Control method of metal powder continuous hydrogenation system

Abstract

The invention relates to the field of hydrogenated metal manufacturing equipment, and discloses a control method of a metal powder continuous hydrogenation system, which comprises the following steps: S1, introducing gas by a gas supply mechanism, and inputting reaction gas with the pressure of 1-6 MPa and the temperature of 50-500 DEG C to form upflow; s2, hydrogenation is conducted, metal powder with the particle size smaller than 2000 micrometers is put in, hydrogenation reaction is conducted under lifting of ascending airflow, meanwhile, a reaction heat exchanger is started to control the temperature, and the temperature needed by reaction is maintained; and S3, gas-solid separation is conducted, reaction products enter a separation device through a discharging pipe, hydrogenated powder and gas are separated, solids enter a finished product bin, and the gas is recycled after being treated. According to the method, gas-solid full contact is achieved through ascending gas flow, the reaction efficiency is improved, radiation and convection combined temperature control is achieved through the convection heat exchange synergistic effect of the reaction heat exchanger and unreacted gas, reaction heat is guided out in time, caking or melting caused by local overheating is prevented, and the product quality and the process stability are guaranteed.

Description

Technical Field

[0001] This solution relates to the field of hydrogenated metal manufacturing equipment, specifically to a control method for a continuous hydrogenation system for 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, storage and transportation, and hydrogen utilization. High-density hydrogen storage and transportation serve as the bridge between hydrogen production and application. 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 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 control method for a continuous hydrogenation system of metal powder 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 control method for a continuous hydrogenation system of metal powder, comprising the following steps: S1 gas supply, starting the gas supply mechanism, and continuously outputting a pressure of 1-6 through the gas supply mechanism. A reaction gas with a pressure of MPa and a temperature of 50-500℃ is introduced into the continuous hydrogenation reactor through the inlet pipe and discharged through the outlet pipe, forming an upward airflow. In S2 hydrogenation, metal powder with a particle size less than 2000μm is fed into the continuous hydrogenation reactor through the inlet pipe and undergoes hydrogenation under the support of the upward airflow, yielding hydrogenated metal powder. The hydrogenated metal powder moves upward under the support of the upward airflow and is discharged through the outlet pipe. Simultaneously, the reaction heat exchanger is activated to exchange heat in the hydrogenation reaction zone, maintaining the temperature within the continuous hydrogenation reactor within the required temperature range for the hydrogenation reaction. In S3 gas-solid separation, the hydrogenated metal powder and reaction gas discharged through the outlet pipe enter the gas-solid separation device, where gas-solid separation occurs, yielding solid hydrogenated metal powder and gas. The solid hydrogenated metal powder is temporarily stored in the finished product silo at atmospheric pressure after switching through the first intermediate chamber; the gas is returned to the continuous hydrogenation reactor via the gas supply mechanism.

[0006] The beneficial effects of this scheme are as follows: This scheme feeds metal powder with a particle size of less than 2000μm into a continuous hydrogenation reactor through a feed pipe, and continuously introduces reaction gas at a pressure of 1-6 MPa and a temperature of 50-500℃ from the bottom of the continuous hydrogenation reactor, and exhausts the reaction gas through an exhaust pipe. During the reaction, the metal powder undergoes hydrogenation under the action of the rising airflow, and the temperature of the reactor body is controlled by a reaction heat exchanger. At the same time, the rising airflow that does not participate in the reaction carries away the heat energy released by the hydrogenation reaction through convection heat transfer. The reaction heat exchanger and the rising airflow work together to form a thermal energy management device, which combines radiation heat transfer and convection heat transfer. This not only ensures the efficiency of the hydrogenation reaction, but also removes the heat of reaction in a timely manner to prevent problems such as agglomeration or melting caused by local overheating.

[0007] Furthermore, S2 hydrogenation also includes S21 refining. Before the hydrogenated metal powder is discharged, the reaction gas is accelerated through a refining nozzle and then injected into the continuous hydrogenation reaction device, causing the hydrogenated metal powder to collide with each other, thus reducing the particle size of the hydrogenated metal powder.

[0008] Furthermore, in the S3 gas-solid separation process, the gas-solid separation device includes a gas-solid separation chamber connected to a discharge pipe, and includes multiple separation chambers connected in series. Each separation chamber is independently connected to a first intermediate chamber. The first intermediate chamber is connected to a stamping pipe and a pressure relief pipe. The stamping pipe is connected to a stamping unit, and the pressure relief pipe is connected to a pressure relief unit. Valves are installed between the first intermediate chamber and the stamping pipe, the pressure relief pipe, the gas-solid separation chamber, and the finished product chamber. During unloading, the rising airflow discharged from the discharge pipe carries the hydride metal powder through the series of separation chambers in sequence. Each separation chamber is equipped with a filter element, and the filter pores of the filter element gradually decrease in size, thereby classifying the particle size of the hydride metal through the filter element, achieving a continuous classification effect of the hydride metal. Then, the valve between the stamping pipe and the first intermediate chamber is opened, and the reaction gas is supplied to the first intermediate chamber through the stamping unit. After the gas pressure in the first intermediate chamber is equal to that in the pressure relief separation chamber, the valve between the first intermediate chamber and the gas-solid separation chamber is opened, and the hydride metal powder separated in the gas-solid separation chamber is transferred to the first intermediate chamber. Then, the valve between the first intermediate chamber and the gas-solid separation chamber is closed, and the valve between the pressure relief pipe and the first intermediate chamber is opened. The reaction gas in the first intermediate chamber is discharged through the pressure relief unit, and the pressure in the first intermediate chamber is equal to that in the finished product chamber. Then, the valve between the first intermediate chamber and the finished product chamber is opened, and the hydride metal powder is continuously transferred to the finished product chamber, thereby achieving the effect of continuous collection of hydride metal powder with different particle size ranges.

[0009] Furthermore, it also includes S4 heat recovery. The continuous hydrogenation system for metal powder includes a heat recovery unit, which includes a first heat exchanger and a reaction heat exchanger. During the hydrogenation reaction, the heat energy released by the hydrogenation reaction is recovered through the heat exchange medium flowing in the first heat exchanger and the reaction heat exchanger.

[0010] Furthermore, it also includes S5 heat utilization. The continuous hydrogenation system for metal powder also includes a heat utilization module. The heat utilization module includes a heat storage device and several heat users. The heat storage device is located between the heat users and the reaction heat exchanger and the first heat exchanger, and connects the reaction heat exchanger and the first heat exchanger to the heat users.

[0011] Furthermore, it also includes S5 heat utilization. The continuous hydrogenation system for metal powder also includes a heat utilization module, which includes a steam turbine and a power generation component. The steam turbine is connected to the heat recovery unit and drives the power generation component to convert the heat energy absorbed by the heat recovery unit into electrical energy.

[0012] Furthermore, the gas supply mechanism 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. The stamping unit and the gas supply unit operate independently and their output ends are interconnected to form a gas supply port. The gas supply port is connected to the continuous hydrogenation reaction device, and the stamping unit is connected to the first intermediate chamber.

[0013] Furthermore, it also includes S4 replacement. The gas supply mechanism includes a replacement unit, which includes a replacement pipe and a vent pipe. The replacement pipe is connected to an inert gas. During maintenance or after the reaction is completed, the inert gas replaces the reaction gas in the hydrogenation system through the replacement pipe and discharges the reaction gas through the vent pipe. Attached Figure Description

[0014] Figure 1 This is a flowchart of an embodiment of the present invention; Figure 2 This is a schematic diagram showing the connection of the continuous hydrogenation reaction apparatus and the heat recovery unit in Embodiment 1 of the present invention; Figure 3 This is a schematic diagram of the gas-solid separation device according to Embodiment 2 of the present invention; Figure 4 This is a schematic diagram showing the connection between the heat recovery unit and the heat utilization module in Embodiment 2 of the present invention; Figure 5 This is a schematic diagram showing the connection between the heat recovery unit and the heat utilization module in Embodiment 3 of the present invention.

[0015] 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, heat recovery unit 300, reaction heat exchanger 310, first heat exchanger 320, second heat exchanger 330, and gas supply mechanism 40. 0. Hydrogen storage tank 410, pressurized compressor 411, depressurization compressor 412, displacement storage tank 420, vent 421, pressurization module 430, intake compressor 431, intake filter 432, intake heater 440, heat utilization module 500, first molten salt pump 501, second molten salt pump 502, heat circulation pump 503, third heat exchanger 510, heat storage unit 520, heat user 530, steam turbine 541, generator 542, transformer 543, hydrogen production unit 544, condenser 545, cooling tower 546, deaerator 547, medium heater 548. Detailed Implementation

[0016] Example 1 Example 1 is basically as shown in the appendix. Figure 1-2 As shown, Figure 1-2The control method of a continuous hydrogenation system for metal powder shown includes the following steps: S1. Gas supply is initiated, the gas supply mechanism 400 is started, and the gas supply mechanism 400 continuously outputs reaction gas with a pressure of 1-6 MPa and a temperature of 50-500℃, and the reaction gas is introduced into the continuous hydrogenation reaction device 100 through the gas inlet pipe 111 and discharged through the discharge pipe, forming an upward airflow, wherein, as Figure 2 , Figure 3 As shown, the gas supply mechanism 400 includes a gas supply unit, which includes a pressurization module 430 and an intake heater 440. The pressurization module 430 includes at least two sets of alternately operating intake compressors 431. The two sets of intake compressors 431 are arranged in parallel and operate alternately to ensure the stability of the output gas. Specifically, the intake ends of the two sets of intake compressors 431 are respectively provided with intake filters 432, and the intake ports of the intake filters 432 are connected to the exhaust gas inlet. The intake heater 440 is located between the outlet end of the pressurization module 430 and the gas supply port. During operation, hydrogen is input from the intake end of the pressurization module 430, filtered by the intake filter 432, and then enters the intake compressor 431 for compression, so that the hydrogen pressure reaches 1-61-6 MPa. After compression, it is input into the continuous hydrogenation reaction device 100 through the intake heater 440 and heated to 50-500°C under the action of the intake heater 440. S2 hydrogenation involves feeding metal powder with a particle size less than 2000 μm into the continuous hydrogenation reactor 100 through the feed pipe 113. The powder undergoes hydrogenation under the support of an upward airflow, yielding hydrogenated metal powder. This powder moves upward with the airflow and is discharged through the discharge pipe. Simultaneously, the reaction heat exchanger 310 is activated to exchange heat in the hydrogenation reaction zone, maintaining the temperature within the continuous hydrogenation reactor 100 within the required range for the hydrogenation reaction. For example... Figure 2As shown, the continuous hydrogenation reactor 100 includes a reactor body and a reaction heat exchanger 310. The reactor body is a vertically arranged cylindrical container. A gas dispersion plate 116 and an inlet pipe 111 are welded to the lower part of the cylindrical container. The gas 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 gas dispersion plate 116. A feed pipe 113 is welded to the middle part, and an outlet pipe 112 is welded to the upper part. The reaction heat exchanger 310 is fixed to the side wall of the cylindrical body and located between the inlet pipe 111 and the feed pipe 113. During operation, the reaction gas input from the gas supply unit flows into the reactor body through the inlet pipe 111. After being dispersed by the airflow dispersion plate 116, the gas flows out through the outlet pipe 112 to form an upward airflow. The metal powder enters the reactor body through the feed pipe 113 and undergoes a hydrogenation reaction under the action of the upward airflow. The temperature of the reactor body is controlled by the reaction heat exchanger 310. At the same time, the upward airflow that does not participate in the reaction carries away the heat energy released by the hydrogenation reaction through convection heat exchange. The reaction heat exchanger 310 and the upward airflow work together to form a thermal energy management device, which combines radiation heat exchange and convection heat exchange. This not only ensures the efficiency of the hydrogenation reaction, but also removes the heat of reaction in time to prevent problems such as agglomeration or melting caused by local overheating.

[0017] S3 gas-solid separation: The hydride metal powder and reaction gas discharged through the discharge pipe enter the gas-solid separation device. Under the action of the gas-solid separation device, gas-solid separation occurs, yielding solid hydride metal powder and gas. The solid hydride metal powder, after switching through the first intermediate chamber 212, enters the finished product chamber under normal pressure for temporary storage; the gas is returned to the continuous hydrogenation reaction unit 100 through the gas supply mechanism 400. Specifically, as follows... Figure 2As shown, the gas supply mechanism 400 also includes a stamping unit, which 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 111 via a valve. It is also connected to the stamping compressor 411 via a valve. The outlet of the stamping compressor 411 is connected to the stamping pipe. The gas-solid separation device includes a pressure relief pipe, a gas-solid separation unit 210, and a pressure relief separation unit 220. The pressure relief pipe is located between the gas-solid separation unit 210 and the pressure relief separation unit 220 and is connected to them via 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 components. In the separation of solid matter, 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 set between the gas-solid separation chamber 211 and the first finished product chamber 213 and is connected to the pressure relief 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 pressure relief 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 set 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 connects the pressure relief separation device 200 to 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, and the powder is discharged into the pressure relief separation unit 220 after being filtered by the filter element of the pressure relief separation device 200.

[0018] 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 inlet and outlet of the pressure relief separation chamber 221 are connected to the hydrogen storage tank 410, and a pressure relief compressor 412 is provided between the second inlet and outlet and the hydrogen storage tank 410. The second intermediate chamber 222 is basically the same as the first intermediate chamber 212, except that the body of 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 body of the chamber 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.

[0019] S4 purging: The gas supply mechanism includes a purging unit, which comprises a purging pipe and a vent pipe. The purging pipe is connected to an inert gas. During maintenance or after the reaction is complete, the inert gas replaces the reactant gas in the hydrogenation system through the purging pipe, and the reactant gas is then discharged through the vent pipe. Specifically, as follows... Figure 2 As shown, the displacement pipe and the vent pipe are connected to the first intermediate chamber 212, the second intermediate chamber 222, and the pressurization module 430 through valves, respectively. The displacement pipe is connected to a displacement storage tank 420, which stores inert gas and is connected to a gas supply pipe through a valve. The vent pipe is equipped with a vent port 421, which is connected to the atmosphere. When production stops or maintenance is performed, the valves corresponding to the first intermediate chamber 212, the second intermediate chamber 222, and the pressurization module 430 are opened, and the inert gas is discharged through the displacement pipe, and the reaction gas in the first intermediate chamber 212, the second intermediate chamber 222, and the pressurization module 430 is discharged through the vent pipe.

[0020] Example 2 Based on Example 1, the process further includes S21 refining: before the hydride metal powder is discharged, the reaction gas is accelerated through a refining nozzle 115 and injected into the continuous hydrogenation reaction device 100, causing the hydride metal powder to collide with each other, thus reducing the particle size of the hydride metal powder. Specifically, refer to... Figure 2 The continuous hydrogenation reactor 100 also includes a refining unit, which includes a main pipe 114. The main pipe 114 is connected to the reaction gas and is equipped with a number of refining nozzles 115. The refining nozzles 115 are welded to the side wall of the reactor body and extend into the reactor body. During operation, the reaction gas enters the refining nozzles 115 through the main pipe 114, is accelerated by the refining nozzles 115 and is sprayed into the reactor body, and drives the hydrogenated metal powder on the spray path to approach each other, thereby causing collision.

[0021] like Figure 4As shown, the gas-solid separation chamber 211 includes multiple separation chambers connected in series. Each separation chamber is independently connected to a first intermediate chamber 212 and a separate first finished product chamber 213. The first intermediate chamber 212 is connected to a stamping pipe and a pressure relief pipe. The stamping pipe is connected to a stamping unit, and the pressure relief pipe is connected to a pressure relief unit. Valves are installed between the first intermediate chamber 212 and the stamping pipe, the pressure relief pipe, the gas-solid separation chamber 211, and the finished product chamber. During unloading, the rising airflow discharged from the discharge pipe carries hydride metal powder through the series of separation chambers in sequence. Each separation chamber is equipped with a filter element, and the filter pores of the filter element gradually decrease in size, thereby classifying the particle size of the hydride metal through the filter element to achieve a continuous classification effect of the hydride metal. Subsequently, the valve between the stamping pipe and the first intermediate chamber 212 is opened, and the powder is discharged into the first intermediate chamber through the stamping unit. The reaction gas is transported to the first intermediate chamber 212 until the gas pressure in the first intermediate chamber 212 is equal to that in the pressure relief separation chamber 221. Then, the valve between the first intermediate chamber 212 and the gas-solid separation chamber 211 is opened to transfer the hydride metal powder separated in the gas-solid separation chamber 211 to the first intermediate chamber 212. After that, the valve between the first intermediate chamber 212 and the gas-solid separation chamber 211 is closed, and the valve between the pressure relief pipe and the first intermediate chamber 212 is opened to discharge the reaction gas in the first intermediate chamber 212 through the pressure relief unit. After that, the pressure in the first intermediate chamber 212 and the first finished product chamber 213 is equal, and the valve between the first intermediate chamber 212 and the first finished product chamber 213 is opened to continuously transfer hydride metal powder of the corresponding particle size range to the corresponding first finished product chamber 213 for storage, thereby achieving the effect of continuous collection of hydride metal powder of different particle size ranges.

[0022] Example 3 Based on Example 1, the system also includes S5 heat utilization; the continuous hydrogenation system for metal powder further includes a heat utilization module 500, such as... Figure 4 As shown, the heat recovery module 500 includes a steam turbine 541, a generator 542, and a condensing assembly. The steam turbine 541 is connected to the heat recovery unit 300 and drives the generator assembly to convert the heat energy absorbed by the heat recovery unit 300 into electrical energy. Specifically, as... Figure 4As shown, the steam turbine 541 includes a rotor and a steam generator. The steam generator is connected to a heat recovery unit 300, which consists of several reaction heat exchangers 310 and a first heat exchanger 320. The steam generator can generate high-pressure steam using the heat collected by the heat recovery unit 300. The high-pressure steam drives the rotor to rotate and performs work on the generator 542, thereby generating electricity using the heat energy collected by the 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 electricity 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 a gas supply mechanism 400. After being pressurized and heated by the gas supply mechanism 400, the hydrogen is delivered to the reactor body for use, thereby achieving partial self-sufficiency of raw materials and reducing the cost of raw material procurement.

[0023] 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 heat recovery.

[0024] 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 heat recovery unit 300 to continue absorbing the heat generated by the hydrogenation reaction.

[0025] A medium heater 548 and a deaerator 547 are connected between the condenser 545 and the heat recovery unit 300. 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 returns to the thermal energy management system to continue to absorb the heat generated by the hydrogenation reaction.

[0026] 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 heating port is connected to the steam turbine 541 to enhance the steam utilization efficiency of the steam turbine 541.

[0027] Example 4 Based on Example 2, the system also includes S5 heat utilization; the continuous hydrogenation system for metal powder further includes a heat utilization module 500, such as... Figure 5As shown, 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 heat recovery unit 300 and the heat utilization unit, and connects the reaction heat exchanger 310 and the first heat exchanger 320 to the heat utilization unit. Thus, the flow of the heat exchange medium enables the heat energy of the reaction heat exchanger 310, the first heat exchanger 320, the heat storage component 520 and the heat utilization unit to be connected, and 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.

[0028] The heat utilization unit includes a third heat exchanger 510 and a heat transfer medium. The third heat exchanger 510 is connected to a number of 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.

[0029] 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 510223 and the heat storage device 520.

[0030] During operation, the heat exchange medium in the heat storage unit 520 is transported by the first molten salt pump 501 to the reaction heat exchanger 310 and the first heat exchanger 320 to absorb the heat generated by the hydrogenation reaction, and then enters the heat storage unit 520 to raise the temperature of the heat exchange medium in the heat storage unit 520. This scheme utilizes the characteristic of molten salt heat storage time to achieve a heat storage capacity of more than 10 hours per day.

[0031] 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.

[0032] 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 control method for a continuous hydrogenation system of metal powder, characterized in that: The process includes the following steps: S1 ventilates, the gas supply mechanism is activated, and the gas supply mechanism continuously outputs a pressure of 1-6. A reaction gas with a pressure of MPa and a temperature of 50-500℃ is introduced into the continuous hydrogenation reactor through the inlet pipe and discharged through the outlet pipe, forming an upward airflow. In S2 hydrogenation, metal powder with a particle size less than 2000μm is fed into the continuous hydrogenation reactor through the inlet pipe and undergoes hydrogenation under the support of the upward airflow, yielding hydrogenated metal powder. The hydrogenated metal powder moves upward under the support of the upward airflow and is discharged through the outlet pipe. Simultaneously, the reaction heat exchanger is activated to exchange heat in the hydrogenation reaction zone, maintaining the temperature within the continuous hydrogenation reactor within the required temperature range for the hydrogenation reaction. In S3 gas-solid separation, the hydrogenated metal powder and reaction gas discharged through the outlet pipe enter the gas-solid separation device, where gas-solid separation occurs, yielding solid hydrogenated metal powder and gas. The solid hydrogenated metal powder is temporarily stored in the finished product silo at atmospheric pressure after switching through the first intermediate chamber; the gas is returned to the continuous hydrogenation reactor after thermal management.

2. The control method for a continuous hydrogenation system of metal powder according to claim 1, characterized in that: S2 hydrogenation also includes S21 refining. Before the hydrogenated metal powder is discharged, the reaction gas is accelerated through a refining nozzle and then injected into the continuous hydrogenation reaction device, causing the hydrogenated metal powder to collide with each other, thus reducing the particle size of the hydrogenated metal powder.

3. The control method for a continuous hydrogenation system of metal powder according to claim 2, characterized in that: In the S3 gas-solid separation process, the gas-solid separation device includes a gas-solid separation chamber connected to a discharge pipe, and comprises multiple separation chambers connected in series. Each separation chamber is independently connected to a first intermediate chamber. The first intermediate chamber is connected to a stamping pipe and a pressure relief pipe. The stamping pipe is connected to a stamping unit, and the pressure relief pipe is connected to a pressure relief unit. Valves are installed between the first intermediate chamber and the stamping pipe, the pressure relief pipe, the gas-solid separation chamber, and the finished product chamber. During unloading, the rising airflow discharged from the discharge pipe carries hydride metal powder through the series of separation chambers sequentially. Each separation chamber is equipped with a filter element, and the filter pores of the filter element gradually decrease in size, thereby classifying the particle size of the hydride metal through the filter element, achieving a continuous classification effect of the hydride metal. Subsequently... The valve between the stamping pipe and the first intermediate chamber is opened, and the reaction gas is supplied to the first intermediate chamber through the stamping unit. After the gas pressure in the first intermediate chamber is equal to that in the pressure relief separation chamber, the valve between the first intermediate chamber and the gas-solid separation chamber is opened, and the hydride metal powder separated in the gas-solid separation chamber is transferred to the first intermediate chamber. Then, the valve between the first intermediate chamber and the gas-solid separation chamber is closed, and the valve between the pressure relief pipe and the first intermediate chamber is opened. The reaction gas in the first intermediate chamber is discharged through the pressure relief unit, and after the pressure in the first intermediate chamber is equal to that in the finished product chamber, the valve between the first intermediate chamber and the finished product chamber is opened, and the hydride metal powder is continuously transferred to the finished product chamber, thereby achieving the effect of continuous collection of hydride metal powder with different particle size ranges.

4. The control method for a continuous hydrogenation system of metal powder according to claim 3, characterized in that: It also includes S4 heat recovery. The continuous hydrogenation system for metal powder includes a heat recovery unit, which includes a first heat exchanger and a reaction heat exchanger. During the hydrogenation reaction, the heat energy released by the hydrogenation reaction is recovered through the heat exchange medium flowing in the first heat exchanger and the reaction heat exchanger.

5. The control method for a continuous hydrogenation system of metal powder according to claim 4, characterized in that: It also includes S5 heat utilization. The continuous hydrogenation system for metal powder also includes a heat utilization module. The heat utilization module includes a heat storage unit and several heat users. The heat storage unit is located between the heat users and the reaction heat exchanger and the first heat exchanger, and connects the reaction heat exchanger and the first heat exchanger to the heat users.

6. The control method for a continuous hydrogenation system of metal powder according to claim 4, characterized in that: It also includes S5 heat utilization. The continuous hydrogenation system for metal powder also includes a heat utilization module, which includes a steam turbine and a power generation component. The steam turbine is connected to the heat recovery unit and drives the power generation component to convert the heat energy absorbed by the heat recovery unit into electrical energy.

7. The control method for a continuous hydrogenation system of metal powder according to claim 1, characterized in that: The gas supply mechanism 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. The stamping unit and the gas supply unit operate independently and their output ends are interconnected to form a gas supply port. The gas supply port is connected to the continuous hydrogenation reaction device, and the stamping unit is connected to the first intermediate chamber.

8. The control method for a continuous hydrogenation system of metal powder according to claim 1, characterized in that: It also includes S4 replacement. The gas supply mechanism includes a replacement unit, which includes a replacement pipe and a vent pipe. The replacement pipe is connected to an inert gas. During maintenance or after the reaction is completed, the inert gas replaces the reaction gas in the hydrogenation system through the replacement pipe and discharges the reaction gas through the vent pipe.

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