A continuous hydrogenation apparatus for metal powder

Abstract

The application discloses a kind of metal powder continuous hydrogenation device, it is related to metal powder hydrogenation technical field, including first reaction shell, second reaction shell, communicating pipe, air distribution plate, first heat exchange sleeve and second heat exchange sleeve, the first end of communicating pipe is connected with the top of first reaction shell and is communicated, the second end of communicating pipe is connected with the top of second reaction shell and is communicated, and the inner diameter of the second end of communicating pipe is the inner diameter of the first end of communicating pipe, the inner cavity cross-sectional dimension of second reaction shell is greater than the inner cavity cross-sectional dimension of first reaction shell, the bottom of first reaction shell is provided with gas inlet, and the side is provided with metal powder inlet, air distribution plate is arranged between gas inlet and metal powder inlet, the bottom of second reaction shell is provided with discharge port, first heat exchange sleeve is sleeved outside first reaction shell, and second heat exchange sleeve is sleeved outside second reaction shell.The application can continuously hydrogenate production to metal powder, greatly shorten the time of hydrogenation, and be heated evenly.

Description

Technical Field

[0001] This invention relates to the field of metal powder hydrogenation technology, and in particular to a continuous metal powder hydrogenation apparatus. Background Technology

[0002] Solid-state metal hydrogen storage materials are commonly prepared using methods such as smelting, sintering, diffusion, and ball milling. Hydrogenation is a crucial process in the preparation of solid-state metal hydrogen storage materials. Hydrogenation is the direct reaction between a metal and hydrogen; solid-state metal hydrogen storage materials can react directly with hydrogen under certain temperature and pressure conditions to form hydrides. The commonly used hydrogenation methods currently include the following: The hydrogenation reaction method involves placing processed metal powder into a reaction vessel, introducing hydrogen gas at the required pressure, heating the reaction vessel to the required temperature, maintaining the temperature for hydrogenation to allow the metal powder and hydrogen gas to react fully, and then stopping the heating to obtain a solid metal hydrogen storage material.

[0003] Mechanical ball milling involves solid-gas or solid-solid reactions during the grinding process, generating new compounds. Typically, pre-processed metal powder is placed in a ball mill, hydrogen gas at the required pressure is introduced, the equipment is heated to the necessary temperature, and under these conditions, solid metallic hydrogen storage materials are produced through ball milling.

[0004] The main problems with the equipment used in the above methods are: the metal powder is fixedly piled up, requiring complete hydrogenation in the entire batch; continuous hydrogenation of solid metal is not possible; and the internal structure of the agglomerated material is difficult to hydrogenate completely, requiring a long waiting time, resulting in long hydrogenation time and low efficiency. Furthermore, the material is heated unevenly during hydrogenation, and localized high temperatures can cause the metal powder to agglomerate and melt, affecting product quality. The heat generated during hydrogenation cannot be transferred in a timely manner, and there are no effective heat exchange measures, making it difficult to achieve large-scale, continuous, and automated production. Therefore, there is an urgent need for a continuous metal powder hydrogenation device to solve the above technical problems. Summary of the Invention

[0005] The purpose of this invention is to provide a continuous hydrogenation apparatus for metal powder to solve the problems existing in the prior art, enabling continuous hydrogenation production of metal powder, significantly shortening the hydrogenation time, and ensuring uniform heating.

[0006] To achieve the above objectives, the present invention provides the following solution: This invention provides a continuous hydrogenation device for metal powder, comprising a first reaction shell, a second reaction shell, a connecting pipe, an air distribution plate, a first heat exchange sleeve, and a second heat exchange sleeve. The first end of the connecting pipe is connected to and communicates with the top of the first reaction shell, and the second end of the connecting pipe is connected to and communicates with the top of the second reaction shell. The inner diameter of the second end of the connecting pipe is the same as the inner diameter of the first end of the connecting pipe. The inner cross-sectional dimension of the second reaction shell is larger than that of the first reaction shell. A gas inlet is provided at the bottom of the first reaction shell, and a metal powder inlet is provided on its side. The air distribution plate is located between the gas inlet and the metal powder inlet. A discharge port is provided at the bottom of the second reaction shell. The lower part of the first reaction shell forms a dense phase region, and the lower part of the second reaction shell forms a moving region. The upper parts of the first and second reaction shells together form a dilute phase region. The material in the dense phase region is in a fluidized state. The first heat exchange sleeve is fitted outside the first reaction shell, and the second heat exchange sleeve is fitted outside the second reaction shell.

[0007] In some embodiments, a partition and a reaction gas outlet shell are also included. The connecting pipe is an inverted U-shaped pipe. The top of the partition is fixedly connected to the second end of the connecting pipe. The bottom of the partition is inserted into the material in the moving area. The reaction gas outlet shell is connected to the partition and the second reaction shell, and a connecting cavity can be formed between the reaction gas outlet shell and the second reaction shell. A reaction gas outlet is provided on the reaction gas outlet shell.

[0008] In some embodiments, the partition divides the top space of the second reaction shell into two parts, one part of which is connected to the second end of the connecting pipe, and the other part is connected to the reaction gas outlet shell.

[0009] In some embodiments, a loosening air supply device is also included, which is disposed on the second reaction shell and is capable of supplying air to the inner wall of the second reaction shell.

[0010] In some embodiments, both the first reaction shell and the second reaction shell include an upper cylindrical structure and a lower conical cylindrical structure.

[0011] In some embodiments, the first heat exchange jacket is provided with a first heat exchange medium inlet and a first heat exchange medium outlet, the first heat exchange medium inlet is provided on the bottom side of the first heat exchange jacket, and the first heat exchange medium outlet is provided on the top side of the first heat exchange jacket. The second heat exchange jacket is provided with a second heat exchange medium inlet and a second heat exchange medium outlet, the second heat exchange medium inlet is provided on the bottom side of the second heat exchange jacket, and the second heat exchange medium outlet is provided on the top side of the second heat exchange jacket.

[0012] In some embodiments, a metal powder inlet pipe is also included, which is disposed at the metal powder inlet and outlet and is inclined, gradually approaching the airflow distribution plate from high to low.

[0013] In some embodiments, a discharge valve is provided at the discharge port, and the discharge valve can adjust the opening degree.

[0014] In some embodiments, the system also includes an oxygen content detector, a pressure sensor, and a safety valve, all of which are mounted on the connecting pipe. The safety valve is used for emergency venting.

[0015] In some embodiments, a temperature monitoring device is also included, which is disposed on the connecting pipe for monitoring the temperature.

[0016] The present invention achieves the following technical effects compared to the prior art: In the continuous hydrogenation apparatus for metal powder provided by this invention, metal powder is introduced through the metal powder inlet. Hydrogen gas enters the first reaction shell under the action of the airflow distribution plate, causing the metal powder to be in a fluidized state. The fluidized metal powder continuously collides with each other, continuously stripping away the dense hydride passivation layer formed on the metal surface and constantly exposing fresh active metal surfaces inside. This avoids the large metal powder surface hydrogenation layer from hindering the inward diffusion of hydrogen gas, thus improving hydrogenation efficiency. After the powder completes rapid pre-hydrogenation and self-pre-crushing in the dense phase region, it is automatically introduced into the second reaction shell by the airflow through the dilute phase region and the connecting pipe. Since the cross-sectional size of the second reaction shell is larger than that of the first reaction shell, the metal powder slows down after reaching the second reaction shell and can fall into the moving area of ​​the second reaction shell for further deep hydrogenation, enabling continuous hydrogenation production. Furthermore, the fluidized metal powder can be dynamically and uniformly heated. On the one hand, unreacted hydrogen flows from bottom to top, forming counter-current convection with the metal powder to achieve heat exchange. On the other hand, the first and second heat exchange jackets are respectively attached to the outer walls of the first and second reaction shells, and heat exchange is achieved through forced circulation of the heat exchange medium. The combination of dual heat exchange and fluidized temperature uniformity avoids local high temperature and uneven heating. Attached Figure Description

[0017] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0018] Figure 1 This is a schematic diagram of the structure of a continuous hydrogenation device for metal powder in some embodiments of the present invention.

[0019] In the diagram: 1-First reaction shell; 2-Second reaction shell; 3-Airflow distribution plate; 4-First heat exchange jacket; 41-First heat exchange medium inlet; 42-First heat exchange medium outlet; 5-Second heat exchange jacket; 51-Second heat exchange medium inlet; 52-Second heat exchange medium outlet; 6-Dense phase zone; 7-Dilute phase zone; 8-Moving zone; 9-Connecting pipe; 10-Metal powder inlet; 11-Metal powder inlet pipe; 12-Loosening air supply device; 13-Air inlet; 4-Reaction gas outlet; 15-Reaction gas outlet; 16-Baffle; 17-Safety valve; 18-Pressure sensor; 19-Temperature monitoring device; 20-Oxygen content detector; 21-Control system; 22-Gas inlet; 23-Outlet; 24-Outlet valve; 25-First control valve; 26-Second control valve; 27-Third control valve; 28-Fourth control valve; 29-Fifth control valve; 30-Sixth control valve; 31-Eighth control valve. Detailed Implementation

[0020] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0021] The purpose of this invention is to provide a continuous hydrogenation apparatus for metal powder to solve the problems existing in the prior art, enabling continuous hydrogenation production of metal powder, significantly shortening the hydrogenation time, and ensuring uniform heating.

[0022] To make the above-mentioned objects, features and advantages of the present invention more apparent and understandable, the present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments.

[0023] like Figure 1As shown, the present invention provides a continuous hydrogenation device for metal powder, including a first reaction shell 1, a second reaction shell 2, a connecting pipe 9, an air distribution plate 3, a first heat exchange jacket 4, and a second heat exchange jacket 5. The first end of the connecting pipe 9 is connected to and communicates with the top of the first reaction shell 1, and the second end of the connecting pipe 9 is connected to and communicates with the top of the second reaction shell 2. The inner diameter of the second end of the connecting pipe 9 is the same as the inner diameter of the first end of the connecting pipe 9. The cross-sectional dimension of the inner cavity of the second reaction shell 2 is larger than that of the inner cavity of the first reaction shell 1. A gas... The gas inlet 22 is provided with a metal powder inlet 10 on the side. The airflow distribution plate 3 is provided between the gas inlet 22 and the metal powder inlet 10. The bottom of the second reaction shell 2 is provided with a discharge port 23. The lower part of the first reaction shell 1 forms a dense phase zone 6, and the lower part of the second reaction shell 2 forms a moving zone 8. The upper part of the first reaction shell 1 and the upper part of the second reaction shell 2 together form a dilute phase zone 7. The material in the dense phase zone 6 is in a fluidized state. The first heat exchange jacket 4 is fitted outside the first reaction shell 1, and the second heat exchange jacket 5 is fitted outside the second reaction shell 2.

[0024] In operation, metal powder is introduced through the metal powder inlet. Hydrogen gas enters the first reaction shell 1 under the action of the airflow distribution plate 3, causing the metal powder to fluidize. The fluidized metal powder continuously collides with each other, continuously stripping away the dense hydride passivation layer formed on the metal surface and constantly exposing fresh active metal surfaces inside. This prevents the hydrogenation layer on the surface of large metal powder pieces from hindering the inward diffusion of hydrogen gas, thus improving hydrogenation efficiency. After the powder completes rapid pre-hydrogenation and self-pre-crushing in the dense phase zone 6, it automatically enters the second reaction shell 2 with the airflow through the dilute phase zone 7 and the connecting pipe 9. Since the cross-sectional size of the second reaction shell 2 is larger than that of the first reaction shell 1, the metal powder slows down after reaching the second reaction shell 2 and can fall into the moving zone 8 of the second reaction shell 2 for further deep hydrogenation, enabling continuous hydrogenation production. Furthermore, the fluidized metal powder can be dynamically and uniformly heated. On the one hand, unreacted hydrogen flows from bottom to top, forming counter-current convection with the metal powder to achieve heat exchange. On the other hand, the first heat exchange jacket 4 and the second heat exchange jacket 5 are respectively attached to the outer walls of the first reaction shell 1 and the second reaction shell 2. Through the forced circulation of the heat exchange medium, heat exchange is achieved. The combination of dual heat exchange and fluidized temperature uniformity avoids local high temperature and uneven heating.

[0025] Furthermore, after testing, the continuous hydrogenation device for metal powder in this embodiment yielded metal powder material with a particle size of 0~2000μm, finished hydrogenated metal powder with a particle size of 0~2000μm (adjustable according to particle size requirements), and a hydrogen storage density of 0~7.6wt% (adjustable according to hydrogenation requirements). The hydrogenation time can be significantly shortened from 2~12h. The first reaction shell 1 and the second reaction shell 2 are made of low-carbon alloy steel (such as S31603), meeting the requirements of pressure 1~6MPa and temperature 50~500℃.

[0026] In some embodiments, the continuous hydrogenation apparatus for metal powder further includes a partition 16 and a reaction gas outlet 14. The connecting pipe 9 is an inverted U-shaped pipe. The top of the partition 16 is fixedly connected to the second end of the connecting pipe 9, and the bottom of the partition 16 is inserted into the material in the moving zone 8. The reaction gas outlet 14 is connected to the partition 16 and the second reaction shell 2, and a connecting cavity can be formed between the reaction gas outlet 14 and the second reaction shell 2. A reaction gas outlet is provided on the reaction gas outlet 14. If the reaction gas wants to be discharged through the reaction gas outlet 14, it must enter the moving zone 8 from the dilute phase zone 7, and after entering the moving zone 8 and fully contacting the material, it can move upwards and be discharged through the reaction gas outlet. The partition 16 completely physically isolates the dilute phase zone 7 of the second reaction shell 2 from the reaction gas outlet 15, blocking the short-circuit channel for unreacted hydrogen to be directly discharged from the dilute phase zone 7. The reactant gas must strictly follow a single, pre-defined path through the material bed in the dilute phase zone 7 and the moving zone 8, the connecting cavity, and the reactant gas outlet. This ensures that all hydrogen gas can effectively contact the metal powder, preventing unreacted gas from being directly discharged. After entering the moving zone 8, the reactant gas flows upwards, forming a counter-current contact with the slowly moving metal powder. This counter-current mass transfer mode achieves deep hydrogenation. The material sealing not only prevents gas short-circuiting but also forms a robust physical barrier, preventing the deeply hydrogenated material that has settled in the second reaction shell 2 from being re-entrained into the dilute phase zone 7 by the rising gas flow. This avoids mixing of materials from different reaction stages, ensuring that the rapid pre-hydrogenation in the dense phase zone 6 and the deep hydrogenation in the moving zone 8 are absolutely independent. This makes the reaction conditions in each zone stable and controllable, improving the consistency of the product's hydrogenation degree. The material seal and the inverted U-shaped connecting pipe 9 form a double anti-backflow barrier, which can effectively prevent the reaction gas in the second reaction shell 2 from flowing back to the first reaction shell 1, ensuring the uniqueness of the gas flow direction in the entire device and avoiding the disruption of the fluidization state of the first reaction shell 1 due to gas backflow.

[0027] In some embodiments, the baffle 16 evenly divides the top space of the second reaction shell 2 into two parts, one part being connected to the second end of the connecting pipe 9, and the other part being connected to the reaction gas outlet shell 14. After the gas flow carrying metal powder is vertically ejected downwards from the inverted U-shaped pipe, it diffuses evenly across the entire cross-sectional area of ​​the first chamber under the constraint of the symmetrical chamber, and then evenly settles into the entire bed cross-section of the lower moving zone 8, achieving uniform material distribution. After passing through the material bed in the moving zone 8, the reaction gas evenly enters the symmetrically distributed second outlet chamber, and then converges to the reaction gas outlet shell 14 for discharge. This uniform inlet and outlet flow pattern across the entire cross-section makes the airflow in the moving zone 8 exhibit an ideal piston flow state, eliminating channeling, short-circuiting, and local dead zone phenomena commonly found in traditional reactors. The physical isolation between the inlet and outlet chambers blocks the channel for the high-speed inlet airflow to directly entrain the settled dust in the outlet chamber, preventing secondary re-entrainment of the settled dust. Combined with the effect of the built-in settling chamber in the original connecting chamber, the dust content in the exhaust gas can be further reduced.

[0028] In some embodiments, the continuous hydrogenation apparatus for metal powder further includes a loosening air supply device 12. The loosening air supply device 12 is disposed on the second reaction shell 2 and can supply air to the inner wall of the second reaction shell 2. The air inlet 13 of the loosening air supply device 12 is connected to the same gas supply device as the gas inlet 22 on the first reaction shell 1. The gas supply device supplies pure hydrogen or a mixture of hydrogen and inert gas. Multiple nozzles are evenly arranged around the inner wall of the second reaction shell 2, continuously injecting low-speed hydrogen gas into the interface between the inner wall and the material bed. This forms a thin gas film in the sidewall region, effectively reducing the friction between particles and the inner wall, as well as between particles themselves. This dynamically breaks up existing arched structures, preventing material blockage and interruption, and ensuring continuous and stable operation of the apparatus. The sidewall airflow generated by the loosening air supply device 12 continuously sweeps the inner wall surface, preventing material adhesion and accumulation on the wall surface, avoiding stagnant layers and scaling on the sidewall, and ensuring that the reactor always maintains its designed effective volume and reaction performance. Furthermore, the fresh hydrogen injected into the sidewall region by the loosening air supply device 12 can directly and fully react with the sidewall material, activating the originally inefficient sidewall reaction zone and increasing the effective reaction volume of the moving zone 8. The micro-turbulence generated by the loosening air supply can break the relatively static gas-solid contact state within the moving bed, promoting gas diffusion in the particle gaps and enhancing the mass transfer process between the gas and solid phases. Additionally, the low-temperature hydrogen injected by the loosening air supply device 12 can directly cool the inner wall and sidewall material of the second reaction shell 2, effectively removing the reaction heat from the sidewall region and preventing localized overheating caused by sidewall stagnation. Combined with the forced circulation heat exchange of the existing second heat exchange jacket 5, the temperature deviation across the entire cross-section of the moving zone 8 is controlled within a small range, avoiding decomposition of metal hydrides and product quality degradation due to localized high temperatures.

[0029] In some embodiments, both the first reaction shell 1 and the second reaction shell 2 include an upper cylindrical structure and a lower conical cylindrical structure, with the taper of the first reaction shell 1 being smaller than that of the second reaction shell 2. The cross-sectional area of ​​the lower conical cylinder of the first reaction shell 1 gradually increases from bottom to top, resulting in a gradient distribution of hydrogen gas flow velocity along the bed height: high velocity at the bottom, suitable velocity in the middle, and low velocity at the top. The small cross-sectional area at the bottom gas inlet 22 creates a sufficiently high initial gas velocity, which can strongly lift the metal powder at the bottom of the bed, eliminate the material deposition dead zone below the air distribution plate, and ensure that all the holes of the air distribution plate 3 can effectively ventilate, avoiding uneven fluidization caused by local blockage. As the cross-sectional area increases upward, the gas velocity gradually decreases to between the critical fluidization velocity and the terminal velocity of the metal powder, forming a stable and uniform bubbling fluidization state. This ensures both intense collision and self-crushing effects between particles and effectively reduces the phenomenon of fine particles being excessively entrained into the dilute phase region 7 by the airflow. The cone angle of the lower conical cylinder of the second reaction shell 2 is optimized (typically around 45°) to match the natural angle of repose of the metal hydride powder. Under gravity, the material can smoothly converge along the conical wall to the bottom outlet 23, avoiding material accumulation, arching, and bridging. Combined with the sidewall purging effect of the loosening air supply device 12, it ensures that the material in the moving zone 8 moves downward in a continuous and uniform piston flow throughout the entire operating cycle. As the material moves downward in the conical cylinder, the bed density naturally increases as the cross-sectional area gradually decreases, forming a gradient bed structure with a loose upper part and a dense lower part. The loose upper bed facilitates the uniform passage of the reaction gas and its full contact with the material, while the dense lower bed forms a good material seal, preventing gas from short-circuiting and leaking from the outlet 23.

[0030] In some embodiments, the first heat exchanger jacket 4 is provided with a first heat exchange medium inlet 41 and a first heat exchange medium outlet 42. The first heat exchange medium inlet 41 is located on the bottom side of the first heat exchanger jacket 4, and the first heat exchange medium outlet 42 is located on the top side of the first heat exchanger jacket 4. The second heat exchanger jacket 5 is provided with a second heat exchange medium inlet 51 and a second heat exchange medium outlet 52. The second heat exchange medium inlet 51 is located on the bottom side of the second heat exchanger jacket 5, and the second heat exchange medium outlet 52 is located on the top side of the second heat exchanger jacket 5. The bottom-in, top-out flow direction ensures that the heat exchange medium forms a stable plunger flow within the heat exchanger jacket, preventing local short circuits or channeling phenomena and ensuring that all heat exchange surfaces are fully utilized.

[0031] In some embodiments, the continuous hydrogenation device for metal powder further includes a metal powder inlet pipe 11, which is located at the outlet of the metal powder inlet 10 and is inclined, gradually approaching the airflow distribution plate 3 from high to low. The metal powder inlet pipe 11 adopts a downward inclined design, allowing the material to slide naturally down the pipe wall by its own gravity, achieving continuous and stable feeding without the need for additional mechanical conveying equipment such as screw conveyors or vibrating feeders.

[0032] In some embodiments, a discharge valve 24 is provided at the discharge port 23, and the opening of the discharge valve 24 can be adjusted. Adjusting the discharge valve 24 effectively controls the hydrogenation time of the metal powder in this region. The hydrogenation reaction rates of different types of metals (magnesium, titanium, zirconium, vanadium, etc.) and their alloys vary significantly. Even for the same metal, the optimal hydrogenation time required for powders of different particle sizes and purities differs. By adjusting the opening of the discharge valve 24, the residence time of the material in the moving zone 8 can be continuously and linearly changed, enabling the device to precisely match the hydrogenation kinetics of different materials and ensure that each material reaches the target degree of hydrogenation at the optimal reaction time. During device operation, by adjusting the opening of the discharge valve 24 in real time, the discharge rate and feed rate are kept dynamically balanced, thereby stabilizing the bed height in the moving zone 8 within a set range. A stable bed height is the foundation for ensuring the piston flow reaction characteristics and forced countercurrent gas-solid contact effect of a moving bed. It can avoid problems such as excessive gas resistance and fluidization disorder caused by an excessively high bed, or material sealing failure and gas short circuit caused by an excessively low bed.

[0033] In some embodiments, the continuous hydrogenation apparatus for metal powder further includes an oxygen content detector 20, a pressure sensor 18, a temperature monitoring device 19, and a safety valve 17. The oxygen content detector 20, pressure sensor 18, and safety valve 17 are all mounted on the connecting pipe 9. The safety valve 17 is used for emergency venting. The temperature monitoring device 19 is preferably a thermocouple mounted on the connecting pipe 9 for temperature monitoring. Hydrogen has a wide explosion limit in air, but under high temperature and pressure, it is highly susceptible to violent explosion when encountering trace amounts of oxygen. The oxygen content detector 20 can monitor in real time online, ensuring that the oxygen concentration in the system remains below the safe threshold. When the pressure inside the apparatus exceeds the set safe value, the valve automatically and quickly opens, releasing some gas and rapidly reducing the internal pressure.

[0034] In a preferred embodiment, the continuous hydrogenation apparatus for metal powder further includes a control system 21, and a first control valve 25, a second control valve 26, a third control valve 27, a fourth control valve 28, a fifth control valve 29, a sixth control valve 30, a seventh control valve, and an eighth control valve 31 connected to the control system 21 via electrical signals. The first control valve 25 is located at the gas inlet 22, the second control valve 26 is located at the air inlet 13 of the loose air supply device 12, the third control valve 27 is located at the first heat exchange medium inlet 41, the fourth control valve 28 is located at the first heat exchange medium outlet 42, the fifth control valve 29 is located at the second heat exchange medium inlet 51, the sixth control valve 30 is located at the second heat exchange medium outlet 52, the seventh control valve is located at the reaction gas outlet 15, and the eighth control valve 31 is located at the metal powder inlet 10. The control system 21 is also electrically connected to the discharge valve 24, the oxygen content detector 20, the pressure sensor 18, the temperature monitoring device 19, and the safety valve 17.

[0035] In the device's operation, the control system 21 can control the working status of all valves, enabling automated production. First, the eighth control valve 31 is opened, allowing metal powder to continuously enter the first reaction shell 1 through the metal powder inlet 10. Then, the first control valve 25 is opened, and the reaction gas (hydrogen) is evenly fed into the first reaction shell 1 through the airflow distributor 3. Hydrogen and metal powder are in a flowing state in the dense phase zone 6. During this process, hydrogen reacts with larger metal powder particles, forming hydride metal on the particle surface. The metal powder continuously collides and peels off the hydride metal on the surface, forming smaller powder. These smaller hydride metal powders enter the moving zone 8 through the dilute phase zone 7 via the airflow. The larger metal powders that are not internally hydrogenated after peeling continue to undergo hydrogenation and pre-crushing in the dense phase zone 6, thereby accelerating the hydrogenation reaction process. A first heat exchange jacket 4 is installed outside the first reaction shell 1. The third and fourth valves are opened, using a heat exchange medium to exchange the heat generated by the hydrogenation reaction out of the device. The first heat exchange jacket 4 uses indirect heat exchange; the heat exchange medium can be gas, water, heat transfer oil, or other heat exchange media. Simultaneously, unreacted gas and metal powder undergo convective heat exchange, with the heat discharged from the device outlet along with the gas. This combination of two heat exchange methods effectively provides sufficient reaction temperature and removes the heat generated by the hydrogenation reaction, preventing insufficient reaction temperature from affecting reaction efficiency and hydrogenation effect, and avoiding localized high temperatures caused by the exothermic hydrogenation reaction, which could lead to metal powder agglomeration and melting, affecting product quality. The flow cross-section of the right side of the entire device (the left side of the second reaction shell 2 and the inverted U-shaped tube) is larger than that of the left side (the right side of the first reaction shell 1 and the inverted U-shaped tube), meaning the flow velocity on the right side is lower than on the left, causing metal powder to deposit in the moving zone 8. The moving zone 8 is equipped with a loosening air supply device 12 to prevent metal powder from caking on the inner wall of the second reaction shell 2. A discharge port 23 is located at the bottom of the moving zone 8, where the metal powder undergoes further hydrogenation. The low airflow velocity in the moving zone 8 causes the metal powder to move slowly downwards. Adjusting the discharge valve 24 effectively controls the hydrogenation time of the metal powder in this area, while significantly reducing material mixing and backflow. Metal powder meeting the hydrogenation requirements is discharged through the discharge port 23. The moving zone 8 is equipped with a second heat exchanger 5, which operates on the same principle as the first heat exchanger 4. By opening the fifth and sixth valves, the heat generated by the hydrogenation reaction is exchanged out of the device using the heat exchange medium. The reaction gas is discharged through the reaction gas outlet shell 14 at the top of the moving zone 8 and sent to subsequent gas processing.

[0036] Specific examples have been used to illustrate the principles and implementation methods of this invention. The descriptions of the above embodiments are only for the purpose of helping to understand the method and core ideas of this invention. Furthermore, those skilled in the art will recognize that, based on the ideas of this invention, there will be changes in the specific implementation methods and application scope. Therefore, the content of this specification should not be construed as a limitation of this invention.

Claims

1. A continuous hydrogenation apparatus for metal powder, characterized in that: The reaction vessel includes a first reaction shell, a second reaction shell, a connecting pipe, an air distribution plate, a first heat exchange sleeve, and a second heat exchange sleeve. The first end of the connecting pipe is connected to the top of the first reaction shell, and the second end of the connecting pipe is connected to the top of the second reaction shell. The inner diameter of the second end of the connecting pipe is the same as the inner diameter of the first end of the connecting pipe. The inner cross-sectional dimension of the second reaction shell is larger than that of the first reaction shell. The first reaction shell has a gas inlet at its bottom and a metal powder inlet on its side. The air distribution plate is positioned between the gas inlet and the metal powder inlet. The second reaction shell has a discharge port at its bottom. The lower part of the first reaction shell forms a dense phase zone, and the lower part of the second reaction shell forms a moving zone. The upper parts of the first and second reaction shells together form a dilute phase zone. The material in the dense phase zone is in a fluidized state. The first heat exchange sleeve is fitted over the first reaction shell, and the second heat exchange sleeve is fitted over the second reaction shell.

2. The continuous hydrogenation apparatus for metal powder according to claim 1, characterized in that: It also includes a partition and a reaction gas outlet shell. The connecting pipe is an inverted U-shaped pipe. The top of the partition is fixedly connected to the second end of the connecting pipe. The bottom of the partition is inserted into the material in the moving area. The reaction gas outlet shell is connected to the partition and the second reaction shell, and a connecting cavity can be formed between the reaction gas outlet shell and the second reaction shell. The reaction gas outlet shell is provided with a reaction gas outlet.

3. The continuous hydrogenation apparatus for metal powder according to claim 2, characterized in that: The partition divides the top space of the second reaction shell into two parts, one part of which is connected to the second end of the connecting pipe, and the other part is connected to the reaction gas outlet shell.

4. The continuous hydrogenation apparatus for metal powder according to claim 1, characterized in that: It also includes a loosening air supply device, which is disposed on the second reaction shell and is capable of supplying air to the inner wall of the second reaction shell.

5. The continuous hydrogenation apparatus for metal powder according to claim 1, characterized in that: Both the first reaction shell and the second reaction shell include an upper cylindrical structure and a lower conical cylindrical structure.

6. The continuous hydrogenation apparatus for metal powder according to claim 1, characterized in that: The first heat exchange jacket is provided with a first heat exchange medium inlet and a first heat exchange medium outlet. The first heat exchange medium inlet is located on the bottom side of the first heat exchange jacket, and the first heat exchange medium outlet is located on the top side of the first heat exchange jacket. The second heat exchange jacket is provided with a second heat exchange medium inlet and a second heat exchange medium outlet. The second heat exchange medium inlet is located on the bottom side of the second heat exchange jacket, and the second heat exchange medium outlet is located on the top side of the second heat exchange jacket.

7. The continuous hydrogenation apparatus for metal powder according to claim 1, characterized in that: It also includes a metal powder inlet pipe, which is located at the metal powder inlet and outlet and is inclined, gradually approaching the airflow distribution plate from high to low.

8. The continuous hydrogenation apparatus for metal powder according to claim 1, characterized in that: A discharge valve is provided at the discharge port, and the opening degree of the discharge valve can be adjusted.

9. The continuous hydrogenation apparatus for metal powder according to claim 1, characterized in that: It also includes an oxygen content detector, a pressure sensor, and a safety valve. The oxygen content detector, the pressure sensor, and the safety valve are all installed on the connecting pipe. The safety valve is used for emergency venting.

10. The continuous hydrogenation apparatus for metal powder according to claim 1, characterized in that: It also includes a temperature monitoring device, which is installed on the connecting pipe and is used to monitor the temperature.

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