Methanol-to-hydrogen reactor group with temperature difference reduction and gas-liquid separation functions

Abstract

The utility model discloses a methanol hydrogen production reactor group with temperature difference reduction and gas-liquid separation functions, which comprises a shell, and a gasification heat exchange cavity, a reforming cavity, a gas-liquid separation cavity and a temperature control device which are arranged in the shell, and a reforming catalyst is arranged in the reforming cavity; the gasification heat exchange cavity is used for inputting a methanol aqueous solution and gasifying the methanol aqueous solution under the action of the temperature control device so as to output methanol steam; the reforming cavity is used for receiving the methanol steam output by the gasification heat exchange cavity, and reforming the methanol steam in combination with a reforming catalyst under the action of the temperature control device, so as to output hydrogen-rich gas after reforming and methanol steam which is not completely reacted; the gas-liquid separation cavity is used for carrying out gas-liquid separation on the fluid output by the reforming cavity so as to output dry hydrogen-rich gas and a methanol aqueous solution; the temperature control device is used for respectively controlling the temperatures of the gasification heat exchange cavity and the reforming cavity. The device can reduce temperature difference and separate gas and liquid, so that methanol steam is fully reformed to produce hydrogen.

Description

Technical Field

[0001] This utility model relates to the field of methanol-to-hydrogen technology, and in particular to a methanol-to-hydrogen reactor group with functions of reducing temperature difference and gas-liquid separation. Background Technology

[0002] To help build a clean, low-carbon, safe and efficient energy system, promoting the development of hydrogen energy is one of the key strategies for achieving a green and low-carbon transformation.

[0003] Fuel cell power generation is clean and efficient, representing a new approach to developing green energy. Hydrogen, with its high calorific value and low pollution, is the primary fuel for fuel cells; however, fuel cell technology is limited by hydrogen storage and transportation technology. In recent years, domestic and international scholars have proposed using liquid low-methanol as a feedstock to provide hydrogen for fuel cells through on-site reforming. Among liquid low-methanol, methanol has advantages such as low price, high C-H ratio, and convenient storage and transportation, making it the most widely used feedstock for reforming hydrogen production. Methanol steam reforming is a major hydrogen production method due to its advantages of producing hydrogen-rich gas with high hydrogen content and low reaction temperature.

[0004] Currently, methanol reforming reactors for hydrogen production mainly include plate reactors, tubular reactors, membrane reactors, and microreactors. During operation, structural issues lead to significant temperature differences in the reactors, affecting the quality of the obtained hydrogen-rich gas and reducing the power generation performance of fuel cells. Furthermore, the hydrogen-rich gas obtained from reforming contains not only hydrogen but also carbon monoxide, carbon dioxide, and unreacted methanol water vapor. Using hydrogen-rich gas containing methanol water vapor as fuel can easily cause catalyst poisoning and flooding in fuel cells, shortening their lifespan. Existing reactors cannot directly separate methanol water vapor. Utility Model Content

[0005] To address the aforementioned problems, this utility model aims to provide a methanol-to-hydrogen reactor group with a simple structure that features reduced temperature difference and gas-liquid separation.

[0006] The technical solution of this utility model is as follows:

[0007] A methanol-to-hydrogen reactor assembly with functions of reducing temperature difference and gas-liquid separation includes a shell and a gasification heat exchange chamber, a reforming chamber, a gas-liquid separation chamber and a temperature control device disposed in the shell, wherein a reforming catalyst is disposed in the reforming chamber.

[0008] The vaporization heat exchange chamber is used to input methanol aqueous solution, and under the action of the temperature control device, the methanol aqueous solution is vaporized, thereby outputting methanol water vapor;

[0009] The reforming cavity is used for receiving the methanol water vapor output by the gasification heat exchange cavity, and under the action of the temperature control device, the methanol water vapor is reformed in combination with the reforming catalyst, so as to output the hydrogen-rich gas after reforming and the uncompletely reacted methanol water vapor;

[0010] The gas-liquid separation cavity is used for gas-liquid separation of the hydrogen-rich gas after reforming and the uncompletely reacted methanol water vapor, so as to output the dry hydrogen-rich gas and the methanol water solution.

[0011] The temperature control device is used for respectively controlling the temperature of the gasification heat exchange cavity to reach the methanol water solution gasification temperature and controlling the temperature of the reforming cavity to reach the methanol water vapor reforming temperature, so as to reduce the temperature difference between the gasification heat exchange cavity and the reforming cavity.

[0012] As a preferred, the gasification heat exchange cavity comprises a parallel cavity section and a vertical cavity section, the parallel cavity section is arranged at the upper part of the reforming cavity, the vertical cavity section is arranged at the right side of the reforming cavity and is communicated with the right end of the parallel cavity section, and the gas-liquid separation cavity is arranged at the lower part of the vertical cavity section and is separated from the vertical cavity section by a partition plate.

[0013] The methanol water solution inlet is arranged at the right side of the parallel cavity section, the methanol water vapor outlet is arranged at the lower part of the left side of the parallel cavity section and is communicated with the reforming cavity, the hydrogen-rich gas outlet after reforming is arranged at the lower part of the right side of the reforming cavity and is communicated with the gas-liquid separation cavity, and the methanol water solution outlet is arranged at the bottom of the gas-liquid separation cavity.

[0014] The shell is provided with a drying pipe, the drying pipe comprises a parallel section drying pipe and a vertical section drying pipe, one end of the vertical section drying pipe is arranged in the gas-liquid separation cavity, the other end of the vertical section drying pipe penetrates through the partition plate and is communicated with the parallel section drying pipe arranged in the parallel cavity section, and the outlet end of the parallel section drying pipe is communicated with the dry hydrogen-rich gas outlet arranged at the upper part of the left side of the parallel cavity section.

[0015] As a preferred, the gasification heat exchange cavity is provided with a gasification pipe, and the two ends of the gasification pipe are respectively communicated with the methanol water solution inlet and the methanol water vapor outlet.

[0016] As a preferred, the parallel section drying pipe is spirally arranged in the parallel cavity section, and the gasification pipe is located at the spiral center of the parallel section drying pipe.

[0017] As a preferred, the reforming cavity is provided with a plurality of flow guide plates, and adjacent two flow guide plates are respectively connected with the front side wall and the rear side wall of the reforming cavity, so as to form a serpentine flow channel in the reforming cavity.

[0018] As preferred, the temperature control device for controlling the temperature in the reforming cavity comprises a temperature controller, a resistance wire and a temperature monitoring device I, the temperature controller is arranged outside the shell, the resistance wire is arranged in the flow plate, and the temperature monitoring device I is used for monitoring the temperature in the reforming cavity.

[0019] As preferred, the temperature monitoring device I is arranged on the lower inner wall of the reforming cavity near the hydrogen-rich gas outlet after reforming, and the temperature monitoring device I is a thermocouple.

[0020] As preferred, the temperature control device for controlling the temperature in the gasification heat exchange cavity comprises heat exchange fins and a temperature monitoring device II, the heat exchange fins are used for heat exchange of the temperature in the reforming cavity to the gasification heat exchange cavity, and the temperature monitoring device II is a thermocouple.

[0021] As preferred, the heat exchange fins are arranged on the right top of the reforming cavity, and the more the number of the heat exchange fins and the longer the length of the heat exchange fins are from left to right.

[0022] As preferred, the methanol water solution inlet, the methanol water vapor outlet and the hydrogen-rich gas outlet after reforming are all conical holes, and the hole diameter of the fluid output end is smaller.

[0023] The beneficial effects of the methanol hydrogen production reactor are as follows:

[0024] The methanol hydrogen production reactor can reduce the temperature difference before and after the reforming cavity, separate the methanol water vapor and the dry hydrogen-rich gas, maximize the quality of hydrogen, and prolong the service life of the reactor. Further, the dry pipe is connected with the gasification heat exchange cavity, the waste heat of the hydrogen-rich gas is used to provide heat for the methanol water solution gasification, and the system energy utilization rate is improved. Further, the thermocouple, the temperature controller and the resistance wire are arranged, the temperature of the gasification reaction cavity and the reforming cavity can be monitored in real time, the temperature difference is controlled, the structure is simple, and the methanol is prevented from being insufficiently reacted due to the large temperature difference. BRIEF DESCRIPTION OF DRAWINGS

[0025] In order to more clearly illustrate the technical scheme in the embodiments of the present application or the prior art, the drawings needed in the following embodiment 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.

[0026] Figure 1 The structure diagram of the methanol hydrogen production reactor group with the temperature difference reduction and gas-liquid separation functions of the present application is shown in the figure.

[0027] Figure 2A schematic view of the structure of the reforming cavity in one embodiment;

[0028] Figure 3 A schematic view of the structure of the methanol aqueous solution inlet in one embodiment;

[0029] Figure 4 A schematic view of the structure of the methanol water vapor outlet in one embodiment;

[0030] Figure 5 A schematic view of the structure of the hydrogen-rich gas outlet after reforming in one embodiment.

[0031] The figure label: 1 - shell, 2 - methanol aqueous solution inlet, 3 - gasification pipe, 4 - gasification heat exchange cavity, 5 - vertical cavity section, 6 - serpentine flow channel, 7 - drying pipe, 8 - hydrogen-rich gas outlet after reforming, 9 - gas-liquid separation cavity, 10 - methanol aqueous solution outlet, 11 - temperature monitoring device one, 12 - reforming cavity, 13 - flow around plate, 14 - resistance wire, 15 - heat exchange fin, 16 - methanol water vapor outlet, 17 - temperature monitoring device two, 18 - dry hydrogen-rich gas outlet. DETAILED DESCRIPTION

[0032] The utility model is further explained below in combination with the drawings and embodiments.

[0033] It should be noted that the embodiments in the present application and the technical features in the embodiments can be combined with each other without conflict.

[0034] It should be noted that, unless otherwise specified, all technical and scientific terms used in the present application have the same meaning as generally understood by those skilled in the art to which the present application belongs.

[0035] In the present utility model, under the condition of not making opposite explanation, the term "first", "second" and the like are used to distinguish similar objects, and are not used to describe a specific order or sequence. It should be understood that the terms used in this way; the terms used in the term "up", "down", "left", "right" and the like are generally directed to the direction shown in the drawings, or are directed to the vertical, vertical or gravity direction of the component itself; similarly, for the convenience of understanding and description, "inner", "outer" and the like refer to the inner and outer relative to the contour of the component itself. But the above orientation words are not used to limit the present utility model.

[0036] As Figures 1-5 shown, the utility model provides a kind of methanol hydrogen production reactor group with reduce temperature difference and gas-liquid separation function, including shell 1 and being arranged in the gasification heat exchange cavity 4 of shell 1, reforming cavity 12, gas-liquid separation cavity 9 and temperature control device, the reforming catalyst is equipped in the reforming cavity 12;

[0037] The gasification heat exchange cavity 4 is used for inputting the methanol aqueous solution and gasifying the methanol aqueous solution under the action of the temperature control device, so as to output methanol water vapor;

[0038] The reforming cavity 12 is used for receiving the methanol water vapor output by the gasification heat exchange cavity 4 and reforming the methanol water vapor in combination with the reforming catalyst under the action of the temperature control device, so as to output the hydrogen-rich gas after reforming and the unreacted methanol water vapor;

[0039] The gas-liquid separation cavity 9 is used for gas-liquid separation of the hydrogen-rich gas after reforming and the unreacted methanol water vapor, so as to output the dry hydrogen-rich gas and the methanol aqueous solution;

[0040] The temperature control device is used for controlling the temperature of the gasification heat exchange cavity 4 to reach the methanol aqueous solution gasification temperature and controlling the temperature of the reforming cavity 12 to reach the methanol water vapor reforming temperature, so as to reduce the temperature difference between the gasification heat exchange cavity 4 and the reforming cavity 12.

[0041] In the above embodiment, by directly inputting the methanol water vapor output by the gasification heat exchange cavity 4 into the reforming cavity 12, the temperature difference before and after the reforming cavity can be reduced, and by arranging the gas-liquid separation cavity 9, the hydrogen-rich gas after reforming and the unreacted methanol water vapor can be subjected to gas-liquid separation, so as to obtain the dry hydrogen-rich gas and the methanol aqueous solution, thereby avoiding directly outputting the hydrogen-rich gas containing the unreacted methanol water vapor, so as to avoid affecting the hydrogen-rich gas as fuel to adversely affect the fuel cell.

[0042] In a specific embodiment, the gasification heat exchange cavity 4 comprises a parallel cavity section and a vertical cavity section 5, the parallel cavity section is arranged at the upper portion of the reforming cavity 12, the vertical cavity section 5 is arranged at the right side of the reforming cavity 12 and communicates with the right end of the parallel cavity section, and the gas-liquid separation cavity 9 is arranged at the lower portion of the vertical cavity section 5 and is separated from the vertical cavity section 5 by a partition plate;

[0043] The methanol aqueous solution inlet 2 is arranged at the right side of the parallel cavity section, the methanol water vapor outlet 16 is arranged at the lower portion of the left side of the parallel cavity section and communicates with the reforming cavity 12, the hydrogen-rich gas outlet 8 after reforming is arranged at the lower portion of the right side of the reforming cavity 12 and communicates with the gas-liquid separation cavity 9, and the methanol aqueous solution outlet 10 is arranged at the bottom of the gas-liquid separation cavity 9;

[0044] The shell 1 is provided with a drying tube 7, which comprises a parallel section drying tube and a vertical section drying tube. One end of the vertical section drying tube is arranged in the gas-liquid separation chamber 9, and the other end of the vertical section drying tube penetrates the partition plate and is connected in communication with the parallel section drying tube arranged in the parallel chamber section. The outlet end of the parallel section drying tube is connected in communication with the drying hydrogen-rich gas outlet 18 arranged on the upper left side of the parallel chamber section.

[0045] In the above embodiment, by arranging the drying tube 7, the reformed hydrogen-rich gas can enter the drying tube 7 under the influence of gas density, and then the hydrogen-rich gas in the drying tube 7 is dried by the temperature in the gasification heat exchange chamber 4, and finally the dried hydrogen-rich gas is output from the drying hydrogen-rich gas outlet 18.

[0046] In a specific embodiment, the gasification heat exchange chamber 4 is provided with a gasification tube 3, and the two ends of the gasification tube 3 are connected in communication with the methanol aqueous solution inlet 2 and the methanol water vapor outlet 16, respectively. Optionally, the parallel section drying tube is arranged in a spiral in the parallel chamber section, and the gasification tube 3 is located at the spiral center of the parallel section drying tube.

[0047] In a specific embodiment, the reforming chamber 12 is provided with a plurality of flow guide plates 13, and adjacent two flow guide plates 13 are connected with the front side wall and the rear side wall of the reforming chamber 12, respectively, so as to form a serpentine flow channel 6 in the reforming chamber 12.

[0048] In the above embodiment, by arranging the flow guide plate 13, the serpentine flow channel is formed in the reforming chamber 12, which can increase the residence time of the fluid in the reforming chamber 12 by using the serpentine flow channel, so as to make the methanol water vapor fully perform the reforming reaction.

[0049] In a specific embodiment, the temperature control device for controlling the temperature in the reforming chamber 12 comprises a temperature controller (not shown in the figure) and a resistance wire 14 and a temperature monitoring device one 11 connected with the temperature controller, respectively. The temperature controller is arranged outside the shell 1, the resistance wire 14 is built in the flow guide plate 13, and the temperature monitoring device one 11 is used for monitoring the temperature in the reforming chamber 12. Optionally, the temperature monitoring device one 11 is arranged on the lower inner wall of the reforming chamber 12 close to the reformed hydrogen-rich gas outlet 8, and the temperature monitoring device one is a thermocouple.

[0050] It should be noted that the above embodiment uses resistance wire for heating, in addition to the use of resistance wire, other heating devices capable of achieving the purpose of heating in the prior art can also be applied to the utility model. In addition, the thermocouple is a commonly used temperature monitoring device, in addition to the device, other temperature monitoring devices such as temperature sensors in the prior art can also be applied to the utility model. Furthermore, the temperature control device is mainly used for monitoring and controlling temperature, which is the prior art, in addition to the temperature control device used in the above embodiment, other devices capable of achieving the purpose in the prior art can also be applied to the utility model.

[0051] In one specific embodiment, the temperature control device for controlling the temperature in the gasification heat exchange cavity 4 includes heat exchange fins 15 for heat exchange of the temperature in the reforming cavity 12 to the gasification heat exchange cavity 4 and a temperature monitoring device two 17 which is a thermocouple. Optionally, the temperature monitoring device two 17 is arranged on the left side wall of the gasification heat exchange cavity 4.

[0052] In the above embodiment, the utility model discloses a heat exchange fin 15, which is used for heat exchange of the temperature in the reforming cavity 12 to the gasification heat exchange cavity 4, so that the heat of the reforming cavity 12 can be used for gasification of the methanol aqueous solution in the gasification heat exchange cavity 4, and energy can be saved. In addition, in the above embodiment, the temperature monitoring device one 11 is arranged at the tail of the reforming cavity, and the temperature monitoring device two is arranged at the tail of the gasification heat exchange cavity 4, so that the temperature difference between the methanol aqueous solution gasification and the methanol steam reforming process can be monitored, and the temperature difference between the gasification heat exchange cavity 4 and the reforming cavity 12 and the temperature difference between the front and rear positions of the reforming cavity 12 can be more easily controlled.

[0053] It should be noted that the heat exchange fin is the prior art, and the specific structure will not be described here. In addition, in addition to the temperature control device used in the above embodiment, two temperature control devices can also be arranged respectively, one of which controls the temperature of the gasification heat exchange cavity 4 alone, and the other controls the temperature of the reforming cavity 12 alone. The temperature control device is the prior art, and the specific structure that can be used will not be described here.

[0054] In one specific embodiment, the heat exchange fin 15 is arranged at the right top of the reforming cavity 12, and the more the number of heat exchange fins 15 from left to right, the longer the length of the heat exchange fin 15. Optionally, the lengths of the heat exchange fins 15 in the fluid channels formed by the adjacent two flow plates 13 are the same.

[0055] In the above embodiment, the heat exchange fins 15 are arranged at the right top of the reforming cavity 12, so that the heat not used at the rear end of the reforming cavity 12 (the reforming reaction mainly occurs at the front end of the reforming cavity, the closer to the hydrogen-rich gas outlet after reforming, the less unreacted gas, and the more remaining heat) can be transmitted to the gasification heat exchange cavity 4 to gasify the methanol aqueous solution, reduce the temperature difference between the front and rear of the reforming cavity 12, and improve the quality of the hydrogen-rich gas.

[0056] In a specific embodiment, the methanol aqueous solution inlet 2, the methanol water vapor outlet 16, and the hydrogen-rich gas outlet after reforming 8 all adopt a tapered hole, and the hole diameter of the fluid output end is smaller.

[0057] In the above embodiment, by adopting the tapered hole of the methanol aqueous solution inlet 2 and the methanol water vapor outlet 16, the flow speed of the fluid can be improved; by adopting the tapered hole of the hydrogen-rich gas outlet after reforming 8, the flow speed of the hydrogen-rich gas outlet can be improved, and the gas-liquid separation effect in the gas-liquid separation cavity can be improved.

[0058] In a specific embodiment of using the methanol hydrogen production reactor group with reduced temperature difference and gas-liquid separation function to produce hydrogen from methanol, the working principle of the present application is as follows:

[0059] First, the resistance wire 14 heats the flow-around plate 13, and the heat is transmitted to the reforming cavity 12 through the flow-around plate 13, and at the same time, the heat enters the gasification heat exchange cavity 4 through the heat exchange fins 15; when the temperature in the reforming cavity 12 reaches the required temperature for the reforming reaction (generally about 300℃), the temperature in the gasification heat exchange cavity 4 also reaches the required temperature for the gasification of the methanol aqueous solution (generally about 60-100℃).

[0060] Secondly, the external water pump injects the methanol aqueous solution into the gasification pipe 3 through the methanol aqueous solution inlet 2, and the methanol aqueous solution is gasified into methanol water vapor in the gasification pipe 3, which enters the reforming cavity 12 through the methanol water vapor outlet 16; the reforming cavity 12 is provided with a reforming catalyst to make the methanol water vapor undergo reforming.

[0061] Then, the hydrogen-rich gas after reforming enters the gas-liquid separation cavity 9 through the hydrogen-rich gas outlet after reforming 8, the unreacted methanol water vapor is cooled and flows out of the shell 1 from the methanol aqueous solution outlet 10, and the hydrogen-rich gas after reforming enters the drying pipe 7 through the bottom inlet of the drying pipe 7; the drying pipe 7 is mostly arranged in the gasification heat exchange cavity 4, which on the one hand provides heat for the gasification of the methanol aqueous solution, and on the other hand uses the heat of the gasification heat exchange cavity for drying, thereby improving the energy utilization rate.

[0062] Finally, the dried hydrogen-rich gas exits the shell 1 from the dried hydrogen-rich gas outlet 18.

[0063] The above merely describes preferred embodiments of the present application and is not intended to limit the present application in any form. Although the present application has been disclosed with preferred embodiments, it is not intended to limit the present application. Any skilled person in the art can make minor changes or modifications to the disclosed technical content without departing from the technical solution of the present application, and any simple modification, equivalent change and modification of the above embodiments based on the technical essence of the present application still belong to the scope of the technical solution of the present application.

Claims

1. A methanol hydrogen production reactor group with reduced temperature difference and gas-liquid separation function, comprising a shell and a gasification heat exchange cavity, a reforming cavity, a gas-liquid separation cavity and a temperature control device arranged in the shell, and a reforming catalyst arranged in the reforming cavity. The gasification heat exchange cavity is used for inputting methanol aqueous solution and vaporizing the methanol aqueous solution under the action of the temperature control device, so as to output methanol water vapor. The reforming cavity is used for receiving the methanol water vapor output by the gasification heat exchange cavity and reforming the methanol water vapor in combination with the reforming catalyst under the action of the temperature control device, so as to output a hydrogen-rich gas after reforming and unreacted methanol water vapor. The gas-liquid separation cavity is used for gas-liquid separation of the hydrogen-rich gas after reforming and the unreacted methanol water vapor, so as to output dry hydrogen-rich gas and methanol aqueous solution. The temperature control device is used for controlling the temperature of the gasification heat exchange cavity to reach the methanol aqueous solution vaporization temperature and controlling the temperature of the reforming cavity to reach the methanol water vapor reforming temperature, so as to reduce the temperature difference between the gasification heat exchange cavity and the reforming cavity.

2. The methanol-to-hydrogen reactor group with reduced temperature difference and gas-liquid separation function according to claim 1, characterized in that, The gasification heat exchange cavity comprises a parallel cavity section and a vertical cavity section, the parallel cavity section is arranged at the upper part of the reforming cavity, the vertical cavity section is arranged at the right side of the reforming cavity and is in communication with the right end of the parallel cavity section, and the gas-liquid separation cavity is arranged at the lower part of the vertical cavity section and is separated from the vertical cavity section by a partition plate. The methanol aqueous solution inlet is arranged at the right side of the parallel cavity section, the methanol water vapor outlet is arranged at the lower part of the left side of the parallel cavity section and is in communication with the reforming cavity, the hydrogen-rich gas outlet after reforming is arranged at the lower part of the right side of the reforming cavity and is in communication with the gas-liquid separation cavity, and the methanol aqueous solution outlet is arranged at the bottom of the gas-liquid separation cavity. The shell is provided with a drying tube, the drying tube comprises a parallel section drying tube and a vertical section drying tube, one end of the vertical section drying tube is arranged in the gas-liquid separation cavity, the other end of the vertical section drying tube penetrates through the partition plate and is in communication with the parallel section drying tube arranged in the parallel cavity section, and the outlet end of the parallel section drying tube is in communication with the dry hydrogen-rich gas outlet arranged at the upper part of the left side of the parallel cavity section.

3. The methanol-to-hydrogen reactor group with reduced temperature difference and gas-liquid separation function according to claim 2, characterized in that, The gasification heat exchange cavity is provided with a gasification tube, and the two ends of the gasification tube are in communication with the methanol aqueous solution inlet and the methanol water vapor outlet, respectively.

4. The methanol-to-hydrogen reactor group with reduced temperature difference and gas-liquid separation function according to claim 3, characterized in that, The parallel section drying tube is spirally arranged in the parallel cavity section, and the gasification tube is located at the spiral center of the parallel section drying tube.

5. The methanol-to-hydrogen reactor group with reduced temperature difference and gas-liquid separation function according to claim 2, characterized in that, The reforming cavity is provided with a plurality of flow guide plates, and adjacent two flow guide plates are connected with the front side wall and the rear side wall of the reforming cavity, respectively, so as to form a serpentine flow channel in the reforming cavity.

6. The methanol-to-hydrogen reactor group with reduced temperature difference and gas-liquid separation function according to claim 5, characterized in that, The temperature control device for controlling the temperature in the reforming cavity comprises a temperature controller, a resistance wire and a temperature monitoring device one connected with the temperature controller, the temperature controller is arranged outside the shell, the resistance wire is arranged in the flow guide plate, and the temperature monitoring device one is used for monitoring the temperature in the reforming cavity.

7. The methanol-to-hydrogen reactor group with reduced temperature difference and gas-liquid separation function according to claim 6, characterized in that, The temperature monitoring device one is arranged on the lower inner wall of the reforming cavity close to the hydrogen-rich gas outlet after reforming, and the temperature monitoring device one is a thermocouple.

8. The methanol-to-hydrogen reactor group with reduced temperature difference and gas-liquid separation function according to claim 6, characterized in that, The temperature control device for controlling the temperature in the gasification heat exchange cavity comprises two heat exchange fins and a temperature monitoring device, the heat exchange fins are used for heat exchange of the temperature in the reforming cavity to the gasification heat exchange cavity, and the temperature monitoring device is a thermocouple.

9. The methanol-to-hydrogen reactor group with reduced temperature difference and gas-liquid separation function according to claim 8, characterized in that, The heat exchange fins are arranged at the right top of the reforming cavity, and the more the number of the heat exchange fins is and the longer the length of the heat exchange fins is from left to right.

10. The methanol-to-hydrogen reactor group with reduced temperature difference and gas-liquid separation function according to any one of claims 2-9, characterized in that, The methanol aqueous solution inlet, the methanol water vapor outlet and the hydrogen-rich gas outlet after reforming all adopt tapered holes, and the hole diameter of the fluid output end is smaller.

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