System for continuous hydrogenation refining of metal powder

Abstract

The invention relates to the technical field of metal hydrogenation, and discloses a metal powder continuous hydrogenation refining system which comprises a continuous hydrogenation reaction device, a pressure relief separation device and a gas supply mechanism. Metal powder enters the vertical reactor from the side wall feeding pipe and is subjected to hydrogenation reaction and pre-crushing under heat management of ascending airflow lifting and outer wall temperature control, and generated hydrogenated powder enters the pressure relief separation device along with airflow through the discharging pipe. And after gas-solid separation, powder is temporarily stored, and tail gas is treated and recycled back to the reactor. Hydrogen and powder continuously flow to react, the reaction efficiency is improved, and the time is shortened; through the combination of heat management and heat convection of unreacted hydrogen, the reaction temperature can be guaranteed, reaction heat can be conducted out in time, caking or melting caused by local overheating is prevented, and the product quality is guaranteed.

Description

Technical Field

[0001] This solution relates to the field of metal hydrogenation technology, specifically to a system for the continuous hydrogenation and refinement of metal powder. Background Technology

[0002] Hydrogen energy is an abundant secondary energy source with a wide range of applications. It boasts advantages such as high energy density, versatility, zero pollution, non-toxicity, abundant reserves, and environmental compatibility, making it an ideal secondary energy carrier to complement primary energy sources and poised to play a significant role in replacing fossil fuels. The entire hydrogen energy industry chain comprises three key links: hydrogen production, hydrogen storage and transportation, and hydrogen utilization. High-density hydrogen storage and transportation serves as the bridge between hydrogen production and application, and is also a bottleneck restricting the global and national hydrogen energy development strategy. Hydrogen storage technologies are mainly divided into cryogenic liquid hydrogen storage, high-pressure gaseous hydrogen storage, and solid-state material hydrogen storage. Solid-state metal hydrogen storage is currently the most reliable, safest, and most efficient hydrogen storage method.

[0003] Currently, solid-state metal hydrogen storage materials are mainly prepared through methods such as smelting, sintering, diffusion, and ball milling. For example, Chinese patent CN102583244B discloses a hydrogenation reaction method. This method involves placing processed metal powder in a reaction vessel, introducing hydrogen gas at the required pressure, heating the vessel to the desired temperature, and maintaining this temperature to allow the metal powder and hydrogen gas to react fully. Heating is then stopped to obtain the solid-state metal hydrogen storage material. However, this hydrogenation reaction method cannot be used for continuous preparation. Each preparation of solid-state metal hydrogen storage materials requires repeating the heating, reaction, cooling, and harvesting processes, resulting in high energy consumption. Summary of the Invention

[0004] The present invention aims to provide a system for continuous hydrogenation and refining of metal powders to continuously prepare solid metal hydrogen storage materials, thereby reducing the energy consumption in the preparation of solid metal hydrogen storage materials.

[0005] To achieve the above objectives, the present invention adopts the following technical solution: a system for continuous hydrogenation and refining of metal powder, characterized in that: it includes a continuous hydrogenation reaction device, a pressure relief and separation device, and a gas supply mechanism; the continuous hydrogenation reaction device includes a reactor body and a reaction heat management device; the reactor body is vertically arranged and has an inlet and a outlet pipe; the inlet includes an inlet pipe and an outlet pipe; the inlet pipe is located on the side wall of the reactor body and can transport metal powder into the reactor body through the inlet pipe; the reaction gas is continuously input into the reactor body through the outlet pipe and discharged through the outlet pipe, forming an upward airflow; the reaction heat management device includes a reaction heat exchanger and part of the upward airflow; the reaction heat exchanger is located on the outer wall of the reactor body and can perform thermal management of the reactor body; the metal powder enters through the inlet pipe. In the hydrogenation reaction zone, the hydrogenation reaction and pre-crushing occur under the support of the rising gas flow and the thermal management of the reaction heat exchanger. Further refinement is then carried out at the top of the reactor to obtain hydrogenated metal powder of the desired particle size. The hydrogenated metal powder, carried by the rising gas flow, enters the pressure relief separation device through the discharge pipe. The pressure relief separation device includes a gas-solid separation unit and a storage chamber. The gas-solid separation unit performs gas-solid separation on the refined hydrogenated metal powder, obtaining tail gas and hydrogenated metal powder. The gas supply mechanism includes a tail gas inlet and a gas supply outlet. The tail gas inlet is connected to the gas-solid separation unit, and the gas supply outlet is connected to the inlet pipe and continuously supplies reaction gas. The tail gas enters the gas supply mechanism through the tail gas inlet for tail gas treatment and then returns to the reactor body through the gas supply outlet. The hydrogenated metal powder enters the storage chamber for temporary storage.

[0006] The beneficial effects of this scheme are as follows: The continuous hydrogenation reaction and heat exchange process in the continuous hydrogenation reactor for metal powder allows metal powder to continuously enter the reactor body for hydrogenation reaction. After the hydrogenated metal is refined, it is discharged through the discharge pipe. During the process, both hydrogen and metal powder are in a flowing state, allowing the hydrogen to fully react with the metal powder, which can effectively shorten the hydrogenation reaction time. At the same time, by setting up a thermal energy management device in the hydrogenation reaction zone of the reactor body, the thermal energy management device is used to control the heat exchange temperature in the hydrogenation reaction zone. Meanwhile, the unreacted hydrogen in the hydrogenation reaction zone undergoes convective heat exchange with the metal powder. The combination of these two heat exchange methods can effectively provide sufficient reaction temperature conditions, preventing insufficient reaction temperature from affecting reaction efficiency and hydrogenation effect. At the same time, the heat generated by the hydrogenation reaction is removed by convective heat exchange, thereby avoiding local high temperatures caused by the exothermic hydrogenation reaction, which could lead to metal powder agglomeration and melting, affecting product quality.

[0007] Furthermore, the continuous hydrogenation reactor also includes a refining mechanism, which includes a refining nozzle. The refining nozzle is fixed on the side wall between the feed inlet and the discharge pipe and is connected to the exhaust port.

[0008] Beneficial effects: By refining the nozzle settings, when the hydride metal powder rises under the influence of the rising airflow and reaches the height of the refining nozzle, the hydride metal powder accelerates and collides away from the refining nozzle due to the interference of the airflow accelerated by the refining nozzle, which further reduces the particle size of the hydride metal.

[0009] Furthermore, the gas-solid separation unit includes a separation chamber and a first intermediate chamber. The gas-solid separation chamber is provided with a first inlet / outlet, a second inlet / outlet, and a third inlet / outlet. The first inlet / outlet is connected to a discharge pipe, the second inlet / outlet is connected to a tail gas inlet, and the third inlet / outlet is connected to the first intermediate chamber. A valve is provided between the third inlet / outlet and the first intermediate chamber. The first intermediate chamber is provided with a pressurizing pipe and a pressure relief pipe. The gas supply mechanism also includes a gas supply unit, which includes a gas source capable of outputting reaction gas at a specific pressure. The pressurizing pipe is connected to the gas source. The pressure relief separation device also includes a pressure relief separation unit, which is located between the gas source and the pressure relief pipe and can replenish the gas discharged from the pressure relief pipe to the gas source.

[0010] Furthermore, the pressure relief separation unit includes a pressure relief separation chamber and a second intermediate chamber. The pressure relief separation chamber is also provided with a first inlet / outlet, a second inlet / outlet, and a third inlet / outlet. The first inlet / outlet is connected to the pressure relief pipe, the second inlet / outlet is connected to the air source, and the third inlet / outlet is connected to the second intermediate chamber. The first intermediate chamber and the second intermediate chamber are respectively provided with discharge valves. The storage chamber includes a first finished product chamber and a second finished product chamber. The first finished product chamber and the second finished product chamber are respectively connected to the first intermediate chamber and the second intermediate chamber through discharge valves.

[0011] Furthermore, the gas supply mechanism also includes a gas supply unit, which includes an intake heater and a pressurization module. The intake heater is located between the gas supply port and the pressurization module and is connected to the gas supply port and the gas outlet of the pressurization module, respectively. The pressurization module includes at least two sets of gas compressors that operate alternately. The intake ends of the two sets of gas compressors are respectively equipped with filters and are connected to the exhaust gas intake port through the filters.

[0012] Furthermore, the gas supply mechanism also includes a displacement unit, which is capable of continuously outputting inert gas. The displacement unit is connected to the first intermediate chamber and the air inlet of the pressurization module.

[0013] Furthermore, it also includes a first heat exchanger and a heat storage device. The first heat exchanger includes a mass transfer chamber and a heat transfer chamber. The gas outlet pipe of the reactor body is connected to a tail gas pipe. The mass transfer chamber is connected to the tail gas pipe. The heat transfer chamber is circulated with a heat exchange medium and can exchange heat with the tail gas in the mass transfer chamber through the flow of the heat exchange medium. Several reaction heat exchangers and the first heat exchanger form a waste heat recovery unit. The waste heat recovery unit is connected to the heat storage device, and the heat energy released by the hydrogenation reaction is transferred to the heat storage device through the waste heat recovery unit.

[0014] Furthermore, the waste heat recovery unit also includes a second heat exchanger, which is located between the outlet pipe and the first heat exchanger and can preheat the gas entering the inlet pipe.

[0015] Furthermore, it also includes a waste heat utilization module, which includes a third heat exchanger and several heat users. The third heat exchanger is located between the heat storage device and the heat users and can transfer heat energy between the heat storage device and the heat users.

[0016] Furthermore, it also includes a waste heat utilization module, which includes a power generation unit. The power generation unit includes a steam turbine and a generator. The generator is connected to the first heat exchanger through the steam turbine and can use the heat energy in the exhaust gas to generate electricity through the first heat exchanger. Attached Figure Description

[0017] Figure 1 This is a schematic diagram showing the connection relationship of the functional units in an embodiment of the present invention; Figure 2 This is a schematic diagram of the pipeline connection in Embodiment 1 of the present invention; Figure 3 This is a schematic diagram of the pipeline connection between the heat utilization module and the waste heat recovery unit in Embodiment 2 of the present invention; Figure 4 This is a schematic diagram of pipeline connection in Embodiment 3 of the present invention; Figure 5 This is a schematic diagram of the pipeline connection between the heat utilization module and the waste heat recovery unit in Embodiment 3 of the present invention; Figure 6 This is a schematic diagram of the pipeline connection between the heat utilization module and the waste heat recovery unit in Embodiment 4 of the present invention; Figure 7 This is a schematic diagram of the pipeline connection between the heat utilization module and the waste heat recovery unit in Embodiment 5 of the present invention.

[0018] The reference numerals in the accompanying drawings include: continuous hydrogenation reactor 100, inlet pipe 111, outlet pipe 112, feed pipe 113, main pipe 114, refining nozzle 115, airflow dispersion plate 116, pressure relief separation device 200, gas-solid separation unit 210, gas-solid separation chamber 211, first intermediate chamber 212, first finished product chamber 213, pressure relief separation unit 220, pressure relief separation chamber 221, second intermediate chamber 222, second finished product chamber 223, waste heat recovery unit 300, reaction heat exchanger 310, first heat exchanger 320, second heat exchanger 330, gas supply mechanism 400, and hydrogen storage tank 410. 411, 412, 420, 421, 430, 431, 432, 440, 500, 501, 502, 503, 510, 520, 521, 522, 530, 541, 542, 543, 544, 545, 546, 547, 548, 548. Detailed Implementation

[0019] Example 1 Example 1 is basically as shown in the appendix. Figure 1-2 As shown, Figure 1-2 The system shown includes a gas supply mechanism 400, a continuous hydrogenation reactor 100, a pressure relief and separation device 200, and a waste heat management mechanism. Connecting pipelines are provided between the gas supply mechanism 400, the continuous hydrogenation reactor 100, the pressure relief and separation device 200, and the waste heat management mechanism. In operation, the gas supply mechanism 400 supplies reaction gas to the continuous hydrogenation reactor 100. The metal powder enters the continuous hydrogenation reactor 100 and undergoes hydrogenation and refinement using the hydrogen supplied by the gas supply mechanism 400. The refined metal powder then enters the pressure relief and separation device 200, where the gas and solid are separated. The gas after gas-solid separation enters the waste heat management mechanism, where it is cooled before returning to the gas supply mechanism 400, forming a closed loop.

[0020] The gas supply mechanism 400 includes a stamping unit, a gas supply unit, and a displacement unit. The stamping unit and the gas supply unit are used to output reaction gas at a specific pressure, and the output ends of the stamping unit and the gas supply unit are connected to each other to form a gas supply port. The displacement unit is used to output inert gas to replace the gas in the system, thereby reducing the hydrogen concentration in the system and ensuring the safety of the system after shutdown.

[0021] Specifically, such as Figure 2As shown, the stamping unit includes a hydrogen storage tank 410, a stamping compressor 411, and a stamping pipe. The hydrogen storage tank 410 stores hydrogen and is connected to a hydrogen supply pipe and a pressure relief inlet pipe via valves. It is also connected to the stamping compressor 411 via valves. The outlet of the stamping compressor 411 is connected to the stamping pipe. The inlet of the gas supply compressor is connected to the gas supply pipe via a flange, and the outlet of the stamping compressor 411 is connected to the gas supply port. In use, hydrogen enters the hydrogen storage tank 410 through the hydrogen supply pipe or the pressure relief inlet pipe, and is output after being compressed by the gas supply compressor.

[0022] The gas supply unit includes a pressurization module 430 and an intake heater 440. Both the pressurization module 430 and the intake heater 440 have an intake end and an outlet end. The intake end of the pressurization module 430 is connected to a tailpipe, and the free end of the tailpipe is the tail gas inlet. The outlet end of the pressurization module 430 is connected to the intake end of the intake heater 440. The pressurization module 430 includes at least two sets of alternately operating intake compressors 431. The intake ends of the two sets of intake compressors 431 are respectively provided with intake filters 432, and the inlets of the intake filters 432 are connected to the tail gas inlets. The intake heater 440 is disposed between the outlet end and the supply end of the pressurization module 430. In this embodiment, the pressurization module 430 includes two sets of intake compressors 431, which are arranged in parallel and operate alternately to ensure the stability of the output gas.

[0023] The replacement unit includes a replacement storage tank 420, a replacement pipe, and a vent pipe. The replacement storage tank 420 stores inert gas and is connected to a gas supply pipe via a valve. The replacement pipe is connected to the replacement storage tank 420, and the vent pipe is connected to the replacement pipe. The vent pipe is equipped with a vent port 421, which is open to the atmosphere. In use, the inert gas enters the replacement storage tank 420 through the inert gas supply pipe and exits through the replacement pipe. Hydrogen gas is discharged into the atmosphere through the vent pipe and vent port 421. This allows for hydrogen replacement during system shutdown, maintenance, or malfunction, ensuring system safety.

[0024] The continuous hydrogenation reactor 100 includes a reactor body, which is a vertically arranged cylindrical container divided vertically into a hydrogenation zone, a transition zone, and a refining zone. A reaction heat exchanger 310 is fixed to the outer wall of the hydrogenation zone. An airflow dispersion plate 116 and an inlet pipe 111 are welded to the lower part of the hydrogenation zone. The airflow dispersion plate 116 is welded to the inner wall of the cylindrical container and located below the hydrogenation zone. The inlet pipe 111 is located below the airflow dispersion plate 116. A feed pipe 113 is welded to the transition zone. A refining drive assembly is fixedly installed in the refining zone. The refining drive assembly includes several refining nozzles 115. Several through holes are provided on the side wall of the refining zone. The outer wall of the nozzles is welded to the through holes to form a sealed connection. A main pipe 114 connects the refining nozzles 115. Both the inlet pipe 111 and the main pipe 114 are connected to a gas supply port. A portion of the hydrogen output from the gas supply port flows into the reactor body through the gas inlet pipe 111. After being dispersed by the airflow dispersion plate 116, it flows sequentially through the hydrogenation zone, the transition zone, and the refining zone, and finally flows out through the gas outlet pipe 112, forming an upward airflow. Another portion of the hydrogen output from the gas supply port enters the refining nozzle 115 through the main pipe 114. After being accelerated by the refining nozzle 115, it is injected into the reactor body.

[0025] The pressure relief separation device 200 includes a pressure relief pipe, a gas-solid separation unit 210, and a pressure relief separation unit 220. The pressure relief pipe is disposed between the gas-solid separation unit 210 and the pressure relief separation unit 220, and the gas-solid separation unit 210 and the pressure relief separation unit 220 are connected by a valve. Specifically, the gas-solid separation unit 210 includes a gas-solid separation chamber 211, a first intermediate chamber 212, a first finished product chamber 213, and a pressure relief pipe. The gas-solid separation chamber 211 is used to separate gas and solid substances. The first finished product chamber 213 is used to store the solid powder separated by the gas-solid separation chamber 211. The first intermediate chamber 212 is disposed between the gas-solid separation chamber 211 and the gas-solid separation unit 220. The first finished product silo 213 is connected to the stamping pipe and the pressure relief pipe respectively through valves, so as to switch between high pressure and low pressure states through the pressure relief pipe and the stamping pipe. In this embodiment, the gas-solid separation chamber 211 is provided with a first inlet and outlet, a second inlet and outlet and a third inlet and outlet. The first inlet and outlet is the material inlet, the second inlet and outlet is the gas outlet and the third inlet and outlet is the solid material outlet. A filter element is provided between the second inlet and outlet and the first inlet and outlet and the third inlet and outlet. The filter element enables the gas-solid separation of the airflow carrying solid particles. The gas is output from the second inlet and outlet and the solid is output from the third inlet and outlet. The first intermediate chamber 212 includes a chamber body with an inlet and an outlet, and is connected to a pressure relief pipe, a stamping pipe, a venting pipe, and a replacement pipe. The chamber body is connected to the pressure relief separation device 200 and the finished product chamber through the inlet and outlet, and is connected to the pressure relief separation unit 220 and the stamping unit through the pressure relief pipe and the stamping pipe, respectively. Through the cooperation of the stamping unit and the pressure relief separation unit 220, the chamber body is switched between high pressure and low pressure, thereby facilitating the transfer of hydride metal powder from the high pressure area to the low pressure first finished product chamber 213. The second inlet and outlet are connected to the first inlet and outlet of the pressure relief separation device 200. After being filtered by the filter element of the pressure relief separation device 200 of the pressure relief separation unit 220, the powder is discharged into the hydrogen storage tank 410. When production needs to be stopped, the hydrogen in the chamber body can be replaced through the venting pipe and the replacement pipe.

[0026] The pressure relief separation unit 220 includes a pressure relief separation chamber 221, a second intermediate chamber 222, and a second finished product chamber 223. The pressure relief separation chamber 221 has a structure that is basically the same as that of the gas-solid separation chamber 211, and will not be described in detail here. The second intermediate chamber 222 is basically the same as that of the first intermediate chamber 212, except that the second intermediate chamber 222 is only provided with an inlet and an outlet, and is connected to the replacement pipe and the vent pipe through valves. The chamber body connects the pressure relief separation device 200 to the finished product chamber through the inlet and outlet, and uses the replacement pipe and the vent pipe to discharge the hydrogen in the chamber. The second finished product chamber 223 is located on the outlet of the second intermediate chamber 222.

[0027] Specifically, the filter element can be made of non-metallic, metallic, or other materials depending on the system's operational requirements. In this embodiment, the filter element is a cylindrical filter bag. During installation, the two ends of the cylindrical filter bag are fixed between the first inlet / outlet and the third inlet / outlet, respectively. The filter bag isolates the second inlet / outlet from the first and third inlet / outlet. The metal hydride enters the intermediate chamber under the obstruction and guidance of the filter bag, while the gas passes through the filter bag and enters the second inlet / outlet, thereby separating the solid and gaseous materials.

[0028] The waste heat management system includes a waste heat recovery unit 300. Several first heat exchangers 320 and second heat exchangers 330 are installed on the exhaust pipe. The reaction heat exchanger 310, the first heat exchangers 320 and the second heat exchangers 330 constitute the waste heat recovery unit 300. The waste heat recovery unit 300 also includes a heat transfer medium. The heat transfer medium is used to flow between the reaction heat exchanger 310, the first heat exchangers 320 and the second heat exchangers 330 and the exhaust pipe, and the heat energy in the exhaust gas is controlled by the flow of the heat transfer medium. In this embodiment, the type of heat transfer medium is not limited. The heat transfer medium can be air, hydrogen, inert gas, water, heat transfer oil or other heat transfer media.

[0029] Both the first heat exchanger 320 and the second heat exchanger 330 include a shell and heat exchange pipes. The shell is mounted on the pipe wall and is made of low-carbon alloy steel (such as 304 stainless steel) to meet the heat exchange environment of pressure 1~6MPa and temperature 50~500℃. The heat exchange medium flows in the heat exchange cavity between the pipe wall and the shell, thereby transferring heat energy between the exhaust gas or rising airflow and the heat exchange medium through indirect heat exchange. The heat exchange pipes are connected to the exhaust gas circulation pipe to form a mass transfer cavity, and the inner wall of the shell and the outer wall of the heat exchange pipes form a heat transfer cavity. The heat transfer cavity is provided with a heat exchange medium inlet and a heat exchange medium outlet. The heat exchange medium flows into the heat exchange cavity through the heat exchange medium inlet and flows out through the heat exchange medium outlet to control the heat energy in the exhaust gas. Specifically, as shown in the figure... Figure 1 As shown, the mass transfer chambers of both the first heat exchanger 320 and the second heat exchanger 330 are connected to the tail gas pipe. The heat transfer medium flows in the heat transfer chamber and transfers heat to the tail gas through the outer wall of the mass transfer chamber, thereby reducing the temperature of the tail gas. The difference is that the purpose of the heat transfer medium flowing in the heat transfer chamber of the first heat exchanger 320 is to reduce the temperature of the tail gas, thereby reducing the difficulty of the pressurization unit to compress the tail gas. The heat transfer medium flowing in the heat transfer chamber of the second heat exchanger 330 is the gas output from the pressurization unit. The purpose is to use the tail gas flowing through the second heat exchanger 330 to preheat the gas output from the pressurization unit, thereby reducing the energy consumption when the subsequent intake heater 440 heats the gas, and allowing the heat energy output from the reactor body to return to the reactor body, reducing the input of external energy during the hydrogenation and refining process, and thus improving the thermal efficiency of the system.

[0030] During production, firstly, the outer wall of the hydrogenation zone is thermally managed by the reaction heat exchanger 310, maintaining the hydrogenation zone at the reaction temperature. Simultaneously, a portion of the reaction gas output from the gas supply port enters the reactor body through the inlet pipe 111, is dispersed by the dispersion plate, and is discharged through the exhaust port, forming an upward airflow. Subsequently, metal powder enters the reactor body through the feed pipe 113 and, under the influence of the upward airflow, passes through the temperature zone to reach the hydrogenation zone, where it undergoes hydrogenation and pre-crushing. Specifically, larger metal powder particles enter the reactor body through the solid feed port and, driven by the upward airflow, decelerate and fall into the hydrogenation reaction zone, where they undergo hydrogenation. During the hydrogenation reaction, hydrogen reacts with the larger metal powder particles, forming hydrogenated metal on the particle surface. The hydrogenation layer slows down the internal hydrogenation. Meanwhile, because the surface of the hydrogenated metal particles is easier to crush, the metal powders in the hydrogenation reaction zone constantly collide and peel off the surface hydrogenated metal, thereby accelerating the hydrogenation reaction process and forming smaller hydrogenated metal powders. The larger metal powders that are not internally hydrogenated continue to undergo hydrogenation and pre-crushing processes in the reaction zone. The hydrogenated metal powders that have completed the reaction are carried into the refining zone of the reactor body by the rising airflow. During the process, both hydrogen and metal powders are in a flowing state, which allows hydrogen to fully react with metal powders, thereby effectively shortening the hydrogenation reaction time. At the same time, the part of the rising airflow that does not participate in the hydrogenation reaction passes through the hydrogenation zone and uses convection heat transfer to carry away the heat energy released by the hydrogenation reaction, so as to avoid local overheating.

[0031] After the hydrogenation reaction and pre-crushing are completed, the particles that have completed the hydrogenation reaction and pre-crushing are carried by the rising airflow through the decomposition zone to the refining zone. Another part of the hydrogen output from the gas supply port flows into the refining nozzle 115 through the main pipe 114. The gas is accelerated by the nozzle and injected into the refining zone to accelerate the metal powder in the refining zone. The accelerated powder collides and refines at the intersection of each nozzle. Powder that does not meet the particle size requirements returns to the refining zone through the side wall and continues to be refined under the drive of the accelerating airflow. The hydrogenated metal powder with the complex particle size is carried by the rising airflow and discharged through the gas outlet, entering the gas-solid separation unit 210. Under the action of the gas-solid separation chamber 211, gas-solid separation is carried out. The solid hydrogenated metal powder is temporarily stored in the gas-solid separation chamber 211. The gas enters the tail gas pipe through the tail gas inlet. After being pressurized by the pressurization module 430 and heated by the heater, it returns to the hydrogenation reactor body through the gas supply port.

[0032] When a certain amount of solid powder is filled in the gas-solid separation chamber 211 and unloading is required, the stamping unit stamps the first intermediate chamber 212 through the stamping pipe until the pressure in the first intermediate chamber 212 is equal to the pressure in the gas-solid separation chamber 211. Then, the valve between the first intermediate chamber 212 and the gas-solid separation chamber 211 is opened, allowing the hydride metal powder in the gas-solid separation chamber 211 to enter the first intermediate chamber 212. Subsequently, the valve between the inlet of the first intermediate chamber 212 and the outlet of the pressure relief separation device 200 is closed, and the pressure relief pipe valve is opened. The first intermediate chamber 212 is connected to the pressure relief separation unit 220 through the pressure relief pipe until the pressure in the first intermediate chamber 212 is equal to the pressure in the first finished product chamber 213. Then, the unloading valve is opened to unload the hydride metal powder in the first intermediate chamber 212 into the first finished product chamber 213.

[0033] Before shutdown or maintenance, the hydrogen in the reactor body, pipelines, and separation unit is discharged through the vent pipe using the inert gas stored in the inert gas storage tank to reduce the hydrogen concentration in the system and thus ensure system safety; or it is used to replace the residual hydrogen in the first intermediate chamber 212 or the second intermediate chamber 222 to ensure continuous system operation. Specifically, after the intermediate chamber is depressurized, the hydrogen in the first intermediate chamber 212 can be replaced by the replacement pipe and the vent pipe to ensure safe system operation.

[0034] Example 2 Based on Example 1, such as Figure 3 As shown, the waste heat management mechanism also includes a waste heat utilization module 500. The waste heat utilization module 500 includes a heat storage component 520 and a heat utilization unit. The heat storage component 520 is disposed between the waste heat recovery unit and the heat utilization unit, which is composed of several reaction heat exchangers 310 and a first heat exchanger 320. It is connected to the reaction heat exchanger 310, the first heat exchanger 320 and the heat utilization unit respectively. Thus, the heat energy of the reaction heat exchanger 310, the first heat exchanger 320, the heat storage component 520 and the heat utilization unit is connected through the flow of the heat exchange medium. The heat energy absorbed by the reaction heat exchanger 310 and the first heat exchanger 320 is transferred to the heat utilization unit through the heat storage component.

[0035] The heat utilization unit includes a third heat exchanger 510 and a heat transfer medium. The third heat exchanger 510 is connected to several heat users 530. A heat circulation pump 503 is installed between the third heat exchanger 510 and the heat users 530. Under the action of the heat circulation pump 503, the heat transfer medium circulates between the heat users 530 and the third heat exchanger 510.

[0036] In this embodiment, the heat storage device 520 is a molten salt storage tank, the heat exchange medium is a molten salt storage tank, and the heat transfer medium is water. Specifically, the molten salt storage tank is provided with two sets of discharge ports and discharge ports. The two discharge ports are respectively provided with a first molten salt pump 501 and a second molten salt pump 502. The first molten salt pump 501 is located between the first heat exchanger 320 and the heat storage device 520, and the second molten salt pump 502 is located between the third heat exchanger 510 and the heat storage device 520.

[0037] During operation, the heat exchange medium in the heat storage device 520 is transported to the first heat exchanger 320 by the first molten salt pump 501 to absorb the heat generated by the hydrogenation reaction, and then enters the heat storage device 520 for temporary storage, which causes the heat exchange medium in the heat storage device 520 to heat up. This scheme utilizes the characteristic of molten salt heat storage time to achieve a heat storage capacity of more than 10 hours per day.

[0038] When heat user 530 needs to use heat energy, the heat exchange medium temporarily stored in the heat storage unit 520 is transported to the third heat exchanger by the second molten salt pump 502, where it releases heat and then returns to the molten salt storage tank. Under the action of the heat circulation pump 503, the heat transfer medium circulating in the third heat exchanger absorbs the heat stored in the molten salt and transfers this heat to other heat users 530 for use.

[0039] Furthermore, to increase the venting speed of the pressure relief pipe, such as... Figure 2 As shown, a pressure relief compressor 412 is installed between the pressure relief separation chamber 221 and the hydrogen storage tank 410. When depressurizing, the pressure relief compressor 412 is started, and the hydrogen in the first intermediate chamber 212 is forced into the hydrogen storage tank 410 through the pressure relief pipe to improve the exhaust efficiency of the pressure relief pipe and increase the unloading speed.

[0040] Example 3 Based on Example 2, such as Figure 4 As shown, the gas-solid separation mechanism includes multiple gas-solid separation units 210. The gas-solid separation chambers 211 of adjacent gas-solid separation units 210 are connected in series, and the filter holes of the separation element in the gas-solid separation chamber 211 are progressively smaller, thereby directly classifying the particle size of the hydride metal powder during the production process to improve the uniformity of the product. At the same time, a balance pipe is provided between adjacent first intermediate chambers 212, and a valve is provided in the middle of the balance pipe. During stamping, the valve in the middle of the balance pipe is opened, and the hydrogen in the hydrogen storage tank 410 is compressed by the stamping compressor 411 and injected into the first intermediate chamber 212 through the stamping pipe, so that multiple first intermediate chambers 212 reach the required pressure simultaneously, reducing the stamping time.

[0041] In addition, to broaden the applicability of the waste heat utilization module 500 and increase the heat storage temperature of the heat storage component 520, such as... Figure 5As shown, the heat storage device 520 includes a first storage chamber 521 and a second storage chamber 522. The first storage chamber 521 and the second storage chamber 522 are respectively disposed between the first heat exchanger 320 and the third heat exchanger 510, and perform heat transfer circulation between the first heat exchanger 320 and the third heat exchanger 510. Specifically, the first storage chamber 521 and the second storage chamber 522 are respectively provided with an inlet and an outlet. A first molten salt pump 501 is provided at the outlet of the second storage chamber 522, which can transport the heat transfer medium temporarily stored in the second storage chamber 522 to the first heat exchanger 320 for heat absorption, and then transport it to the first storage chamber 521. A second molten salt pump 502 is provided at the outlet of the first storage chamber 521, which can transport the heat transfer medium temporarily stored in the first storage chamber 521 to the third heat exchanger 510 for heat release, and then transport it to the second heat exchange chamber.

[0042] By dividing the heat storage component 520 into an independently configured first storage chamber 521 and a second storage chamber 522, the heat transfer medium with higher temperature and the heat transfer medium with lower temperature are transferred through the first storage chamber 521 and the second storage chamber 522 respectively. After absorbing heat energy, the heat transfer medium with higher temperature is temporarily stored in the first storage chamber 521, and after releasing heat energy, the heat transfer medium with lower temperature is temporarily stored in the second storage chamber 522. This avoids the overall temperature of the molten salt in the heat storage component 520 from decreasing when supplying a large amount of heat, which would affect the temperature stability of the continuous heating supply to the heat user 530. This makes it suitable for heating requirements in fields with strong heat demand such as large-area heating, industrial steam supply, and power generation.

[0043] Example 4 Based on Example 1, such as Figure 6 As shown, the waste heat management structure also includes a waste heat utilization module 500. The waste heat utilization module 500 includes a power generation component, which includes a steam turbine 541, a generator 542, and a condensation component. The steam turbine 541 includes a rotor and a steam generator. The steam generator is connected to the first heat exchanger 320 and can use the heat collected by the first heat exchanger 320 to generate high-pressure steam. The high-pressure steam drives the rotor to rotate and does work on the generator 542, thereby generating electricity using the heat energy collected by the waste heat recovery unit 300. The output end of the generator 542 is connected to an electrolytic water hydrogen production device 544. A transformer 543 is installed between the generator 542 and the electrolytic water hydrogen production device 544. The transformer 543 converts the power output by the generator 542 into direct current to power the electrolytic water hydrogen production device 544 to produce hydrogen. The electrolytic water hydrogen production device 544 then produces hydrogen and supplies it to the gas supply mechanism 400. After being pressurized and heated by the gas supply mechanism 400, the hydrogen is transported to the reactor body for use, thereby achieving partial self-supply of raw materials and reducing the cost of raw material procurement.

[0044] The condensing assembly includes a condenser 545, a cooling tower 546, and a feedwater pump. The condenser 545 is connected to the steam turbine 541. The cooling tower 546 contains cooling water. The feedwater pump is located between the condenser 545 and the cooling tower 546 and can drive the cooling water to circulate between the cooling tower 546 and the condenser 545. This allows the cooling water to cool the heat transfer medium after it has completed its work, thereby increasing the temperature difference between the heat transfer medium and the exhaust gas and improving the efficiency of waste heat recovery.

[0045] During power generation, the heat exchange medium absorbs the heat generated by the hydrogenation reaction through the second heat exchanger 330, and then enters the steam turbine 541 through a pipeline to drive the generator 542 to perform work, converting the heat absorbed by the heat exchange medium into electrical energy through the generator 542. After being processed by the steam turbine 541 and cooled by the condenser 545, the heat exchange medium returns to the first heat exchanger 320 to continue absorbing the heat generated by the hydrogenation reaction.

[0046] Example 5 Based on Example 4, such as Figure 7 As shown, to further improve thermal energy utilization efficiency, the power generation assembly also includes a medium heater 548 and a deaerator 547. The deaerator includes an inlet, an outlet, and a heating port. The inlet is connected to the heater, the outlet is connected to the first heat exchanger 320, and the deaerator heating port is connected to the steam turbine 541 to enhance the steam utilization efficiency of the steam turbine 541.

[0047] After the heat exchange medium is cooled by the condenser 545, it enters the medium heater 548 for heating, so that the heat exchange medium maintains a certain temperature. After being heated by the medium heater 548, it enters the deaerator 547 for deoxygenation, and then returns to the thermal energy management system to continue to absorb the heat generated by the hydrogenation reaction.

[0048] The above descriptions are merely embodiments of the present invention, and common knowledge such as specific technical solutions and / or characteristics are not described in detail here. It should be noted that the technical means for solving problems in the above embodiments of the present invention can be used in combination to solve multiple technical problems simultaneously. For those skilled in the art, several modifications and improvements can be made without departing from the technical solutions of the present invention, and these should also be considered within the scope of protection of the present invention. These modifications and improvements will not affect the effectiveness of the implementation of the present invention or the practicality of the patent. The scope of protection claimed in this application should be determined by the content of its claims, and the specific embodiments described in the specification can be used to interpret the content of the claims.

Claims

1. A system for continuous hydrogenation and refining of metal powder, characterized in that: The system includes a continuous hydrogenation reactor, a pressure relief and separation device, and a gas supply mechanism. The continuous hydrogenation reactor comprises a reactor body and a reaction heat management device. The reactor body is vertically positioned and equipped with an inlet and a outlet pipe. The inlet includes a feed pipe and a gas inlet pipe. The feed pipe is located on the side wall of the reactor body and allows metal powder to be fed into the reactor body. Reaction gas is continuously input into the reactor body through the gas inlet pipe and discharged through the outlet pipe, forming an upward gas flow. The reaction heat management device includes a reaction heat exchanger and part of the upward gas flow. The reaction heat exchanger is located on the outer wall of the reactor body and performs thermal management of the reactor body. The metal powder enters the hydrogenation reaction zone through the feed pipe and is lifted by the upward gas flow and the reaction heat exchanger... Under thermal management, hydrogenation reaction and pre-crushing are carried out, and further refinement is performed at the top of the reactor to obtain hydride metal powder of the required particle size. The hydride metal powder is carried by the rising gas flow and enters the pressure relief separation device through the discharge pipe. The pressure relief separation device includes a gas-solid separation unit and a storage chamber. The gas-solid separation unit performs gas-solid separation on the hydride metal powder carrying the refined powder to obtain tail gas and hydride metal powder. The gas supply mechanism includes a tail gas inlet and a gas supply outlet. The tail gas inlet is connected to the gas-solid separation unit, and the gas supply outlet is connected to the inlet pipe and continuously supplies reaction gas. The tail gas enters the gas supply mechanism through the tail gas inlet for processing and then returns to the reactor body through the gas supply outlet. The hydride metal powder enters the storage chamber for temporary storage.

2. The system for continuous hydrogenation and refining of metal powder according to claim 1, characterized in that: The continuous hydrogenation reactor also includes a refining mechanism, which includes a refining nozzle fixed on the side wall between the feed inlet and the discharge pipe and connected to the exhaust port; it also includes a first heat exchanger and a heat storage unit. The first heat exchanger includes a mass transfer chamber and a heat transfer chamber. The reactor body's exhaust pipe is connected to a tail gas pipe. The mass transfer chamber is connected to the tail gas pipe. The heat transfer chamber circulates a heat exchange medium and can exchange heat with the tail gas in the mass transfer chamber through the flow of the heat exchange medium. Several reaction heat exchangers and the first heat exchanger form a waste heat recovery unit. The waste heat recovery unit is connected to the heat storage unit and transfers the heat energy released by the hydrogenation reaction to the heat storage unit through the waste heat recovery unit.

3. The system for continuous hydrogenation and refining of metal powder according to claim 2, characterized in that: The pressure relief separation device includes several gas-solid separation units. Each gas-solid separation unit includes a gas-solid separation chamber and a first intermediate chamber. The gas-solid separation chamber is provided with a first inlet / outlet, a second inlet / outlet, and a third inlet / outlet. The first inlet / outlet is connected to a discharge pipe, the second inlet / outlet is connected to a tail gas inlet, and the third inlet / outlet is connected to the first intermediate chamber. A valve is provided between the third inlet / outlet and the first intermediate chamber. A stamping pipe is connected to the first intermediate chamber. The gas-solid separation chambers of adjacent gas-solid separation units are connected in series, and a filter element with progressively smaller pore sizes is fixed inside the gas-solid separation chamber. The filter element isolates the third inlet / outlet from the first and second inlet / outlets. The gas supply mechanism also includes a stamping unit, which includes a gas source capable of outputting a reaction gas at a specific pressure. The stamping pipe is connected to the gas source. The pressure relief separation device also includes a pressure relief separation unit, which is located between the gas source and the pressure relief pipe and can replenish the gas discharged from the pressure relief pipe to the gas source.

4. The system for continuous hydrogenation and refining of metal powder according to claim 3, characterized in that: The pressure relief separation unit includes a pressure relief separation chamber and a second intermediate chamber. The pressure relief separation chamber is also provided with a first inlet / outlet, a second inlet / outlet, and a third inlet / outlet. The first inlet / outlet is connected to the pressure relief pipe, the second inlet / outlet is connected to the air source, and the third inlet / outlet is connected to the second intermediate chamber. The first intermediate chamber and the second intermediate chamber are respectively provided with discharge valves. The storage chamber includes a first finished product chamber and a second finished product chamber. The first finished product chamber and the second finished product chamber are respectively connected to the first intermediate chamber and the second intermediate chamber through discharge valves.

5. A system for continuous hydrogenation and refining of metal powder according to claim 4, characterized in that: The gas supply mechanism also includes a gas supply unit, which further includes a heater and a pressurization module. The heater is located between the gas supply port and the pressurization module and is connected to the gas supply port and the gas outlet of the pressurization module, respectively. The pressurization module includes at least two sets of gas compressors that operate alternately. The inlet end of each of the two sets of gas compressors is equipped with a filter and is connected to the exhaust gas inlet through the filter.

6. A system for continuous hydrogenation and refining of metal powder according to claim 5, characterized in that: The gas supply mechanism also includes a displacement unit, which is capable of continuously outputting inert gas. The displacement unit is connected to the first intermediate chamber and the air inlet of the pressurization module.

7. A system for continuous hydrogenation and refining of metal powder according to claim 6, characterized in that: The waste heat recovery unit also includes a second heat exchanger, which is located between the outlet pipe and the first heat exchanger and can preheat the gas entering the inlet pipe.

8. A system for continuous hydrogenation and refining of metal powder according to claim 7, characterized in that: It also includes a waste heat utilization module, which includes a third heat exchanger and several heat users. The third heat exchanger is located between the heat storage device and the heat users and can transfer the heat energy between the heat storage device and the heat users.

9. A system for continuous hydrogenation and refining of metal powder according to claim 7, characterized in that: It also includes a waste heat utilization module, which includes a power generation unit. The power generation unit includes a steam turbine and a generator. The generator is connected to the first heat exchanger through the steam turbine and can generate electricity by utilizing the heat energy in the exhaust gas through the first heat exchanger.

10. A system for continuous hydrogenation and refining of metal powder according to claim 1, characterized in that: The reaction gas is pure hydrogen or a mixture of hydrogen and inert gas at a pressure of 1-6 MPa and a temperature of 50-500℃; the metal powder material is an alloy powder or mixture powder with a particle size of less than 2000 μm, suitable for storing hydrogen, and the content of hydrogen storage metal in the alloy powder or mixture powder is greater than 70%; the hydrogen storage density of the hydride metal powder is 0~7.6 wt%.

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