A method and device for regenerating and recycling copper-containing battery negative electrode materials

Abstract

This invention relates to the field of battery anode material recycling technology, and discloses a method and apparatus for regenerating copper-containing battery anode materials. This recycling method includes: Step S1, initial screening of raw materials, where waste anode materials from used batteries or generated during production are screened to remove obvious impurities and non-metallic materials, yielding recycled raw materials; Step S2, aeration separation, where the recycled raw materials obtained in Step S1 are fed into an aeration separation device. After aeration separation, the liquid is a graphite-containing liquid, and the precipitate is a copper current collector; Step S3, separate recovery of the aeration-separated liquid and precipitate. This invention features a reasonable design, high separation efficiency, simple process flow, good environmental friendliness, and low recycling cost.

Description

Technical Field

[0001] This invention relates to the field of battery negative electrode material recycling technology, and in particular to a method and apparatus for regenerating and recycling copper-containing battery negative electrode materials. Background Technology

[0002] Used batteries are a major source of copper-containing negative electrode sheets. These batteries need to be recycled at the end of their lifespan to recover valuable metal components. Recycling copper and graphite from used batteries not only reduces resource waste but also lowers the production costs of new materials. At the same time, battery recycling helps reduce environmental pollution from waste, making it an important sustainable development measure.

[0003] With the deepening of the concept of resource recycling, the recycling of metal resources contained in waste batteries, especially copper and graphite, has gradually become a research hotspot. To recover these materials, they need to be separated from the batteries. Common separation methods include mechanical crushing and acid leaching, which can effectively separate copper foil and graphite. The separated copper foil and graphite need further separation to obtain high-purity final products. A common separation method is physical sieving, where a mixture of copper foil and graphite is fed into a sieving device with multiple screens. Vibration or rotation separates materials of different particle sizes, progressively screening out copper foil and graphite. However, this sieving method is inefficient, involves complex multi-stage screen operation, and easily causes environmental pollution.

[0004] Copper anode materials from spent batteries not only possess high recycling value but are also highly regarded in numerous industrial applications due to their superior performance in chemical catalysis and mass transfer. In particular, the oxidation of copper, producing copper oxide, is widely used in high-value-added fields such as catalytic reactions and electronic components due to its excellent chemical stability and multiphase catalytic activity. However, existing technologies for oxidizing pure copper to copper oxide generally face limitations such as high energy demand, low oxidation efficiency, and poor purity of the target product. These technological bottlenecks not only inhibit the possibility of efficiently converting copper resources into industrial-grade copper oxide but also restrict the sustainable production of low-energy-consumption and high-purity oxidation products during industrialization. To address these issues, it is urgent to introduce refined reaction control mechanisms into the oxidation process design and optimize energy transfer pathways to achieve optimal copper resource conversion and a breakthrough improvement in product performance. Summary of the Invention

[0005] The technical problem to be solved by the present invention is to overcome the shortcomings of the prior art and provide a method and device for regenerating and recycling copper-containing battery negative electrode materials.

[0006] The technical solution adopted by this invention to solve its technical problem is: a method for regenerating and recycling copper-containing battery negative electrode materials, specifically including the following steps:

[0007] Step S1: Initial screening of raw materials. Waste negative electrode materials from waste batteries or generated during the production process are screened to remove obvious impurities and non-metallic materials, thus obtaining recycled raw materials.

[0008] Step S2, aeration separation: The recovered raw material obtained in step S1 is fed into the aeration separation device. After the aeration separation is completed, the liquid is a graphite-containing liquid and the precipitate is a copper current collector.

[0009] Step S3: Recover the liquid and precipitate after aeration and separation respectively;

[0010] The liquid recovery includes:

[0011] Step S4: Sedimentation and separation. The graphite-containing liquid obtained in step S2 is introduced into a sedimentation tank. The clear liquid at the top of the sedimentation tank is returned to the aeration tank. The bottom of the sedimentation tank is graphite slurry.

[0012] Step S5: Two-stage gasification. The graphite slurry obtained in step S4 is mixed with water at a solid-liquid ratio of 1:1 and then fed into a first-stage gasification device. The first-stage gasification temperature is 300℃~400℃ and the first-stage gasification time is 1h~3h to remove moisture and organic impurities, resulting in dried graphite. Then, the dried graphite is fed into a second-stage gasification device. The second-stage gasification temperature is 2800℃~3000℃ and the second-stage gasification time is 2h~4h to remove metallic impurities, resulting in primary graphite.

[0013] Step S6: Ball milling. The primary graphite obtained in step S5 is placed in a ball mill. The ball milling time is 4 hours, the ball milling media ratio is 1:3, the rotation speed is controlled at 150 rpm, and the particle size after pulverization is required to reach D90<10μm.

[0014] Step S7: Repair graphite. Place the ball-milled graphite into a repair furnace, introduce a hydrogen atmosphere, repair at 800℃, repair for 2 hours. During the repair process, the hydrogen flow rate needs to be controlled at 100ml / min. After the repair is completed, the finished graphite is obtained.

[0015] The precipitate recovery includes:

[0016] Step S8: Dehydration. The precipitate obtained in step S2 is passed through a dehydration device to remove excess water, and a primary copper current collector is obtained.

[0017] Step S9: Crushing. The primary copper current collector obtained in step S8 is fed into the crushing equipment. The crusher speed is 500 rpm and the crushing time is 30 minutes. The copper particle size after crushing is less than or equal to 5 mm.

[0018] Step S10: Oxidation treatment. Copper particles are loaded into an oxidation furnace and oxidized to obtain copper oxide.

[0019] Step S11: Cool and collect to obtain the finished copper oxide.

[0020] Further, step S2, aeration separation, specifically involves: putting the recovered raw material obtained in step S1 into an aeration tank, adding pure water, maintaining a solid-liquid ratio of 1:2 to 1:4, starting the aeration equipment, and setting the air flow rate to 500 L / min to 700 L / min; during the aeration process, the stirring speed is 150 rpm to 250 rpm, the temperature is at room temperature, the aeration time is 2 h to 5 h, and the aeration separation ends.

[0021] Further, step S10, the oxidation treatment, specifically involves: loading the crushed copper particles into an oxidation furnace, introducing oxygen or air, maintaining an oxygen flow rate of 100L / min to 300L / min, an oxidation temperature of 450℃ to 550℃, and an oxidation time of 2h to 6h, to complete the oxidation reaction and obtain copper oxide.

[0022] A recycling device using the above-mentioned copper-containing battery negative electrode material regeneration and recycling method includes a screen and an aeration separation device arranged sequentially along the material travel direction. The aeration separation device is connected to a liquid recovery component and a sediment recovery component. The liquid recovery component includes a sedimentation tank, two-stage gasification equipment, a ball mill, a repair furnace, and a graphite collection tank arranged sequentially. The sediment recovery component includes a dehydration device, a crushing device, an oxidation furnace, a cooling device, and a copper oxide collection tank arranged sequentially. The aeration separation device is equipped with an inlet pipe at the top to facilitate the entry of pure water, and the sedimentation tank is equipped with a return pipe connected to the aeration separation device at the top.

[0023] Furthermore, the aeration separation device includes an aeration tank, which is divided into an aeration zone and a sedimentation zone by a partition. The upper end of the partition has a connecting hole that connects the aeration zone and the sedimentation zone. A feed pipe is provided at the upper end of the aeration tank, and a water inlet pipe is provided at the lower end of the aeration tank. Both the feed pipe and the water inlet pipe are connected to the aeration zone. An aeration assembly is provided in the aeration zone for supplying air to the aeration zone. A stirring assembly is provided on the aeration tank, with the stirring end of the stirring assembly extending into the aeration zone. A second extraction assembly for extracting the separated graphite floating matter is provided at the upper end of the sedimentation zone, and a first extraction assembly for extracting the separated copper sheets is provided at the lower end of the sedimentation zone.

[0024] Furthermore, the aeration assembly includes an air compressor, an air inlet pipe, and a central guide tube. The central guide tube is located within the aeration zone, and its lower end is connected to the air compressor via the air inlet pipe. The air compressor is located outside the lower end of the aeration tank.

[0025] Furthermore, the two-stage gasification equipment includes a first-stage gasification device, a transmission device, and a second-stage gasification device arranged sequentially. The first-stage gasification device includes a first gasifier, in which a furnace tube is rotatably installed. The graphite mixture to be heated enters from one end of the furnace tube. A first heater is arranged around the inner wall of the first gasifier, located outside the furnace tube. The second-stage gasification device includes a second gasifier, in which a heating chamber is opened. A furnace door is provided at the upper end of the second gasifier for adding graphite after the first stage of gasification. A second heater is arranged in the heating chamber. One end of the transmission device is connected to the other end of the furnace tube, and the other end of the transmission device is located above the furnace door. The graphite after the first stage of gasification is discharged from the other end of the furnace tube and transported to the heating chamber of the second gasifier through the transmission device.

[0026] Furthermore, the gasification device also includes a drive assembly, a first mounting base, and a first feed hopper. The drive assembly and the first gasifier are both mounted on the first mounting base. The upper end of the drive assembly is fitted onto the other end of the furnace tube. The drive assembly is used to drive the furnace tube to rotate. The first feed hopper is located on one end of the furnace tube.

[0027] Furthermore, the oxidation furnace includes a crusher assembly, an oxidation furnace assembly, and a cooling device. The oxidation furnace assembly includes a furnace body, a first drive mechanism, and an air inlet pipe. The first drive mechanism is used to drive the furnace body to rotate. Several stirring blades are spirally arranged on the inner wall of the furnace body. A heater is provided inside the furnace body. Valves for feeding and discharging are provided on the side wall of the furnace body. At least a portion of the crusher assembly is located above the valves, and at least a portion of the cooling device is located below the valves. One end of the air inlet pipe is connected to the furnace body. The crusher assembly includes a crushing chamber, a rotor, and an impact component. A crushing cavity is formed inside the crushing chamber. The rotor is rotatably arranged inside the crushing cavity. The impact component is arranged on the rotor and is used to collide with the material. A collision plate is provided inside the crushing cavity. The collision plate is arranged on one side of the rotor. After colliding with the impact component, the material hits the collision plate.

[0028] Furthermore, the first drive mechanism includes a first drive motor, a first drive wheel, a first driven wheel, a first connecting shaft, and a first belt. The first drive wheel is mounted on the motor shaft of the first drive motor. The first drive wheel and the first driven wheel are driven by the first belt. The two ends of the first connecting shaft are respectively connected to the first driven wheel and the furnace body.

[0029] The beneficial effects of this invention are as follows: This invention is rationally designed and has the following advantages:

[0030] (1) The recycling method has high separation efficiency, simple process flow, good environmental protection and low recycling cost;

[0031] (2) In the aeration separation device, the aeration tank is divided into an aeration zone and a sedimentation zone by setting a partition. Then, with the help of the stirring component and the aeration component, the copper negative electrode raw material can achieve the effect of separating the copper sheet from the graphite powder. After the aeration is completed, the liquid containing graphite floating matter and copper sheet enters the sedimentation zone through the connecting hole and settles in the sedimentation zone. After sedimentation, the graphite floating matter floats on the liquid surface, while the heavier copper sheet sinks to the bottom of the sedimentation zone, which can make the copper sheet and graphite powder fully separated.

[0032] (3) In the two-stage gasification equipment, the first gasifier, the first heater, and the rotatable furnace tube dry the moisture in the graphite obtained from aeration separation and remove organic impurities, keeping the graphite in a dry state. A transmission device is set up for cooling. The graphite after the first stage of gasification needs to be cooled to prevent thermal shock when it directly enters the high-temperature second stage of gasification. The second gasifier and the second heater further remove excess metal impurities from the graphite and perform secondary graphitization to improve the purity and performance of the graphite. Removing moisture and organic impurities at a lower temperature avoids the energy waste and unnecessary complexity of high-temperature treatment. By removing most of the impurities at a lower temperature first, the time and energy required for high-temperature treatment can be reduced, saving energy and reducing costs. The two-stage gasification process is more energy-efficient than single high-temperature treatment. Approximately 25% of energy is used; organic matter is removed at low temperatures to avoid the decomposition at high temperatures that would produce harmful gases such as dioxins, thus reducing air pollution and protecting the environment; gradual heating can prevent excessive sintering of materials or other forms of thermal damage, improving the quality of the final product; at high temperatures, metallic impurities can be completely removed, and the high-temperature conditions help optimize the crystal structure of graphite, improving its purity and performance; gradual heating can reduce the heat load and stress on equipment, extend equipment life, and reduce maintenance and replacement costs; staged gasification allows for better control of the reaction process and parameters at each stage, ensuring the stability and controllability of the process, especially at high temperatures, ensuring optimal treatment results; and by gradually heating in stages, the risk of sudden thermal reactions and equipment failures can be reduced, improving the overall safety of the process.

[0033] (4) In the oxidation furnace, this oxidation device first crushes the pure copper obtained from aeration separation. The crushed pure copper particles are more uniform, increasing the contact area between copper and working gas, which is beneficial for subsequent oxidation treatment. Then, the oxidation furnace is preheated to ensure a stable oxidation environment inside the furnace. The crushed pure copper particles are evenly loaded into the furnace body. With the cooperation of the stirring blades, the copper particles are evenly distributed, ensuring that the particles are heated more evenly to improve the oxidation efficiency. Oxidation treatment is carried out under these parameters to ensure that the pure copper particles are fully in contact with the working gas, reducing the oxidation time from 8 hours to 4 hours and the processing energy consumption from 800 kWh to 400 kWh, a reduction of about 50% in energy consumption. The purity of copper oxide is increased from 95% to 99%, which has the advantages of low energy consumption, high oxidation efficiency, and high copper oxide purity. Attached Figure Description

[0034] To more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0035] Figure 1 This is a flowchart of the recycling method in this invention;

[0036] Figure 2 This is a schematic diagram of the recycling device in this invention;

[0037] Figure 3 This is a schematic diagram of the aeration separation device in this invention;

[0038] Figure 4 yes Figure 3 Top view;

[0039] Figure 5 yes Figure 4 Sectional view at point AA;

[0040] Figure 6 This is a schematic diagram of the separation principle of the aeration separation device in this invention;

[0041] Figure 7 This is a schematic diagram of the two-stage gasification device in this invention;

[0042] Figure 8 yes Figure 7 A partial sectional view;

[0043] Figure 9 This is a schematic diagram of the structure of a gasification device in this invention;

[0044] Figure 10This is a schematic diagram of the two-stage gasification equipment in this invention;

[0045] Figure 11 yes Figure 10 A sectional view;

[0046] Figure 12 This is a schematic diagram of the oxidation furnace in this invention;

[0047] Figure 13 yes Figure 12 Top view;

[0048] Figure 14 yes Figure 13 Sectional view at point BB;

[0049] Figure 15 yes Figure 12 The left view.

[0050] In the diagram: 1. Screen, 2. Aeration and separation device, 3. Inlet pipe, 4. Sedimentation tank, 5. Two-stage gasification equipment, 6. Ball mill, 7. Repair furnace, 8. Dewatering equipment, 9. Crushing equipment, 10. Oxidation furnace, 11. Cooling equipment, 12. Graphite collection tank, 13. Copper oxide collection tank; 2-1. Aeration tank, 2-2. Baffle plate, 2-3. Aeration zone, 2-4. Sedimentation zone, 2-5. Connecting hole, 2-6. Feed pipe, 2-8. Air compressor, 2-9. Air inlet pipe, 2-10. Central guide tube, 2-11. Vent hole, 2-12. Agitator motor, 2-13. Agitator motor mounting base, 2-14. Bearing, 2-15. Agitator shaft, 2-16. Agitator impeller, 2-17. 2-18. First pump; 2-19. First discharge pipe; 2-20. Graphite collection tank; 2-21. Second pump; 2-22. Second discharge pipe; 2-23. Inclined guide plate; 2-24. Separation tank support base; 2-25. Hopper; 5-1. First gasifier; 5-2. Furnace tube; 5-3. First heater; 5-4. Second gasifier; 5-5. Heating chamber; 5-6. Furnace door; 5-7. Second heater; 5-8. First mounting base; 5-9. First feed hopper; 5-10. Driven wheel; 5-11. Drive wheel; 5-12. Drive motor; 5-13. Motor mounting base; 5-14. Handle; 5-15. Intermediate buffer tank; 5-16. Conveyor; 5-17. Support. 5-18. Conveying bin, 5-19. Second feed hopper, 5-20. Vent pipe, 5-21. Conveying structure, 5-22. Feeding trolley, 5-23. Conveying track, 5-24. Gasification chamber; 10-1. Crusher assembly, 10-2. Oxidizer assembly, 10-4. Furnace body, 10-6. Oxidation air inlet pipe, 10-7. Stirring blade, 10-8. Valve, 10-9. Crushing bin, 10-10. Rotor, 10-11. Impact component, 10-12. Crushing chamber, 10-13. Collision plate, 10-14. First drive motor, 10-15. First driving wheel, 10-16. First driven wheel, 10-17. First connecting shaft, 10-18. First belt, 10-19. Support base; 10-20. First bearing housing; 10-21. Feed inlet; 10-22. Discharge outlet; 10-23. Second drive motor; 10-24. Second drive wheel; 10-25. Second driven wheel; 10-26. Second connecting shaft; 10-27. Second belt; 10-28. Second bearing housing; 10-29. Bracket; 10-30. Discharge hopper; 10-31. Screening cylinder; 10-32. Guide plate; 10-33. Conveyor belt; 10-34. Feed inlet; 10-35. Discharge outlet; 10-36. Third drive motor; 10-37. Third bearing housing; 10-38. Support frame; 10-39. Conveying roller; 10-40. Conveyor belt. Detailed Implementation

[0051] The following will clearly and completely describe the technical solutions of the present invention in conjunction with the embodiments. Obviously, the embodiments described are only some embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of the present invention.

[0052] like Figure 2 The recycling device shown is a recycling method using copper-containing battery negative electrode material. Along the material travel direction, a screen 1 and an aeration separation device 2 are arranged in sequence. The aeration separation device 2 is connected to a liquid recovery component and a sediment recovery component. The liquid recovery component includes a sedimentation tank 4, a two-stage gasification device 5, a ball mill 6, a repair furnace 7, and a graphite collection tank 12 arranged in sequence. The sediment recovery component includes a dehydration device 8, a crushing device 9, an oxidation furnace 10, a cooling device 11, and a copper oxide collection tank 13 arranged in sequence. The top of the aeration separation device 2 is provided with an inlet pipe 3 to facilitate the entry of pure water, and the top of the sedimentation tank 4 is provided with a return pipe connected to the aeration separation device 2.

[0053] like Figures 3-6 The aeration separation device 2 shown includes an aeration tank 2-1. A partition 2-2 is installed inside the aeration tank 2-1 to divide the aeration tank 2-1 into an aeration zone 2-3 and a sedimentation zone 2-4. A connecting hole 2-5 is opened at the upper end of the partition 2-2 to connect the aeration zone 2-3 and the sedimentation zone 2-4. A feed pipe 2-6 is installed at the upper end of the aeration tank 2-1, and a water inlet pipe 3 is installed at the lower end of the aeration tank 2-1. Both the feed pipe 2-6 and the water inlet pipe 3 are connected to the aeration zone 2-3. An aeration component is installed inside the aeration zone 2-3 for supplying air to the aeration zone 2-3.

[0054] An agitator is installed on the aeration tank 2-1, with the agitator end extending into the aeration zone 2-3. A second extraction component for extracting the separated graphite floating matter is installed at the upper end of the sedimentation zone 2-4, and a first extraction component for extracting the separated copper sheets is installed at the lower end of the sedimentation zone 2-4.

[0055] By setting up a partition 2-2, the aeration tank 2-1 is divided into an aeration zone 2-3 and a sedimentation zone 2-4. With the help of a stirring component and an aeration component, the copper-containing negative electrode raw material can achieve the effect of separating copper sheets from graphite powder. After aeration, the liquid containing graphite floating matter and copper sheets enters the sedimentation zone 2-4 through the connecting hole 2-5 and settles in the sedimentation zone 2-4. After sedimentation, the graphite floating matter floats on the liquid surface, while the heavier copper sheets sink to the bottom of the sedimentation zone 2-4, which can fully separate the copper sheets from the graphite powder.

[0056] The aeration assembly includes an air compressor 2-8, an air inlet pipe 2-9, and a central guide tube 2-10. The central guide tube 2-10 is located within the aeration zone 2-3. The lower end of the central guide tube 2-10 is connected to the air compressor 2-8 via the air inlet pipe 2-9. The air compressor 2-8 is located outside the lower end of the aeration tank 2-1. Several ventilation holes 2-11 are provided on the side wall of the central guide tube 2-10, connecting the interior of the central guide tube 2-10 with the aeration zone 2-3.

[0057] The copper-containing negative electrode raw material and pure water are mixed and placed in the aeration zone 2-3. Air is continuously injected into the aeration zone 2-3 by the air compressor 2-8. Due to the different motion characteristics of materials with different densities in the gas-liquid two-phase flow, the lighter materials will be carried to the liquid surface by the airflow, while the heavier materials will sink to the bottom of the pool.

[0058] The mixing assembly includes a mixing motor 2-12, a mixing motor mounting base 2-13, a bearing 2-14, a mixing shaft 2-15, and a mixing impeller 2-16. The mixing motor 2-12 is mounted on the mixing motor mounting base 2-13, which is located at the upper end of the aeration tank 2-1 and above the aeration zone 2-3. The upper end of the mixing shaft 2-15 is connected to the motor shaft of the mixing motor 2-12, and the lower end of the mixing shaft 2-15 extends into the aeration zone 2-3. The mixing impeller 2-16 is located at the lower end of the mixing shaft 2-15.

[0059] The stirring motor 2-12 drives the stirring impeller 2-16 to rotate, thereby achieving the stirring effect. Stirring can enhance the contact and mixing between the solids in the liquid and the gas flow, improve the uniformity of the gas-liquid two-phase flow, and help improve the separation effect. It can also change the flow characteristics of the liquid, such as the flow rate, thereby affecting the generation, rising and breaking of bubbles, and thus adjusting the separation effect.

[0060] The first extraction assembly includes a first pump 2-17 and a first discharge pipe 2-18. One end of the first discharge pipe 2-18 is connected to the first pump 2-17, and the other end extends into the lower end of the sedimentation zone 2-4 for extracting the separated copper sheets. The separated copper sheets that have sunk to the bottom of the tank are extracted by the first pump 2-17 and the first discharge pipe 2-18 and then subjected to subsequent crushing.

[0061] The second extraction assembly includes a graphite collection tank 2-19, a second pump 2-20, and a second discharge pipe 2-21. One end of the second discharge pipe 2-21 is connected to the graphite collection tank 2-19, and the other end extends into the upper end of the sedimentation zone 2-4 for extracting the separated graphite floating matter. The second pump 2-20 is installed on the second discharge pipe 2-21. The second pump 2-20 and the second discharge pipe 2-21 extract the graphite floating matter on the liquid surface into the graphite collection tank 2-19 for further processing.

[0062] An inclined guide plate 2-22 is formed within the sedimentation zone 2-4, and the inclined guide plate 2-22 is inclined downward from the upper end to the lower end of the sedimentation zone 2-4. The design of the inclined guide plate 2-22 serves a guiding function, allowing the copper sheet to sink to the bottom of the pool better, facilitating subsequent extraction.

[0063] The aeration separation device 2 also includes several support bases 2-23, which are located at the lower end of the aeration tank 2-1; the aeration separation device 2 also includes a hopper 2-24 for feeding copper negative electrode raw materials, and the lower end of the hopper 2-24 is connected to the feed pipe 2-6.

[0064] The separation steps of the aeration separation device 2 are as follows:

[0065] Step S21: The copper-containing negative electrode raw material is fed into the aeration zone 2-3 through the feed pipe 2-6;

[0066] Step S22: Add pure water into aeration zone 2-3 through water inlet pipe 3. The ratio of copper-containing negative electrode raw material to pure water added in step S21 is 1:2 to 1:4.

[0067] Step S23: Start the air compressor 2-8. Air enters the central guide tube 2-10 through the air inlet pipe 2-9 and enters the aeration zone 2-3 through several air vents 2-11 on the central guide tube 2-10. Set the air flow rate to 500L / min~700L / min.

[0068] Step S24: Start the stirring motor 2-12, which drives the stirring shaft 2-15 to rotate and in turn drives the stirring impeller 2-16 to rotate. Set the stirring speed to 150 rpm to 250 rpm.

[0069] Step S25: Maintain a constant temperature of 25°C and set the aeration time to two hours, i.e., run steps S23 and S24 for 2 to 5 hours.

[0070] Step S26: The liquid containing graphite floats and copper flakes enters the sedimentation zone 2-4 through the connecting hole 2-5 and settles in the sedimentation zone 2-4. After sedimentation, the graphite floats on the liquid surface, while the heavier copper flakes sink to the bottom of the sedimentation zone 2-4.

[0071] Step S27: Start the second pump 2-20 to extract the graphite floating matter through the second discharge pipe 2-21 into the graphite collection tank 2-19 for further processing;

[0072] Step S28: Start the first pump 2-17 to discharge the copper sheets from the first discharge pipe 2-18 and collect them for the next crushing process.

[0073] After aeration, graphite, due to its lower density, floats on the liquid surface, while the heavier copper sheets sink to the bottom. The aeration separation process can fully separate the copper sheets from the graphite powder. This method not only improves separation efficiency but also reduces operational complexity and environmental pollution, making it the preferred process for treating copper-containing negative electrode sheets.

[0074] like Figures 7-11 The two-stage gasification device 5 shown includes a first-stage gasification device, a transmission device, and a second-stage gasification device arranged in sequence. The first-stage gasification device includes a first gasifier 5-1, in which a furnace tube 5-2 is rotatably installed. The graphite mixture to be heated enters from one end of the furnace tube 5-2. A first heater 5-3 is arranged around the inner wall of the first gasifier 5-1, located outside the furnace tube 5-2. The second-stage gasification device includes a second gasifier 5-4, in which a heating chamber 5-5 is opened. A furnace door 5-6 for adding graphite after the first stage of gasification is provided at the upper end of the second gasifier 5-4. A second heater 5-7 is arranged in the heating chamber 5-5. One end of the transmission device is connected to the other end of the furnace tube 5-2, and the other end of the transmission device is located above the furnace door 5-6. The graphite after the first stage of gasification is discharged from the other end of the furnace tube 5-2 and transported to the heating chamber 5-5 of the second gasifier 5-4 through the transmission device.

[0075] The graphite obtained from aeration separation is dried by the first gasifier 5-1, the first heater 5-3, and the rotatable furnace tube 5-2, and organic impurities are removed to keep the graphite in a dry state. The graphite after the first gasification needs to be cooled by a transmission device to prevent thermal shock when it directly enters the high-temperature second gasification stage. The graphite is further removed by the second gasifier 5-4 and the second heater 5-7, and a second graphitization process is carried out to improve the purity and performance of the graphite.

[0076] The gasification equipment also includes a drive assembly, a first mounting base 5-8 and a first feed hopper 5-9. The drive assembly and the first gasifier 5-1 are both mounted on the first mounting base 5-8. The upper end of the drive assembly is fitted onto the other end of the furnace tube 5-2. The drive assembly is used to drive the furnace tube 5-2 to rotate. The first feed hopper 5-9 is located on one end of the furnace tube 5-2.

[0077] The drive assembly includes a driven wheel 5-10 and two drive units, which are respectively located on both sides of the driven wheel 5-10. Each drive unit includes a drive wheel 5-11, a drive motor 5-12, and a motor mounting base 13. The driven wheel 5-10 is sleeved on the other end of the furnace tube 5-2. The drive wheel 5-11 is mounted on the moving end of the drive motor 5-12 and meshes with the driven wheel 5-10 for transmission. The drive motor 5-12 is mounted on the motor mounting base 5-13, which is mounted on the first mounting base 5-8. The transmission structure using the driven wheel 5-10 and drive wheel 5-11 is simple, has strong resistance to impact and vibration, a long service life, high reliability, lower noise, and smoother transmission. The passive wheel and drive wheel transmission can drive the furnace tube 5-2 to rotate 360°, which is suitable for the uniform sintering of graphite.

[0078] The axis of the furnace tube 5-2 is inclined downwards towards the conveying equipment. The axis of the moving end of the drive motor 5-12 is parallel to the axis of the furnace tube 5-2. The two drive wheels 5-11 rotate in the same direction, while the drive wheels 5-11 and the driven wheels 5-10 rotate in opposite directions. The inclined furnace tube 5-2 facilitates material discharge.

[0079] The second gasifier 5-4 is an ultra-high temperature induction heating furnace. The second heater 5-7 includes an electromagnetic induction heating coil and a heating controller. The heating controller is installed on the second gasifier 5-4. The electromagnetic induction heating coil is spiral-shaped and located only inside the heating chamber 5-5. A handle 5-14 is provided on the furnace door 5-6 of the second gasifier 5-4.

[0080] The transmission equipment includes an intermediate buffer tank 5-15 and a conveyor 5-16 connected in sequence. One end of the intermediate buffer tank 5-15 is connected to the other end of the furnace tube 5-2 through a first feed pipe, and the other end of the intermediate buffer tank 5-15 is connected to one end of the conveyor 5-16 through a first discharge pipe. The other end of the conveyor 5-16 is located above the furnace door 5-6. The transmission equipment is used for cooling, as the graphite after the first stage of gasification needs to be cooled to prevent thermal shock during direct entry into the high-temperature second stage of gasification. The intermediate buffer tank 5-15 is used to temporarily store the graphite after the first stage of gasification.

[0081] The conveyor 5-16 includes a support base 5-17, a conveying bin 5-18, a second feed hopper 5-19, a vent pipe 5-20, and a conveying structure 5-21. The conveying bin 5-18 is installed on the support base 5-17. A transport channel is opened inside the conveying bin 5-18 from the intermediate buffer tank 5-15 toward the furnace door 5-6. The conveying structure 5-21 is set in the transport channel to transport graphite to the second gasifier 5-4. The second feed hopper 5-19 is set at one end of the conveying bin 5-18 and is connected to the first discharge pipe. A drop pipe is set at the lower end of the other end of the conveying bin 5-18 and is set above the furnace door 5-6. The vent pipe 5-20 connects from the outside of the conveying bin 5-18 to the conveying channel. A section of gasified graphite is transported to the second gasifier 5-4 using a conveyor structure 5-21. During the transport process, inert gas is introduced into the conveying chamber 5-18 through a vent pipe 5-20 to prevent oxidation. The conveyor structure 5-21 can be a conveyor belt or a spiral conveyor shaft, and a high-temperature resistant conveyor belt can be used.

[0082] A gasification unit also includes: a feeding trolley 5-22, a conveying track 5-23, and a gasification chamber 5-24. The first gasifier 5-1 is located inside the gasification chamber 5-24. The conveying track 5-23 is laid from the outside of the gasification chamber 5-24 to below one end of the first gasifier 5-1. The feeding trolley 5-22 is slidably connected to the conveying track 5-23.

[0083] The gasification process of the two-stage gasification unit 5 removes graphite and metal impurities, including the following steps:

[0084] Step S51: After the graphite mixture to be heated is fed to one end of the furnace tube 5-2 by the feeding trolley 5-22, the unloaded feeding trolley 5-22 exits the gasification chamber 5-24 and the door of the gasification chamber 5-24 is closed.

[0085] Step S52: Turn on the first heater 5-3 and adjust the first heater 5-3 to the heating temperature required for the first stage of gasification through the external temperature control system. Set the first stage gasification temperature to 300℃~400℃. Turn on the drive motor 5-12 and drive the furnace tube 5-2 to rotate through the driven wheel 5-10 and the drive wheel 5-11. Set the first stage gasification time to 1h~3h.

[0086] Step S53: The graphite obtained in step S52, after removing moisture and organic impurities, is fed into the intermediate buffer tank 5-15 through the first feed pipe for cooling.

[0087] Step S54: After being cooled in step S53, the graphite enters the conveying chamber 5-18 through the first discharge pipe and the second feed hopper 5-19. The graphite is then conveyed from the discharge pipe to the second gasifier 5-4 through the conveying structure 5-21. At the same time, inert gas is introduced into the conveying chamber 5-18 through the vent pipe 5-20.

[0088] Step S55: Close the furnace door 5-6, turn on the second heater 5-7, and adjust the second heater 5-7 to the heating temperature required for the second stage gasification through the external temperature control system. Set the second stage gasification temperature to 2800℃~3000℃ and the second stage gasification time to 2h~4h.

[0089] Step S56: After the second-stage gasification in step S55, graphite with metal impurities removed is obtained.

[0090] Removing moisture and organic impurities at lower temperatures avoids the energy waste and unnecessary complexity of high-temperature processing; removing organic matter at low temperatures prevents the decomposition of harmful gases such as dioxins at high temperatures, reducing air pollution and protecting the environment; gradual heating avoids excessive sintering or other forms of thermal damage to materials, improving the quality of the final product; at high temperatures, metallic impurities can be completely removed, and the high-temperature conditions help optimize the crystal structure of graphite, improving its purity and performance; by removing most impurities at lower temperatures first, the time and energy required for high-temperature processing can be reduced, saving energy and lowering costs. Using a two-stage gasification process saves approximately 25% of energy compared to single-stage high-temperature processing; gradual heating reduces the thermal load and stress on equipment, extending equipment lifespan and reducing maintenance and replacement costs; staged gasification allows for better control of the reaction process and parameters at each processing stage, ensuring the stability and controllability of the processing, especially at high temperatures, ensuring optimal processing results; and staged gradual heating reduces the risk of sudden thermal reactions and equipment failures, improving the overall safety of the process.

[0091] The purpose of setting the vaporization temperature of the first stage to 300℃~400℃ is:

[0092] (1) Moisture removal: Within a temperature range of 300℃ to 400℃, the moisture in the material will be effectively evaporated and removed. This step is crucial to prevent the risk of rapid vaporization and explosion at higher temperatures (such as 2800℃). By removing moisture, damage to equipment and changes in the material's structure can be avoided;

[0093] (2) Decompose low-temperature volatile organic impurities. In copper-containing anode materials, there may be some residual binders (such as PVDF) and solvents (such as NMP). These substances can be removed by pyrolysis or evaporation in the range of 300℃~400℃, thereby reducing their interference and the generation of harmful gases during high-temperature processing.

[0094] (3) Reduce energy consumption. Removing volatile organic impurities and moisture at lower temperatures can reduce the energy consumption of subsequent high-temperature treatment. If the treatment is carried out directly at high temperatures, all volatile components will consume more energy to vaporize. By pre-treating at low temperatures, the energy consumption of the high-temperature stage can be reduced, making the overall process more energy-efficient (e.g., from 800kWh to 400kWh).

[0095] Additionally, PVDF (polyvinylidene fluoride): PVDF begins to thermally decompose within the temperature range of 300℃ to 400℃, producing hydrofluoric acid (HF) and some low-molecular-weight fluorinated organic compounds (such as fluorinated hydrocarbons). Due to the relatively low temperature, this decomposition reaction is relatively slow, producing fewer byproducts, mainly hydrofluoric acid (HF) and small amounts of gases such as tetrafluoroethylene. Decomposition under these temperature conditions avoids violent reactions at higher temperatures and controls the amount of harmful gases generated.

[0096] Removal efficiency: At 300℃~400℃, the pyrolysis of PVDF is relatively mild and the removal efficiency is high, but it will produce a certain amount of HF gas and other volatile organic compounds. An effective gas treatment system is needed to capture these harmful gases.

[0097] If PVDF is directly treated at a high temperature of 1700℃, it will undergo violent pyrolysis and combustion, generating more fluorides (such as hydrofluoric acid HF) and some more complex fluorocarbons. This high-temperature decomposition reaction is extremely rapid and may lead to the production of large amounts of toxic gases (such as HF and carbon tetrafluoride). Furthermore, the high temperature of 1700℃ may also cause equipment corrosion and other uncontrollable side reactions.

[0098] Removal effect: Although high temperature can ensure the complete removal of PVDF, it will produce more harmful byproducts, such as hydrofluoric acid and other toxic fluorides. It is very important to control the emission of these harmful substances.

[0099] NMP (N-methylpyrrolidone): NMP also undergoes pyrolysis in the temperature range of 300℃ to 400℃, generating some nitrogen oxides (NO). x NMP contains carbon monoxide (CO), carbon dioxide (CO2), and other low-molecular-weight nitrogen-containing organic compounds. NMP decomposes at a relatively low temperature, therefore, within this temperature range, most NMP is removed by evaporation or pyrolysis.

[0100] Removal efficiency: Within this temperature range, NMP can be removed relatively effectively with relatively little harmful gas production. Lower temperatures can reduce the formation of toxic byproducts.

[0101] If treated directly at a high temperature of 1700℃, NMP will be completely burned or decomposed into simple molecules such as carbon dioxide (CO2), water (H2O), and nitrogen oxides (NO). x The reaction produces nitrogen oxides (NOx) and carbon monoxide (CO). Due to the extremely high temperature, the decomposition reaction is very thorough, but it may also produce large amounts of nitrogen oxides, which are highly harmful to the environment and health.

[0102] Removal effect: NMP can be completely removed at high temperatures, but it will produce a large amount of gases such as nitrogen oxides and carbon monoxide, requiring strict gas treatment and monitoring measures.

[0103] Therefore, in summary, compared to processing directly at a high temperature of 1700℃, the advantages of setting the first-stage vaporization temperature to 300℃~400℃ are as follows:

[0104] Removal efficiency: At a high temperature of 1700℃, PVDF and NMP decompose more completely, but this produces a large amount of harmful gases, such as hydrofluoric acid (HF) and nitrogen oxides (NOx). x (etc.) At 300℃~400℃, although the removal efficiency is slightly lower, it can better control the generation of harmful gases and reduce the impact on the environment;

[0105] Energy consumption: The energy required for temperature conditions of 300℃~400℃ is much lower than that for 1700℃, so using a lower temperature pretreatment can significantly reduce the overall energy consumption;

[0106] Equipment wear and safety: A high temperature of 1700℃ increases the heat load on the equipment, which may lead to corrosion or damage to the furnace body. In contrast, a processing temperature of 300℃~400℃ is more moderate, causing less wear and tear on the equipment and ensuring higher safety.

[0107] The purpose of setting the second-stage vaporization temperature to 2800℃~3000℃ is:

[0108] (1) Achieving secondary graphitization, the temperature requirements for secondary graphitization: Graphitization is usually carried out at high temperatures of 2000℃~3000℃. The graphitization process requires sufficiently high temperatures to break the disordered structure in carbon materials, causing carbon atoms to rearrange into a highly ordered graphite layer structure. Graphitization at 2800℃ or above will be more thorough, significantly improving the crystallinity and purity of graphite, making it suitable for high-performance applications;

[0109] (2) Removal of metallic impurities: Most metallic impurities, such as copper, iron, and nickel, have high boiling points. Higher temperatures are required to evaporate or oxidize these metals into a removable form. For example, copper has a boiling point of 2562℃, iron 2862℃, and nickel 2913℃. Therefore, temperatures of at least 2800℃ to 3000℃ or higher are necessary to effectively remove these metallic impurities.

[0110] In addition, at temperatures of 2800℃~3000℃ or higher, not only can secondary graphitization be fully achieved, but all possible metallic impurities and other non-metallic impurities (such as sulfur, phosphorus, etc.) can also be oxidized or volatilized, ultimately obtaining high-purity graphite.

[0111] like Figures 12-15 The oxidation furnace 10 shown includes a crusher assembly 10-1, an oxidation furnace assembly 10-2, and a cooling device 11. The oxidation furnace assembly 10-2 includes a furnace body 10-4, a first drive mechanism, and an oxidation inlet pipe 10-6. The first drive mechanism is used to drive the furnace body 10-4 to rotate. Several stirring blades 10-7 are spirally arranged on the inner wall of the furnace body 10-4. A heater is provided inside the furnace body 10-4. A valve 10-8 for feeding and discharging is provided on the side wall of the furnace body 10-4. At least a part of the crusher assembly 10-1 is located above the valve 10-8, and at least a part of the cooling device 11 is located below the valve 10-8. One end of the inlet pipe 10-6 is connected to the furnace body 10-4.

[0112] The crusher assembly 10-1 includes a crushing chamber 10-9, a rotor 10-10, and an impact component 10-11. A crushing cavity 10-12 is formed inside the crushing chamber 10-9. The rotor 10-10 is rotatably disposed inside the crushing cavity 10-12. The impact component 10-11 is disposed on the rotor 10-10 and is used to collide with the material. A collision plate 10-13 is disposed inside the crushing cavity 10-12. The collision plate 10-13 is disposed on one side of the rotor 10-10. After colliding with the impact component 10-11, the material hits the collision plate 10-13.

[0113] The rotor 10-10 rotates, causing the impact component 10-11 to rotate as well. This causes the pure copper to be broken by the impact component 10-11. The broken pure copper is then thrown onto the collision plate 10-13 under the action of centrifugal force, where it is further broken down to a particle size of less than or equal to 5 mm. This makes the broken pure copper particles more uniform, which is beneficial for subsequent oxidation treatment. By setting a rotating furnace body 10-4 and spirally arranging several stirring blades 10-7 on the inner wall of the furnace body 10-4, the distribution of copper particles is ensured to be uniform, and the particles are heated more evenly. This allows the particles to fully contact the working gas inside the furnace body 10-4 to complete the oxidation reaction.

[0114] The first drive mechanism includes a first drive motor 10-14, a first driving wheel 10-15, a first driven wheel 10-16, a first connecting shaft 10-17, and a first belt 10-18. The first driving wheel 10-15 is mounted on the motor shaft of the first drive motor 10-14. The first driving wheel 10-15 and the first driven wheel 10-16 are driven by the first belt 10-18. The two ends of the first connecting shaft 10-17 are connected to the first driven wheel 10-16 and the furnace body 10-4, respectively. By setting the first drive motor 10-14 and the belt drive, the furnace body 10-4 can rotate during the oxidation reaction, making the pure copper particles inside the furnace body 10-4 more evenly heated.

[0115] The oxidation furnace assembly 10-2 also includes two support bases 10-19 and two first bearing seats 10-20. The two first bearing seats 10-20 are respectively disposed on the support bases 10-19 and located at both ends of the furnace body 10-4. The first connecting shaft 10-17 is mounted on one of the first bearing seats 10-20 via bearings, and the oxidation inlet pipe 10-6 is mounted on the other first bearing seat 10-20 via bearings. The upper end of the crushing chamber 10-9 has a feed inlet 10-21, and the lower end of the crushing chamber 10-9 has a discharge outlet 22. The crusher assembly 10-1 also includes two second drive mechanisms and a screening and conveying assembly. The two second drive mechanisms are respectively located on both sides outside the crushing chamber 10-9 and connected to both ends of the rotor 10-10. The two drive mechanisms are used to drive the rotor 10-10 to rotate. The screening and conveying assembly is disposed below the discharge port 10-35 and is used to receive the crushed material. One end of the screening and conveying assembly extends above the valve 10-8.

[0116] Each second drive mechanism includes a second drive motor 10-23, a second drive wheel 10-24, a second driven wheel 10-25, a second connecting shaft 10-26, a second belt 10-27, and a second bearing housing 10-28. The second drive wheel 10-24 is mounted on the motor shaft of the second drive motor 10-23. The second drive wheel 10-24 and the second driven wheel 10-25 are driven by the second belt 10-27. The two ends of the second connecting shaft 10-26 are connected to the second driven wheel 10-25 and the rotor 10-10, respectively. The second bearing housing 10-28 is mounted on the outer wall of the crushing chamber 10-9. The second connecting shaft 10-26 is mounted on the second bearing housing 10-28 by bearings. By setting a second drive motor 10-23 and a belt drive, the rotor 10-10 can rotate at high speed, causing the impact component 10-11 to collide with the pure copper material at high speed to break the pure copper material. Moreover, the pure copper material that is not broken thoroughly is thrown out by centrifugal force and thrown onto the collision plate 10-13 for further impact and breakage.

[0117] The screening and conveying assembly includes a support frame 10-29, a discharge bin 10-30, a screening cylinder 10-31, a guide plate 10-32, and a conveyor belt 10-33. The discharge bin 10-30 is located above the support frame 10-29. An inlet 10-34 is located at the upper end of the discharge bin 10-30, which communicates with an outlet 10-22. A discharge port 10-35 is located at the lower end of the discharge bin 10-30. The screening cylinder 10-31 is installed at an angle on the support frame 10-29. One end of the screening cylinder 10-31 is connected to the discharge port 10-35. Several screen holes are provided on the side wall of the screening cylinder 10-31. The guide plate 10-32 is set on the other end of the screening cylinder 10-31. The guide plate 10-32 is set below the discharge port 10-35. The conveyor belt 10-33 is set on the support 10-29. One end of the conveyor belt 10-33 is located below the screen holes of the screening cylinder 10-31, and the other end of the conveyor belt 10-33 extends to the top of 10-8.

[0118] The crushed pure copper particles fall into the feeding hopper 10-30 and are further screened by the screening cylinder 10-31 to ensure that the diameter of the pure copper particles entering the oxidation furnace is less than or equal to 5mm, thereby improving the oxidation efficiency. Copper blocks larger than 5mm continue to roll along the screening cylinder 10-31 onto the guide plate 10-32 and are collected for secondary crushing.

[0119] A third drive motor 10-36 and a third bearing housing 10-37 are mounted on the support frame 10-29. The motor shaft of the third drive motor 10-36 is connected to the other end of the screening cylinder 10-31. The third bearing housing 10-37 is mounted on the support frame 10-29, and the motor shaft of the third drive motor 10-36 is mounted on the third bearing housing 10-37 via bearings. By setting up the third drive motor 10-36, the screening cylinder 10-31 can rotate, thereby improving screening efficiency.

[0120] The cooling device 11 includes a support frame 10-38, a conveyor roller 10-39, and a conveyor belt 10-40. The conveyor roller 10-39 is rotatably mounted on the upper end of the support frame 10-38, and the conveyor belt 10-40 is located outside the conveyor roller 10-39, below the valve 10-8. The conveyor belt 10-40 is positioned below the valve 10-8 to allow the copper oxide, after oxidation, to fall directly onto the conveyor belt 10-40 for cooling. Through the cooperation of the conveyor roller 10-39 and the conveyor belt 10-40, the copper oxide cooled to room temperature can be transported to the next process for collection or packaging.

[0121] The oxidation process in oxidation furnace 10 oxidizes recycled copper powder into copper oxide, which includes the following steps:

[0122] Step S101: Crushing Process. The second drive motor 10-23 is activated, driving the second drive wheel 10-24 to rotate. The second drive wheel 10-24 and the second driven wheel 10-25 are driven by the second belt 10-27, causing the rotor 10-10 to rotate. This causes the impact component 10-11 mounted on the rotor 10-10 to rotate along with the rotor. The pure copper obtained from aeration separation is fed into the crushing chamber 10-12 of the crushing bin 10-9 through the feed inlet 10-21. The pure copper is crushed by the impact of the impact component 10-11. The crushed pure copper is thrown onto the collision plate 10-13 under the action of centrifugal force, and is further crushed. The crushed copper blocks fall from the discharge port 10-22 into the discharge bin 30, and then enter the screening cylinder 10-31 through the discharge port 10-35 of the discharge bin 10-30. The screen hole diameter on the screening cylinder 10-31 is 5mm. Copper blocks smaller than or equal to 5mm fall onto the conveyor belt 10-33 through the screen holes, while copper blocks larger than 5mm continue to roll along the screening cylinder 10-31 at an incline onto the guide plate 10-32, and are collected for secondary crushing.

[0123] Step S102: Preheat the oxidation furnace. Connect the heater to an external power source, turn on the heater, and raise the temperature of the oxidation zone to the range of 450℃~550℃. Set the heating rate to 5℃ / min~15℃ / min.

[0124] Step S103: Loading. Open conveyor belt 10-33 to transport the crushed copper blocks less than or equal to 5mm obtained in step S101 into the oxidation furnace. Open valve 10-8 and the crushed copper blocks fall into the furnace body 10-4.

[0125] Step S104: Oxidation treatment. The temperature of the oxidation zone is maintained within the range of 450℃~550℃. Oxygen or air is introduced into the furnace body 10-4 through the oxidation air inlet pipe 10-6. The air inlet flow rate is set to 1L / min~3L / min. At the same time, the first drive motor 10-14 is turned on to drive the first drive wheel 10-15 to rotate. The first drive wheel 10-15 and the first driven wheel 10-16 are driven by the first belt 10-18, which causes the furnace body 10-4 to rotate. The copper blocks in the furnace body 10-4 are stirred by the stirring blade 10-7 as they rotate.

[0126] Step S105: Discharge and cooling. After the oxidation reaction is completed, turn off the first drive motor 10-14 and open the valve 10-8. The copper oxide that has been oxidized in step S104 will fall from the valve 10-8 onto the conveyor belt 10-40.

[0127] Step S106: Cooling and collecting. After the copper oxide on conveyor belt 10-40 cools to room temperature, it is collected and packaged.

[0128] This oxidation process first involves crushing the pure copper obtained from aeration separation. The crushed copper particles are more uniform, increasing the contact area between the copper and the working gas, which is beneficial for subsequent oxidation treatment. The oxidation furnace is then preheated to ensure a stable oxidation environment. The crushed pure copper particles are then evenly loaded into the furnace body 10⁻⁴. With the assistance of the stirring blades 10⁻⁷, the copper particles are evenly distributed, ensuring more uniform heating and improving oxidation efficiency. Oxidation is carried out under these parameters, ensuring that the pure copper particles are in full contact with the working gas. This reduces the oxidation time from 8 hours to 4 hours and the processing energy consumption from 800 kWh to 400 kWh, a reduction of approximately 50%. The purity of copper oxide is increased from 95% to 99%, offering advantages such as low energy consumption, high oxidation efficiency, and high copper oxide purity.

[0129] Example 1

[0130] Aeration tank 2-1 is designed with a capacity of 800L. The raw material for the copper-containing negative electrode sheet is 100kg, with a copper content of 20% and a graphite content of 60%.

[0131] like Figure 1 The method for regenerating and recycling copper-containing battery negative electrode materials, as shown, specifically includes the following steps:

[0132] Step S1: Initial screening of raw materials. Waste negative electrode materials from waste batteries or generated during the production process are screened to remove obvious impurities and non-metallic materials, thus obtaining recycled raw materials.

[0133] Step S2, Aeration and Separation: The recovered raw material obtained in Step S1 is fed into the aeration and separation device. After aeration and separation, the liquid is a graphite-containing liquid, and the precipitate is a copper current collector. Specifically, the recovered raw material obtained in Step S1 is fed into the aeration tank, 400L of pure water is added, the solid-liquid ratio is maintained at 1:3, the aeration equipment is started, and the air flow rate is 600L / min. During the aeration process, the stirring speed is 220rpm, the temperature is room temperature, and the aeration time is 3.5h. The aeration and separation is then completed.

[0134] Step S3: Recover the liquid and precipitate after aeration and separation respectively;

[0135] Liquid recovery includes:

[0136] Step S4: Sedimentation and separation. The graphite-containing liquid obtained in step S2 is introduced into a sedimentation tank. The clear liquid at the top of the sedimentation tank is returned to the aeration tank. The bottom of the sedimentation tank is graphite slurry.

[0137] Step S5: Two-stage gasification. The graphite slurry obtained in step S4 is mixed with water at a solid-liquid ratio of 1:1 and then fed into a first-stage gasification device. The first-stage gasification temperature is 300℃ and the first-stage gasification time is 2 hours to remove moisture and organic impurities, resulting in dried graphite. Then, the dried graphite is fed into a second-stage gasification device. The second-stage gasification temperature is 2900℃ and the second-stage gasification time is 3 hours to remove metallic impurities, resulting in primary graphite.

[0138] Step S6: Ball milling. The primary graphite obtained in step S5 is placed in a ball mill. The ball milling time is 4 hours, the ball milling media ratio is 1:3, the rotation speed is controlled at 150 rpm, and the particle size after pulverization is required to reach D90<10μm.

[0139] Step S7: Repair graphite. Place the ball-milled graphite into a repair furnace, introduce a hydrogen atmosphere, repair at 800℃, repair for 2 hours. During the repair process, the hydrogen flow rate needs to be controlled at 100ml / min. After the repair is completed, the finished graphite is obtained.

[0140] Sediment recovery includes:

[0141] Step S8: Dehydration. The precipitate obtained in step S2 is passed through a dehydration device to remove excess water, and a primary copper current collector is obtained.

[0142] Step S9: Crushing. The primary copper current collector obtained in step S8 is fed into the crushing equipment. The crusher speed is 500 rpm and the crushing time is 30 minutes. The copper particle size after crushing is less than or equal to 5 mm.

[0143] Step S10: Oxidation treatment. Copper particles are loaded into an oxidation furnace and oxidized to obtain copper oxide. Specifically, the crushed copper particles are loaded into the oxidation furnace, oxygen is introduced, oxygen concentration: 100% (pure oxygen), oxidation atmosphere: pure oxygen atmosphere, heating rate: 10℃ / min, cooling rate: natural cooling, oxygen flow rate: 2L / min, oxidation temperature: 450℃, oxidation time: 4h, and the oxidation reaction is completed to obtain copper oxide.

[0144] Step S11: Cool and collect to obtain the finished copper oxide.

[0145] The separation results in step S2 were as follows: the graphite purity was 97%, and the copper sheet recovery rate was 92%.

[0146] In step S5, the removal rate of moisture and organic impurities in the first stage was 98%; the removal rate of metal impurities in the second stage was 99.9%. Results: Graphite purity 98%, metal impurity content 0.03%, energy consumption 400 kWh, dioxin formation 0.02 ng / m³. 3 .

[0147] Results of step S10: Copper oxide purity 95%, energy consumption 375 kWh, oxygen consumption 0.12 m³ / s.3 / h.

[0148] Example 2

[0149] The difference from Example 1 is that: the amount of pure water added is 480L, the solid-liquid ratio of copper-containing negative electrode material to pure water is 1:3, the air flow rate is set to 600L / min, the stirring speed is set to 220rpm, and the aeration time is set to 3.5h.

[0150] Separation results: Graphite purity was 99.2%, and copper recovery rate was 94%.

[0151] Example 3

[0152] The difference from Example 1 is that: the amount of pure water added is 600L, the solid-liquid ratio of copper-containing negative electrode material to pure water is 1:3, the air flow rate is set to 600L / min, the stirring speed is set to 220rpm, and the aeration time is set to 3.5h.

[0153] Separation results: Graphite purity was 96%, and copper recovery rate was 90%.

[0154] From Examples 1 to 3, it can be seen that when other parameters are the same, the graphite purity and copper sheet recovery rate are highest when the amount of pure water added is 480L.

[0155] Example 4

[0156] The difference from Example 1 is that: the amount of pure water added is 480L, the solid-liquid ratio of copper-containing negative electrode material to pure water is 1:2, the air flow rate is set to 600L / min, the stirring speed is set to 220rpm, and the aeration time is set to 3.5h.

[0157] Separation results: Graphite purity 95%, copper recovery rate 91%.

[0158] Example 5

[0159] The difference from Example 1 is that: the amount of pure water added is 480L, the solid-liquid ratio of copper-containing negative electrode material to pure water is 1:4, the air flow rate is set to 600L / min, the stirring speed is set to 220rpm, and the aeration time is set to 3.5h.

[0160] Separation results: Graphite purity 96%, copper recovery rate 92%.

[0161] From Examples 2, 4 and 5, it can be seen that when other parameters are the same, the graphite purity and copper recovery rate are the highest when the solid-liquid ratio of copper-containing negative electrode raw material to pure water is 1:3.

[0162] Example 6

[0163] The difference from Example 1 is that: the amount of pure water added is 480L, the solid-liquid ratio of copper-containing negative electrode material to pure water is 1:3, the air flow rate is set to 500L / min, the stirring speed is set to 220rpm, and the aeration time is set to 3.5h.

[0164] Separation results: Graphite purity 97%, copper recovery rate 92%.

[0165] Example 7

[0166] The difference from Example 1 is that: the amount of pure water added is 480L, the solid-liquid ratio of copper-containing negative electrode material to pure water is 1:3, the air flow rate is set to 700L / min, the stirring speed is set to 220rpm, and the aeration time is set to 3.5h.

[0167] Separation results: Graphite purity 96%, copper recovery rate 91%.

[0168] From Examples 2, 6 to 7, it can be seen that when other parameters are the same, setting the air flow rate to 600 L / min results in the highest graphite purity and copper sheet recovery rate.

[0169] Example 8

[0170] The difference from Example 1 is that: the amount of pure water added is 480L, the solid-liquid ratio of copper-containing negative electrode material to pure water is 1:3, the air flow rate is set to 600L / min, the stirring speed is set to 200rpm, and the aeration time is set to 3.5h.

[0171] Separation results: Graphite purity 97%, copper recovery rate 92%.

[0172] Example 9

[0173] The difference from Example 1 is that: the amount of pure water added is 480L, the solid-liquid ratio of copper-containing negative electrode material to pure water is 1:3, the air flow rate is set to 600L / min, the stirring speed is set to 250rpm, and the aeration time is set to 3.5h.

[0174] Separation results: Graphite purity 96%, copper recovery rate 91%.

[0175] As can be seen from Examples 2, 8 and 9, when other parameters are the same, setting the stirring speed to 220 rpm results in the highest graphite purity and copper sheet recovery rate.

[0176] Example 10

[0177] The difference from Example 1 is that: the amount of pure water added is 480L, the solid-liquid ratio of copper-containing negative electrode material to pure water is 1:3, the air flow rate is set to 600L / min, the stirring speed is set to 220rpm, and the aeration time is set to 2h.

[0178] Separation results: Graphite purity 95%, copper recovery rate 90%.

[0179] Example 11

[0180] The difference from Example 1 is that: the amount of pure water added is 480L, the solid-liquid ratio of copper-containing negative electrode material to pure water is 1:3, the air flow rate is set to 600L / min, the stirring speed is set to 220rpm, and the aeration time is set to 5h.

[0181] Separation results: Graphite purity 97%, copper recovery rate 92%.

[0182] As can be seen from Examples 2, 10 and 11, when other parameters are the same, setting the aeration time to 3.5h results in the highest graphite purity and copper sheet recovery rate.

[0183] From Examples 1 to 11, it can be seen that the following optimal process parameters result in the highest graphite purity and copper sheet recovery rate:

[0184] Aeration tank 2-1 capacity: 800L; added pure water: 480L; copper-containing negative electrode raw material to pure water solid-liquid ratio: 1:3; air flow rate set: 600L / min; stirring speed set: 220rpm; temperature: ambient temperature 25℃; aeration time set: 3.5h. The optimal process parameters yielded the following separation results: graphite purity 99.2%, copper recovery rate 94%.

[0185] Example 12

[0186] The differences from Example 1 are as follows: First-stage gasification temperature: 350℃; First-stage gasification time: 2h; First-stage moisture and organic impurity removal rate: 98%; Second-stage gasification temperature: 2900℃; Second-stage gasification time: 3h; Second-stage metal impurity removal rate: 99.9%. Results: Graphite purity 99.2%, metal impurity content 0.01%, energy consumption 375kWh, dioxin formation <0.01ng / m³. 3 .

[0187] Example 13

[0188] The differences from Example 1 are as follows: First-stage gasification temperature: 400℃; First-stage gasification time: 2h; First-stage moisture and organic impurity removal rate: 98%; Second-stage gasification temperature: 2900℃; Second-stage gasification time: 3h; Second-stage metal impurity removal rate: 99.9%. Results: Graphite purity 97.5%, metal impurity content 0.02%, energy consumption 380kWh, dioxin formation 0.01ng / m³. 3 .

[0189] From Examples 1, 12 and 13, it can be seen that when other parameters are the same, the graphite purity is the highest and the metal impurity content, energy consumption and dioxin generation are the lowest when the gasification temperature is 350°C.

[0190] Example 14

[0191] The differences from Example 1 are as follows: First-stage gasification temperature: 350℃; First-stage gasification time: 1h; First-stage moisture and organic impurity removal rate: 98%; Second-stage gasification temperature: 2900℃; Second-stage gasification time: 3h; Second-stage metal impurity removal rate: 99.9%. Results: Graphite purity 98.5%, metal impurity content 0.015%, energy consumption 370kWh, dioxin formation <0.01ng / m³. 3 .

[0192] Example 15

[0193] The differences from Example 1 are as follows: First-stage gasification temperature: 350℃; First-stage gasification time: 3h; First-stage moisture and organic impurity removal rate: 98%; Second-stage gasification temperature: 2900℃; Second-stage gasification time: 3h; Second-stage metal impurity removal rate: 99.9%. Results: Graphite purity 99%, metal impurity content 0.012%, energy consumption 380kWh, dioxin formation <0.01ng / m³. 3 .

[0194] From Examples 12, 14 and 15, it can be seen that when other parameters are the same, the graphite purity is the highest and the metal impurity content, energy consumption and dioxin generation are the lowest when the gasification time is 2 hours.

[0195] Example 16

[0196] The differences from Example 1 are as follows: First-stage gasification temperature: 350℃; First-stage gasification time: 2h; First-stage moisture and organic impurity removal rate: 95%; Second-stage gasification temperature: 2900℃; Second-stage gasification time: 3h; Second-stage metal impurity removal rate: 99.9%. Results: Graphite purity 98.8%, metal impurity content 0.015%, energy consumption 385kWh, dioxin formation <0.01ng / m³. 3 .

[0197] Example 17

[0198] The differences from Example 1 are as follows: First-stage gasification temperature: 350℃; First-stage gasification time: 2h; First-stage moisture and organic impurity removal rate: 99%; Second-stage gasification temperature: 2900℃; Second-stage gasification time: 3h; Second-stage metal impurity removal rate: 99.9%. Results: Graphite purity 99.2%, metal impurity content 0.01%, energy consumption 375kWh, dioxin formation <0.01ng / m³.3 .

[0199] From Examples 12, 16 and 17, it can be seen that when other parameters are the same, the optimal removal rate of moisture and organic impurities is 98%, at which point the effect is the best.

[0200] Example 18

[0201] The differences from Example 1 are as follows: First-stage gasification temperature: 350℃; First-stage gasification time: 2h; First-stage moisture and organic impurity removal rate: 98%; Second-stage gasification temperature: 2800℃; Second-stage gasification time: 3h; Second-stage metal impurity removal rate: 99.9%. Results: Graphite purity 98.7%, metal impurity content 0.02%, energy consumption 370kWh, dioxin formation <0.01ng / m³. 3 .

[0202] Example 19

[0203] The differences from Example 1 are as follows: First-stage gasification temperature: 350℃; First-stage gasification time: 2h; First-stage moisture and organic impurity removal rate: 98%; Second-stage gasification temperature: 3000℃; Second-stage gasification time: 3h; Second-stage metal impurity removal rate: 99.9%. Results: Graphite purity 99.2%, metal impurity content 0.01%, energy consumption 375kWh, dioxin formation <0.01ng / m³. 3 .

[0204] As can be seen from Examples 12, 18 and 19, when other parameters are the same, the overall effect is best when the second-stage vaporization temperature is 2900℃.

[0205] Example 20

[0206] The differences from Example 1 are as follows: First-stage gasification temperature: 350℃; First-stage gasification time: 2h; First-stage moisture and organic impurity removal rate: 98%; Second-stage gasification temperature: 2900℃; Second-stage gasification time: 2h; Second-stage metal impurity removal rate: 99.9%. Results: Graphite purity 98.9%, metal impurity content 0.02%, energy consumption 370kWh, dioxin formation <0.01ng / m³. 3 .

[0207] Example 21

[0208] The differences from Example 1 are as follows: First-stage gasification temperature: 350℃; First-stage gasification time: 2h; First-stage moisture and organic impurity removal rate: 98%; Second-stage gasification temperature: 2900℃; Second-stage gasification time: 4h; Second-stage metal impurity removal rate: 99.9%. Results: Graphite purity 99.3%, metal impurity content 0.01%, energy consumption 380kWh, dioxin formation <0.01ng / m³. 3 .

[0209] From Examples 12, 20 and 21, it can be seen that when other parameters are the same, the overall effect is best when the two-stage gasification time is 3h.

[0210] Example 22

[0211] The differences from Example 1 are as follows: First-stage gasification temperature: 350℃; First-stage gasification time: 2h; First-stage moisture and organic impurity removal rate: 98%; Second-stage gasification temperature: 2900℃; Second-stage gasification time: 3h; Second-stage metal impurity removal rate: 98%. Results: Graphite purity 98.5%, metal impurity content 0.02%, energy consumption 375kWh, dioxin formation <0.01ng / m³. 3 .

[0212] Example 23

[0213] The differences from Example 1 are as follows: First-stage gasification temperature: 350℃; First-stage gasification time: 2h; First-stage moisture and organic impurity removal rate: 98%; Second-stage gasification temperature: 2900℃; Second-stage gasification time: 3h; Second-stage metal impurity removal rate: 99.99%. Results: Graphite purity 99.2%, metal impurity content 0.01%, energy consumption 375kWh, dioxin formation <0.01ng / m³. 3 .

[0214] As can be seen from Examples 12, 22 and 23, when other parameters are the same, the optimal removal rate of metal impurities in the two-stage process is 99.9%, and the overall effect is the best.

[0215] From Examples 1, 12 to 23, it was found that the optimal process parameters for the two-stage gasification of graphite were as follows: First-stage gasification temperature: 350℃; First-stage gasification time: 2h; First-stage removal rate: 98% (optimal removal rate); Second-stage gasification temperature: 2900℃ (optimal temperature); Second-stage gasification time: 3h (optimal effect); Second-stage removal rate: 99.9% (optimal removal rate). The results obtained from the optimal process parameters are: graphite purity 99.2%, metal impurity content 0.01%, energy consumption 375kWh, and dioxin formation <0.01ng / m³. 3 .

[0216] Example 24

[0217] The differences from Example 1 are as follows: oxidation temperature: 500℃; oxidation time: 4h; oxygen concentration: 100% (pure oxygen); oxidation atmosphere: pure oxygen atmosphere; heating rate: 10℃ / min; cooling rate: natural cooling; gas flow rate: 2L / min. Results: copper oxide purity 99%, energy consumption 400kWh, oxygen consumption 0.12m³. 3 / h.

[0218] Example 25

[0219] The differences from Example 1 are as follows: oxidation temperature: 550℃; oxidation time: 4h; oxygen concentration: 100% (pure oxygen); oxidation atmosphere: pure oxygen atmosphere; heating rate: 10℃ / min; cooling rate: natural cooling; gas flow rate: 2L / min. Results: copper oxide purity 98%, energy consumption 425kWh, oxygen consumption 0.12m³ / min. 3 / h.

[0220] The oxidation temperature was examined, and it can be seen from Examples 1, 24 and 25 that when other parameters are the same, the oxidation temperature of 500°C is the best.

[0221] Example 26

[0222] The differences from Example 1 are as follows: oxidation temperature: 500℃; oxidation time: 2h; oxygen concentration: 100% (pure oxygen); oxidation atmosphere: pure oxygen atmosphere; heating rate: 10℃ / min; cooling rate: natural cooling; gas flow rate: 2L / min. Results: copper oxide purity 96%, energy consumption 350kWh, oxygen consumption 0.12m³. 3 / h.

[0223] Example 27

[0224] The differences from Example 1 are as follows: oxidation temperature: 500℃; oxidation time: 6h; oxygen concentration: 100% (pure oxygen); oxidation atmosphere: pure oxygen atmosphere; heating rate: 10℃ / min; cooling rate: natural cooling; gas flow rate: 2L / min. Results: copper oxide purity 99.5%, energy consumption 450kWh, oxygen consumption 0.12m³. 3 / h.

[0225] The oxidation time was examined, and it can be seen from Examples 24, 26 and 27 that when other parameters are the same, the oxidation time of 4 hours is the best.

[0226] Example 28

[0227] The differences from Example 1 are as follows: oxidation temperature: 500℃; oxidation time: 4h; oxygen concentration: 21wt%; oxidation atmosphere: air; heating rate: 10℃ / min; cooling rate: natural cooling; airflow rate: 2L / min. Results: copper oxide purity 90%, energy consumption 350kWh, oxygen consumption 0.0252m³ / min. 3 / h.

[0228] Example 29

[0229] The differences from Example 1 are as follows: oxidation temperature: 500℃; oxidation time: 4h; oxygen concentration: 50wt%; oxidation atmosphere: oxygen / air mixed atmosphere; heating rate: 10℃ / min; cooling rate: natural cooling; gas flow rate: 2L / min. Results: copper oxide purity 95%, energy consumption 375kWh, oxygen consumption 0.06m³ / min. 3 / h.

[0230] By examining the oxygen concentration, as shown in Examples 24, 28, and 29, it can be concluded that when all other parameters are the same, an oxygen concentration of 100% yields the best results.

[0231] Example 30

[0232] The differences from Example 1 are as follows: oxidation temperature: 500℃; oxidation time: 4h; oxygen concentration: 80wt%; oxidation atmosphere: 80wt% oxygen + 20wt% inert gas (such as nitrogen or argon); heating rate: 10℃ / min; cooling rate: natural cooling; gas flow rate: 2L / min. Results: copper oxide purity 97%, energy consumption 400kWh, oxygen consumption 0.096m³ / min. 3 / h.

[0233] The results of examining the oxidizing atmosphere, as shown in Examples 24 and 30, indicate that when all other parameters are the same, the oxidizing atmosphere is pure oxygen, which yields the best results.

[0234] Example 31

[0235] The differences from Example 1 are as follows: oxidation temperature: 500℃; oxidation time: 4h; oxygen concentration: 100% (pure oxygen); oxidation atmosphere: pure oxygen atmosphere; heating rate: 5℃ / min; cooling rate: natural cooling; gas flow rate: 2L / min. Results: copper oxide purity 98%, energy consumption 380kWh, oxygen consumption 0.12m³. 3 / h.

[0236] Example 32

[0237] The differences from Example 1 are as follows: oxidation temperature: 500℃; oxidation time: 4h; oxygen concentration: 100% (pure oxygen); oxidation atmosphere: pure oxygen atmosphere; heating rate: 15℃ / min; cooling rate: natural cooling; gas flow rate: 2L / min. Results: copper oxide purity 97.5%, energy consumption 420kWh, oxygen consumption 0.12m³. 3 / h.

[0238] The heating rate was examined in Examples 24, 31 and 32. It was found that when other parameters were the same, the heating rate of 10℃ / min was the best.

[0239] Example 33

[0240] The differences from Example 1 are as follows: oxidation temperature: 500℃; oxidation time: 4 hours; oxygen concentration: 100% (pure oxygen); oxidation atmosphere: pure oxygen atmosphere; heating rate: 10℃ / min; cooling rate: controlled cooling; gas flow rate: 2L / min. Results: copper oxide purity 98.5%, energy consumption 410kWh, oxygen consumption 0.12m³. 3 / h.

[0241] Example 34

[0242] The differences from Example 1 are as follows: oxidation temperature: 500℃; oxidation time: 4h; oxygen concentration: 100% (pure oxygen); oxidation atmosphere: pure oxygen atmosphere; heating rate: 10℃ / min; cooling rate: rapid cooling; gas flow rate: 2L / min. Results: copper oxide purity 96%, energy consumption 420kWh, oxygen consumption 0.12m³. 3 / h.

[0243] The cooling rate was examined in Examples 24, 33, and 34. It was found that, with other parameters being equal, the cooling rate of natural cooling was the most effective.

[0244] Example 35

[0245] The differences from Example 1 are as follows: oxidation temperature: 500℃; oxidation time: 4h; oxygen concentration: 100% (pure oxygen); oxidation atmosphere: pure oxygen atmosphere; heating rate: 10℃ / min; cooling rate: natural cooling; gas flow rate: 1L / min. Results: copper oxide purity 97%, energy consumption 390kWh, oxygen consumption 0.06m³. 3 / h.

[0246] Example 36

[0247] The differences from Example 1 are as follows: oxidation temperature: 500℃; oxidation time: 4h; oxygen concentration: 100% (pure oxygen); oxidation atmosphere: pure oxygen atmosphere; heating rate: 10℃ / min; cooling rate: natural cooling; gas flow rate: 3L / min. Results: copper oxide purity 98.5%, energy consumption 410kWh, oxygen consumption 0.18m³. 3 / h.

[0248] Examining the airflow rate, as shown in Examples 24, 35, and 36, it can be concluded that when other parameters are the same, an airflow rate of 2 L / min yields the best results.

[0249] In summary, the following process parameters for the oxidation furnace, as demonstrated in Examples 1, 24, and 36, yielded the best results: oxidation temperature of 500℃; oxidation time of 4 hours; oxygen concentration of 100% pure oxygen atmosphere; oxidation atmosphere of pure oxygen atmosphere; heating rate of 10℃ / min; cooling rate of natural cooling; and airflow rate of 2L / min. The optimal process parameters resulted in: copper oxide purity of 99%, energy consumption of 400kWh, and oxygen consumption of 0.12m³ / min. 3 / h.

[0250] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it. Although the present invention has been described in detail with reference to the above embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the above embodiments, or replace some or all of the technical features therein with equivalents. However, these modifications or replacements do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A method for regenerating and recycling copper-containing battery negative electrode materials, characterized in that: Specifically, the steps include the following: Step S1: Initial screening of raw materials. Waste negative electrode materials from waste batteries or generated during the production process are screened to remove obvious impurities and non-metallic materials, thus obtaining recycled raw materials. Step S2, aeration separation: The recovered raw material obtained in step S1 is fed into the aeration separation device. After the aeration separation is completed, the liquid is a graphite-containing liquid and the precipitate is a copper current collector. Step S3: Recover the liquid and precipitate after aeration and separation respectively; The liquid recovery includes: Step S4: Sedimentation and separation. The graphite-containing liquid obtained in step S2 is introduced into a sedimentation tank. The clear liquid at the top of the sedimentation tank is returned to the aeration tank. The bottom of the sedimentation tank is graphite slurry. Step S5: Two-stage gasification. The graphite slurry obtained in step S4 is mixed with water at a solid-liquid ratio of 1:1 and then fed into a first-stage gasification device. The first-stage gasification temperature is 300℃~400℃ and the first-stage gasification time is 1h~3h to remove moisture and organic impurities, resulting in dried graphite. Then, the dried graphite is fed into a second-stage gasification device. The second-stage gasification temperature is 2800℃~3000℃ and the second-stage gasification time is 2h~4h to remove metallic impurities, resulting in primary graphite. Step S6: Ball milling. The primary graphite obtained in step S5 is placed in a ball mill. The ball milling time is 4 hours, the ball milling media ratio is 1:3, the rotation speed is controlled at 150 rpm, and the particle size after pulverization is required to reach D90<10μm. Step S7: Repair graphite. Place the ball-milled graphite into a repair furnace, introduce a hydrogen atmosphere, repair at 800℃, repair for 2 hours. During the repair process, the hydrogen flow rate needs to be controlled at 100ml / min. After the repair is completed, the finished graphite is obtained. The precipitate recovery includes: Step S8: Dehydration. The precipitate obtained in step S2 is passed through a dehydration device to remove excess water, and a primary copper current collector is obtained. Step S9: Crushing. The primary copper current collector obtained in step S8 is fed into the crushing equipment. The crusher speed is 500 rpm and the crushing time is 30 minutes. The copper particle size after crushing is less than or equal to 5 mm. Step S10: Oxidation treatment. Copper particles are loaded into an oxidation furnace and oxidized to obtain copper oxide. Step S11: Cool and collect to obtain the finished copper oxide.

2. The method for regenerating and recycling copper-containing battery negative electrode materials according to claim 1, characterized in that: The aeration separation step S2 is specifically as follows: the recovered raw material obtained in step S1 is put into the aeration tank, pure water is added, the solid-liquid ratio is maintained at 1:2 to 1:4, the aeration equipment is started, the air flow rate is 500L / min to 700L / min; during the aeration process, the stirring speed is 150rpm to 250rpm, the temperature is room temperature, the aeration time is 2h to 5h, and the aeration separation is completed.

3. The method for regenerating and recycling copper-containing battery negative electrode materials according to claim 1, characterized in that: The oxidation process in step S10 specifically involves: loading the crushed copper particles into an oxidation furnace, introducing oxygen or air, maintaining an oxygen flow rate of 100L / min to 300L / min, an oxidation temperature of 450℃ to 550℃, and an oxidation time of 2h to 6h to complete the oxidation reaction and obtain copper oxide.

4. A recycling apparatus using the regeneration and recycling method for copper-containing battery negative electrode material as described in any one of claims 1 to 3, characterized in that: Along the material travel direction, a screen and an aeration separation device are arranged in sequence. The aeration separation device is connected to a liquid recovery component and a sediment recovery component. The liquid recovery component includes a sedimentation tank, a two-stage gasification device, a ball mill, a repair furnace, and a graphite collection tank arranged in sequence. The sediment recovery component includes a dewatering device, a crushing device, an oxidation furnace, a cooling device, and a copper oxide collection tank arranged in sequence. The aeration separation device is equipped with an inlet pipe at the top to facilitate the entry of pure water, and the sedimentation tank is equipped with a return pipe at the top that is connected to the aeration separation device.

5. The device for recycling copper-containing battery negative electrode material according to claim 4, characterized in that: The aeration separation device includes an aeration tank, which is divided into an aeration zone and a sedimentation zone by a partition. The upper end of the partition has a connecting hole that connects the aeration zone and the sedimentation zone. A feed pipe is provided at the upper end of the aeration tank, and a water inlet pipe is provided at the lower end of the aeration tank. Both the feed pipe and the water inlet pipe are connected to the aeration zone. An aeration component is provided in the aeration zone for supplying air to the aeration zone. A stirring assembly is provided on the aeration tank, with the stirring end of the stirring assembly extending into the aeration zone. A second extraction assembly for extracting the separated graphite floating matter is provided at the upper end of the sedimentation zone, and a first extraction assembly for extracting the separated copper sheets is provided at the lower end of the sedimentation zone.

6. The device for recycling copper-containing battery negative electrode material according to claim 5, characterized in that: The aeration assembly includes an air compressor, an air inlet pipe, and a central guide tube. The central guide tube is located within the aeration zone, and its lower end is connected to the air compressor via the air inlet pipe. The air compressor is located outside the lower end of the aeration tank.

7. The recycling device for copper-containing battery negative electrode material according to claim 4, characterized in that: The two-stage gasification equipment includes a first-stage gasification equipment, a transmission equipment, and a second-stage gasification equipment arranged in sequence. The first-stage gasification equipment includes a first gasification furnace, in which a furnace tube is rotatably arranged. The graphite mixture to be heated enters from one end of the furnace tube. A first heater is arranged around the inner wall of the first gasification furnace, and the first heater is located outside the furnace tube. The two-stage gasification equipment includes a second gasifier, which has a heating chamber. The upper end of the second gasifier is provided with a furnace door for adding graphite that has undergone one stage of gasification. A second heater is provided in the heating chamber. One end of the transmission device is connected to the other end of the furnace tube, and the other end of the transmission device is located above the furnace door. After a period of gasification, the graphite is discharged from the other end of the furnace tube and transported to the heating chamber of the second gasification furnace through the transmission device.

8. The device for recycling copper-containing battery negative electrode material according to claim 7, characterized in that: The gasification equipment also includes a drive assembly, a first mounting base, and a first feed hopper. The drive assembly and the first gasifier are both mounted on the first mounting base. The upper end of the drive assembly is fitted onto the other end of the furnace tube. The drive assembly is used to drive the furnace tube to rotate. The first feed hopper is located on one end of the furnace tube.

9. The recycling device for copper-containing battery negative electrode material according to claim 4, characterized in that: The oxidation furnace includes a crusher assembly, an oxidation furnace assembly, and a cooling device. The oxidation furnace assembly includes a furnace body, a first drive mechanism, and an air inlet pipe. The first drive mechanism is used to drive the furnace body to rotate. Several stirring blades are spirally arranged on the inner wall of the furnace body. A heater is provided inside the furnace body. Valves for feeding and discharging are provided on the side wall of the furnace body. At least a portion of the crusher assembly is located above the valves, and at least a portion of the cooling device is located below the valves. One end of the air inlet pipe is connected to the furnace body. The crusher assembly includes a crushing chamber, a rotor, and an impact component. A crushing cavity is formed inside the crushing chamber. The rotor is rotatably disposed inside the crushing cavity. The impact component is disposed on the rotor and is used to collide with the material. A collision plate is disposed inside the crushing cavity and is arranged on one side of the rotor. After colliding with the impact component, the material hits the collision plate.

10. The device for recycling copper-containing battery negative electrode material according to claim 9, characterized in that: The first driving mechanism includes a first driving motor, a first driving wheel, a first driven wheel, a first connecting shaft, and a first belt. The first driving wheel is mounted on the motor shaft of the first driving motor. The first driving wheel and the first driven wheel are driven by the first belt. The two ends of the first connecting shaft are respectively connected to the first driven wheel and the furnace body.

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