CN116037312A - Method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder - Google Patents
Method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder Download PDFInfo
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- CN116037312A CN116037312A CN202310021988.9A CN202310021988A CN116037312A CN 116037312 A CN116037312 A CN 116037312A CN 202310021988 A CN202310021988 A CN 202310021988A CN 116037312 A CN116037312 A CN 116037312A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B9/00—General arrangement of separating plant, e.g. flow sheets
- B03B9/06—General arrangement of separating plant, e.g. flow sheets specially adapted for refuse
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B5/00—Washing granular, powdered or lumpy materials; Wet separating
- B03B5/02—Washing granular, powdered or lumpy materials; Wet separating using shaken, pulsated or stirred beds as the principal means of separation
- B03B5/04—Washing granular, powdered or lumpy materials; Wet separating using shaken, pulsated or stirred beds as the principal means of separation on shaking tables
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B5/00—Washing granular, powdered or lumpy materials; Wet separating
- B03B5/48—Washing granular, powdered or lumpy materials; Wet separating by mechanical classifiers
- B03B5/52—Spiral classifiers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M10/00—Secondary cells; Manufacture thereof
- H01M10/54—Reclaiming serviceable parts of waste accumulators
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03B—SEPARATING SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS
- B03B9/00—General arrangement of separating plant, e.g. flow sheets
- B03B9/06—General arrangement of separating plant, e.g. flow sheets specially adapted for refuse
- B03B2009/066—General arrangement of separating plant, e.g. flow sheets specially adapted for refuse the refuse being batteries
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/84—Recycling of batteries or fuel cells
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Abstract
The invention discloses a method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder. According to the invention, the black powder is prepared into suspension, the suspension is subjected to flotation roughing, then the qualified graphite carbon powder is separated through flotation concentration, the black powder subjected to flotation scavenging decarburization is sequentially subjected to spiral chute and multistage shaking table gravity separation, the copper foil powder, the aluminum foil powder and the electrode powder are finally separated, and the separated carbon powder, copper foil powder and aluminum foil powder have higher grade and recovery rate, so that the recovery rate of the black powder of the waste power battery is remarkably improved.
Description
Technical Field
The invention relates to the field of waste power battery recovery, in particular to a method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder.
Background
At present, three-element lithium batteries, lithium iron phosphate and the like are mostly adopted as power batteries for new energy automobiles in China, and the battery capacity of the power batteries can be slowly attenuated due to cyclic charge and discharge, so that a large number of power lithium batteries can be expected to enter a retirement period within two or three years, and if the retired power batteries cannot be safely and environmentally-friendly recovered, huge harm is brought to the environment and society. Firstly, heavy metals such as nickel, cobalt, manganese and the like in waste power batteries, fluorine-containing organic matters such as electrolyte and the like pollute the environment; secondly, because the waste power batteries still contain higher voltage, if the waste power batteries are improperly operated in the recovery, disassembly and treatment processes, various problems such as fire explosion, heavy metal pollution, organic waste gas emission and the like can be caused. Therefore, the development of the green recovery research of the retired power battery has important social value, not only can realize good economic benefit, but also can avoid the pollution to the environment caused by discarding the retired power battery. Particularly, part of harmful substances such as hydrofluoric acid and the like remain in the negative electrode material of the waste lithium ion battery, and the negative electrode material has great hidden danger to life and environment, so that the recovery of the negative electrode material in the waste lithium ion battery is necessary to remove the harmful impurities.
Chinese patent CN106636649a discloses a method for recovering power lithium ion positive electrode material of waste lithium battery, specifically discloses that the positive electrode material is obtained by removing binder through high temperature treatment of the positive electrode sheet obtained by disassembly, and the power lithium ion is obtained by sintering after ball milling at high speed.
Chinese patent CN101921917a discloses a method for recovering valuable metals from waste lithium batteries, chinese patent CN107240731a discloses a method for recovering waste power lithium ion batteries, and the two patent technologies mainly aim at recovering lithium elements, and other components such as copper and aluminum are not recovered, so that great resource waste exists.
Chinese patent CN112635867a discloses a method for recovering graphite material from waste lithium battery, which adopts a physical method of combination of scrubbing-magnetic separation-gravity separation-pyrolysis-floatation to recover graphite material, and the mixed powder of anode and cathode materials obtained by crushing and sorting waste power lithium battery is stirred and scrubbed, so that the adhesion between the cathode material and other substances is reduced, and the subsequent high-gradient strong magnetic separation effect is improved; the high-gradient strong magnetic separation realizes the separation of the positive electrode material and the graphite by utilizing the difference of the specific magnetization coefficient of the positive electrode material and the graphite. The proposal mainly recovers graphite, and valuable metals such as copper and aluminum are separated and led out together in the form of impurities, and the proposal does not recover the valuable metals such as copper and aluminum well.
The above-mentioned prior art shows that, in the prior art, when separating and recovering carbon powder, copper powder and aluminum powder from the waste power battery black powder, the three materials cannot have higher grade and recovery rate, so a new waste power battery black powder recovery means is required to be provided.
Disclosure of Invention
The invention aims to provide a method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder, which is used for solving the problem that the separation and recovery of high-grade carbon powder, high-grade copper powder and high-grade aluminum powder from waste power battery black powder are difficult to realize in the prior art.
In order to solve the technical problems, the invention provides a method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder, which is characterized by comprising the following steps:
flotation roughing: and (3) carrying out flotation on the crushed raw ore with the granularity of-0.6 mm, and classifying the crushed raw ore into flotation rougher tailings and flotation rougher concentrate after screening.
And (3) flotation scavenging: and (3) carrying out flotation scavenging on the flotation rougher tailings, and separating the flotation scavenging tailings and the flotation scavenging concentrate after screening.
Flotation and selection: and (3) carrying out flotation concentration on the flotation roughing concentrate, separating the flotation roughing concentrate into carbon powder materials and flotation concentration tailings after screening, collecting the flotation concentration tailings and flotation scavenging concentrate, and refluxing the collected flotation concentration tailings and the flotation scavenging concentrate for carrying out the flotation roughing step again.
Sorting by a spiral chute: the flotation scavenger tailings are led into a spiral chute for flushing, and are divided into spiral chute tailings and spiral chute concentrate after flushing, and the spiral chute concentrate is recycled as electrode powder.
Sorting by a primary shaking table: the spiral chute tailings are led into a shaking table for water flow flushing, and the flushing is divided into primary coarse-grained ore, primary medium-grained ore and primary fine-grained ore.
Sorting by a secondary shaking table: leading the primary medium-sized particle ore into a shaking table for water flow flushing, dividing the primary medium-sized particle ore into secondary coarse-sized particle ore, secondary medium-sized particle ore and secondary fine-sized particle ore after flushing, refluxing the secondary medium-sized particle ore, and carrying out the primary shaking table sorting step again, wherein the primary fine-sized particle ore and the secondary fine-sized particle ore are collected and recycled as electrode powder.
Sorting by a three-stage shaking table: and leading the primary coarse particle ore and the secondary coarse particle ore into a shaking table for water flow flushing, and recovering the tertiary coarse particle ore as copper powder, the tertiary medium particle ore and the tertiary fine particle ore after flushing, wherein the tertiary medium particle ore reflows to perform a tertiary shaking table separation step again, and the tertiary fine particle ore is recovered as aluminum powder.
Wherein, the technological conditions of flotation roughing are: the aeration amount is 20-60ml/min, the pH value is 6-8, the kerosene content is 100-500g/t, and the flotation time is 1-4min.
Wherein, the technological conditions of the flotation scavenging step are as follows: the aeration amount is 40-120ml/min, the pH value is 6-8, the kerosene content is 100-250g/t, and the flotation time is 3-6min. It should be noted that the aeration amount of flotation rougher is required to be smaller than that of flotation scavenger so that carbon powder materials with smaller particle sizes can be screened out in advance as much as possible, and the small-particle-size carbon powder material components contained in flotation scavenger tailings are maintained at a lower duty ratio level, so that electrode powder, aluminum powder and copper powder products obtained by subsequent screening can have higher grades.
Wherein, the technological conditions of the flotation and selection step are as follows: the aeration amount is 80-120ml/min, the pH value is 6-8, the kerosene content is 50g/t, and the flotation time is 3-6min.
Wherein the water flow rate in the spiral chute step is 14-16L/min, the water flow rate in the primary shaking table sorting step is 4-6L/min, the water flow rate in the secondary shaking table sorting step is 7-9L/min, and the water flow rate in the tertiary shaking table sorting step is 10-13L/min. The water flow speed in the spiral chute step is set to be the maximum, and the purpose is to screen electrode powder through a larger water flow speed; the water flow speed is sequentially increased in the steps of primary shaking table sorting, secondary shaking table sorting and tertiary shaking table sorting, and the method aims at gradually washing impurities through a gradient increasing shaking table screening setting mode, so that finally obtained aluminum powder and copper powder products have higher grades.
Wherein, still include before the flotation rougher step: and (3) sequentially carrying out disassembly, discharge, cleaning and drying, primary crushing, pyrolysis and secondary crushing on the waste power batteries to obtain raw ores with the granularity of-0.6 mm.
The slag after the pyrolysis step contains a metal mixture and electrode active substances, and the slag is cooled and then subjected to secondary crushing to obtain raw ore.
The beneficial effects of the invention are as follows: compared with the prior art, the invention provides a method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder, which comprises the steps of preparing the black powder into suspension, carrying out flotation roughing, carrying out flotation concentration, separating qualified graphite carbon powder, carrying out spiral chute and multistage shaking table reselection on the black powder after flotation, scavenging and decarburization in sequence, finally separating to obtain copper foil powder, aluminum foil powder and electrode powder, wherein the separated carbon powder, copper foil powder and aluminum foil powder have higher grade and recovery rate, and the recovery rate of the waste power battery black powder is remarkably improved.
Drawings
FIG. 1 is a flow chart of an embodiment of a method of separating carbon powder, copper powder and aluminum powder from waste power cell black powder in the present invention.
Detailed Description
The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present invention without making any inventive effort, are intended to fall within the scope of the present invention.
Example 1
Referring to fig. 1, in this embodiment, the method for separating carbon powder, copper powder and aluminum powder from the black powder of the waste power battery comprises the following steps:
1) And (3) sequentially carrying out disassembly, discharge, cleaning and drying, primary crushing, pyrolysis and secondary crushing on the waste power batteries, wherein slag after the pyrolysis step contains a metal mixture and electrode active substances, and cooling the slag and carrying out secondary crushing to obtain raw ore, so as to obtain the raw ore with the granularity of-0.6 mm.
2) Flotation roughing: and (3) carrying out flotation on the crushed raw ore with the granularity of-0.6 mm, and classifying the crushed raw ore into flotation rougher tailings and flotation rougher concentrate after screening. In the step, the process conditions of flotation roughing are as follows: the aeration amount is 20-60ml/min, the pH value is 6-8, the kerosene content is 100-500g/t, and the flotation time is 1-4min; because the granularity range of the raw ore is wider, the raw ore needs to be subjected to primary flotation so as to ensure that the carbon powder material with better quality can be obtained after the follow-up flotation and concentration.
3) And (3) flotation scavenging: and (3) carrying out flotation scavenging on the flotation rougher tailings, and separating the flotation scavenging tailings and the flotation scavenging concentrate after screening. In the step, the process conditions of the flotation and scavenging step are as follows: the aeration amount is 80ml/min, the pH value is 7, the kerosene content is 150g/t, and the flotation time is 5min.
4) Flotation and selection: and (3) carrying out flotation concentration on the flotation roughing concentrate, separating the flotation roughing concentrate into carbon powder materials and flotation concentration tailings after screening, collecting the flotation concentration tailings and flotation scavenging concentrate, and refluxing the collected flotation concentration tailings and the flotation scavenging concentrate for carrying out the flotation roughing step again. In this step, the process conditions of the flotation beneficiation step are: the aeration amount is 100ml/min, the pH value is 7, the kerosene content is 50g/t, and the flotation time is 5min; and (3) carrying out component measurement on the recovered carbon powder material, wherein the grade of C is 89.32%, the recovery rate of C is 92.17%, and the recovered carbon powder material has higher grade and recovery rate.
5) Sorting by a spiral chute: the flotation scavenger tailings are led into a spiral chute for flushing, and are divided into spiral chute tailings and spiral chute concentrate after flushing, and the spiral chute concentrate is recycled as electrode powder. In this step, the preferred flow rate of the water stream is 15L/min. In the practical experiment process, when the water flow speed of flushing water is smaller, ore pulp cannot be loosened to obtain a stable and effective separation effect; when the flow speed of the flushing water is too high, more copper and aluminum can be flushed into the electrode powder, so that the finally obtained electrode powder contains more copper and aluminum, and further, the recovery amount of the separately obtained copper powder and aluminum powder is lower; that is, the change of the flow rate of the flushing water flow can influence the recovery rate of copper powder and aluminum powder, and the flow rate of the water flow during the spiral chute sorting needs to be strictly controlled.
6) Sorting by a primary shaking table: the spiral chute tailings are led into a shaking table for water flow flushing, and the flushing is divided into primary coarse-grained ore, primary medium-grained ore and primary fine-grained ore. In this step, the preferred flow rate of the water stream is 5L/min.
7) Sorting by a secondary shaking table: leading the primary medium-sized particle ore into a shaking table for water flow flushing, dividing the primary medium-sized particle ore into secondary coarse-sized particle ore, secondary medium-sized particle ore and secondary fine-sized particle ore after flushing, refluxing the secondary medium-sized particle ore, and carrying out the primary shaking table sorting step again, wherein the primary fine-sized particle ore and the secondary fine-sized particle ore are collected and recycled as electrode powder. In this step, the preferred flow rate of the water stream is 8L/min.
8) Sorting by a three-stage shaking table: and leading the primary coarse particle ore and the secondary coarse particle ore into a shaking table for water flow flushing, and recovering the tertiary coarse particle ore as copper powder, the tertiary medium particle ore and the tertiary fine particle ore after flushing, wherein the tertiary medium particle ore reflows to perform a tertiary shaking table separation step again, and the tertiary fine particle ore is recovered as aluminum powder. In this step, the preferred flow rate of the water stream is 12L/min. The components of the electrode powder, copper powder and aluminum powder obtained by recycling in this embodiment are measured, and specific results are shown in table 1, the recycling rate of copper powder can reach more than 90%, and the recycling rate of aluminum powder can reach more than 85%, so that the recycled carbon powder material, copper powder and aluminum powder all have higher grade and recycling rate, and the recycled carbon powder material, copper powder and aluminum powder can meet the standard of direct common sale.
TABLE 1 recovery and grade of copper powder, aluminum powder, electrode powder in example 1
Comparative example 1
In this comparative example, compared with example 1, the following spiral chute sorting and three-stage shaking table sorting steps were directly and sequentially performed without performing the steps of flotation roughing, flotation refining and flotation scavenging, and then the carbon powder material in example 1 was collected into the electrode powder, and the process parameters of the spiral chute sorting and three-stage shaking table sorting steps were kept the same as in example 1. Finally, the components of the obtained electrode powder, copper powder and aluminum powder are measured, the specific results are shown in table 2, and compared with table 1, the grade and recovery rate of the copper powder and aluminum powder in the comparative example are obviously lower than those of the embodiment 1, which means that the flotation roughing, flotation selecting and flotation scavenging steps are arranged before the spiral chute sorting step in the embodiment 1, so that the grade and recovery rate of the carbon powder materials, copper powder and aluminum powder can be obviously improved.
TABLE 2 recovery and grade of copper powder, aluminum powder, electrode powder in comparative example 1
Comparative example 2
In this comparative example, compared with example 1, the three-stage shaking table separation step was not performed, but replaced by a conventional three-stage spiral chute gravity separation method, and the above-described flotation roughing, flotation beneficiation and flotation scavenging steps remained consistent with the process conditions of example 1, i.e., the obtained carbon powder material was consistent. Finally, the components of the obtained copper powder and aluminum powder are measured, and compared with the table 3, the grade and the recovery rate of the copper powder and the aluminum powder in the comparative example are lower, and the explanation is that the three-stage shaking table is arranged after the spiral chute sorting step in the embodiment 1, so that the grade and the recovery rate of the copper powder and the aluminum powder can be remarkably improved compared with the existing common three-stage spiral chute reselection.
TABLE 3 recovery and grade of copper powder, aluminum powder, electrode powder in comparative example 2
As is clear from the comparison between the above example 1 and the comparative examples 1 to 2, the combination of flotation-spiral chute-multistage shaking table separation in the present invention, each separation step cannot be split, but needs to be strictly performed in order, so that the grade and recovery rate of carbon powder, copper foil powder and aluminum foil powder can be obtained with higher level.
Compared with the prior art, the invention provides a method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder, which comprises the steps of preparing the black powder into suspension, carrying out flotation roughing, carrying out flotation concentration, separating qualified graphite carbon powder, carrying out spiral chute and multistage shaking table reselection on the black powder after flotation, scavenging and decarburization in sequence, finally separating to obtain copper foil powder, aluminum foil powder and electrode powder, and obtaining carbon powder, copper foil powder and aluminum foil powder which have higher grade and recovery rate, thereby remarkably improving the recovery rate of the waste power battery black powder.
The foregoing examples merely illustrate embodiments of the invention and are described in more detail and are not to be construed as limiting the scope of the invention. It should be noted that it will be apparent to those skilled in the art that several variations and modifications can be made without departing from the spirit of the invention, which are all within the scope of the invention. Accordingly, the scope of protection of the present invention is to be determined by the appended claims.
Claims (9)
1. A method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder is characterized by comprising the following steps:
flotation roughing: flotation is carried out on the crushed raw ore with the granularity of-0.6 mm, and the raw ore is separated into flotation roughing tailings and flotation roughing concentrate after screening;
and (3) flotation scavenging: carrying out flotation scavenging on the flotation rougher tailings, and separating the flotation rougher tailings into flotation scavenging tailings and flotation scavenging concentrate after screening;
flotation and selection: carrying out flotation concentration on the flotation roughing concentrate, screening the flotation roughing concentrate into carbon powder materials and flotation concentration tailings, collecting the flotation concentration tailings and flotation scavenging concentrate, and refluxing the flotation concentration tailings and the flotation scavenging concentrate to carry out the flotation roughing step again;
sorting by a spiral chute: introducing the flotation scavenger tailings into a spiral chute for flushing, and dividing the flotation scavenger tailings into spiral chute tailings and spiral chute concentrates after flushing, wherein the spiral chute concentrates are recycled as electrode powder;
sorting by a primary shaking table: introducing the spiral chute tailings into a shaking table for water flow flushing, and dividing the flushing into primary coarse-grained ore, primary medium-grained ore and primary fine-grained ore;
sorting by a secondary shaking table: the primary medium-sized particle ore is guided into a shaking table for water flow flushing, and is divided into secondary coarse particle ore, secondary medium-sized particle ore and secondary fine particle ore after flushing, the secondary medium-sized particle ore is refluxed for the primary shaking table sorting step again, and the primary fine particle ore and the secondary fine particle ore are collected and recycled as electrode powder;
sorting by a three-stage shaking table: the primary coarse particle ore and the secondary coarse particle ore are led into a shaking table for water flow flushing, three-level coarse particle ore, three-level medium particle ore and three-level fine particle ore are washed, the three-level coarse particle ore is recovered as copper powder, the three-level medium particle ore is refluxed and subjected to the three-level shaking table separation step again, and the three-level fine particle ore is recovered as aluminum powder;
the flotation roughing process conditions are as follows: the aeration amount is 20-60ml/min, the pH value is 6-8, the kerosene content is 100-500g/t, and the flotation time is 1-4min.
2. The method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder according to claim 1, wherein the process conditions of the flotation scavenging step are as follows: the aeration amount is 40-120ml/min, the pH value is 6-8, the kerosene content is 100-250g/t, and the flotation time is 3-6min;
the aeration quantity in the flotation roughing step is smaller than that in the flotation scavenging step.
3. The method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder according to claim 1, wherein the process conditions of the flotation and selection step are as follows: the aeration amount is 80-120ml/min, the pH value is 6-8, the kerosene content is 50g/t, and the flotation time is 3-6min.
4. The method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder according to claim 1, wherein the water flow rate in the spiral chute step is 14-16L/min.
5. The method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder according to claim 1, wherein the water flow rate in the primary shaking table separation step is 4-6L/min.
6. The method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder according to claim 1, wherein the flow rate of water in the secondary shaking table separation step is 7-9L/min.
7. The method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder according to claim 1, wherein the water flow rate in the three-stage shaking table separation step is 10-13L/min.
8. The method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder according to claim 1, wherein the flotation roughing step is preceded by:
and (3) sequentially carrying out disassembly, discharge, cleaning and drying, primary crushing, pyrolysis and secondary crushing on the waste power batteries to obtain raw ores with the granularity of-0.6 mm.
9. The method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder according to claim 8, wherein the slag after the pyrolysis step contains a metal mixture and electrode active substances, and the slag is cooled and then subjected to secondary crushing to obtain raw ore.
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| CN202310021988.9A CN116037312A (en) | 2023-01-07 | 2023-01-07 | Method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder |
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| CN202310021988.9A CN116037312A (en) | 2023-01-07 | 2023-01-07 | Method for separating carbon powder, copper powder and aluminum powder from waste power battery black powder |
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