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WO2025118266A1 - Procédé de séparation de nickel et de fer à partir de matière première contenant du ferronickel - Google Patents

Procédé de séparation de nickel et de fer à partir de matière première contenant du ferronickel Download PDF

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Publication number
WO2025118266A1
WO2025118266A1 PCT/CN2023/137412 CN2023137412W WO2025118266A1 WO 2025118266 A1 WO2025118266 A1 WO 2025118266A1 CN 2023137412 W CN2023137412 W CN 2023137412W WO 2025118266 A1 WO2025118266 A1 WO 2025118266A1
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Prior art keywords
nickel
iron
raw material
separating
material according
Prior art date
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Application number
PCT/CN2023/137412
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English (en)
Chinese (zh)
Inventor
徐琪鹏
阮丁山
李长东
陈若葵
乔延超
何芳
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hunan Brunp Recycling Technology Co Ltd
Guangdong Brunp Recycling Technology Co Ltd
Original Assignee
Hunan Brunp Recycling Technology Co Ltd
Guangdong Brunp Recycling Technology Co Ltd
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Application filed by Hunan Brunp Recycling Technology Co Ltd, Guangdong Brunp Recycling Technology Co Ltd filed Critical Hunan Brunp Recycling Technology Co Ltd
Priority to CN202380012371.9A priority Critical patent/CN117940378B/zh
Priority to PCT/CN2023/137412 priority patent/WO2025118266A1/fr
Publication of WO2025118266A1 publication Critical patent/WO2025118266A1/fr
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G49/00—Compounds of iron
    • C01G49/02—Oxides; Hydroxides
    • C01G49/06—Ferric oxide [Fe2O3]
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G53/00—Compounds of nickel
    • C01G53/04—Oxides
    • 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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • 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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/16—Extraction of metal compounds from ores or concentrates by wet processes by leaching in organic solutions
    • 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 present disclosure relates to the technical field of hydrometallurgy, and in particular to a method for separating nickel and iron from nickel-containing iron raw materials.
  • Nickel metal is an important element of ternary lithium batteries. As the market demand for lithium battery capacity becomes higher and higher, ternary positive electrode materials are gradually developing in the direction of high nickel, and the demand for nickel sulfate is increasing.
  • Low-grade nickel matte and nickel-iron alloy contain rich nickel resources.
  • the hydrometallurgical extraction of nickel compared with the pyrometallurgical extraction of nickel from low-grade nickel matte, the hydrometallurgical extraction of nickel has the advantages of low energy consumption, simple process, simple equipment and low investment cost.
  • the separation and recovery of high-concentration nickel and iron elements in the wet leaching solution of low-grade nickel matte generally adopts the method of removing iron impurities first and then treating the nickel elements in the solution.
  • the general iron removal methods include the goethite method, the hematite method, and the sodium iron alum precipitation method.
  • the purpose of the present disclosure is to provide a method for separating nickel and iron from nickel-containing iron raw materials, which has a simple process, convenient utilization of by-products and low waste residue output.
  • the present disclosure provides a method for separating nickel and iron from a nickel-containing iron raw material, comprising:
  • the nickel-iron raw material is mixed with the oxalic acid solution and reacted and solid-liquid separated to obtain nickel-rich and iron-rich slag and nickel-poor and iron-poor liquid;
  • the nickel-rich and iron-rich slag is subjected to oxygen roasting and magnetic separation in sequence to obtain nickel oxide and ferric oxide.
  • the nickel-iron-containing raw material includes at least one of low-grade nickel matte and nickel-iron alloy.
  • the initial concentration of the oxalic acid solution is 1 mol/L-4 mol/L.
  • the initial concentration of the oxalic acid solution is 1 mol/L-2 mol/L.
  • the nickel-iron raw material is added to the oxalic acid solution at 0.8-1.1 times the stoichiometric ratio and mixed.
  • the temperature of the reaction step is 50°C-100°C, and the time is 30min-120min.
  • the temperature of the reaction step is 70°C-80°C, and the time is 90min-120min.
  • the pH value of the nickel-poor iron-poor liquid is 1.5-3.
  • the iron content in the nickel-depleted iron-depleted liquid is less than 0.05 g/L, and/or the nickel content in the nickel-depleted iron-depleted liquid is less than 0.045 g/L.
  • the temperature of the oxygen calcination step is 200° C.-450° C., and the time is 1 h-4 h.
  • the temperature of the oxygen calcination step is 300°C-350°C, and the time is 2h-3h.
  • the magnetic field strength of the magnetic separation step is 200Gs-2000Gs, and the magnetic separation time is 0.1h-1h.
  • the magnetic field strength of the magnetic separation step is 500Gs-1500Gs, and the magnetic separation time is 0.5h-1h.
  • the mass fraction of nickel in the nickel-containing iron raw material is 20wt%-35wt%, and/or the mass fraction of iron in the nickel-containing iron raw material is 60wt%-70wt%.
  • the particle size of the nickel-iron raw material is 60 mesh-300 mesh.
  • the particle size of the nickel-iron raw material is 200 mesh-300 mesh.
  • the nickel-poor iron-poor liquid is used to prepare oxalic acid solution.
  • the mass fraction of iron in the ferric oxide is greater than 67wt%, the mass fraction of nickel is less than 0.06wt%, and the content of cobalt is less than 0.03wt%.
  • the mass fraction of iron in the nickel oxide is less than 0.04wt%, the mass fraction of nickel is greater than 77wt%, and the content of cobalt is less than 0.05wt%.
  • the present invention uses oxalic acid as a leaching and precipitation agent, and while precipitating nickel and iron, most of the impurities of calcium, chromium, copper, zinc, and silicon are left in the solution, which plays a certain role in removing impurities.
  • the precipitate is then aerobically roasted to generate ferric oxide and nickel oxide, which can be separated into nickel oxide and ferric oxide with high purity after magnetic separation, wherein the nickel oxide is used as a raw material for the production of ion batteries, and the ferric oxide can also be directly sold as a by-product.
  • the method for separating nickel and iron from nickel-containing iron raw materials disclosed in the present invention is simple in process, the by-product ferric oxide is easy to use, and the waste residue output is low.
  • FIG. 1 is a process flow chart of an embodiment of the present disclosure.
  • This embodiment provides a method for separating nickel and iron from a nickel-containing iron raw material, comprising:
  • the nickel-iron raw material is mixed with the oxalic acid solution and reacted and solid-liquid separated to obtain nickel-rich and iron-rich slag and nickel-poor and iron-poor liquid;
  • the nickel-rich and iron-rich slag is subjected to oxygen roasting and magnetic separation in sequence to obtain nickel oxide and ferric oxide.
  • the reactions of formula (1) to formula (3) mainly occur, wherein the nickel-iron raw material reacts with oxalic acid in the reaction shown in formula (1), and during oxygen roasting, the reactions shown in formula (2) and formula (3) occur.
  • Ni 2+ +Fe 2+ +2C 2 O 4 2- +4H 2 O NiC 2 O 4 ⁇ 2H 2 O ⁇ +FeC 2 O 4 ⁇ 2H 2 O ⁇ (1)
  • NiC 2 O 4 ⁇ H 2 O NiO+2CO 2 +H 2 O (2)
  • 2FeC 2 O 4 ⁇ 2H 2 O Fe 2 O 3 +4CO 2 +H 2 O (3)
  • the oxalic acid solution is acidic, and can be leached with nickel and iron in the nickel-iron raw material to generate nickel oxalate and ferrous oxalate precipitation, thereby precipitating the nickel and iron elements.
  • impurity elements such as calcium, chromium, copper, zinc, and silicon in the nickel-iron raw material react with oxalic acid to generate soluble components that are transferred to the nickel-poor and iron-poor liquid, and some impurity elements such as carbon and sulfur react with oxalic acid to generate gas. Only a few elements such as Co will generate precipitation and affect the precipitation composition.
  • the content of nickel oxalate and ferrous oxalate in the obtained precipitation is high, which is convenient for the subsequent separation of nickel and iron.
  • the precipitated nickel oxalate and ferrous oxalate are roasted in an oxygen atmosphere to obtain nickel oxide and ferric oxide.
  • the nickel oxide has magnetism, while the ferric oxide has no magnetism.
  • the nickel oxide and the ferric oxide can be effectively separated after magnetic separation.
  • the atmosphere in the oxygen roasting step can be an oxygen atmosphere, or other atmospheres containing oxygen, such as air, or a mixed gas of oxygen and nitrogen.
  • This embodiment uses oxalic acid as a leaching and precipitation agent. While precipitating nickel and iron, most of the impurities of calcium, chromium, copper, zinc, and silicon are left in the solution, which plays a certain role in removing impurities. The precipitate is then aerobically roasted to generate ferric oxide and nickel oxide. After magnetic separation, nickel oxide and ferric oxide with high purity can be separated, wherein the nickel oxide is used as a raw material for the production of ion batteries, and ferric oxide can also be directly sold as a by-product. The method for separating nickel and iron from nickel-containing iron raw materials in this embodiment is simple in process, the by-product ferric oxide is easy to use, and the waste residue output is low.
  • the nickel-iron-containing raw material includes at least one of low-grade nickel matte and nickel-iron alloy, both of which contain a large amount of nickel and iron elements.
  • the initial concentration of the oxalic acid solution is 1 mol/L-4 mol/L, specifically 1 mol/L, 1.5 mol/L, 2 mol/L, 2.5 mol/L, 3 mol/L, 3.5 mol/L, 4 mol/L or any value between 1 mol/L and 4 mol/L.
  • the oxalic acid concentration is high, and the reaction rate of oxalic acid and the elements in the nickel-iron raw material is relatively faster, but in the present embodiment, since nickel and iron are leached, nickel oxalate and ferrous oxalate precipitation will be generated with oxalate, if the oxalic acid concentration is too high, the rate of precipitation generation is too fast, and the generated precipitation may be wrapped in the surface of the nickel-iron raw material particles, not only will not increase the precipitation rate, but may reduce the contact area of oxalic acid and the internal elements of the nickel-iron raw material particles, and then the leaching of elements such as nickel and iron will be suppressed, therefore, the concentration of oxalic acid solution should not be too large.
  • the initial concentration of the oxalic acid solution is 1mol/L-3mol/L, and in some embodiments, the initial concentration of the oxalic acid solution is 1mol/L-2mol/L, while ensuring the leaching precipitation effect, maintaining a higher reaction rate. In order to improve the reaction rate, in some embodiments, the reaction solution is also stirred as needed.
  • the nickel-iron raw material is added to the oxalic acid solution at 0.8-1.1 times the stoichiometric ratio, specifically 0.8, 0.85, 0.9, 0.95, 1.0, 1.05, 1.1 times or any value between 0.8 and 1.1 times.
  • the utilization rate of the raw materials for the reaction of nickel-iron raw materials and oxalic acid according to the stoichiometric ratio is higher, but in order to allow the elements in the nickel-iron raw materials to be fully leached, oxalic acid can be slightly excessive.
  • the amount of nickel-iron raw materials added is 0.8-1.0 times the stoichiometric ratio.
  • the content of each component in the nickel-iron raw material can be determined first, and then the stoichiometric ratio of the reaction of the nickel-iron raw material and oxalic acid can be calculated according to the reaction formula, and then the amount of oxalic acid and the nickel-iron raw material can be determined; for example, in theory, each component in the nickel-iron raw material a g completely reacts with oxalic acid and requires oxalic acid b g, then in the leaching step, (0.8-1.1) ⁇ a g nickel-iron raw material is added to the oxalic acid solution containing b g oxalic acid to carry out the leaching reaction.
  • the temperature of the reaction step is 50°C-100°C, specifically 50°C, 60°C, 70°C, 80°C, 90°C, 100°C or any value between 50°C-100°C; the time is 30min-120min, specifically can be 30min, 40min, 50min, 60min, 70min, 80min, 90min, 100min, 110min, 120min or any value between 30min-120min.
  • the reaction temperature In order to balance the residual amounts of ferrous oxalate and nickel oxalate, the reaction temperature needs to be reasonably set. In addition, the reaction temperature also affects the reaction rate of the nickel-containing iron raw material with oxalic acid, which in turn affects the precipitation efficiency. In some embodiments, the temperature of the reaction step is 70°C-80°C, and the time is 90min-120min, taking into account the precipitation effect and reaction efficiency of ferrous oxalate and nickel oxalate.
  • the pH value of the nickel-depleted and iron-depleted liquid is 1.5-3, specifically, it can be 1.5, 1.8, 2.1, 2.4, 2.7, 3 or any value between 1.5 and 3.
  • Oxalic acid is used to leach nickel and iron in nickel-iron containing raw materials, and excess oxalic acid remains in the nickel-depleted and iron-depleted leachate.
  • excess oxalic acid is beneficial to the full leaching of elements in the nickel-iron containing raw materials, and reduces the residual nickel and iron in the nickel-depleted and iron-depleted leachate.
  • the solubility of ferrous oxalate is greatly reduced, and the presence of oxalic acid also reduces the solubility of nickel oxalate.
  • other elements in the nickel-iron containing raw materials such as magnesium oxalate, are more soluble under acidic conditions. Therefore, maintaining acidic conditions in the nickel-depleted and iron-depleted liquid is more conducive to the separation of nickel and iron from other elements.
  • the iron content in the nickel-poor iron-poor liquid is less than 0.05 g/L, and/or the nickel content in the nickel-poor iron-poor liquid is less than 0.045 g/L.
  • the nickel and iron elements in the nickel-containing iron raw material are leached and precipitated with oxalic acid, and the residual amounts of nickel and iron in the nickel-poor iron-poor liquid are very low.
  • the iron content in the nickel-poor iron-poor liquid can reach 0.032 g/L, and the nickel content can reach 0.026 g/L.
  • the temperature of the oxygen roasting step is 200°C-450°C, specifically 200°C, 230°C, 270°C, 300°C, 330°C, 360°C, 390°C, 420°C, 450°C or any value between 200°C and 450°C; the time is 1h-4h, specifically 1h, 1.5h, 2h, 2.5h, 3h, 3.5h, 4h or any value between 1h-4h.
  • the purpose of oxygen roasting is to fully oxidize the elements in the nickel-rich and iron-rich slag, especially to oxidize the non-magnetic nickel oxalate into magnetic nickel oxide.
  • the non-magnetic iron oxalate is oxidized into non-magnetic ferric oxide, and the difference in magnetism is used to separate the nickel oxide from other components.
  • the temperature and time of the aerobic roasting step need to be reasonably set.
  • the temperature of the aerobic roasting step is 300°C-350°C and the time is 2h-3h to ensure that nickel oxalate and ferrous oxalate can be fully oxidized to nickel oxide and ferric oxide.
  • the magnetic field strength of the magnetic separation step is 200Gs-2000Gs, specifically 200Gs, 400Gs, 600Gs, 800Gs, 1000Gs, 1200Gs, 1400Gs, 1600Gs, 1800Gs, 2000Gs or any value between 200Gs and 2000Gs;
  • the magnetic separation time is 0.1h-1h, specifically 0.1h, 0.2h, 0.4h, 0.6h, 0.8h, 1h or any value between 0.1h-1h.
  • the increase in magnetic field strength is conducive to reducing the residual nickel oxide in ferric oxide, which is conducive to the complete separation of nickel oxide, but it will also cause the content of ferric oxide mixed in the separated nickel oxide to increase, resulting in excessive impurity content in nickel oxide, but the recovery rate of nickel element is relatively high, considering the purity and recovery rate of the separated nickel oxide, the magnetic field strength should not be too large, but the magnetic field strength is too small, which will also cause incomplete separation of nickel oxide, and the recovery rate is relatively low, and the magnetic separation efficiency will also be reduced, so the magnetic field strength and magnetic separation time need to be reasonably set.
  • the magnetic field strength of the magnetic separation step is 500Gs-1500Gs, and the magnetic separation time is 0.5h-1h, taking into account the purity and recovery rate of nickel oxide.
  • the mass fraction of nickel in the nickel-containing iron raw material is 20wt%-35wt%, specifically 20wt%, 23wt%, 26wt%, 29wt%, 32wt%, 35wt% or any value between 20wt% and 35wt%; and/or the mass fraction of iron in the nickel-containing iron raw material is 60wt%-70wt%, specifically 60wt%, 62wt%, 64wt%, 66wt%, 68wt%, 70wt% or any value between 60wt% and 70wt%.
  • the total content of nickel and iron in nickel-containing iron raw materials such as low-grade nickel matte is about 90wt%, and the content of other impurities is relatively small.
  • the method disclosed in the present invention can also be applied.
  • the particle size of the nickel-iron raw material is 60 mesh-300 mesh, specifically, it can be 60 mesh, 100 mesh, 150 mesh, 200 mesh, 250 mesh, 300 mesh or any value between 60 mesh and 300 mesh.
  • Crushing the nickel-iron raw material is beneficial to increasing the contact area between the nickel-iron raw material and oxalic acid, thereby facilitating the leaching of elements in the nickel-iron raw material.
  • precipitate is generated while nickel-iron is leached. If the particle size of the nickel-iron raw material is too large, the reaction difficulty and reaction time will increase. If the particle size is too small, it will be difficult to crush, and the equipment requirements and energy consumption will be high.
  • the particle size of the nickel-iron raw material is 200 mesh to 300 mesh, which ensures the leaching effect while controlling the cost.
  • the nickel-depleted and iron-depleted liquid is used to prepare an oxalic acid solution, and excess oxalic acid that is not combined with nickel and iron is transferred to the nickel-depleted and iron-depleted solution, which contains only a small amount of soluble impurity components. Using it for the preparation of the oxalic acid solution is beneficial to improving the utilization efficiency of raw materials and reducing raw material costs and waste liquid emissions.
  • the mass fraction of iron in the ferric oxide is greater than 67wt%, the mass fraction of nickel is less than 0.06wt%, and the content of cobalt is less than 0.03wt%.
  • the purity of the ferric oxide obtained after magnetic separation (assuming that the contents of ferrous oxide and ferroferric oxide are negligible, and iron exists in the form of ferric oxide) is greater than 96.6%, and can reach up to 98.9%, which can be directly used as a by-product, or further purified according to the needs.
  • the mass fraction of iron in the nickel oxide is less than 0.04wt%, the mass fraction of nickel is greater than 77wt%, and the content of cobalt is less than 0.05wt%.
  • the purity of the nickel oxide obtained after magnetic separation is greater than 98.25%, and can reach up to 98.7% at most.
  • the impurity content is low, and it can be used directly, and it is also convenient to further purify according to the needs.
  • a method for separating nickel and iron from nickel-containing iron raw materials as shown in FIG1, the specific process is:
  • the powder obtained by calcining step (2) is magnetically separated at a magnetic separation intensity of 1500 Gs for 0.5 h to obtain separated nickel oxide and ferric oxide.
  • a method for separating nickel and iron from nickel-containing iron raw materials is:
  • the powder obtained by calcining step (2) is magnetically separated at a magnetic separation intensity of 1000 Gs for 0.5 h to obtain separated nickel oxide and ferric oxide.
  • a method for separating nickel and iron from nickel-containing iron raw materials is:
  • the powder obtained by calcining step (2) is magnetically separated at a magnetic separation intensity of 500 Gs for 1 hour to obtain separated nickel oxide and ferric oxide.
  • the iron-poor nickel solution obtained in step 1 of the above embodiment 1-3 was analyzed for element content, and the results are shown in Table 1.
  • the ferric oxide powder obtained after magnetic separation contains low nickel and cobalt content and is mainly iron, which can be further processed into iron products.
  • step 3 of the above embodiment 1-3 was analyzed for element content, and the results are shown in the following table:
  • a method for separating nickel and iron from nickel-containing iron raw materials which differs from Example 1 only in that: the roasting is carried out in a nitrogen atmosphere, the roasting temperature is 500°C, and the slag phase after roasting and magnetic separation is black, which is different from the black and red mixed phase in Example 1.
  • a method for separating nickel and iron from nickel-containing iron raw materials which differs from Example 1 only in that the calcination is carried out in an argon atmosphere, the calcination temperature is 520° C., and the slag phase after calcination and magnetic separation is black.
  • Example 4 The components of the nickel oxide powders obtained in Example 4 and Example 5 were analyzed. The results are shown in Table 4.
  • a method for separating nickel and iron from a nickel-containing iron raw material which differs from Example 1 only in that: 1.5 mol/L of oxalic acid is used, and the reaction is carried out after 1 hour of filtration to obtain an iron-depleted and nickel-depleted solution in which the iron and nickel concentrations are 0.025 g/L and 0.046 g/L, respectively.
  • a method for separating nickel and iron from a nickel-containing iron raw material the difference from Example 1 is that the oxalic acid used is 1 mol/L, and the reaction is carried out for 4 hours before filtration to obtain an iron-poor and nickel-poor solution with iron and nickel concentrations of 0.065 g/L and 0.025 g/L, respectively.
  • Example 6 Comparing Examples 6 and 7 with Example 1, the nickel and iron concentrations in the nickel-depleted and iron-depleted liquids are both trace amounts, but their reaction times are different.
  • the nickel oxalate concentration in Example 7 is lower, and its leaching + precipitation time is longer.
  • the reaction time of Example 6 was shortened, but it was prolonged when the oxalic acid concentration was increased to 2 mol/L in Example 1. This may be because the reaction rate was slow at low concentration, while the large amount of precipitation generated at high concentration hindered the leaching and precipitation of the raw materials.
  • the present disclosure provides a method for separating nickel and iron from a nickel-iron alloy, comprising:
  • step 1 Add the diluted nickel-iron sulfate solution in step 1 to an autoclave and heat to 100°C with continuous stirring. Oxygen is introduced to exclude the air in the reactor, and the oxygen pressure is controlled to be 0.3MPa. Subsequently, a crude nickel carbonate intermediate is continuously added to the reaction system, and the feeding rate is controlled at 1.4-1.45g/min (a total amount of 257g, which is the amount of nickel per 98% of the total iron molar amount in the mixed solution) to control the reaction pH value to not exceed 2.5. When all the crude nickel carbonate intermediates have been added, continue the reaction for 30 minutes to ensure that the reaction is completely carried out. Stop the reaction and filter to obtain a crude nickel sulfate solution and goethite slag. The components of the crude nickel carbonate intermediate and the crude nickel sulfate solution are shown in Table 5.
  • an oxidant ferrous oxide is added and then a nickel-cobalt intermediate is used to control the pH to remove iron from the leachate in the form of goethite. This will cause the goethite slag to be mixed with a certain amount of nickel, resulting in nickel loss, and the iron element with the largest metal content in nickel iron is not effectively utilized.
  • the present invention uses oxalic acid as a leaching and precipitation agent, and while precipitating nickel and iron, most of the impurities of calcium, chromium, copper, zinc, and silicon are left in the solution, which plays a certain role in removing impurities.
  • the precipitate is then aerobically roasted to generate ferric oxide and nickel oxide, which can be separated into nickel oxide and ferric oxide with high purity after magnetic separation, wherein the nickel oxide is used as a raw material for the production of ion batteries, and the ferric oxide can also be directly sold as a by-product.
  • the method for separating nickel and iron from nickel-containing iron raw materials in this embodiment is simple in process, the by-product ferric oxide is easy to use, and the waste residue output is low.

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Abstract

Procédé de séparation de nickel et de fer d'une matière première contenant du ferronickel, consistant à : utiliser de l'acide oxalique en tant qu'agent de lixiviation et agent de précipitation, laissant la plupart des impuretés telles que le calcium, le chrome, le cuivre, le zinc et le silicium dans une solution tout en précipitant le nickel et le fer, de façon à obtenir un certain effet d'élimination d'impuretés ; puis réaliser une torréfaction aérobie sur des précipités pour produire de l'oxyde ferrique et de l'oxyde de nickel ; et réaliser une séparation magnétique pour obtenir de l'oxyde de nickel et de l'oxyde ferrique de pureté élevée, l'oxyde de nickel étant utilisé en tant que matière première pour la production de batteries ioniques, et l'oxyde ferrique, en tant que sous-produit, pouvant également être directement vendu. Le procédé présente les avantages d'un processus simple, d'une utilisation pratique de l'oxyde ferrique sous-produit et d'un faible rendement de résidus de déchets.
PCT/CN2023/137412 2023-12-08 2023-12-08 Procédé de séparation de nickel et de fer à partir de matière première contenant du ferronickel Pending WO2025118266A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
CN202380012371.9A CN117940378B (zh) 2023-12-08 2023-12-08 从含镍铁原料中分离镍和铁的方法
PCT/CN2023/137412 WO2025118266A1 (fr) 2023-12-08 2023-12-08 Procédé de séparation de nickel et de fer à partir de matière première contenant du ferronickel

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Citations (9)

* Cited by examiner, † Cited by third party
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