Reactor, reaction system and method for producing silicon-carbon anode materials in a flexible heat transfer fluidized bed

Abstract

This invention proposes a reactor, reaction system, and method for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed, relating to the field of silicon-carbon anode material preparation technology. The reactor includes a reactor body, a microjet auxiliary device, and a heat extraction device. The reactor body is hollow, forming a reaction chamber. The reaction chamber includes, from bottom to top, a pre-distribution section, a fluidized reaction zone, a partitioned fluidized reaction zone, and a gas-solid separation zone. The microjet auxiliary device includes an air inlet module and multiple air inlet nozzles. The multiple air inlet nozzles are located in the fluidized reaction zone, and the air inlet module is connected to the multiple air inlet nozzles, delivering turbulent airflow to the fluidized reaction zone through each air inlet nozzle. The heat extraction device includes multiple heat extraction tubes located in the fluidized reaction zone. The two ends of each heat extraction tube are sealed, penetrating the side wall of the reactor body and extending outside the reactor body, connected to a cooling medium source. This invention can enhance the reaction rate of the silicon-carbon anode material production process.

Description

Technical Field

[0001] This invention relates to the field of silicon-carbon anode material preparation technology, and in particular to a reactor, reaction system and method for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed. Background Technology

[0002] Silicon-carbon anode materials, by combining high-capacity silicon (or silicon suboxide) with buffering / conductive carbon materials, effectively alleviate the problem of huge volume expansion of silicon anodes, making them a key material for significantly improving the energy density of lithium-ion batteries. Currently, silicon-carbon anode materials have entered a stage of expansion from consumer electronics to power batteries, and industrialization is accelerating.

[0003] Fluidized bed chemical vapor deposition (FCVD) for preparing silicon-carbon anode materials is expected to become the mainstream production method for silicon-carbon anode materials. The FCVD process uses porous carbon as a raw material, introducing fluidizing gas to suspend the porous carbon within the fluidized bed. At high temperatures, silane gases are cracked, causing silicon to deposit inside the porous carbon, forming a silicon-carbon composite material. This composite material is then carbon-coated under high-temperature cracking of the carbon source gas, ultimately yielding this novel silicon-carbon anode material. Most fluidized bed reactors employ a vertical cylindrical structure, with a gas distributor at the bottom and single-stage heating on the sidewalls to achieve material fluidization and high-temperature cracking of the process gas. Existing fluidized bed reactors generally have the following drawbacks:

[0004] 1) The electrode material (porous carbon) in the fluidized bed is a typical Geldart C type viscous particle. Due to the strong van der Waals forces between the particles, the particles are difficult to fluidize normally or the fluidization is uneven in the fluidized bed. Traditional fluidized beds use single-point / multi-point air inlet, resulting in vigorous fluidization in the area near the air inlet and insufficient fluidization in the edge area. High-speed stirring devices are required for forced mixing, but the strong shear force can easily damage the structure of lightweight porous carbon particles, reduce the mechanical strength of the material, and increase the risk of pulverization. At the same time, excessively high flow rates can cause raw material entrainment, leading to reduced yield, reduced electrochemical performance of the material, and increased production costs.

[0005] 2) Severe particle agglomeration in the fluidized bed reactor and uneven flow field cause process gas to be carried out in some areas without sufficient reaction, resulting in low gas-solid contact efficiency of raw materials and reduced residence time in the fluidized bed reactor. This reduces the amount of silicon deposition and carbon coating, leading to raw material waste, reduced process gas utilization, increased by-products, and reduced production efficiency.

[0006] 3) High-temperature pyrolysis of silicon source gas and high-temperature pyrolysis of carbon source gas are accompanied by high reaction enthalpy. Long-term reaction can easily form local hot spots, which can cause silicon particle melting and carbon support sintering, affecting the stability and sustainability of the reaction and reducing product quality.

[0007] 4) Existing fluidized bed chemical vapor deposition equipment operates discontinuously, with a long overall process time. The fluidized bed reactor needs to be heated and then cooled, resulting in low energy utilization and overall production efficiency.

[0008] In view of this, based on years of experience in production design in this and related fields, the inventor has designed a reactor, reaction system and method for producing silicon-carbon anode materials in a flexible heat transfer fluidized bed through repeated experiments, in order to solve the problems existing in the prior art. Summary of the Invention

[0009] The purpose of this invention is to provide a reactor, reaction system, and method for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed, thereby enhancing the reaction rate of the silicon-carbon anode material production process.

[0010] To achieve the above objectives, this invention proposes a reactor for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed, wherein the reactor comprises:

[0011] The reactor body is hollow inside and forms a reaction chamber, which includes a pre-distribution section, a fluidized reaction zone, a partitioned fluidized reaction zone and a gas-solid separation zone arranged sequentially from bottom to top.

[0012] A micro-jet auxiliary device includes an air intake module and multiple air intake nozzles. The multiple air intake nozzles are disposed in the fluidized reaction zone. The air intake module is connected to the multiple air intake nozzles and delivers turbulent airflow to the fluidized reaction zone through each air intake nozzle.

[0013] The heat extraction device includes multiple heat extraction tubes disposed in the fluidized reaction zone. Both ends of each heat extraction tube are sealed and penetrate the side wall of the reactor body and extend out of the reactor body and are connected to a cooling medium source.

[0014] This invention also proposes a reaction system for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed, wherein the reaction system comprises sequentially connected components:

[0015] Raw material conveying device, used to convey porous carbon raw materials;

[0016] A silicon deposition fluidized bed reactor is used to achieve silicon deposition inside the porous carbon raw material to obtain silicon-carbon anode material;

[0017] A carbon-coated fluidized bed reactor is used to achieve surface carbon coating of the silicon-carbon anode material, thereby obtaining a carbon-coated silicon-carbon anode material.

[0018] A cooling discharge device is used to perform fluidized cooling on the carbon-coated silicon-carbon anode material;

[0019] Both the silicon deposition fluidized bed reactor and the carbon-coated fluidized bed reactor use the reactors described above.

[0020] This invention also proposes a method for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed, wherein the method for producing silicon-carbon anode materials includes:

[0021] An inert gas is used as a fluidizing gas to keep the porous carbon in a fluidized suspension state.

[0022] An inert gas or a mixture of an inert gas and a silicon source gas is used as a secondary gas to agitate the porous carbon in a fluidized suspension state.

[0023] The porous carbon in a fluidized suspension state is heated to a target temperature, and then a silicon source gas is introduced to cause the silicon source gas to decompose inside the porous carbon, thereby depositing silicon inside the porous carbon to obtain a silicon-carbon anode material.

[0024] The silicon-carbon anode material is kept in a fluidized suspension state by the fluidizing gas.

[0025] An inert gas or a mixture of an inert gas and a silicon source gas is used as a secondary gas to agitate the silicon-carbon anode material in a fluidized suspension state.

[0026] The silicon-carbon anode material in a fluidized suspension state is heated to a target temperature, and then a carbon source gas is introduced to cause the carbon source gas to decompose on the surface of the silicon-carbon anode material, so that carbon is coated on the surface of the silicon-carbon anode material, and carbon-coated silicon-carbon anode material is obtained.

[0027] The carbon-coated silicon-carbon anode material is kept in a fluidized suspension state by the fluidizing gas, and the carbon-coated silicon-carbon anode material is gradually cooled.

[0028] Compared with the prior art, the present invention has the following features and advantages:

[0029] This invention proposes a reactor, reaction system, and method for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed. By designing a microjets auxiliary device on the outer wall of the reactor's dense phase zone and using nozzles to introduce gas, multi-dimensional gas disturbance is achieved, solving the problem of poor fluidization quality in porous carbon and improving the residence time and gas-solid contact efficiency of the raw materials. Simultaneously, a heat extraction device is added to the reactor, allowing for precise heat transfer based on the high enthalpy generated during the high-temperature pyrolysis of silicon and carbon source gases. This reduces local hot spots in the fluidized bed reaction zone, ensuring uniformity of silicon deposition and carbon coating, thereby improving the electrochemical performance of the product. Furthermore, independent zoned temperature control is implemented within the fluidized bed, utilizing the heat of the process waste gas to preheat the process gas. This allows for faster reaction of the process gas within the fluidized bed and precise control of the pyrolysis temperature of the process gas or supplemental heat to the device, achieving gradient utilization of thermal energy and reducing overall production time and energy loss. The system features flexible heat transfer, continuous and efficient production, simple operation, high-quality mass production, high production safety, and low cost. Attached Figure Description

[0030] The accompanying drawings described herein are for illustrative purposes only and are not intended to limit the scope of the invention in any way. Furthermore, the shapes and proportions of the components in the drawings are merely illustrative to aid in understanding the invention and do not specifically limit the shapes and proportions of the components. Those skilled in the art, guided by the teachings of this invention, can select various possible shapes and proportions to implement the invention according to specific circumstances.

[0031] Figure 1 This is a schematic diagram of the reactor for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed, as proposed in this invention.

[0032] Figure 2 This is a schematic diagram of the reaction system for producing silicon-carbon anode materials according to the present invention;

[0033] Figure 3 This is a schematic diagram of the silicon deposition fluidized bed reactor in this invention;

[0034] Figure 4 This is a schematic diagram of the carbon-coated fluidized bed reactor in this invention;

[0035] Figure 5 This is a schematic diagram of the cooling discharge device in this invention;

[0036] Figure 6 This is a schematic diagram (I) of the microjet auxiliary device in this invention;

[0037] Figure 7 This is a schematic diagram (II) of the microjet auxiliary device in this invention.

[0038] Figure 8 This is a schematic diagram (III) of the microjet auxiliary device in this invention.

[0039] Figure 9 This is a schematic diagram (IV) of the microjet auxiliary device in this invention.

[0040] Figure 10 This is a schematic diagram of the heat extraction pipe in this invention.

[0041] Explanation of reference numerals in the attached figures

[0042] 100. Reactor body; 101. Fluidized gas inlet; 102. Pre-distribution section; 103. Gas distributor; 104. Material outlet; 105. Microjet auxiliary device; 1051. Inlet nozzle; 106. Fluidized reaction zone; 107. Heating device; 108. Heat extraction device; 109. Solid particle inlet; 110. Zoned fluidized reaction zone; 111. Gas-solid separation device; 1. Raw material conveying device; 2. Silicon deposition fluidized bed reactor; 3. Carbon-coated fluidized bed reactor; 4. Cooling discharge device; 10. Gas mixer; 11. Silicon source gas mixture inlet; 12. Silicon source gas pyrolysis tail gas outlet; 13. Thermal oxidation system; 14. Gas separator; 18. Gas mixer; 201. Silicon source gas mixture inlet; 202. Mixed gas pre-distribution section; 203. Perforated plate gas distributor; 204. 205. Silicon-carbon anode material outlet; 206. Microjet auxiliary device; 207. Fluidized reaction zone; 208. Heating device; 209. Heat extraction device; 2001. Heat extraction pipe; 2002. Porous carbon inlet; 210. Zoned fluidized reaction zone; 211. Gas-solid separation device; 212. Porous sintered filter element; 301. Carbon source gas mixed gas inlet; 302. Mixed gas pre-distribution section; 303. Porous plate gas distributor; 304. Carbon-coated silicon-carbon anode material outlet; 305. Microjet auxiliary device; 306. Fluidized reaction zone; 307. Heating device; 308. Heat extraction device; 309. Silicon-carbon anode material inlet; 310. Zoned fluidized reaction zone; 311. Gas-solid separation device; 312. Porous sintered filter element; 401. Inert gas inlet; 402. Mixed gas pre-distribution section; 403. Gas distributor; 4031. Porous plate gas distributor; 4032. Ring pipe gas distributor; 404. Product outlet; 405. Microjet auxiliary device; 406. Fluidization zone; 407. Heat extraction device; 408. Inlet of carbon-coated silicon-carbon anode material; 409. Zoned fluidization zone; 410. Gas-solid separation device; 411. Porous sintered filter element. Detailed Implementation

[0043] The details of the present invention can be more clearly understood by referring to the accompanying drawings and the description of specific embodiments. However, the specific embodiments of the present invention described herein are for illustrative purposes only and should not be construed as limiting the invention in any way. Under the teachings of this invention, those skilled in the art can conceive of any possible modifications based on the invention, and these should all be considered to fall within the scope of the invention.

[0044] like Figure 1 As shown, the reactor for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed proposed in this invention includes a reactor body 100, a microjet auxiliary device 105, and a heat extraction device 108.

[0045] The reactor body 100 is hollow inside and forms a reaction chamber, which includes a pre-distribution section 102, a fluidized reaction zone 106, a partitioned fluidized reaction zone 110 and a gas-solid separation zone arranged sequentially from bottom to top.

[0046] The micro-jet auxiliary device 105 includes an air intake module and multiple air intake nozzles 1051. The multiple air intake nozzles 1051 are disposed in the fluidized reaction zone 106. The air intake module is connected to the multiple air intake nozzles 1051 and delivers turbulent airflow to the fluidized reaction zone 106 through each air intake nozzle 1051.

[0047] The heat extraction device 108 includes multiple heat extraction tubes disposed in the fluidized reaction zone 106. Both ends of each heat extraction tube are sealed and penetrate the side wall of the reactor body 100 and extend out of the reactor body 100 and are connected to the cooling medium source through a pipe.

[0048] The reactor for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed proposed in this invention features a micro-jet auxiliary device 105 in the reactor body 100. Multiple air inlet nozzles 1051 introduce gas jets into the fluidized reaction zone 106, creating multi-dimensional gas disturbance within the fluidized reaction zone 106. This results in a more uniform distribution of solid particles within the fluidized reaction zone 106, effectively breaking up particle agglomeration and reducing channeling. The disturbance from multiple airflows increases the residence time of solid particles in the fluidized reaction zone 106, improving the gas-solid contact efficiency within the reactor. This increases the utilization rate of process gases within the same time frame, ensuring uniformity of silicon deposition and carbon coating. It solves the problem of poor fluidization effect in porous carbon, improves product quality, and is suitable for efficient industrial production.

[0049] The reactor for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed proposed in this invention has a heat-extraction device 108 installed on the reactor body 100. The high enthalpy of the gas during cracking causes the temperature in the fluidized reaction zone 106 to rise. The heat-extraction device 108 quickly removes excess heat from the fluidized reaction zone 106 to reduce local hot spots in the fluidized bed. This flexible heat-transfer feature enables temperature control within the fluidized reaction zone 106, avoiding solid particle sintering caused by excessively high local temperatures in the fluidized reaction zone 106 and improving product quality.

[0050] In an optional embodiment of the present invention, the fluidized reaction zone 106 includes a dense phase zone and a dilute phase zone disposed above the dense phase zone, with multiple air inlet nozzles 1051 disposed in the dense phase zone. The dense phase zone is the core region of the gas-solid reaction; the dilute phase zone is the region where solid particles are entrained and raised by the airflow.

[0051] In an optional embodiment of the invention, the fluidized reaction region 106 is used for silicon deposition and carbon coating processes in chemical vapor deposition.

[0052] In an optional embodiment of the present invention, such as Figures 6 to 9 As shown, multiple air inlet nozzles 1051 are spaced apart along the axial and / or circumferential direction of the reactor body 100.

[0053] In one optional example of this embodiment, a plurality of air inlet nozzles 1051 are arranged at equal intervals along the axial and / or circumferential direction of the reactor body 100.

[0054] In an optional embodiment of the present invention, one end of each air inlet nozzle 1051 is fixedly connected to the outer wall of the reactor body 100, and the other end of each air inlet nozzle 1051 is sealed through the side wall of the reactor body 100 and extends into the fluidized reaction zone 106.

[0055] In an optional embodiment, the other end of the air inlet nozzle 1051 is provided with an air outlet, and the air outlet coincides with the inner wall of the reactor body 100.

[0056] In an optional example of this embodiment, the air intake nozzle 1051 includes a nozzle body and an air intake pipe. The air intake port of the nozzle body is fixedly connected to the air intake pipe, and a disturbed airflow (i.e., a secondary airflow) is introduced into the end of the air intake pipe.

[0057] In an alternative example, the end of the intake pipe is connected to a flow meter and a valve, which control the ejection speed of the turbulent airflow from the intake nozzle 1051.

[0058] In one optional example, the nozzle body and the intake pipe are welded or threaded together.

[0059] In one optional example, the intake pipe is made of stainless steel.

[0060] In one alternative example, the nozzle body is a tapered shape with a gradually narrowing diameter, and the diameter of the outlet of the nozzle body is smaller than the diameter of the inlet of the nozzle body.

[0061] In an optional example of this embodiment, the outlet diameter of the air inlet nozzle 1051 is 120~520μm; preferably 127~254μm. Those skilled in the art can adjust the outlet diameter of the air inlet nozzle according to the actual process conditions.

[0062] In an optional example of this embodiment, the other end of the air intake nozzle 1051 is provided with an air intake port, which is sealed to a stainless steel tube with an inner diameter of 6 mm.

[0063] In an optional example, when the intake nozzle 1051 is arranged in a horizontal tangential direction, the tilt angle α of the intake nozzle 1051 is 10°~45°, preferably 15°~45°, and the tilt angle α is the acute angle between the central axis of the nozzle and the vertical plane of the axis of symmetry where the intake nozzle is located.

[0064] In an optional example, when the air intake nozzle 1051 is inclined upward, the inclination angle β of the air intake nozzle 1051 is 10°~60°, preferably 30°~60°, and the inclination angle β is the acute angle between the central axis of the nozzle and the central axis of the fluidized bed.

[0065] In an optional example, when the air intake nozzle 1051 is inclined downward, the inclination angle γ of the air intake nozzle 1051 is 10°~60°, preferably 30°~60°, and the inclination angle γ is the acute angle between the central axis of the nozzle and the central axis of the fluidized bed.

[0066] In one optional example of this implementation, such as Figure 10 As shown, multiple heat collection tubes 2081 are spaced apart along the circumference of the reactor body 100.

[0067] In one optional example of this implementation, each heat pipe 2081 is one of a finned tube, a studded tube, and a bare tube.

[0068] In an optional example of this implementation, the cooling medium source delivers the cooling medium to each heat exchanger through a pipeline. The cooling medium absorbs heat in the fluidized reaction zone 106 in the heat exchanger to transfer the heat in the fluidized reaction zone 106 and reduce the temperature in the fluidized reaction zone 106.

[0069] In one optional example, the cooling medium source is either a liquid cooling medium source or an air cooling medium source.

[0070] In an optional example, the upper and lower ends of the heat pipe 2081 pass through the reactor body 100 respectively. The lower end of the heat pipe 2081 is the inlet of the cooling medium, and the upper end of the heat pipe 2081 is the outlet of the cooling medium. The cooling medium passes through the fluidized reaction zone 106 from bottom to top and transfers the heat in the fluidized reaction zone 106 away.

[0071] In an optional embodiment of the invention, the reactor further includes a heating device 107 having multiple heating elements mounted on the reactor body 100 and heating the fluidized reaction zone 106. The heating device 107 is used to heat the entire reactor so that the temperature of the fluidized reaction zone 106 reaches the temperature of the gas cracking reaction.

[0072] In one optional embodiment of this implementation, multiple heating elements are disposed on the inner or outer wall of the reactor body 100. When the heating elements are disposed on the outer wall of the reactor body 100, the heating elements heat the reactor by means of heat conduction; when the heating elements are disposed on the inner wall of the reactor body 100, the heating elements heat the reactor by means of heat convection and heat radiation.

[0073] In one optional example of this embodiment, multiple heating elements are spaced apart along the axial and / or circumferential direction of the reactor body 100.

[0074] In one alternative example, multiple heating elements are arranged at equal intervals along the axial and / or circumferential direction of the reactor body 100.

[0075] Preferably, each heating component is independently controlled, thereby achieving zoned heating to precisely control the axial reaction temperature within the fluidized reaction zone 106.

[0076] In one optional example of this implementation, the heating element is a heating resistor, which heats the entire reactor by means of thermal convection and thermal radiation.

[0077] In one optional example, a protective sleeve is provided around the heating resistor.

[0078] In an optional embodiment of the present invention, a gas distributor 103 is provided in the pre-distribution section, through which fluidizing gas is introduced into the reaction chamber, and the distribution of fluidizing gas in the reaction chamber is made more uniform, thereby improving the fluidization uniformity of the powder.

[0079] In one optional example of this implementation, the gas distributor 103 is one of a perforated plate gas distributor, a shower head gas distributor, and a ring pipe gas distributor.

[0080] In an optional embodiment of the present invention, a gas-solid separation device 211 is provided in the gas-solid separation area. The gas-solid separation device 211 is located above the partitioned fluidized reaction area and is used to trap ultrafine particles entrained in the gas.

[0081] In an optional example of this embodiment, the gas-solid separation device 111 is a particulate filter, which includes a backflush gas inlet and a porous sintered filter element. The backflush gas inlet is supplied with inert gas to blow off solid particles attached to the porous sintered filter element.

[0082] In another alternative example of this embodiment, the gas-solid separation device 111 may also employ one of a cyclone separator and a coupling separator.

[0083] In an optional embodiment of the present invention, a partitioned fluidized reaction zone 110 is disposed above the fluidized reaction zone, and the partitioned fluidized reaction zone adopts a variable diameter structure to reduce the velocity of the powder material in the upper part of the bed reactor and reduce the equipment height while ensuring sufficient fluidization of the powder.

[0084] In an optional embodiment of the present invention, the reactor body 100 is provided with a solid particle inlet 109, a fluidizing gas inlet 101, and a material outlet 104.

[0085] In one optional embodiment, the fluidizing gas inlet is located at the bottom of the reactor body 100, the solid particle inlet is located at the top of the reactor body 100, the material outlet is located at the bottom of the fluidized reaction zone 106, and the exhaust gas outlet is located at the top of the reactor body 100.

[0086] like Figure 2 As shown, this invention also proposes a reaction system for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed reactor. This system includes a raw material conveying device 1, a silicon deposition fluidized bed reactor 2, a carbon-coated fluidized bed reactor 3, and a cooling discharge device 4, connected in sequence. The raw material conveying device 1 is used to convey porous carbon raw materials; the silicon deposition fluidized bed reactor 2 is used to achieve silicon deposition inside the porous carbon raw materials to obtain silicon-carbon anode materials; the carbon-coated fluidized bed reactor 3 is used to achieve carbon coating on the surface of the silicon-carbon anode materials to obtain carbon-coated silicon-carbon anode materials; and the cooling discharge device 4 is used to perform fluidized cooling on the carbon-coated silicon-carbon anode materials. Both the silicon deposition fluidized bed reactor 2 and the carbon-coated fluidized bed reactor 3 employ the fluidized bed reactors described above.

[0087] The present invention proposes a reaction system for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed reactor. This system is used to prepare carbon-coated silicon-carbon anode battery materials. Porous carbon is prepared into silicon-carbon anode materials through a silicon deposition fluidized bed reactor 2, and then carbon-coated silicon-carbon anode materials are obtained by carbon coating through a carbon coating fluidized bed reactor 3. This enhances process continuity and improves production efficiency.

[0088] The reaction system for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed proposed in this invention achieves uniform fluidization of porous carbon by adding a micro-jet auxiliary device 105 to the outer wall of the shell in the dense phase region of each reactor, thereby increasing the residence time of process gas and particles, increasing the gas-solid contact efficiency of the raw materials in the fluidized bed, and improving the operating space for flexible heat transfer. At the same time, by adding a heat removal device 108 to each reactor to flexibly remove the high reaction enthalpy generated during the high-temperature cracking of process gas, local hot spots are prevented from causing silicon particle melting and carbon support sintering.

[0089] In an optional embodiment of the present invention, the cooling discharge device 4 also employs the reactor described above.

[0090] In an optional embodiment of the present invention, such as Figure 3 As shown, the silicon deposition fluidized bed reactor 2 includes a reactor body, a microjet auxiliary device 205, a heat extraction device 208, and a heating device 207. The reactor body is equipped with a mixed gas pre-distribution section 202, a porous plate gas distributor 203, a fluidized reaction zone 206, a zoned fluidized reaction zone 210, a gas-solid separation device 211, and a porous sintered filter element 212. The reactor body is provided with a silicon source gas mixed gas inlet 201, a porous carbon inlet 209, and a silicon-carbon anode material outlet 204.

[0091] In an optional embodiment of the present invention, such as Figure 4 As shown, the carbon-coated fluidized bed reactor 3 includes a reactor body, a microjet auxiliary device 305, a heat extraction device 308, and a heating device 307. The reactor body is equipped with a mixed gas pre-distribution section 302, a porous plate gas distributor 303, a fluidized reaction zone 306, a zoned fluidized reaction zone 310, a gas-solid separation device 311, and a porous sintered filter element 312. The reactor body is provided with a carbon source gas mixed gas inlet 301, a silicon-carbon anode material inlet 309, and a carbon-coated silicon-carbon anode material outlet 304.

[0092] In an optional embodiment of the present invention, such as Figure 5As shown, the cooling discharge device 4 includes a reactor body, a micro-jet auxiliary device 405, and a heat extraction device 407. The reactor body is equipped with a mixed gas pre-distribution section 402, a gas distributor 403, a fluidization zone 406, a gas-solid separation device 410, and a porous sintered filter element 411. The reactor body is provided with an inert gas inlet 401, a product outlet 404, and a carbon-coated silicon-carbon anode material inlet 408.

[0093] In an optional example of this implementation, the gas distributor 403 includes a perforated plate gas distributor 4031 and a ring pipe gas distributor 4032.

[0094] In an optional embodiment of the present invention, the reaction system for producing silicon-carbon anode materials further includes an inlet pipe and an exhaust gas pipe. The process gas inlet pipe is connected to the bottom of the silicon deposition fluidized bed reactor 2 and the carbon-coated fluidized bed reactor 3, and process gas is introduced according to process requirements. The exhaust gas from the silicon deposition fluidized bed reactor 2 and the carbon-coated fluidized bed reactor 3 is discharged through the exhaust gas pipe after treatment.

[0095] In one optional example of this implementation, the exhaust gas pipeline is connected to a separation device. After the process waste gas is thermally oxidized and separated by the separation device, the process gas can be reused. The heat of the high-temperature process gas itself is used to preheat the process gas in the silicon deposition and carbon coating process, so as to control the silicon source gas and carbon source gas to be nearly completely decomposed or to supplement the heat, thereby realizing the gradient utilization of heat, which saves process gas, reduces energy consumption, and reduces energy loss and carbon emissions.

[0096] The reaction system for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed proposed in this invention also includes a gas mixer 10, a gas mixer 18, thermal oxidation systems 13 and 21, and gas separators 14 and 22. Silane cracking tail gas is connected to thermal oxidation system 13 and gas separator 14 via the silane cracking tail gas outlet, and acetylene cracking tail gas is connected to thermal oxidation system 21 and gas separator 22 via the acetylene cracking tail gas outlet. The resulting high-temperature N2 is connected to high-temperature inert gas inlet via the high-temperature inert gas outlet, serving as the fluidizing gas for silicon deposition fluidized bed reactor 2 and carbon-coated fluidized bed reactor 3. Simultaneously, the heat from the separated high-temperature N2 is used to preheat silane and acetylene in gas mixers 10 and 18, controlling the cracking temperature of silane and acetylene or supplementing the heat, thus achieving gradient utilization of thermal energy.

[0097] The present invention also proposes a method for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed, the method comprising:

[0098] Inert gas is used as the fluidizing gas to keep porous carbon in a fluidized suspension state.

[0099] Inert gas or a mixture of inert gas and silicon source gas is used as secondary silicon source gas to agitate porous carbon in a fluidized suspension state.

[0100] The porous carbon in a fluidized suspension state is heated to the target temperature, and then silicon source gas is introduced to cause the silicon source gas to decompose inside the porous carbon, thereby depositing silicon inside the porous carbon to obtain silicon-carbon anode material.

[0101] The silicon-carbon anode material is kept in a fluidized suspension state by using fluidizing gas;

[0102] Inert gas or a mixture of inert gas and carbon source gas is used as the secondary carbon source gas to agitate the silicon-carbon anode material in a fluidized suspension state.

[0103] The silicon-carbon anode material in a fluidized suspension state is heated to the target temperature, and then a carbon source gas is introduced to cause the carbon source gas to decompose and coat the surface of the silicon-carbon anode material, thus obtaining a carbon-coated silicon-carbon anode material.

[0104] The silicon-carbon anode material coated with carbon is cooled by fluidized gas.

[0105] The method for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed proposed in this invention involves multi-dimensional gas disturbance of the fluidized suspension raw material (fixed particles) through secondary gas replenishment, thereby improving the fluidization performance of the raw material and the gas-solid contact efficiency, further reducing local reaction hotspots, and increasing the operating space for flexible heat transfer.

[0106] In an optional embodiment of the present invention, the method for producing silicon-carbon anode materials using the above-described reaction system for producing silicon-carbon anode materials includes:

[0107] The raw material conveying device 1, the silicon deposition fluidized bed reactor 2, the carbon-coated fluidized bed reactor 3, and the cooling discharge device 4 are connected in sequence to form a complete system;

[0108] Inert gas is introduced into the silicon deposition fluidized bed reactor 2 to replace the oxygen inside. Porous carbon is transferred to the silicon deposition fluidized bed reactor 2 through the raw material conveying device 1. Inert gas is introduced as a fluidizing gas to keep the porous carbon in a fluidized suspension state. Then, the micro-jet auxiliary device 205 is turned on to introduce inert gas or a mixture of inert gas and silicon source gas as a secondary gas into the dense phase zone. The reaction temperature is controlled. The mixture of inert gas and silicon source gas is introduced to cause the silicon source gas to decompose inside the porous carbon, and silicon is deposited inside the porous carbon. The reaction time is controlled at 0.5~6h. During this period, heat is flexibly removed through the heat extraction device according to the heat of reaction to ensure temperature uniformity and raw material activity. After the predetermined silicon content is reached, silicon-carbon anode material is obtained.

[0109] Inert gas is introduced into the carbon-coated fluidized bed reactor 3 to replace the oxygen inside the reactor 3, transferring the silicon-carbon anode material to the reactor 3. Inert gas is introduced as the fluidizing gas to keep the silicon-carbon anode material in a fluidized suspension state. Then, the micro-jet auxiliary device 305 is turned on to introduce inert gas or a mixture of inert gas and carbon source gas as secondary gas into the dense phase region. The reaction temperature is controlled, and the mixture of inert gas and carbon source gas is introduced to cause the carbon source gas to decompose and coat the surface of the silicon-carbon anode material. The reaction time is controlled at 0.5~6h. During this period, heat is flexibly removed through the heat extraction device according to the heat of reaction to ensure temperature uniformity and coating uniformity, thus obtaining the carbon-coated silicon-carbon anode material.

[0110] Inert gas is introduced into the cooling discharge device 4 as a fluidizing gas to transfer the carbon-coated silicon-carbon anode material to the final product cooling discharge device, so that the carbon-coated silicon-carbon anode material is in a fluidized suspension state. Then, the micro-jet auxiliary device 405 is turned on to introduce inert gas into the dense phase region as a secondary gas. After the particle cooling is accelerated by the heat extraction device 407, the material is discharged to obtain the final product.

[0111] The silicon source gas pyrolysis tail gas from silicon deposition fluidized bed reactor 2 and the carbon source gas pyrolysis tail gas from carbon-coated fluidized bed reactor 3 are thermally oxidized, and then impurities are separated from inert gas by a gas separator to obtain high-temperature inert gas. The high-temperature inert gas is connected to the inert gas inlet of silicon deposition fluidized bed reactor 2 and carbon-coated fluidized bed reactor 3 by pipeline to serve as fluidizing gas. At the same time, the heat of the high-temperature inert gas itself is used to preheat the process gas in the gas mixer to control the pyrolysis temperature of the process gas or to supplement the heat.

[0112] The present invention proposes a method for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed. A heat extraction device is added to the silicon deposition fluidized bed reactor 2, the carbon-coated fluidized bed reactor 3, and the cooling discharge device 4. Combined with the heating device, a segmented temperature control technology is adopted to adjust the heat according to the reaction heat generated during the cracking of process gases, thereby reducing local reaction hotspots, avoiding silicon particle melting and carbon carrier sintering, and achieving flexible heat transfer.

[0113] The present invention proposes a method for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed. By adding a micro-jet auxiliary device in the dense phase region of the fluidized reaction zone, multi-dimensional gas disturbance is achieved through nozzle gas supply, which improves the fluidization performance of the raw materials and the gas-solid contact efficiency, further reduces local reaction hotspots, and increases the operating space for flexible heat transfer.

[0114] The present invention proposes a method for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed, which reuses the heat of the process gas pyrolysis tail gas, preheats the process gas, controls the pyrolysis temperature, and accelerates the reaction rate.

[0115] In an optional embodiment of the present invention, the method for producing silicon-carbon anode materials using the above-described flexible heat-transfer fluidized bed reaction system specifically includes the following steps:

[0116] Step S1: Connect the raw material conveying device 1, the silicon deposition fluidized bed reactor 2, the carbon-coated fluidized bed reactor 3, and the final product cooling and discharge device 4 in sequence to form a complete reaction system;

[0117] Step S2: Inert gas is introduced into the silicon deposition fluidized bed reactor 2 to replace the oxygen in the reactor. Porous carbon is transferred to the silicon deposition fluidized bed reactor 2 through the raw material conveying device 1. Inert gas is introduced as a fluidizing gas to keep the porous carbon in a fluidized suspension state. Then, the micro-jet auxiliary device is turned on to introduce inert gas or a mixture of inert gas and silicon source gas as a secondary gas into the dense phase zone. The reaction temperature is controlled. The mixture of inert gas and silicon source gas is introduced to cause the silicon source gas to decompose inside the porous carbon, depositing silicon inside the porous carbon. The reaction time is controlled at 0.5~6h. During this period, heat is flexibly removed through the heat extraction device according to the heat of reaction to ensure temperature uniformity and raw material activity. After reaching the predetermined silicon content, silicon-carbon anode material is obtained. Furthermore, the temperature regulation method in the silicon deposition fluidized bed reactor 2 is determined by the carbon source gas. Furthermore, the reaction time and heat regulation are controlled by detecting the pressure change of the bed in the silicon deposition fluidized bed reactor 2 and the concentration of silicon-containing gas at the silicon source gas decomposition tail gas.

[0118] Step S3: Inert gas is introduced into the carbon-coated fluidized bed reactor 3 to replace the oxygen in the fluidized bed reactor, and the silicon-carbon anode material is transferred to the carbon-coated fluidized bed reactor 3. Then, step S2 is repeated to produce the next batch of silicon-carbon anode material in the silicon deposition fluidized bed reactor 2.

[0119] Step S4: Inert gas is introduced into the carbon-coated fluidized bed reactor 3 as a fluidizing gas to keep the silicon-carbon anode material in a fluidized suspension state. Then, the micro-jet auxiliary device is turned on to introduce inert gas or a mixture of inert gas and carbon source gas as a secondary gas into the dense phase region. The reaction temperature is controlled, and the mixture of inert gas and carbon source gas is introduced to cause the carbon source gas to decompose and coat the surface of the silicon-carbon anode material. The reaction time is controlled at 0.5~6h. During this period, heat is flexibly removed through a heat extraction device according to the heat of reaction to ensure temperature uniformity and coating uniformity, thus obtaining the carbon-coated silicon-carbon anode material. Furthermore, the temperature regulation method in the carbon-coated fluidized bed reactor 3 is determined by the carbon source gas. Furthermore, the reaction time and heat regulation are controlled by detecting the pressure change of the bed layer in the carbon-coated fluidized bed reactor 3 and the concentration of carbon-containing gas at the carbon source gas decomposition tail gas.

[0120] Step S5: Transfer the carbon-coated silicon-carbon anode material to the final product cooling and discharge device 4, and then repeat step S4 to produce the next batch of carbon-coated silicon-carbon anode material in the carbon-coated fluidized bed reactor 3.

[0121] Step S6: Inert gas is introduced into the cooling discharge device 4 as a fluidizing gas to keep the carbon-coated silicon-carbon anode material in a fluidized suspension state. Then, the micro-jet auxiliary device is turned on to introduce inert gas into the dense phase region as a secondary gas. The particles are cooled by the heat extraction device and then discharged to obtain the final product.

[0122] Step S7: After unloading is completed, repeat step S6 to produce the next batch of final products;

[0123] Step S8: After thermal oxidation, the silicon source gas pyrolysis tail gas and carbon source gas pyrolysis tail gas are separated from impurities and inert gas by a gas separator to obtain high-temperature inert gas. The high-temperature inert gas is connected to the inert gas inlet of silicon deposition fluidized bed reactor 2 and carbon coating fluidized bed reactor 3 by pipeline to serve as fluidizing gas. At the same time, the heat of the high-temperature inert gas itself is used to preheat the process gas in the gas mixer to control the pyrolysis temperature of the process gas or to supplement the heat.

[0124] In an optional embodiment of the present invention, the gas velocity of the fluidizing gas is 1.5 Umf to Ut, preferably 1.5 to 4 Umf.

[0125] In an optional embodiment of the present invention, the pressure of the fluidizing gas is 0.1 MPa to 0.6 MPa, preferably 0.4 to 0.5 MPa.

[0126] In an optional embodiment of the present invention, the secondary gas flow rate of the intake nozzle 1501 is 10% to 40% of the total fluidizing gas flow rate, preferably 15% to 30%; the secondary gas pressure of the intake nozzle 1501 is 0.4 MPa to 1.2 MPa; preferably 0.6 MPa to 0.8 MPa.

[0127] In an optional embodiment of the present invention, the silicon source gas is one or more of the following: silane, silane, propane, trichlorosilane, dichlorosilane, and chloromethylsilane.

[0128] In an optional embodiment of the present invention, the carbon source gas is one or more of methane, C2, C6 alkanes, alkenes, and alkynes.

[0129] In an optional embodiment of the present invention, the inert gas is one or more combinations of nitrogen, argon, helium and krypton.

[0130] In an optional embodiment of the present invention, the volume ratio of silicon source gas to inert gas in the mixture of silicon source gas and inert gas is 1:X, where X is any value from 1 to 9.

[0131] In an optional embodiment of the present invention, the volume ratio of carbon source gas to inert gas in the mixture of carbon source gas and inert gas is 1:X, where X is any value from 1 to 9.

[0132] In an optional embodiment of the present invention, the temperature at which the silicon source gas undergoes a cracking reaction in the silicon deposition fluidized bed reactor is 300~1000℃.

[0133] In an optional embodiment of the present invention, the temperature at which the carbon source gas undergoes a cracking reaction in the carbon-coated fluidized bed reactor is 300~1000℃.

[0134] To enable those skilled in the art to more clearly understand the present invention, the following is combined with Figure 1 The following examples provide a detailed description of the reactor, reaction system, and method for producing silicon-carbon anode materials proposed in this invention.

[0135] Example 1

[0136] First, N2 is supplied from the inert gas inlet 9 to the silicon deposition fluidized bed reactor 2 and the carbon-coated fluidized bed reactor 3 to replace the oxygen in the reactor. After the residual oxygen is removed, the inert gas inlet 9 is closed to stop the supply of N2.

[0137] See also Figure 1 The porous carbon is fed into the raw material conveying device 1 through the porous carbon inlet by an automatic feeding device, and then leaves the raw material conveying device 1 through the porous carbon outlet and enters the silicon deposition fluidized bed reactor 2 through the porous carbon inlet.

[0138] See also Figure 1N2 is introduced into the silicon deposition fluidized bed reactor 2 as a fluidizing gas (gas velocity controlled at 0.15 μmf) through the inert gas inlet of the silicon deposition fluidized bed, so that the porous carbon is in a fluidized suspension state. Then, the micro-jet auxiliary device 205 (nozzles arranged horizontally at 30° tangentially, nozzle diameter of 254 μm) is turned on, and N2 is introduced into the dense phase region as a secondary gas (gas flow rate controlled at 15% of the total fluidizing gas flow rate). The reaction temperature of the silicon deposition fluidized bed reactor 2 is controlled at 550℃. The silicon source gas (silane) and N2 are mixed in the gas mixer 10 (N2 to silane volume ratio of 4:1), and then enter the silicon deposition fluidized bed reactor 2 through the silicon source gas mixing inlet 11, so that the silane is cracked inside the porous carbon and silicon is deposited inside the porous carbon. The reaction time is controlled at 4 hours. During this period, the heat of reaction is accurately removed by the heat removal device 208 to ensure temperature uniformity and raw material activity. After the predetermined silicon content is reached, silicon-carbon anode material is obtained. In this embodiment, the reaction time and heat regulation are controlled by detecting the pressure change of the bed in the silicon deposition fluidized bed reactor 2 and the concentration of silane at the silane cracking tail gas.

[0139] See also Figure 1 The silicon-carbon anode material exits the silicon deposition fluidized bed reactor 2 through the silicon-carbon anode material outlet and then enters the carbon-coated fluidized bed reactor 3 through the silicon-carbon anode material inlet. N2 is introduced into the carbon-coated fluidized bed reactor 3 as a fluidizing gas (gas velocity controlled at 0.15 μmf) from the carbon-coated fluidized bed inert gas inlet, keeping the silicon-carbon anode material in a fluidized suspension state. Then, the micro-jet auxiliary device 305 (nozzles arranged horizontally at 30° tangentially, nozzle diameter 254 μm) is activated, introducing N2 as a secondary gas into the dense phase region (gas flow rate controlled at...). The reaction temperature of the carbon-coated fluidized bed reactor 3 is controlled at 580℃ (15% of the total fluidizing gas flow). The carbon source gas (acetylene) and N2 are mixed in the gas mixer 18 (N2 to acetylene volume ratio is 4:1), and then enter the carbon-coated fluidized bed reactor 3 through the carbon source gas mixture inlet 19. This causes the acetylene to crack and coat the surface of the silicon-carbon anode material. The reaction time is controlled at 4 hours. During this time, the heat of reaction is accurately removed through the heat extraction device 308 to ensure temperature and coating uniformity, resulting in carbon-coated silicon-carbon anode material. In this embodiment, the reaction time and heat regulation are controlled by detecting the pressure change in the bed layer of the carbon-coated fluidized bed reactor 3 and the acetylene concentration at the acetylene cracking tail gas. During this embodiment, after the silicon-carbon anode material leaves the silicon deposition fluidized bed reactor 2 through the silicon-carbon anode material outlet 15, the silicon deposition process is immediately repeated for the production of the next batch of silicon-carbon anode material.

[0140] See also Figure 1The carbon-coated silicon-carbon anode material exits the carbon-coated fluidized bed reactor 3 through the carbon-coated silicon-carbon anode material outlet, and then enters the final product cooling discharge device 4 through the carbon-coated silicon-carbon anode material inlet. N2 is introduced into the final product cooling discharge device 4 from the inert gas inlet of the final product cooling discharge system as a fluidizing gas (gas velocity controlled at 0.2 μmf) to keep the carbon-coated silicon-carbon anode material in a fluidized suspension state. Then, the micro-jet auxiliary device 405 (nozzles arranged horizontally at 30° tangentially, nozzle diameter of 254 μm) is turned on to introduce N2 into the dense phase region as a secondary gas (gas flow rate controlled at 15% of the total fluidizing gas flow rate). The particle cooling is accelerated by the heat extraction device 108. After cooling is completed, the product exits the final product cooling discharge device 4 through the final product outlet to obtain the final product. In this embodiment, after the carbon-coated silicon-carbon anode material leaves the carbon-coated fluidized bed reactor 3 through the carbon-coated silicon-carbon anode material outlet, the carbon coating process is immediately repeated to produce the next batch of carbon-coated silicon-carbon anode material. In this embodiment, after unloading is completed, the fluidized cooling process is immediately repeated to produce the next batch of final product.

[0141] See also Figure 1 The silane cracking tail gas is connected to the thermal oxidation system 13 and gas separator 14 via the silane cracking tail gas outlet, and the acetylene cracking tail gas is connected to the thermal oxidation system 21 and gas separator 22 via the acetylene cracking tail gas outlet. The resulting high-temperature N2 is connected to the high-temperature inert gas inlet via the high-temperature inert gas outlet 28, serving as the fluidizing gas for the silicon deposition fluidized bed reactor 2 and the carbon-coated fluidized bed reactor 3. Simultaneously, the heat from the separated high-temperature N2 is used to preheat the silane and acetylene in the gas mixers 10 and 18, controlling the silane and acetylene cracking temperatures or supplementing the heat, thus achieving gradient utilization of thermal energy. In this embodiment, the amount of silane and acetylene added is controlled to ensure near-complete cracking of the silane and acetylene.

[0142] In this embodiment, the gas-solid separation device periodically supplies N2 to the reactor through the backflushing inlet according to the pressure change in the fluidized bed, which is used to blow off the solid particles attached to the porous sintered filter element; in this embodiment, the pressure of the fluidizing gas is 0.4 MPa and the pressure of the secondary gas is 0.8 MPa.

[0143] Example 2

[0144] This embodiment relates to the reactor, reaction system, and method for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed proposed in this invention. The difference between this embodiment and Embodiment 1 is that the fluidizing gas velocity of the silicon deposition fluidized bed reactor 2 and the carbon coating fluidized bed reactor 3 is 0.2 μmf, the secondary gas flow rate of the inlet nozzle of the micro-assisted fluidization device is 20% of the total fluidizing gas flow rate, and the inlet nozzles are arranged in a horizontal radial configuration. The remaining steps are the same as in Embodiment 1.

[0145] Example 3

[0146] This embodiment relates to the reactor, reaction system, and method for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed proposed in this invention. The difference between this embodiment and Embodiment 1 is that the fluidizing gas velocity of the silicon deposition fluidized bed reactor 2 and the carbon coating fluidized bed reactor 3 is 0.25 μmf, the secondary gas flow rate of the inlet nozzle of the micro-assisted fluidization device is 25% of the total fluidizing gas flow rate, and the inlet nozzle is arranged at an upward 60° angle. The remaining steps are the same as in Embodiment 1.

[0147] Example 4

[0148] This embodiment relates to the reactor, reaction system, and method for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed proposed in this invention. The difference between this embodiment and Embodiment 1 is that the fluidizing gas velocity of the silicon deposition fluidized bed reactor 2 and the carbon coating fluidized bed reactor 3 is 0.3 μmf, the secondary gas flow rate of the inlet nozzle of the micro-assisted fluidization device is 30% of the total fluidizing gas flow rate, and the inlet nozzle is arranged at a downward 60° angle. The remaining steps are the same as in Embodiment 1.

[0149] This embodiment addresses the reactor, reaction system, and method for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed proposed in this invention. By designing a micro-jet auxiliary device on the outer wall of the reactor's dense phase zone, and using nozzle-based gas inlet, multi-dimensional gas disturbance is achieved, solving the problem of poor fluidization quality in porous carbon and improving the residence time and gas-solid contact efficiency of the raw materials. Simultaneously, a heat extraction device is added to the reactor, enabling precise heat transfer based on the high enthalpy generated during the high-temperature pyrolysis of silicon and carbon source gases. This reduces local hot spots in the fluidized bed reaction zone, ensuring uniformity of silicon deposition and carbon coating, thereby improving the electrochemical performance of the product. Furthermore, independent zoned temperature control is implemented within the fluidized bed, utilizing the heat of the process waste gas itself to preheat the process gas. This allows for faster reaction of the process gas within the fluidized bed and precise control of the pyrolysis temperature of the process gas or supplemental heat to the device, achieving gradient utilization of thermal energy and reducing overall production time and energy loss. The system features flexible heat transfer, continuous and efficient production, simple operation, high-quality mass production, high production safety, and low cost.

[0150] The detailed explanations of the above embodiments are intended only to explain the present invention so as to facilitate a better understanding of the present invention. However, these descriptions should not be construed as limiting the present invention for any reason. In particular, the various features described in different embodiments can be arbitrarily combined with each other to form other embodiments. Unless there is an explicit description to the contrary, these features should be understood to be applicable to any embodiment, and not limited to the described embodiments.

Claims

1. A reactor for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed, characterized in that, The reactor includes: The reactor body is hollow inside and forms a reaction chamber, which includes a pre-distribution section, a fluidized reaction zone, a partitioned fluidized reaction zone and a gas-solid separation zone arranged sequentially from bottom to top. The micro-jet auxiliary device includes an air intake module and multiple air intake nozzles. The multiple air intake nozzles are disposed in the fluidized reaction zone. The air intake module is connected to the multiple air intake nozzles and delivers turbulent airflow to the fluidized reaction zone through each air intake nozzle. The outlet diameter of the air intake nozzle is 120~520μm. The heat extraction device includes multiple heat extraction tubes disposed in the fluidized reaction zone. Both ends of each heat extraction tube are sealed and penetrate the side wall of the reactor body and extend out of the reactor body and are connected to a cooling medium source. The fluidized reaction zone includes a dense phase zone and a dilute phase zone disposed above the dense phase zone, and the plurality of air inlet nozzles are disposed in the dense phase zone.

2. The reactor for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed as described in claim 1, characterized in that, The plurality of air inlet nozzles are spaced apart along the axial and / or circumferential direction of the reactor body.

3. The reactor for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed as described in claim 1, characterized in that, The cooling medium source is either a liquid cooling medium source or an air cooling medium source.

4. The reactor for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed as described in claim 3, characterized in that, Multiple heat-extracting tubes are spaced apart along the axial and / or circumferential direction of the reactor body.

5. The reactor for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed as described in claim 1, characterized in that, The reactor also includes a heating device, which has multiple heating components installed on the reactor body and heating the fluidized reaction zone.

6. The reactor for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed as described in claim 5, characterized in that, The plurality of heating elements are disposed on the inner wall of the reactor body; or, the plurality of heating elements are disposed on the outer wall of the reactor body.

7. The reactor for producing silicon-carbon anode materials using a flexible heat transfer fluidized bed as described in claim 5, characterized in that, Multiple heating components are spaced apart along the axial and / or circumferential direction of the reactor body.

8. A reaction system for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed, characterized in that, The reaction system comprises sequentially connected: Raw material conveying device, used to convey porous carbon raw materials; A silicon deposition fluidized bed reactor is used to achieve silicon deposition inside the porous carbon raw material to obtain silicon-carbon anode material; A carbon-coated fluidized bed reactor is used to achieve surface carbon coating of the silicon-carbon anode material, thereby obtaining a carbon-coated silicon-carbon anode material. A cooling discharge device is used to perform fluidized cooling on the carbon-coated silicon-carbon anode material; Both the silicon deposition fluidized bed reactor and the carbon-coated fluidized bed reactor are reactors as described in any one of claims 1-7.

9. A method for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed, comprising the reaction system for producing silicon-carbon anode materials using a flexible heat-transfer fluidized bed as described in claim 8, characterized in that, The method for producing silicon-carbon anode materials includes: An inert gas is used as a fluidizing gas to keep the porous carbon in a fluidized suspension state. An inert gas or a mixture of an inert gas and a silicon source gas is used as a secondary gas. The secondary gas is introduced through an inlet nozzle with an outlet diameter of 120~520μm, and the porous carbon in a fluidized suspension state is disturbed by the secondary gas. The porous carbon in a fluidized suspension state is heated to a target temperature, and then a silicon source gas is introduced to cause the silicon source gas to decompose inside the porous carbon, thereby depositing silicon inside the porous carbon to obtain a silicon-carbon anode material. The silicon-carbon anode material is kept in a fluidized suspension state by the fluidizing gas. An inert gas or a mixture of an inert gas and a silicon source gas is used as a secondary gas. The secondary gas is introduced through an inlet nozzle with an outlet diameter of 120~520μm, and the silicon-carbon anode material in a fluidized suspension state is disturbed by the secondary gas. The silicon-carbon anode material in a fluidized suspension state is heated to a target temperature, and then a carbon source gas is introduced to cause the carbon source gas to decompose on the surface of the silicon-carbon anode material, so that carbon is coated on the surface of the silicon-carbon anode material, and carbon-coated silicon-carbon anode material is obtained. The carbon-coated silicon-carbon anode material is kept in a fluidized suspension state by the fluidizing gas, and the carbon-coated silicon-carbon anode material is gradually cooled.

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