CN219174216U - Hydrogen purification device - Google Patents

Abstract

The utility model relates to the field of hydrogen purification, in particular to a hydrogen purification device, which comprises a heating mechanism and a reaction mechanism which are arranged in a split mode, wherein the heating mechanism is positioned above the reaction mechanism, the heating mechanism comprises a heating tank, a first air inlet and a first air outlet which are convexly arranged on the outer side of the heating tank, the reaction mechanism comprises a reaction tank, a second air inlet and a second air outlet which are convexly arranged on the outer side of the reaction tank, a cavity is arranged in the reaction tank, and a first flow guiding mechanism, a catalytic reaction layer and a second flow guiding mechanism are sequentially arranged in the cavity from top to bottom. According to the utility model, the heating mechanism and the reaction mechanism are arranged in a split mode, so that the consistency of a temperature field of a reaction area in the reaction mechanism can be better ensured, and a uniform flow field, a temperature field and a reaction field are realized; by arranging the first diversion mechanism and the second diversion mechanism in the reaction mechanism, the primary distribution and the secondary diversion can be realized, so that the air flow is more uniform.

Description

Hydrogen purification device

Technical Field

The utility model relates to the field of hydrogen purification, in particular to a hydrogen purification device.

Background

Hydrogen is an important industrial raw material and clean energy, and can be widely applied to industries such as petrochemical industry, electric power, metallurgy and the like, but at present, each industry has higher requirements on the purity of the hydrogen. In chemical production, raw material hydrogen often contains oxygen, and the existence of higher oxygen does not meet the hydrogenation process requirement or the safety requirement.

In the water electrolysis hydrogen production technology, the hydrogen generated by the electrolytic tank contains oxygen, a catalytic oxidation method is generally adopted in a hydrogen purification system, the hydrogen reacts with the oxygen to generate water, so as to remove oxygen impurities, the process is a hydrogen deoxidation and purification process, and the catalyst generally adopts porous oxide loaded palladium metal with high catalytic activity and the like. The existing hydrogen purification device consists of a heating cylinder, a catalytic cylinder and a heat preservation layer, wherein the heating cylinder is provided with an electric heating element, the electric heating element consists of a heating wire and a heating pipe and is used for heating gas and a catalyst, so that the reaction is maintained within the range of 60-200 ℃, and the optimal reaction temperature is 160 ℃ generally; the catalytic cylinder is filled with deoxidizing catalyst, which is the place where deoxidizing reaction occurs. When the deoxidizer body works, gas enters the heating cylinder from the gas inlet, enters the catalytic cylinder after being heated, enters the deoxidization reaction, and hydrogen is discharged from the gas outlet after the deoxidization reaction.

The existing hydrogen purification device has the following problems: 1. the temperature field in the catalytic tube is uneven, the temperature of the upper end and the lower end of the heating tube is inconsistent under the flushing of gas, the temperature of the upper end and the lower end of the catalytic tube is inconsistent, the catalytic tube is heated by radiation, and the temperature of the inner side and the outer side is inconsistent; 2. the length of the gas flow path in the catalytic cylinder is different, so that a local dead zone is formed, and the utilization rate of the catalyst is not high; 3. the gas flow velocity in the catalytic cylinder is unevenly distributed, and the catalyst in the area with high gas flow velocity reaches the service life end first, so that the overall catalytic effect is reduced, and the frequency of replacing the catalyst is increased.

Disclosure of Invention

Aiming at the defects of the prior art, the utility model aims to provide a hydrogen purification device so as to solve the problems of uneven catalytic reaction temperature, low catalyst utilization rate and uneven gas flow rate in a catalytic cylinder in the existing hydrogen purification device.

The utility model provides a hydrogen purification device, which comprises a heating mechanism and a reaction mechanism, wherein the heating mechanism and the reaction mechanism are arranged in a split manner and are provided with independent cavities, the heating mechanism is positioned above the reaction mechanism, the heating mechanism comprises a heating tank, and a first air inlet and a first air outlet which are convexly arranged at the outer side of the heating tank, and the first air inlet and the first air outlet are respectively arranged at the upper side and the lower side of the heating tank;

the reaction mechanism comprises a reaction tank, and a second air inlet and a second air outlet which are convexly arranged on the outer side of the reaction tank, wherein the second air inlet and the second air outlet are convexly arranged on the upper side and the lower side of the reaction tank, the second air inlet, the reaction tank and the second air outlet are all positioned on the same central axis, and the second air inlet is communicated with the first air outlet;

the reaction tank is internally provided with a cavity, and a first flow guiding mechanism, a catalytic reaction layer and a second flow guiding mechanism are sequentially arranged in the cavity from top to bottom.

Further, the first flow guiding mechanism comprises a distribution plate and a flow guiding plate, the distribution plate is arranged between the second air inlet and the flow guiding plate, a plurality of vent holes are formed in the distribution plate, and the vent holes gradually increase from the center of the distribution plate to the outer hole diameter; the guide plate is provided with a plurality of guide cavities.

Further, the distribution plate is arranged to be planar.

Further, the distribution plate is arranged such that the middle portion protrudes upward, and the height of the protruding portion is smaller than the distance from the distribution plate to the top of the reaction chamber.

Further, the guide plate is composed of a plurality of layers of annular thin plates and a plurality of connecting plates, the inner diameters of the annular thin plates are sequentially increased from the center of the guide plate to the outside, and the connecting plates are circumferentially distributed in the guide plate to divide the guide plate into at least 6 parts.

Further, the cross section of the flow guiding cavity is arranged in a honeycomb shape, a square grid shape or a triangle shape.

Further, the second flow guiding mechanism comprises a supporting net and a grid, wherein the supporting net is positioned between the catalytic reaction layer and the grid, and the pore diameter of the supporting net is smaller than the particle diameter of the catalyst.

Further, the reaction mechanism further comprises a feed inlet and a discharge outlet, the feed inlet and the discharge outlet are all provided with protrusions and are arranged on the outer side of the reaction tank, the feed inlet and the discharge outlet are arranged between the first flow guiding mechanism and the second flow guiding mechanism, and the feed inlet is arranged above the discharge outlet.

Further, the reaction tank at least comprises two layers of interlayers, a first interlayer is arranged close to the inner wall of the reaction tank and is a buffer layer, a second interlayer is arranged outside the first interlayer, and the second interlayer is an insulation layer.

Compared with the prior art, the utility model has the beneficial effects that:

1. according to the utility model, the heating mechanism and the reaction mechanism are arranged in a split mode, so that on one hand, the consistency of the temperature field of the reaction area in the reaction mechanism can be better ensured, and a uniform flow field, a uniform temperature field and a uniform reaction field are realized; on the other hand, the raw material gas is heated to reach enough reaction temperature, and meanwhile, the heat accumulation formed by the heating temperature and the heat release temperature can be avoided;

2. the first flow guiding mechanism and the second flow guiding mechanism are arranged in the reaction mechanism, so that primary distribution and secondary flow guiding can be realized, wherein the first flow guiding mechanism can ensure that the gas distribution flow field of the raw material gas is uniformly distributed when the raw material gas enters the reaction mechanism, so that the raw material gas is uniformly and fully filled in the catalytic reaction layer to react with the catalyst, the overall catalytic reaction effect is improved, the phenomenon that the flow velocity distribution is not uniform when the gas enters the catalytic reaction layer, the catalyst in a region with a fast gas flow velocity reaches the end of service life firstly is avoided, and the catalytic reaction effect is reduced; the second flow guiding mechanism can play a role in guiding gas, so that the deoxidized and purified raw gas is enabled to uniformly flow out of the reaction tank.

Drawings

FIG. 1 is a schematic diagram of a hydrogen purification device according to the present utility model;

FIG. 2 is a schematic view of an embodiment 1 of a distribution plate according to the present utility model;

FIG. 3 is a schematic view of an embodiment 2 of a distribution plate according to the present utility model;

FIG. 4 is a schematic view of a baffle according to embodiment 1 of the present utility model;

FIG. 5 is a schematic view of a baffle according to embodiment 2 of the present utility model;

FIG. 6 is a schematic view of the structure of the support net of the present utility model;

fig. 7 is a schematic view of the structure of the grid of the present utility model.

Reference numerals:

1. a heating mechanism; 101. a heating tank; 102. a first air inlet; 103. a first air outlet; 2. a reaction mechanism; 201. a reaction tank; 202. a second air inlet; 203. a second air outlet; 204. a distribution plate; 205. a deflector; 206. a catalytic reaction layer; 207. a support net; 208. a grid; 209. a feed inlet; 210. and a discharge port.

Detailed Description

In order to better understand the technical solutions in the present application, the following description will clearly and completely describe the technical solutions in the embodiments of the present application in conjunction with the drawings in the embodiments of the present application, and it is obvious that the described embodiments are only some embodiments of the present application, not all embodiments. All other embodiments, which can be made by one of ordinary skill in the art without undue burden from the present disclosure, are within the scope of the present disclosure.

It should be noted that, in the description of the present utility model, it should be noted that, directions or positional relationships indicated by terms such as "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., are directions or positional relationships based on the drawings, are merely for convenience of describing the present utility model and simplifying the description, and do not indicate or imply that the devices or elements to be referred to must have a specific direction, be configured and operated in the specific direction, and thus should not be construed as limiting the present utility model; the terms "first," "second," "third," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying relative importance, and furthermore, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "coupled," and the like are to be construed broadly, and may be fixedly coupled, detachably coupled, or integrally coupled, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present utility model will be understood in specific cases by those of ordinary skill in the art.

As shown in fig. 1, the utility model provides a hydrogen purification device, which comprises a heating mechanism 1 and a reaction mechanism 2, wherein the heating mechanism 1 and the reaction mechanism 2 are arranged in a split type and are provided with independent cavities, and the heating mechanism 1 is positioned above the reaction mechanism 2. Compared with the integral design of the heating mechanism 1 and the reaction mechanism 2 in the prior art, the utility model can ensure the consistency of the temperature fields of the reaction areas in the heating mechanism 1 and the reaction mechanism 2 by arranging the heating mechanism 1 and the reaction mechanism 2 in a split mode; on the other hand, the reaction of hydrogen and oxygen to generate water is exothermic, if the heating mechanism 1 and the reaction mechanism 2 are uniformly arranged in the same reaction device, the combination of the heating temperature and the exothermic reaction temperature can lead to the rapid temperature rise in the reaction device to form heat accumulation, thereby damaging the reaction device.

The heating mechanism 1 comprises a heating tank 101, a first air inlet 102 and a first air outlet 103, wherein the heating tank 101 is of a tank-shaped structure and is transversely arranged, the first air inlet 102 is convexly arranged on the upper side of the heating tank 101, the first air outlet 103 is convexly arranged on the lower side of the heating tank 101, meanwhile, the first air inlet 102 and the first air outlet 103 are respectively arranged on the left side and the right side of the heating tank 101, raw material gas is caused to flow in through the first air inlet 102, the residence time of the raw material gas in the heating tank 101 is prolonged, the raw material gas is caused to be sufficiently heated, the phenomenon that the raw material gas cannot react with a deoxidizing catalyst due to insufficient temperature is avoided, and the purification effect is lost.

The heating tank 101 may adopt an electric heating or steam heating mode, and when adopting an electric heating mode, a heating element is arranged in the heating tank 101, and the heating element is composed of a heating wire and the heating tank 101. The reaction of hydrogen and oxygen is required to be carried out under combustion or high-temperature heating, so the heating mechanism 1 is provided for heating the raw material hydrogen to a temperature at which it can be reacted. The outside of the heating tank 101 is also provided with a pressure display and a temperature display, the pressure display and the temperature display can be used for respectively displaying the pressure and the temperature in the heating tank 101, whether raw material gas exists in the heating tank 101 or not is determined according to the pressure, if the pressure is close to an initial state, the heating is stopped when the raw material gas does not exist, and the situation that the heating element generates full-power dry burning is avoided under the condition that the raw material gas does not exist; whether the raw material gas is heated to the temperature capable of reacting can be judged in real time according to the temperature, so that the reaction efficiency is ensured.

The reaction mechanism 2 comprises a reaction tank 201, a second air inlet 202 and a second air outlet 203, wherein the reaction tank 201 is in a tank-shaped structure and is vertically arranged, the second air inlet 202 is convexly arranged on the upper side of the reaction tank 201, the second air outlet 203 is convexly arranged on the lower side of the reaction tank 201, the second air inlet 202, the reaction tank 201 and the second air outlet 203 are all positioned on the same central axis, and the second air inlet 202 is communicated with the first air outlet 103. By locating the first air outlet 103, the second air inlet 202, the reaction tank 201 and the second air outlet 203 on the same vertical line, the heated raw material gas can be promoted to flow into the reaction tank 201 more smoothly and fully react with the catalyst in the reaction tank 201; meanwhile, the situation that the flow paths of the raw material gases in the reaction tank 201 are different in length to form a local dead zone so as to influence the utilization rate of the catalyst can be avoided.

The reaction tank 201 is made of stainless steel or low carbon steel, nickel is plated in the reaction tank, and the section of the tank can be round, oval or other shapes. The reaction tank 201 at least comprises two layers of interlayers, wherein a first interlayer is arranged near the inner wall of the reaction tank 201, and is a buffer layer made of elastic structural materials with buffer function. A second interlayer is arranged outside the first interlayer, and the second interlayer is an insulation layer, and can be made of rare earth insulation materials or novel inorganic insulation materials; in other embodiments, the insulation may also be provided outside the reactor tank 201, such as with an aluminum silicate cotton sleeve outside the reactor tank 201. By arranging the heat-insulating layer, the heat dissipation rate of the heated raw material gas in the reaction tank 201 can be reduced, so that the raw material gas in the reaction tank 201 is still at the reaction temperature, and the catalytic reaction is prevented from being influenced due to insufficient temperature.

A reaction chamber is provided in the reaction tank 201, and a first flow guiding mechanism, a catalytic reaction layer 206 and a second flow guiding mechanism are provided in this chamber from top to bottom. The first diversion mechanism comprises a distribution plate 204 and a diversion plate 205, wherein the distribution plate 204 is arranged between the second air inlet 202 and the diversion plate 205, a plurality of vent holes are arranged on the distribution plate 204, and the aperture of the vent holes gradually increases from the center of the distribution plate 204 to the outside; the baffle 205 is provided with a plurality of baffle cavities. The distribution plate 204 plays a role in gas distribution, and after the raw material gas enters the reaction tank 201, the raw material gas is distributed through the vent holes on the distribution plate 204 to become small air flow to flow downwards, so that the flow distribution function can be achieved to a certain extent, and the heated raw material gas can be more uniformly introduced into the lower layer structure; the baffle 205 further plays a role of uniform gas, and the split raw gas passes through the baffle 205, so that the raw gas is enabled to be changed into uniform laminar flow from turbulent flow, and then the raw gas is enabled to be uniformly and fully filled in the catalytic reaction layer 206 to react with the catalyst, thereby improving the overall catalytic reaction effect, avoiding uneven flow velocity distribution of the gas when entering the catalytic reaction layer 206, leading to the catalyst in a region with high gas flow velocity reaching the service life end, reducing the catalytic reaction effect, increasing the catalyst replacement frequency and causing the catalyst cost to be increased.

As shown in fig. 2, in embodiment 1, the distribution plate 204 is provided in a flat surface, which can function as gas distribution, while the flat surface structure is relatively simple and easy to manufacture.

As shown in fig. 3, in embodiment 2, the distribution plate 204 is provided with a middle portion protruding upward, the height of the protruding portion is smaller than the distance from the distribution plate 204 to the top of the cavity, and the inner diameter of the protruding portion is smaller than 2/3 of the diameter of the distribution plate 204. The center of the distribution plate 204 corresponds to the second air inlet 202, and the center part is arranged to be upwards convex, so that on one hand, the convex part can also play a certain role in guiding, the raw material gas is guided to the periphery along the outer contour of the convex part after entering, and the raw material gas is prevented from being excessively concentrated at the center of the distribution plate 204.

The distribution plate 204 may be made of 316L stainless steel material, or other stainless steel, nickel plate, etc. The distribution plate 204 is fixed inside the reaction tank 201 by welding, or may be fixed by a mechanical structure.

As shown in fig. 4, in embodiment 1, the baffle 205 is composed of a plurality of annular thin plates with inner diameters sequentially increasing from the center of the baffle 205 to the outside, and a plurality of connecting plates circumferentially distributed in the baffle 205 and dividing the baffle 205 into at least 6 portions, the height of the baffle 205 being about 2-5cm. The guide plates 205 are arranged in an annular structure and are matched with the structure of the distribution plate 204, so that the small raw gas flows distributed by the distribution plate 204 are sequentially increased from the center to the outside, and are uniformly distributed in the whole catalytic reaction layer 206 after passing through the guide plates 205, so that excessive concentration in the center position is avoided; meanwhile, the annular guide plate 205 is simple in structure and easy to manufacture.

As shown in fig. 5, in embodiment 2, the baffle 205 is composed of a plurality of small-sized baffle cavities with honeycomb, square or triangle cross sections, and compared with the annular structure, the baffle 205 provided in this technical scheme has a more uniform structure, and the baffle cavities are more dense and can disperse the flow of the raw gas more uniformly.

The catalytic reaction layer 206 is internally provided with a deoxidizing catalyst, which is mainly used for carrying out the reaction of hydrogen and oxygen, the catalytic reaction layer 206 is provided with a feed inlet 209 and a discharge outlet 210, wherein the feed inlet 209 and the discharge outlet 210 are both convexly arranged on the outer side of the reaction tank 201, the feed inlet 209 is arranged between a first flow guiding mechanism and a second flow guiding mechanism, the feed inlet 209 is arranged above the discharge outlet 210, the feed inlet 209 is close to the first flow guiding mechanism, and the discharge outlet 210 is close to the second flow guiding mechanism, so that the catalyst is convenient to throw in and replace. Compared with the conventional catalyst, the catalyst has the characteristics of high deoxidization activity, deep deoxidization depth, large gas treatment capacity, high temperature resistance, strong water resistance, continuous long-term use activity, long service life and the like, and the activity range of the catalyst on oxygen content in raw material gas can reach 2%.

As shown in fig. 6 to 7, the second flow guiding structure comprises a supporting net 207 and a grid 208, the supporting net 207 is located between the catalytic reaction layer 206 and the grid 208, the supporting net 207 is configured as a net structure, and the pore diameter of the supporting net 207 is smaller than the catalyst particle diameter, so that the raw gas after deoxidization and purification can smoothly flow out through the supporting net 207, and the catalyst can be prevented from falling into the lower space of the reaction tank 201 as much as possible. The grid 208 is provided with a plurality of through holes, the aperture of the through holes is smaller than the particle size of the catalyst, so that the catalyst can be further prevented from falling off, and meanwhile, the gas diversion effect can be achieved, and the raw gas after deoxidation and purification is promoted to uniformly flow out of the reaction tank 201; the grid 208 is spaced from the second outlet 203 of the reaction tank 201 to temporarily store the gas.

The application method of the hydrogen purification device provided by the utility model comprises the following steps:

s1: closing the discharge port 210, and filling the deoxidizing catalyst into the catalytic reaction layer 206 of the reaction mechanism 2 through the feed port 209;

s2: starting a heater in the heating mechanism 1, and when the heater is determined to rise to a reactable temperature through a temperature display, introducing raw material gas into the heating mechanism 1 through a first gas inlet 102 for heating;

s3: the heated raw material gas enters the reaction mechanism 2 through the first air outlet 103 and the second air inlet 202, is sequentially subjected to gas distribution and flow guide through the first flow guide mechanism, deoxidization and purification through the catalytic reaction layer 206, secondary flow guide through the second flow guide mechanism and finally flows out through the second air outlet 203 in the reaction mechanism 2.

When the raw material gas passes through the first flow guiding mechanism, gas distribution is performed through the distribution plate 204, the raw material gas is changed into small air flow to flow downwards, and then the small air flow passes through the flow guiding plate 205, so that the raw material gas is changed into uniform laminar flow from turbulent flow; when passing through the second diversion mechanism, the raw material gas passes through the supporting net 207 and then passes through the grid 208, so that the raw material gas after catalytic purification is diverted, and flows out more uniformly.

The technical scheme of the utility model achieves the following effects:

according to the hydrodynamic calculation design, the gas flow velocity distribution in the catalyst is uniform, and the error of 1.5% is only in the measurement of the inside by using a micro differential pressure transmitter. The temperature field is uniformly distributed, and the temperature difference between the upper part and the lower part of the catalyst is less than 1 ℃. In the hydrogen purification system, a uniform flow field, a temperature field and a reaction field are realized.

Under the condition of the same hydrogen concentration in 1ppm oxygen and the same service life of 16000 hours, the technical scheme of the utility model can reduce the usage amount of the catalyst by 30% compared with the prior catalyst; or if the catalyst with the same oxygen volume is used, the technical scheme of the utility model can prolong the service life of the catalyst by 42 percent and greatly reduce the use cost of the deoxidized catalyst.

It should be understood that the structures, proportions, sizes, etc. shown in the drawings are for illustration purposes only and should not be construed as limiting the scope of the present disclosure, since any structural modifications, proportional changes, or dimensional adjustments made by those skilled in the art should not be made in the present disclosure without affecting the efficacy or achievement of the present disclosure.

Although the utility model has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit and scope of the technical solutions of the embodiments of the present utility model.

Claims (9)

1. The utility model provides a hydrogen purification device, includes heating mechanism (1) and reaction mechanism (2), its characterized in that, heating mechanism (1) and reaction mechanism (2) components of a whole that can function independently set up and all have independent cavity, heating mechanism (1) are located reaction mechanism (2) top, heating mechanism (1) are including heating jar (101) and protrusion set up in first air inlet (102) and first gas outlet (103) in heating jar (101) outside, first air inlet (102), first gas outlet (103) are in respectively the upper and lower side of heating jar (101);

the reaction mechanism (2) comprises a reaction tank (201), and a second air inlet (202) and a second air outlet (203) which are convexly arranged outside the reaction tank (201), wherein the second air inlet (202) and the second air outlet (203) are convexly arranged on the upper side and the lower side of the reaction tank (201), the second air inlet (202), the reaction tank (201) and the second air outlet (203) are all positioned on the same central axis, and the second air inlet (202) is communicated with the first air outlet (103);

a cavity is arranged in the reaction tank (201), and a first flow guiding mechanism, a catalytic reaction layer (206) and a second flow guiding mechanism are sequentially arranged in the cavity from top to bottom.

2. The hydrogen purification device according to claim 1, wherein the first diversion mechanism comprises a distribution plate (204) and a diversion plate (205), the distribution plate (204) is arranged between the second air inlet (202) and the diversion plate (205), a plurality of ventilation holes are arranged on the distribution plate (204), and the ventilation holes gradually increase from the center of the distribution plate (204) to the outer hole diameter; a plurality of flow guide cavities are arranged on the flow guide plate (205).

3. A hydrogen purification device according to claim 2, characterized in that the distribution plate (204) is arranged in a plane.

4. A hydrogen purification device according to claim 2, wherein the distribution plate (204) is arranged with its middle part protruding upwards, the height of the protruding part being smaller than the distance of the distribution plate (204) to the top of the chamber.

5. A hydrogen purification device according to claim 2, wherein the baffle (205) is composed of a plurality of annular thin plates and a plurality of connecting plates, the inner diameters of the annular thin plates of the plurality of layers are sequentially increased from the center of the baffle (205) to the outside, the connecting plates are circumferentially distributed in the baffle (205), and the baffle (205) is divided into at least 6 parts.

6. A hydrogen purification device according to claim 2, wherein the flow-directing chamber cross-section is arranged in a honeycomb, a square or a triangle.

7. A hydrogen purification device according to claim 1, wherein the second flow guiding means comprises a support mesh (207) and a grid (208), the support mesh (207) being located between the catalytic layer (206) and the grid (208), the support mesh (207) having a pore size smaller than the catalyst particle size.

8. The hydrogen purification device according to claim 1, wherein the reaction mechanism (2) further comprises a feed inlet (209) and a discharge outlet (210), the feed inlet (209) and the discharge outlet (210) are both provided with protrusions and are arranged on the outer side of the reaction tank (201), the feed inlet (209) and the discharge outlet (210) are arranged between the first diversion mechanism and the second diversion mechanism, and the feed inlet (209) is arranged above the discharge outlet (210).

9. The hydrogen purification device according to claim 1, wherein the reaction tank (201) comprises at least two layers of interlayers, a first interlayer is arranged close to the inner wall of the reaction tank (201), the first interlayer is a buffer layer, a second interlayer is arranged outside the first interlayer, and the second interlayer is a heat insulation layer.

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