Methanol atomization cracking hydrogen production device

Abstract

The utility model relates to a device for producing hydrogen by atomizing and cracking methanol, which is provided with an atomizing spray head, so that methanol enters a reactor in a form of fine liquid drops, and is quickly vaporized under the action of high temperature and certain pressure of the reactor to form a stable environmental condition, so that the methanol cracking process is complete, almost no methanol is left, and the efficiency of producing hydrogen by cracking methanol is improved; meanwhile, in the original cracking hydrogen production process, a shift reaction process is removed, namely absolute methanol is used as a raw material, and no water participates in the reaction in a reactor, so that the reaction conditions in the reactor are easier to control, and almost no methanol is left in a reaction product; as the shift reaction process is a heat absorption process, energy consumption is reduced by removing the process; the mixture of H2 and CO obtained by the reaction can be directly used as an energy carrier, and the requirements can be met only by separating and purifying CO and H2 in some occasions requiring the purity of H2.

Description

Technical Field

[0001] The utility model relates to the field of industrial hydrogen production, and particularly relates to a methanol atomization cracking hydrogen production device. Background Art

[0002] Compared with traditional fossil energy, the product of hydrogen energy in the reaction process is water, which has the characteristics of cleanness and high efficiency, and is one of the most potential energy carriers in the future. In the hydrogen production process, the methanol cracking hydrogen production process uses methanol as the raw material, and the raw material source is wide and the price is low; the molecular formula of methanol is CH3OH, with a high hydrogen content and a high utilization rate of hydrogen elements; the size of the hydrogen production device is small, and it can be made into a mobile hydrogen production device. Methanol cracking hydrogen production shows broad application prospects.

[0003] In the traditional methanol cracking hydrogen production process, hydrogen is produced through the methanol cracking process and the water-gas shift reaction process. The reaction processes are as follows:

[0004] Methanol cracking process: CH3OH → CO + 2H2

[0005] Water-gas shift reaction process: CO + H2O → CO2 + H2

[0006] Both the methanol cracking process and the water-gas shift reaction process are endothermic processes and need to be carried out under certain temperature, certain pressure and the action of a catalyst. Usually, in order to promote the methanol cracking process, a higher temperature is adopted to heat and vaporize the liquid methanol. In the reaction, methanol exists in both liquid and gaseous forms. At the same time, the water-gas shift reaction process also has an impact on the methanol cracking process, making the environment of the methanol cracking process more complex and easily leading to the residue of unreacted methanol. Usually, the residual methanol exists in gaseous form, and after heat dissipation and condensation with carbon dioxide and hydrogen generated after the reaction, the residual methanol is condensed into a liquid and continues to participate in the subsequent methanol cracking process as a raw material. The existence of residual methanol reduces the efficiency of the cracking hydrogen production process.

[0007] In the water-gas shift reaction process, the raw material CO is obtained from the methanol cracking process. CO itself can be used as fuel, and the CO and H2 mixture obtained from the methanol cracking process can also be used as fuel. Although the water-gas shift reaction process increases the hydrogen production rate, it consumes CO and a large amount of heat, reducing the economy of the process. Although in some energy supply links, there are requirements for the purity of H2, making the CO and H2 mixture obtained from the methanol cracking process unable to meet the requirements. At this time, only by separating and purifying CO and H2 in the mixer can the requirements be met. Therefore, it is more economical and efficient to abandon the water-gas shift reaction process. Summary of the Utility Model

[0008] It solves the problem that methanol residue in the reaction products reduces the reaction efficiency due to incomplete vaporization of methanol and complex reaction components during the methanol cracking to produce hydrogen; it solves the problem that methanol residue in the reaction products is caused by the existence of the shift reaction process in the traditional methanol cracking to produce hydrogen process, which makes the reaction conditions difficult to control; it solves the problem that more energy is consumed due to the existence of the shift reaction process in the traditional methanol cracking to produce hydrogen process.

[0009] To achieve the above object, the utility model is realized through the following technical solutions:

[0010] A methanol atomization cracking hydrogen production device is provided with a methanol inlet, the methanol inlet is connected with an atomizing nozzle, and a reactor is also provided. The reactor is provided with a reaction inlet and a reaction outlet. The atomizing nozzle extends into the inner cavity of the reactor through the reaction inlet. A heat conduction tube is arranged in the inner cavity of the reactor, and a heat conduction medium is circulated through the heat conduction tube; a catalyst is also attached to the inner cavity of the reactor, and a first pressure gauge is connected to the inner cavity of the reactor.

[0011] Preferably, a radiator is connected to the reaction outlet of the reactor.

[0012] Preferably, a heat exchanger is also arranged between the methanol inlet and the atomizing nozzle. The heat exchanger is provided with a cold medium inlet, a cold medium outlet, a hot medium inlet, and a hot medium outlet. A heat exchange tube is arranged in the inner cavity of the heat exchanger. The inlet and outlet of the heat exchange tube are respectively connected to the cold medium inlet and the cold medium outlet. The hot medium inlet and the hot medium outlet are both connected to the inner cavity of the heat exchanger; the methanol inlet is connected to the cold medium inlet of the heat exchanger, and the cold medium outlet of the heat exchanger is connected to the atomizing nozzle; the reaction outlet of the reactor is connected to the hot medium inlet of the heat exchanger, and the hot medium outlet of the heat exchanger is connected to a radiator.

[0013] Preferably, the reactor is provided with a top cover and a bottom cover. The space surrounded by the top cover, the bottom cover and the inner wall of the reactor forms the inner cavity of the reactor. A heat conduction tube is arranged between the bottom cover and the bottom cover, and the heat conduction tube penetrates through the lower end of the top cover and the upper end of the bottom cover. Through holes corresponding to the heat conduction tube are arranged on the top cover and the bottom cover; a plurality of heat conduction tubes are arranged; an upper head is connected to the upper end of the top cover, a lower head is connected to the lower end of the bottom cover, the lower head is connected to a heat conduction medium inlet, the upper head is connected to a heat conduction medium outlet, a circulation pump is arranged between the heat conduction medium inlet and the heat conduction medium outlet, and a heating device is also connected between the circulation pump and the heat conduction medium outlet. The heat conduction medium is heat conduction oil; a plurality of fixing plates are also arranged between the top cover and the bottom cover. The fixing plates are used to fix the heat conduction tube, and the fixing plates are fixedly connected to the inner wall of the reactor. Catalysts are attached to the surfaces of the fixing plates, the lower end of the top cover, and the upper end of the bottom cover.

[0014] Preferably, a first switching valve is provided between the methanol inlet and the atomizing nozzle, a booster pump is provided between the methanol inlet and the switching valve, and a second pressure gauge is provided between the booster pump and the first switching valve.

[0015] Preferably, a second switching valve is provided between the methanol inlet and the cold medium inlet of the heat exchanger, a booster pump is provided between the methanol inlet and the second switching valve, and a second pressure gauge is provided between the booster pump and the second switching valve; a first switching valve is provided between the cold medium outlet and the atomizing nozzle, and a third pressure gauge is provided between the cold medium outlet and the first switching valve.

[0016] Preferably, the heat exchange tubes are arranged in a spiral shape.

[0017] Preferably, a liquid level gauge is provided on the reactor, the liquid level gauge is connected to the inner cavity of the reactor, and a first blowdown valve is also provided on the reactor, and the first blowdown valve is connected to the lower part of the inner cavity of the reactor.

[0018] Preferably, a second blowdown valve is connected to the lower end of the lower head.

[0019] A methanol atomization cracking hydrogen production skid is provided with a skid chassis, and the methanol atomization cracking hydrogen production device as described in any one of the above is provided on the skid chassis.

[0020] The present utility model provides a methanol atomization cracking hydrogen production device. It has the following beneficial effects:

[0021] An atomizing nozzle is provided, so that methanol enters the reactor in the form of fine droplets. Under the action of high temperature and certain pressure in the reactor, it quickly vaporizes, forming stable environmental conditions, making the methanol cracking process complete, with almost no methanol residue, and improving the efficiency of methanol cracking hydrogen production.

[0022] In the original cracking hydrogen production process, the shift reaction process is removed, that is, anhydrous methanol is used as the raw material, and no water participates in the reaction in the reactor, making the reaction conditions in the reactor easier to control, and there is almost no methanol residue in the reaction products; since the shift reaction process is an endothermic process, removing this process reduces energy consumption; the obtained H2 and CO mixture can be directly used as an energy carrier. In some occasions where requirements for H2 purity are put forward, it can meet the requirements only by separating and purifying CO and H2. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Figure 1 It is a schematic diagram of the structure of the present utility model or the connection relationship between components (excluding the heat exchanger);

[0024] Figure 2 It is a schematic diagram of the structure of the present utility model or the connection relationship between components (including the heat exchanger).

[0025] In the figure, 1 is the methanol inlet, 2 is the atomizing nozzle, 3 is the reactor, 30 is the liquid level gauge, 31 is the reaction inlet, 32 is the reaction outlet, 33 is the heat conduction tube, 34 is the catalyst, 35 is the top cover, 36 is the bottom cover, 37 is the upper head, 371 is the heat conduction medium outlet, 38 is the lower head, 381 is the heat conduction medium inlet, 39 is the fixing plate, 4a is the first pressure gauge, 4b is the second pressure gauge, 4c is the third pressure gauge, 5 is the radiator, 6 is the heat exchanger, 61 is the cold medium inlet, 62 is the cold medium outlet, 63 is the hot medium inlet, 64 is the hot medium outlet, 65 is the heat exchange tube, 7a is the circulation pump, 71 is the heating device, 7b is the booster pump, 8a is the first switching valve, 8b is the second switching valve, 9a is the first blowdown valve, and 9b is the second blowdown valve. Detailed implementation manners

[0026] Next, the technical solutions in the embodiments of the present invention will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present invention without creative efforts shall fall within the protection scope of the present invention.

[0027] In the description of the embodiments of the present invention, it should be noted that unless otherwise clearly defined and limited, the terms "connected" and "coupled" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium. For those of ordinary skill in the art, the specific meanings of the above terms in the embodiments of the present invention can be understood according to specific situations.

[0028] In the description of the embodiments of the present invention, it should be noted that the orientation or positional relationship indicated by the terms "upper", "lower", "inner", "outer", etc. is based on the orientation or positional relationship shown in the drawings, and is only for the convenience of describing the embodiments of the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be construed as a limitation to the embodiments of the present invention.

[0029] Please refer to Figure 1, an embodiment of the present utility model provides a technical solution, a methanol atomization cracking hydrogen production device, which is provided with a methanol inlet 1, the methanol inlet 1 is connected to an atomizing nozzle 2, and a reactor 3 is also provided. The reactor 3 is provided with a reaction inlet 31 and a reaction outlet 32. The atomizing nozzle 2 extends into the inner cavity of the reactor 3 through the reaction inlet 31. A heat conduction tube 33 is arranged in the inner cavity of the reactor 3, and a heat conduction medium is circulated through the heat conduction tube 33; a catalyst 34 is also attached to the inner cavity of the reactor 3, and a first pressure gauge 4a is connected to the inner cavity of the reactor 3. It should be particularly noted that: in this embodiment, the chemical reaction formula involved is: CH3OH → CO + 2H2, and this reaction is an endothermic process, which needs to be completed under high temperature, certain pressure and the action of the catalyst 34; the liquid methanol is sprayed into the inner cavity of the reactor 3 in the form of a spray through the atomizing nozzle 2, and quickly vaporizes in a high-temperature environment; anhydrous methanol is used for methanol, and there is no water participation in the reactor 3, which makes the reaction condition control simpler, that is, providing sufficient methanol vaporization heat and the heat required for the reaction, appropriate pressure, sufficient catalyst 34 and appropriate methanol supply, so that the methanol cracking process reacts completely and there is no methanol residue in the reaction products; the atomizing nozzle 2 can refer to the light hydrocarbon atomization device disclosed in the authorized patent publication number: CN218914991U.

[0030] Please refer to Figure 1 , in this embodiment, the reaction outlet 32 of the reactor 3 is connected to a radiator 5. It should be particularly noted that: the function of the radiator 5 is to cool the H2 and CO mixed gas after the reaction, and the cooling principle is the heat exchange between the high-temperature mixer and the external low-temperature environment.

[0031] Please refer to Figure 2 , in this embodiment, a heat exchanger 6 is also arranged between the methanol inlet 1 and the atomizing nozzle 2. The heat exchanger 6 is provided with a cold medium inlet 61, a cold medium outlet 62, a heat medium inlet 63, and a heat medium outlet 64. A heat exchange tube 65 is arranged in the inner cavity of the heat exchanger 6. The inlet and outlet of the heat exchange tube 65 are respectively connected to the cold medium inlet 61 and the cold medium outlet 62, and the heat medium inlet 63 and the heat medium outlet 64 are both connected to the inner cavity of the heat exchanger 6; the methanol inlet 1 is connected to the cold medium inlet 61 of the heat exchanger 6, and the cold medium outlet 62 of the heat exchanger 6 is connected to the atomizing nozzle 2; the reaction outlet 32 of the reactor 3 is connected to the heat medium inlet 63 of the heat exchanger 6, and the heat medium outlet 64 of the heat exchanger 6 is connected to a radiator 5. It should be particularly noted that: the significance of arranging the heat exchanger 6 is to enable the liquid methanol to exchange heat with the high-temperature H2 and CO mixed gas generated during the methanol cracking process, effectively utilize the waste heat after the reaction to heat the liquid methanol, and can reduce the heat required for the vaporization of methanol in the reactor 3.

[0032] Please refer to Figures 1 - 2, in this embodiment, the reactor 3 is provided with a top cover 35 and a bottom cover 36. The space enclosed by the top cover 35, the bottom cover 36 and the inner wall of the reactor 3 forms the inner cavity of the reactor 3. A heat conduction tube 33 is arranged between the bottom cover 36 and the bottom cover 36. The heat conduction tube 33 penetrates through the lower end of the top cover 35 and the upper end of the bottom cover 36. Through holes corresponding to the heat conduction tube 33 are arranged on the top cover 35 and the bottom cover 36; The heat conduction tubes 33 are arranged in multiple numbers; The upper end of the top cover 35 is connected with an upper head 37, the lower end of the bottom cover 36 is connected with a lower head 38, the lower head 38 is connected with a heat conduction medium inlet 381, the upper head 37 is connected with a heat conduction medium outlet 371, a circulation pump 7a is arranged between the heat conduction medium inlet 381 and the heat conduction medium outlet 371, and a heating device 71 is also connected between the circulation pump 7a and the heat conduction medium outlet 371. The heat conduction medium is heat conduction oil; A plurality of fixing plates 39 are also arranged between the top cover 35 and the bottom cover 36. The fixing plates 39 are used to fix the heat conduction tubes 33. The fixing plates 39 are fixedly connected with the inner wall of the reactor 3. Catalysts 34 are attached to the surfaces of the fixing plates 39, the lower end of the top cover 35 and the upper end of the bottom cover 36. It should be particularly noted that: in this embodiment, the structure of the reactor 3 is specifically described. In the reactor 3, the heat required for the vaporization of liquid methanol and the methanol cracking process is provided by circulating heat conduction oil.

[0033] Please refer to Figure 1 , in this embodiment, a first switching valve 8a is arranged between the methanol inlet 1 and the atomizing nozzle 2, a booster pump 7b is arranged between the methanol inlet 1 and the switching valve, and a second pressure gauge 4b is arranged between the booster pump 7b and the first switching valve 8a. It should be particularly noted that: arranging the booster pump 7b can better control the pressure of liquid methanol, thereby affecting the atomization degree of methanol entering the atomizing nozzle 2; Arranging the first switching valve 8a can better regulate the methanol supply according to the pressure value in the inner cavity of the reactor 3. When the pressure value in the inner cavity of the reactor 3 reaches a certain pressure limit, cutting off the first switching valve 8a can better control the methanol supply in the reactor 3, ensure complete reaction in the methanol cracking process, and avoid methanol residue.

[0034] Please refer to Figure 2, in this embodiment, a second switching valve 8b is provided between the methanol inlet 1 and the cold medium inlet 61 of the heat exchanger 6. A booster pump 7b is provided between the methanol inlet 1 and the second switching valve 8b, and a second pressure gauge 4b is provided between the booster pump 7b and the second switching valve 8b. A first switching valve 8a is provided between the cold medium outlet 62 and the atomizing nozzle 2, and a third pressure gauge 4c is provided between the cold medium outlet 62 and the first switching valve 8a. It should be particularly noted that: setting the booster pump 7b can better control the pressure of the liquid methanol, thereby affecting the atomization degree of the methanol entering the atomizing nozzle 2; setting the first switching valve 8a can better regulate the methanol supply according to the pressure value in the inner cavity of the reactor 3. When the pressure value in the inner cavity of the reactor 3 reaches a certain pressure limit, cutting off the first switching valve 8a can better control the methanol supply in the reactor 3, ensuring complete reaction during the methanol cracking process and no methanol residue; setting the second switching valve 8b can control the opening and closing of the second switching valve 8b according to the opening and closing conditions of the first switching valve 8a. For example, when the first switching valve 8a is closed, the second switching valve 8b is also closed, avoiding the ineffective supply of liquid methanol.

[0035] Please refer to Figure 2 , in this embodiment, the heat exchange tube 65 is arranged in a spiral shape.

[0036] Please refer to Figures 1 - 2 , in this embodiment, a liquid level gauge 30 is provided on the reactor 3. The liquid level gauge 30 is connected to the inner cavity of the reactor 3. A first blowdown valve 9a is also provided on the reactor 3, and the first blowdown valve 9a is connected to the lower part of the inner cavity of the reactor 3. It should be particularly noted that: setting the liquid level gauge 30 can be used to check the cumulative amount of impurities contained in the methanol. When it accumulates to a certain extent, it can be discharged through the first blowdown valve 9a.

[0037] Please refer to Figures 1 - 2 , in this embodiment, a second blowdown valve 9b is connected to the lower end of the lower head 38. It should be particularly noted that: the oil stain in the heat transfer oil can be discharged through the second blowdown valve 9b.

[0038] An embodiment of the present invention provides a technical solution, a methanol atomization cracking hydrogen production skid-mounted unit, which is provided with a skid-mounted chassis, and the above-mentioned methanol atomization cracking hydrogen production device is arranged on the skid-mounted chassis. It should be particularly noted that: due to the simple structure of the methanol atomization cracking hydrogen production device in the foregoing embodiment, it is convenient for miniaturization. Setting it on the skid-mounted chassis can achieve skid-mounted transportation and meet the mobile hydrogen production requirements.

[0039] The working principle and usage process of the present invention: When in use, as Figure 2As shown, liquid methanol is introduced through the methanol inlet 1, pressurized by the booster pump 7b, and enters the cold medium inlet 61 of the heat exchanger 6. Then it enters the heat exchange tube 65 and exchanges heat with the hot mixed gas entering from the hot medium inlet 63 in the inner cavity of the heat exchanger 6, causing the methanol to heat up and be discharged from the cold medium outlet 62. Then it is sprayed through the atomizing nozzle 2 in a mist form into the inner cavity of the reactor 3. The reactor 3 is heated by circulating heat-conducting oil, causing the misty methanol to quickly vaporize. Under a certain pressure and catalyzed by the catalyst 34 attached to the top cover 35, bottom cover 36, and fixing plate 39, a cracking reaction occurs: CH3OH → CO + 2H2. Due to the preheating effect of the heat exchanger 6, the atomized methanol can be more easily and quickly completely vaporized in the high-temperature environment of the reactor 3. The appropriate temperature, pressure, and catalytic action enable the cracking reaction to be complete without methanol vapor residue. The high-temperature mixed gas of H2 and CO after the reaction enters the inner cavity of the heat exchanger 6 through the hot medium inlet 63, exchanges heat with the methanol entering from the cold medium inlet 61, the temperature decreases, and then is discharged through the hot medium outlet 64 of the heat exchanger 6 and enters the radiator 5 to exchange heat with the external environment, and the temperature further decreases. At this time, the mixed gas can be collected for standby. Since both the H2 or CO mixed gas can be used as an energy carrier for energy supply, this mixed gas can be used as an energy source. In cases where there are requirements for the purity of H2, H2 and CO can also be separated and purified to obtain higher-purity H2. Since in the above reaction process, anhydrous ethanol is used as the raw material and no water participates in the reactor 3, compared with the traditional hydrogen production process by cracking, the shift reaction process is reduced, the reaction conditions are simpler and easier to control, the methanol cracking process is complete, no methanol residue is produced after the reaction, the hydrogen production efficiency is improved, and the shift reaction process is an endothermic process. Reducing this process also reduces energy consumption.

[0040] The above shows and describes the basic principles, main features, and advantages of the present invention. For those skilled in the art, it is obvious that the present invention is not limited to the details of the above exemplary embodiments, and can be implemented in other specific forms without departing from the spirit or basic features of the present invention. Therefore, from any point of view, the embodiments should be regarded as exemplary and non-restrictive. The scope of the present invention is defined by the appended claims rather than the above description. Therefore, all changes falling within the meaning and scope of the equivalent elements of the claims are intended to be included in the present invention. Any reference signs in the claims should not be regarded as limiting the claimed rights.

[0041] In addition, it should be understood that although this specification is described in terms of embodiments, not every embodiment contains only one independent technical solution. This narrative manner of the specification is only for clarity. Those skilled in the art should regard the specification as a whole, and the technical solutions in each embodiment can also be appropriately combined to form other embodiments that can be understood by those skilled in the art.

Claims

1. A methanol atomization cracking hydrogen production device, characterized in that: A methanol inlet (1) is provided, the methanol inlet (1) is connected to an atomizing nozzle (2), and a reactor (3) is also provided, the reactor (3) is provided with a reaction inlet (31) and a reaction outlet (32), the atomizing nozzle (2) extends into the inner cavity of the reactor (3) through the reaction inlet (31), the inner cavity of the reactor (3) is provided with a heat conducting pipe (33), and a heat conducting medium is circulated in the heat conducting pipe (33); a catalyst (34) is also attached to the inner cavity of the reactor (3), and the inner cavity of the reactor (3) is connected to a first pressure gauge (4a).

2. A methanol atomization cracking hydrogen production device according to claim 1, characterized in that: The reaction outlet (32) of the reactor (3) is connected to a radiator (5).

3. A methanol atomization cracking hydrogen production device according to claim 1, characterized in that: A heat exchanger (6) is further arranged between the methanol inlet (1) and the atomizing nozzle (2). The heat exchanger (6) is provided with a cold medium inlet (61), a cold medium outlet (62), a hot medium inlet (63), and a hot medium outlet (64). The inner cavity of the heat exchanger (6) is provided with a heat exchange tube (65). The inlet and outlet of the heat exchange tube (65) are respectively connected to the cold medium inlet (61) and the cold medium outlet (62), and the hot medium inlet (63) and the hot medium outlet (64) are both connected to the inner cavity of the heat exchanger (6); the methanol inlet (1) is connected to the cold medium inlet (61) of the heat exchanger (6), and the cold medium outlet (62) of the heat exchanger (6) is connected to the atomizing nozzle (2); the reaction outlet (32) of the reactor (3) is connected to the hot medium inlet (63) of the heat exchanger (6), and the hot medium outlet (64) of the heat exchanger (6) is connected to a radiator (5).

4. A methanol atomization cracking hydrogen production device according to any one of claims 1 to 3, characterized in that: The reactor (3) is provided with a top cover (35) and a bottom cover (36); the space surrounded by the top cover (35), the bottom cover (36) and the inner wall of the reactor (3) forms an inner cavity of the reactor (3); a heat conducting pipe (33) is provided between the top cover (35) and the bottom cover (36); the heat conducting pipe (33) passes through the lower end of the top cover (35) and the upper end of the bottom cover (36); the top cover (35) and the bottom cover (36) are provided with through holes corresponding to the heat conducting pipe (33); a plurality of heat conducting pipes (33) are provided; the upper end of the top cover (35) is connected to an upper end cover (37); the lower end of the bottom cover (36) is connected to a lower end cover (38); the lower end cover (38) is connected to a heat conducting medium (33); The reactor (3) has a heat transfer medium inlet (381), the upper cover (37) is connected to a heat transfer medium outlet (371), a circulation pump (7a) is arranged between the heat transfer medium inlet (381) and the heat transfer medium outlet (371), a heating device (71) is also connected between the circulation pump (7a) and the heat transfer medium outlet (371), and the heat transfer medium is heat transfer oil; a plurality of fixing plates (39) are also arranged between the top cover (35) and the bottom cover (36), the fixing plates (39) are used to fix the heat transfer pipes (33), the fixing plates (39) are fixedly connected to the inner wall of the reactor (3), and catalysts (34) are attached to the surfaces of the fixing plates (39), the lower end of the top cover (35), and the upper end of the bottom cover (36).

5. A methanol atomization cracking hydrogen production device according to claim 1 or 2, characterized in that: A first switch valve (8a) is arranged between the methanol inlet (1) and the atomizing nozzle (2), a booster pump (7b) is arranged between the methanol inlet (1) and the switch valve, and a second pressure gauge (4b) is arranged between the booster pump (7b) and the first switch valve (8a).

6. A methanol atomization cracking hydrogen production device according to claim 3, characterized in that: A second switch valve (8b) is arranged between the methanol inlet (1) and the cold medium inlet (61) of the heat exchanger (6), a booster pump (7b) is arranged between the methanol inlet (1) and the second switch valve (8b), and a second pressure gauge (4b) is arranged between the booster pump (7b) and the second switch valve (8b); a first switch valve (8a) is arranged between the cold medium outlet (62) and the atomizing nozzle (2), and a third pressure gauge (4c) is arranged between the cold medium outlet (62) and the first switch valve (8a).

7. A methanol atomization cracking hydrogen production device according to claim 3 or 6, characterized in that: The heat exchange tube (65) is arranged in a spiral shape.

8. A methanol atomization cracking hydrogen production device according to any one of claims 1, 2, 3, and 6, characterized in that: The reactor (3) is provided with a liquid level meter (30), and the liquid level meter (30) is connected to the inner cavity of the reactor (3). The reactor (3) is also provided with a first sewage valve (9a), and the first sewage valve (9a) is connected to the lower part of the inner cavity of the reactor (3).

9. A methanol atomization cracking hydrogen production device according to claim 4, characterized in that: The lower end of the lower sealing head (38) is connected to a second sewage valve (9b).

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