WO2024045530A1 - Procédé de récupération de nickel - Google Patents

Procédé de récupération de nickel Download PDF

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Publication number
WO2024045530A1
WO2024045530A1 PCT/CN2023/079348 CN2023079348W WO2024045530A1 WO 2024045530 A1 WO2024045530 A1 WO 2024045530A1 CN 2023079348 W CN2023079348 W CN 2023079348W WO 2024045530 A1 WO2024045530 A1 WO 2024045530A1
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Prior art keywords
nickel
aluminum
iron
liquid
leaching agent
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PCT/CN2023/079348
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English (en)
Chinese (zh)
Inventor
陈佳佳
李长东
阮丁山
陈若葵
乔延超
曾志佳
Original Assignee
广东邦普循环科技有限公司
湖南邦普循环科技有限公司
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Publication of WO2024045530A1 publication Critical patent/WO2024045530A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F7/00—Compounds of aluminium
    • C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
    • C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
    • C01F7/14—Aluminium oxide or hydroxide from alkali metal aluminates
    • C01F7/141—Aluminium oxide or hydroxide from alkali metal aluminates from aqueous aluminate solutions by neutralisation with an acidic agent
    • C01F7/142—Aluminium oxide or hydroxide from alkali metal aluminates from aqueous aluminate solutions by neutralisation with an acidic agent with carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B21/00—Obtaining aluminium
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00—Obtaining nickel or cobalt
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the invention belongs to the technical field of waste battery recycling and relates to a method for recycling nickel.
  • Batteries have developed rapidly in recent years and are widely used in many fields such as digital electronics, smart grids, electric vehicles, and large-scale energy storage materials.
  • battery cycle life is always limited, which means that the generation of used batteries is also increasing year by year.
  • the waste materials in used batteries include heavy metals such as nickel, iron, and aluminum. These waste materials will pollute soil, air, and water sources, posing a great threat to the environment.
  • hydrosmelting processes are generally used to process the above-mentioned waste materials, and in the impurity removal process, the main purpose is to remove iron and aluminum impurities.
  • Industrially by adding sodium hydroxide or soda ash, the iron in the solution is precipitated in the form of sodium vitriol or ferric hydroxide, and the aluminum is precipitated in the form of aluminum vitriol or aluminum hydroxide.
  • the resulting slag is filtered and washed. Recycle.
  • the above treatment process will leave a large amount of nickel in the iron-aluminum slag obtained after removing iron and aluminum, resulting in the loss of metallic nickel and a low recovery rate of nickel.
  • the present invention aims to solve at least one of the technical problems existing in the prior art. To this end, the present invention proposes a method for recovering nickel, which realizes the separation of nickel and impurity metals.
  • step S2 Mix the solid phase product obtained in step S1 with the leaching agent, separate the solid and liquid, and collect the liquid phase product;
  • the leaching agent includes at least one of ammonia water and ammonium salt solution
  • the nickel-containing waste residue also includes iron, aluminum and sodium elements,
  • the nickel-containing waste residue also includes SO 4 2- ;
  • step S1 the molar ratio of NH 4 + in the leaching agent and SO 4 2- in the nickel-containing waste residue is (2-2.05):1.
  • the present invention uses a leaching agent to reduce slag while increasing the nickel content in the slag, and then uses the valuable metal nickel to combine with free ammonia to form complex ions and enter the solution, while impurity ions such as iron and aluminum remain in the slag, thereby achieving valuable Separation of metallic nickel from metallic impurities.
  • NH 4 + in the leaching agent and SO 4 2- in the nickel-containing waste residue are within the molar ratio within the above range to ensure that the (NH 4 ) 2 SO 4 while avoiding the leaching of nickel.
  • the aluminum compound includes NaAl 3 (SO 4 ) 2 (OH) 6 .
  • the iron compound includes NaFe 3 (SO 4 ) 2 (OH) 6 .
  • the solute of the ammonium salt solution includes at least one of ammonium chloride, ammonium sulfate, ammonium bicarbonate and ammonium carbonate.
  • the iron compound and the aluminum compound are in the form of NaAl 3 (SO 4 ) 2 (OH) 6 and NaFe 3 (SO 4 ) 2 (OH) 6 Yes, in step S1 of the present invention, the leachate is added and the solid-liquid separation is performed to obtain a liquid phase (a mixture of sodium sulfate and ammonium sulfate) and a solid phase (remaining iron-aluminum slag containing nickel 1).
  • the reaction equation after adding the leaching agent in step S2 is as shown in formulas (1) and (2).
  • the ability of ammonia molecules (NH 3 ) to complex nickel is stronger than the ability of CO 3 2- /OH - to precipitate nickel, which is valuable.
  • Metal nickel combines with free ammonia to form complex ions and enters the solution, making the reaction more conducive to the formation of the nickel ammonia complex [Ni(NH 3 ) n ] 2+ , thereby speeding up the leaching rate of nickel and improving the leaching of nickel. Rate.
  • the contents of aluminum and iron in the leachate are both less than 0.1mg/L, so almost all nickel can be recovered in the leachate, and a relatively pure nickel leachate can be obtained, achieving the separation of metallic nickel and iron and aluminum slag.
  • step S1 the mass fraction of aluminum in the solid phase product is 10%-30%, the mass fraction of iron is 15%-35%, and the mass fraction of nickel is 2%-6%.
  • step S1 the liquid phase product obtained after solid-liquid separation is subjected to impurity removal treatment to form the leaching agent.
  • the mass concentration of ammonium salt is 5-30g/L.
  • the liquid phase product collected after the solid-liquid separation includes sodium salt solution.
  • step S1 when step S1 includes sodium element, the leaching rate of sodium salt is greater than 60%
  • the leaching agent is formed from the liquid phase product obtained after solid-liquid separation in step S1 after impurity removal treatment.
  • the impurity removal includes cooling crystallization.
  • step S2 the temperature of the cooling crystallization is 2-6°C.
  • the crystallization of sodium sulfate is ensured, and the recovery rate of sodium salt under cooling crystallization is more than 60%. At the same time, the increase in energy consumption caused by too low temperature is avoided.
  • the obtained leaching agent can be directly used in step S1 for recycling.
  • the molar concentration of ammonia water is 0.3-1 mol/L.
  • the molar amount of the ammonium salt solution is 0.3-1 mol/L.
  • the solid-liquid ratio of the nickel-containing waste residue and the leaching agent is (5-10):1; the solid-liquid ratio is a mass ratio.
  • leaching agent within the above range not only ensures the leaching rate of nickel, but also avoids waste caused by excessive concentration of leaching agent.
  • the leaching agent is a mixture of ammonia water and ammonium salt solution.
  • step S2 a mixture of ammonia water and ammonium salt solution is used as the leachate.
  • the ammonium salt is basically saturated, continuing to add ammonia water to the solution can further increase the total ammonia amount in the solution and the ammonia gas molecules.
  • the ability of (NH 3 ) to complex nickel is stronger than the ability of CO 3 2- /OH - to precipitate nickel.
  • Valuable metal nickel combines with free ammonia to form complex ions and enters the solution, making the reaction more conducive to the formation of nickel ammonia complex.
  • the direction of [Ni(NH 3 ) n ] 2+ moves to speed up the leaching rate of nickel and increase the nickel leaching rate.
  • the aluminum and iron contents in the leachate are both less than 0.1mg/L, so basically all nickel can be recovered in the leachate, and a relatively pure nickel leachate can be obtained, achieving the separation of valuable metal nickel and impurity metals.
  • step S1 the mixing temperature is 30-50°C.
  • the reaction temperature within the above range not only ensures the leaching rate of nickel, but also avoids waste caused by excessive concentration of leaching agent.
  • the leaching agent further includes additional added ammonia water.
  • step S2 the amount of additional ammonia water added is 0.3-1 mol.
  • the mixing includes stirring and mixing, and the stirring speed is 200-700 r/min.
  • step S2 the mixing time is 1-10 h.
  • step S2 the mixing temperature is 30-70°C.
  • step S2 the mixing temperature is 30-35°C.
  • the mixing includes stirring and mixing, and the stirring speed is 200-700 r/min.
  • step S2 after the solid-liquid separation, the solid phase product is also collected,
  • the collected solid phase products include iron-containing compounds and aluminum-containing compounds (remaining iron-aluminum slag 2).
  • step S2 also includes the following steps:
  • step S4 The liquid phase product obtained in step S3 is prepared by carbon separation method to obtain aluminum hydroxide and recovered; the solid phase product obtained in step S3 is recycled to step S1 to continue the reaction.
  • the liquid alkali includes at least one of sodium hydroxide solution, sodium carbonate solution and calcium carbonate solution.
  • the mass concentration of the liquid caustic soda is 15%-45%
  • step S2 the temperature at which the solid phase product and the liquid alkali are mixed is 70-150°C.
  • the above temperature ensures the leaching of aluminum while avoiding high energy consumption caused by excessive temperature.
  • step S2 the mixing method of the solid phase product and the liquid alkali includes stirring.
  • step S2 the stirring speed of the solid phase product and the liquid caustic soda is 200-700 r/min.
  • step S2 the stirring time of the solid phase product and the liquid caustic soda is 1-10 h.
  • the causticity ratio of the mixture of the solid phase product and the liquid alkali is 2.5-7.5.
  • the mass concentration of aluminum is 10-40g/L, and the mass concentration of nickel and iron is less than 0.1 mg/L.
  • the carbon separation method includes mixing the liquid phase product and carbon dioxide.
  • step S4 the introduction rate of carbon dioxide is 2-8L/min.
  • the rate within the above range ensures the reaction efficiency and avoids tank leakage.
  • step S4 the mixing of the liquid phase product and carbon dioxide includes stirring and mixing.
  • step S4 the liquid phase product and carbon dioxide are mixed and stirred at a rate of 200-500 r/min.
  • step S4 the pH of the mixed liquid after mixing is 9.5-11.5.
  • step S4 the temperature at which the liquid phase product and carbon dioxide are mixed is 30-90°C.
  • the carbon separation method further includes an aging reaction.
  • the aging stirring speed is 10-100 r/min.
  • the stirring time of the aging reaction is 6-12 h.
  • the temperature of the aging reaction is 60-90°C.
  • step S3 and step S4 of the present invention are as follows:
  • the solid phase product in step S3 is iron-aluminum slag, in which aluminum exists in the form of aluminum vitriol, which can be generated by alkali leaching to generate sodium metaaluminate solution, while the iron element in the iron-aluminum slag is enriched and retained in the slag.
  • the sodium metaaluminate solution is prepared by carbon separation method and then the aluminum is recovered.
  • the by-product sodium carbonate solution is obtained, and the alkali slag containing iron is returned to the system. .
  • This alkali slag treatment process can turn the original hazardous waste iron and aluminum slag into usable aluminum hydroxide products, sodium carbonate solution, and economically valuable goethite.
  • the invention processes hazardous solid waste iron and aluminum slag into resources, not only recovers high-priced nickel metal that is harmful to the environment, but also utilizes the aluminum in it to produce aluminum hydroxide with economic value.
  • the process of the invention is simple and feasible, and can realize the separation of nickel, iron and aluminum, so as to treat them as resources respectively;
  • the aluminum hydroxide post-liquid obtained in the process is sodium carbonate solution, which can be reused in the system, and no waste water is generated in this process.
  • Figure 1 is a process flow chart of a method for recovering nickel in Embodiment 1 of the present invention.
  • This embodiment discloses a method for recovering nickel, which is used to process nickel-containing waste residue.
  • the components of the nickel-containing waste residue are: in terms of mass percentage: 3.15% nickel, 67.18% sulfate, 7.29% aluminum, 9.68%
  • the process flow chart of iron-aluminum slag is shown in Figure 1.
  • the test standards in steps A1-A4 are ICP element tests:
  • A1 Iron-aluminum slag reduction process: Take 100g of the above nickel-containing waste slag in a beaker, prepare a mixed solution of ammonia water and ammonium sulfate of 0.5 mol/L, and stir the mixed solution and nickel-containing waste slag into a liquid-to-solid ratio of 5:1 The slurry has a temperature of 30°C and is reacted at a constant temperature for 3 hours at a stirring speed of 300 r/min. After the reaction is completed, filter it while it is hot to obtain about 60 g of remaining iron-aluminum slag and sodium sulfate-ammonium sulfate mixed solution.
  • the sodium sulfate-ammonium sulfate mixture was freeze-crystallized in a refrigerated reaction kettle at a crystallization temperature of 5°C and stirred at a rotation speed of 300 r/min for 3 hours. After the crystallization was completed, it was quickly centrifuged and dried to obtain an ammonium sulfate solution and sodium sulfate crystals.
  • the remaining nickel-containing waste residue (iron-aluminum slag 1) contains 5.25% nickel, 16.13% iron, and 12.15% aluminum; the sodium sulfate recovery rate is 60%.
  • A2 Leach 60g of iron-aluminum slag 1 from the above step A1.
  • the leaching liquid is an ammonia-ammonium salt mixture with 0.5 mol of ammonia added to the ammonium sulfate solution in step A1.
  • the liquid-to-solid ratio is 5:1 and the leaching temperature is 40 Stir the reaction for 2 hours at °C, filter it while hot after the reaction is completed, and obtain the iron-aluminum slag 2 and the nickel-containing leachate; the nickel content in the iron-aluminum slag 2 is less than 1%, and the iron content is 19.4%.
  • A3 Take the remaining iron and aluminum slag 2 from step A2 in a beaker, add 86.5g of sodium hydroxide with a mass concentration of 30%, and react at a constant temperature of 80°C for 3 hours at a stirring speed of 500r/min. After the reaction is completed, the slurry is filtered while it is hot. Sodium metaaluminate solution and alkali slag are obtained; among them, the nickel and iron in the sodium metaaluminate solution are both less than 0.1ppm, and the aluminum content is 34.73g/L. The alkali slag contains less than 1% nickel, 29.8% iron content, and 3.97% aluminum. .
  • This embodiment discloses a method for recovering nickel to process nickel-containing waste slag.
  • the components of nickel-containing waste slag are: based on mass concentration: 3.15% nickel, 67.18% sulfate, 7.29% aluminum, 9.68% iron iron-aluminum slag. .
  • the test standard in steps A1-A4 is ICP element testing. The specific steps are:
  • A1 Iron-aluminum slag reduction process: Take 100g of the above nickel-containing waste slag in a beaker, prepare a mixed solution of 0.5mol/L ammonia water and 0.6mol/L ammonium sulfate, and mix the mixed solution and the nickel-containing waste slag with a liquid-to-solid ratio of 6:1. The nickel waste residue was stirred into a slurry at a temperature of 40°C, and reacted at a constant temperature for 4 hours at a stirring speed of 350 r/min. After the reaction was completed, it was filtered while it was hot to obtain about 50g of the remaining iron-aluminum slag and sodium sulfate-ammonium sulfate mixture.
  • the sodium sulfate-ammonium sulfate mixture was frozen and crystallized in a refrigerated reaction kettle.
  • the crystallization temperature was 4°C and the rotation speed was 350 r/min.
  • the mixture was stirred for 4 hours. After the crystallization, it was quickly centrifuged and dried to obtain an ammonium sulfate solution and sodium sulfate crystals.
  • the remaining nickel-containing waste residue (iron-aluminum slag 1) contains 6.3% nickel, 19.36% iron, and 14.58% aluminum; the sodium sulfate recovery rate is 75%.
  • A2 Leach 50g of iron-aluminum slag 1 from the above step A1.
  • the leaching liquid is an ammonia-ammonium salt mixture with 0.6 mol of ammonia added to the ammonium sulfate solution in step A1.
  • the liquid-to-solid ratio is 6:1 and the leaching temperature is 50 Stir and react at °C for 3 hours. After the reaction is completed, filter while hot to obtain iron-aluminum slag 2 and nickel-containing leachate.
  • the nickel content in iron-aluminum slag 2 is less than 1%, the iron content is 20.5%, and the aluminum content is 17.22%.
  • A3 Take the remaining iron and aluminum slag 2 from step A2 in a beaker, add 153.08g of sodium hydroxide solution with a mass concentration of 25% based on 1.5 times the mole number of aluminum, and react at a constant temperature of 90°C for 4 hours at a stirring speed of 450r/min. , after the reaction is completed, the slurry is filtered while hot to obtain sodium metaaluminate solution and alkali slag respectively; among them, the nickel and iron in the sodium metaaluminate solution are both less than 0.1ppm, the aluminum content is 35.52g/L, and the nickel content of the alkali slag is less than 1 %, iron content 29.8%, aluminum content 2.81%.
  • This embodiment discloses a method for recovering nickel to process nickel-containing waste slag.
  • the components of nickel-containing waste slag are: based on mass concentration: 3.15% nickel, 67.18% sulfate, 7.29% aluminum, 9.68% iron iron-aluminum slag.
  • the test standard in steps A1-A4 is ICP element test, the specific steps are:
  • A1 Iron-aluminum slag reduction process: Take 100g of the above nickel-containing waste slag in a beaker, prepare a mixed solution of 0.5mol/L ammonia water and 0.7mol ammonium sulfate, and mix the mixed solution and nickel-containing waste slag with a liquid-to-solid ratio of 7:1 Stir into a slurry at a temperature of 50°C and react at a constant temperature for 5 hours at a stirring speed of 400r/min. After the reaction is completed, filter while it is hot to obtain about 40g of remaining iron-aluminum slag and sodium sulfate-ammonium sulfate mixed solution.
  • the sodium sulfate-ammonium sulfate mixture was frozen and crystallized in a refrigerated reaction kettle.
  • the crystallization temperature was 3°C and the rotation speed was 400 r/min.
  • the mixture was stirred for 5 hours. After the crystallization, it was quickly centrifuged and dried to obtain an ammonium sulfate solution and sodium sulfate crystals.
  • the remaining nickel-containing waste residue (iron-aluminum slag 1) contains 7.86% nickel, 24.2% iron, and 18.23% aluminum; the sodium sulfate recovery rate is 89%.
  • A2 Leach 40g of iron-aluminum slag 1 from the above step A1.
  • the leaching liquid is an ammonia-ammonium salt mixture with 0.7 mol of ammonia added to the ammonium sulfate solution in step A1.
  • the liquid-to-solid ratio is 7:1 and the leaching temperature is 60 Stir and react at °C for 4 hours. After the reaction is completed, filter while hot to obtain iron-aluminum slag 2 and nickel-containing leachate.
  • the nickel content in iron-aluminum slag 2 is less than 1%, the iron content is 32.1%, and the aluminum content is 24.3%.
  • step A3 Take the remaining iron and aluminum slag 2 from step A2 in a beaker, add 288.02g of sodium hydroxide solution with a mass concentration of 20% based on 2 times the mole number of aluminum, and react at a constant temperature of 100°C for 5 hours at a stirring speed of 400r/min. , after the reaction is completed, the slurry is filtered while hot to obtain sodium metaaluminate solution and alkali slag respectively; among them, the nickel and iron in the sodium metaaluminate solution are both less than 0.1ppm, the aluminum content is 36.88g/L, and the nickel in the alkali slag is less than 1% , iron content 29.8%, aluminum 0.99%.
  • This comparative example discloses a method for recycling nickel to process nickel-containing waste residue. The specific steps are:

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Abstract

La présente invention concerne un procédé de récupération de nickel. Le procédé comprend les étapes suivantes consistant à : S1, mélanger un résidu de déchets contenant du nickel et un agent de lixiviation, réaliser une séparation solide-liquide, et collecter un produit en phase solide ; et S2, mélanger le produit en phase solide obtenu à l'étape S1 et un agent de lixiviation, réaliser une séparation solide-liquide, et collecter un produit en phase liquide. L'agent de lixiviation comprend au moins l'un parmi l'hydroxyde d'ammonium et une solution de sel d'ammonium, le résidu de déchets contenant du nickel comprend en outre du fer, de l'aluminium et du sodium, et le résidu de déchets contenant du nickel comprend en outre du SO4 2-. À l'étape S1, le rapport molaire de NH4+ dans l'agent de lixiviation à SO4 2- dans le résidu de déchets contenant du nickel est (2-2,05):1. Le procédé de la présente invention permet d'obtenir une séparation du nickel et de métaux présents en tant qu'impuretés.
PCT/CN2023/079348 2022-09-01 2023-03-02 Procédé de récupération de nickel WO2024045530A1 (fr)

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CN202211062581.2A CN115821041A (zh) 2022-09-01 2022-09-01 一种回收镍的方法
CN202211062581.2 2022-09-01

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2808263A1 (de) * 1977-03-01 1978-09-07 Univ Tohoku Verfahren zur rueckgewinnung von nickel aus nickelhaltigen rueckstaenden
KR20010001055A (ko) * 1999-06-01 2001-01-05 김수태 폐기물에서 닉켈 또는 닉켈 화합물의 회수방법
CN103343232A (zh) * 2013-07-11 2013-10-09 岳阳鼎格云天环保科技有限公司 一种从废FCC催化剂中回收Ni的方法
CN107230811A (zh) * 2016-03-25 2017-10-03 中国科学院过程工程研究所 一种正极材料中金属组分的选择性浸出剂及回收方法
CN113249574A (zh) * 2021-04-07 2021-08-13 广东邦普循环科技有限公司 利用选择性浸出回收废正极片中铝的方法及其应用
CN113789447A (zh) * 2021-08-31 2021-12-14 广东邦普循环科技有限公司 回收电池粉浸出所得铁铝渣中镍的方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2808263A1 (de) * 1977-03-01 1978-09-07 Univ Tohoku Verfahren zur rueckgewinnung von nickel aus nickelhaltigen rueckstaenden
KR20010001055A (ko) * 1999-06-01 2001-01-05 김수태 폐기물에서 닉켈 또는 닉켈 화합물의 회수방법
CN103343232A (zh) * 2013-07-11 2013-10-09 岳阳鼎格云天环保科技有限公司 一种从废FCC催化剂中回收Ni的方法
CN107230811A (zh) * 2016-03-25 2017-10-03 中国科学院过程工程研究所 一种正极材料中金属组分的选择性浸出剂及回收方法
CN113249574A (zh) * 2021-04-07 2021-08-13 广东邦普循环科技有限公司 利用选择性浸出回收废正极片中铝的方法及其应用
CN113789447A (zh) * 2021-08-31 2021-12-14 广东邦普循环科技有限公司 回收电池粉浸出所得铁铝渣中镍的方法

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