material.

11. The method according to claim 10, characterized in that The cooling end point temperature is 450-500°C.

12. The method according to claim 7, characterized in that The catalyst in the shift catalyst is a carbon monoxide shift catalyst.

13. The method according to claim 12, characterized in that The carbon monoxide conversion catalyst includes a medium-conversion series low-conversion catalyst.

14. The method according to claim 7, characterized in that The temperature of the shift catalysis is 200-500°C.

15. The method according to any one of claims 7 to 14, characterized in that: The method comprises: preheating the raw gas and passing it through a combustion zone of an auxiliary gas, and then successively performing a reforming reaction, cooling and a conversion catalysis to obtain a hydrogen-rich gas; The volume ratio of natural gas to water vapor in the raw gas is 1:(1-2.5); The cooling end point temperature is 450-500°C; The temperature of the shift catalysis is 200-500°C.

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