WO2024239283A1 - 粗制氢氧化钴连续选择性浸出工艺、浸出装置及二段浸出设备、钴产品生产工艺及生产系统 - Google Patents

粗制氢氧化钴连续选择性浸出工艺、浸出装置及二段浸出设备、钴产品生产工艺及生产系统 Download PDF

Info

Publication number
WO2024239283A1
WO2024239283A1 PCT/CN2023/096095 CN2023096095W WO2024239283A1 WO 2024239283 A1 WO2024239283 A1 WO 2024239283A1 CN 2023096095 W CN2023096095 W CN 2023096095W WO 2024239283 A1 WO2024239283 A1 WO 2024239283A1
Authority
WO
WIPO (PCT)
Prior art keywords
slurry
leaching
cobalt hydroxide
component
crude cobalt
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/CN2023/096095
Other languages
English (en)
French (fr)
Inventor
邱颖
唐盛贺
刘胜卿
王皓
李长东
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
Yichang Brunp Recycling Technology Co Ltd
Yichang Brunp Contemporary Amperex Co Ltd
Original Assignee
Hunan Brunp Recycling Technology Co Ltd
Guangdong Brunp Recycling Technology Co Ltd
Yichang Brunp Recycling Technology Co Ltd
Yichang Brunp Contemporary Amperex Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Hunan Brunp Recycling Technology Co Ltd, Guangdong Brunp Recycling Technology Co Ltd, Yichang Brunp Recycling Technology Co Ltd, Yichang Brunp Contemporary Amperex Co Ltd filed Critical Hunan Brunp Recycling Technology Co Ltd
Priority to CN202380009229.9A priority Critical patent/CN116964232A/zh
Priority to PCT/CN2023/096095 priority patent/WO2024239283A1/zh
Publication of WO2024239283A1 publication Critical patent/WO2024239283A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/06—Refining
    • 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
    • C22B3/02—Apparatus therefor
    • 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
    • C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions

Definitions

  • This article relates to a continuous selective leaching process for crude cobalt hydroxide, a leaching device and a two-stage leaching equipment, a cobalt product production process and a production system.
  • Nonferrous metals are basic materials for the development of the national economy. With the rapid development of my country's economy, the demand for nonferrous metals is increasing, and nonferrous metal extraction and metallurgical technology should also continue to innovate with the development of science and technology.
  • cobalt Since cobalt has similar chemical properties to nickel, iron, manganese and copper, they are often found together in natural minerals, and minerals often contain these elements at the same time.
  • cobalt-containing mineral raw materials There are many kinds of cobalt-containing mineral raw materials, and there are many methods for extracting cobalt with different processes. They can be classified according to different mineral types, mainly oxidized minerals, arsenic minerals and sulfide minerals. They are usually processed by the process of pyrometallurgical enrichment-hydrometallurgical smelting. Currently, the research and application of the full hydrometallurgical process is developing.
  • Hydrometallurgy is an important technical means in the field of metallurgy. It is a scientific technology that transfers ore, concentrated ore or other raw materials through leaching agents into liquid phase to achieve metal separation, enrichment and extraction. Hydrometallurgy includes leaching, metal enrichment, solution purification and other processes. Leaching is an important process in hydrometallurgy. In the leaching process, different leaching agents have their unique applications. Cyanide leaching is the oldest method for extracting gold and silver. Metals such as copper sulfate that are directly soluble in water are directly leached with water.
  • Copper, nickel, cobalt, zinc and phosphorus oxides can be leached with sulfuric acid
  • chalcopyrite can be leached with hydrochloric acid
  • niobium and tantalum can be leached with hydrofluoric acid
  • scheelite and uranium ore can be leached with sodium carbonate
  • copper, nickel and cobalt sulfides can be leached with ammonia water
  • copper, cobalt, manganese and other metals can also be leached with bacterial leaching agents.
  • Crude cobalt hydroxide is a cobalt intermediate, which includes Co, Mn, Cu, Ni, Ca, Mg, Fe, Al and water. Cobalt in the crude cobalt hydroxide can be selectively leached.
  • the traditional selective leaching process has the following problems: the two-stage leaching is used to not only leach divalent cobalt, but also use a reducing agent to leach trivalent cobalt.
  • the addition of the reducing agent introduces more impurities, which in turn affects the purification quality of cobalt.
  • the reducing agent will reduce the iron ions to ferrous ions, which are difficult to precipitate at a lower pH. Therefore, after the reduction leaching, an oxidant needs to be added to oxidize the ferrous ions to ferric ions; the addition of the oxidant further introduces more impurities.
  • the reducing agent is at least one of sodium pyrosulfite, sodium sulfite, sulfur dioxide and sulfur; the oxidant is at least one of sodium chlorate and manganese dioxide.
  • the slurry is added with manganese dioxide ore for pre-oxidation treatment.
  • Manganese dioxide oxidizes Fe 2+ to Fe 3+ .
  • the reducing agent is sodium pyrosulfite, i.e., Na 2 S 2 O 5.
  • the addition of the reducing agent introduces sodium ions.
  • the oxidizing agent is manganese dioxide, i.e., MnO 2.
  • the addition of the oxidizing agent introduces manganese ions, which reduces the purity of the selective leaching solution, that is, affects the purification quality of cobalt.
  • a continuous selective leaching process for crude cobalt hydroxide comprises the following steps:
  • the precipitate and the selective leaching solution are subjected to a solid-liquid separation operation to obtain a first-stage leaching solution and acid leaching residue respectively.
  • the step of preparing the crude cobalt hydroxide slurry is specifically: preparing the crude cobalt hydroxide slurry by mixing crude cobalt hydroxide and water in a mass ratio of 1:(2.5-4).
  • the step of preparing the crude cobalt hydroxide slurry by mixing crude cobalt hydroxide and water in a mass ratio of 1:(2.5-4) is specifically as follows: preparing the crude cobalt hydroxide slurry by mixing crude cobalt hydroxide and water in a mass ratio of 1:(2.5-4) under stirring.
  • the acidic solution is at least one of sulfuric acid or hydrochloric acid.
  • the pH of the preliminary leachate is 2.0-2.5.
  • a portion of the crude cobalt hydroxide slurry and the acidic solution are mixed under heating conditions until the crude cobalt hydroxide slurry is dissolved in the acidic solution to obtain a primary leaching solution.
  • another portion of the crude cobalt hydroxide slurry is added to the preliminary leachate under heating conditions for mixing to obtain an adjusted leachate.
  • a portion of the crude cobalt hydroxide slurry and the acidic solution are mixed at 60° C. to 70° C. until the crude cobalt hydroxide slurry is dissolved in the acidic solution to obtain a primary leaching solution.
  • another portion of the crude cobalt hydroxide slurry is added to the preliminary leachate at 60° C. to 70° C. to mix and obtain an adjusted leachate.
  • the time for the steps of mixing a portion of the crude cobalt hydroxide slurry and the acidic solution until the crude cobalt hydroxide slurry is dissolved in the acidic solution to obtain a preliminary leachate is 0.8 h to 1.2 h.
  • the time for the steps of mixing a portion of the crude cobalt hydroxide slurry and the acidic solution until the crude cobalt hydroxide slurry is dissolved in the acidic solution to obtain a preliminary leachate is 1 hour.
  • the step of mixing a portion of the crude cobalt hydroxide slurry and the acidic solution until the crude cobalt hydroxide slurry is dissolved in the acidic solution to obtain a preliminary leachate is specifically:
  • a portion of the crude cobalt hydroxide slurry and the acidic solution are subjected to at least two mixing and stirring leaching operations to obtain the preliminary leaching solution.
  • the step of performing at least two mixing and stirring leaching operations on a portion of the crude cobalt hydroxide slurry and the acidic solution to obtain the preliminary leachate is specifically:
  • the secondary leaching solution is subjected to a third leaching operation to obtain a preliminary leaching solution.
  • the pH of the primary leachate is 1.0-1.5.
  • the pH of the secondary leachate is 1.5-2.0.
  • the pH of the preliminary leachate is 2.0-2.5.
  • the sum of the time for the step of adding another portion of the crude cobalt hydroxide slurry to the preliminary leachate to obtain an adjusted leachate and the step of performing a selective precipitation operation on the adjusted leachate to form a precipitate and a selective leachate is 0.8h to 1.2h.
  • the sum of the time for the step of adding another portion of the crude cobalt hydroxide slurry to the preliminary leachate to obtain an adjusted leachate and the step of performing a selective precipitation operation on the adjusted leachate to form a precipitate and a selective leachate is 1 hour.
  • the step of performing a selective precipitation operation on the adjusted leachate to form a precipitate and a selective leachate is specifically:
  • the adjusted leachate is subjected to at least one selective precipitation operation to form a precipitate and a selective leachate.
  • the step of performing a selective precipitation operation on the adjusted leachate to form a precipitate and a selective leachate is specifically:
  • the secondary selective leaching solution is subjected to a third selective precipitation operation to obtain a selective leaching solution and a third precipitate.
  • the pH of the primary selective leaching solution is 3.5-4.0.
  • the pH of the secondary selective leaching solution is 4.0-4.5.
  • the pH of the selective leaching solution is 5.0-5.5.
  • the pH of the primary selective leaching solution is 3.2-3.4.
  • the pH of the secondary selective leaching solution is 4.7.
  • the pH of the selective leaching solution is 5.0-6.7.
  • the step of mixing a portion of the crude cobalt hydroxide slurry and the acidic solution is specifically:
  • a portion of the crude cobalt hydroxide slurry and the acidic solution are added simultaneously and mixed.
  • the step of mixing a portion of the crude cobalt hydroxide slurry and the acidic solution is specifically as follows: the volume ratio of the portion of the crude cobalt hydroxide slurry to the acidic solution is 14-16.
  • the step of adding another portion of the crude cobalt hydroxide slurry to the preliminary leachate to obtain the adjusted leachate is specifically as follows: the volume ratio of the portion of the crude cobalt hydroxide slurry to the acidic solution is 15.
  • the first-stage leaching solution that has undergone the extraction treatment is processed to obtain a first-stage leaching cobalt product.
  • a continuous selective leaching device for crude cobalt hydroxide which adopts the continuous selective leaching process for crude cobalt hydroxide described in any of the above embodiments to perform leaching operation, wherein the crude cobalt hydroxide continuous selective leaching process
  • the selective leaching device includes:
  • a leaching mechanism at least comprising a slurry dissolving component, a slurry replenishing component and a selective precipitation component, the slurry dissolving component is provided with the first overflow port, the first overflow port is connected to the slurry replenishing component, the slurry replenishing component is provided with the second overflow port, the second overflow port is connected to the selective precipitation component, and the selective precipitation component is provided with the third overflow port;
  • a transfer mechanism the transfer mechanism is connected to the third overflow port, and the transfer mechanism is used to be connected to the primary leachate storage mechanism and the leachate residue pulping device respectively.
  • the selective precipitation component is connected to the slurry dissolving component.
  • the slurry dissolving component is connected to the transfer component.
  • the grouting component is connected to the transfer component.
  • the slurry dissolving component comprises at least a primary slurry dissolving kettle and a secondary slurry dissolving kettle which are connected to each other, and the first overflow port is formed in the secondary slurry dissolving kettle.
  • the slurry dissolving component further includes an intermediate slurry dissolving kettle, and the intermediate slurry dissolving kettle is respectively connected to the primary slurry dissolving kettle and the secondary slurry dissolving kettle.
  • the selective precipitation component comprises at least a first hydrolysis precipitation tank and a second hydrolysis precipitation tank that are connected to each other, and the third overflow port is formed in the second hydrolysis precipitation tank.
  • the crude cobalt hydroxide continuous selective leaching device further includes a filter press mechanism, which is connected to the transfer mechanism, and the filter press mechanism is used to be connected to the leaching residue slurry making device.
  • the leaching mechanism further includes a heating component, and an active end of the heating component acts on the slurry component.
  • the heating component is a steam heating component
  • the steam heating component is provided with a steam output end, and the steam output end is connected to the slurry dissolving component.
  • the slurry dissolving component is provided with a first pH measuring component.
  • the grouting component is provided with a second pH measuring component.
  • the selective precipitation component is provided with a third pH measurement component.
  • the leaching mechanism further includes at least a first stirring component, and a stirring end of the first stirring component is disposed in the slurry component.
  • the slurry dissolving component is formed with a slurry inlet groove and a slurry inlet port which are connected, and the slurry inlet groove is connected to the first overflow port.
  • the leaching mechanism further includes a first slurry supply component, and the first slurry supply component is connected to the dissolving slurry component.
  • the first slurry supply component includes a first pH meter, a first flow rate monitor, a first movable baffle and a first slurry supply trough body, the first slurry supply trough body is connected to the slurry dissolving component, the first movable baffle is arranged at the connection point between the first slurry supply trough body and the slurry dissolving component, the detection end of the first pH meter is arranged in the slurry dissolving component, and the active end of the first flow rate monitor is arranged at the first overflow port.
  • the first slurry supply component is used to set the flow rate of the crude cobalt hydroxide slurry to 1 m 3 /h to 3 m 3 /h.
  • the slurry replenishment component is provided with a slurry storage tank and a feeding port that are connected to each other, and the slurry storage tank is connected to the first overflow port and the selective precipitation component respectively.
  • the leaching mechanism further includes a second slurry supply component, and the second slurry supply component is connected to the slurry replenishment component.
  • the present invention also provides a two-stage leaching device for crude cobalt hydroxide, comprising a first-stage leachate storage mechanism, a leaching residue slurry making device and the crude cobalt hydroxide continuous selective leaching device described in any of the above embodiments, wherein the filter press mechanism is respectively connected to the first-stage leachate storage mechanism and the leaching residue slurry making device.
  • the leached residue pulping device includes a two-stage leaching mechanism and a two-stage leaching liquid storage mechanism that are connected.
  • a cobalt product production system comprises a first-stage leachate treatment device, a second-stage leachate treatment device and the crude cobalt hydroxide second-stage leaching device described in any one of the above embodiments, wherein the first-stage leachate treatment device is connected to the first-stage leachate storage mechanism, and the second-stage leachate treatment device is connected to the second-stage leachate storage device.
  • the acidic solution leach the divalent cobalt ions, trivalent iron ions, aluminum ions, copper ions and impurity ions in the crude cobalt hydroxide slurry to obtain a preliminary leachate, and then the added crude cobalt hydroxide slurry is gradually dissolved in the acidic solution to gradually increase the pH value until the pH value is within a range where the divalent cobalt ions do not precipitate and most of the impurity ions precipitate, so that the divalent cobalt ions exist in the form of ions and most of the impurities exist in the precipitate, thereby separating the divalent cobalt ions from most of the impurities in the solid-liquid state, and thus realizing the selective leaching of crude cobalt hydroxide.
  • the continuous selective leaching process for crude cobalt hydroxide in this article not only avoids the problem of introducing sodium ions by adding a reducing agent, introducing sodium ions or tetravalent manganese ions by adding an oxidant, and introducing sodium ions or potassium ions by adding an alkaline auxiliary material in the leachate due to the traditional crude cobalt hydroxide selective leaching process, but also simplifies the subsequent treatment process for sodium ions, tetravalent manganese ions and potassium ions, thereby improving production efficiency, and reduces the concentrations of sodium ions, tetravalent manganese ions and potassium ions, ensuring the quality of the cobalt products produced subsequently.
  • FIG1 is a flow chart of the method steps of a continuous selective leaching process for crude cobalt hydroxide according to an embodiment
  • FIG. 2 is a flow chart of the method steps of a cobalt product production process according to an embodiment of the present invention.
  • This article provides a continuous selective leaching process for crude cobalt hydroxide.
  • the continuous selective leaching process for crude cobalt hydroxide in this article the following is a further explanation of the continuous selective leaching process for crude cobalt hydroxide in this article:
  • the continuous selective leaching process of crude cobalt hydroxide includes part or all of the following steps:
  • the crude cobalt hydroxide slurry and the acidic solution are added at the same time, and the acidic solution can be sulfuric acid or hydrochloric acid, which alleviates the problem of long feeding time and reduced production efficiency caused by adding the crude cobalt hydroxide slurry first and then adding the acidic solution in the traditional crude cobalt hydroxide selective leaching process.
  • the cobalt hydroxide slurry and the acidic solution are not limited to being added at the same time, that is, the cobalt hydroxide slurry and the acidic solution are added separately.
  • the crude cobalt hydroxide slurry includes metal hydroxides and metal oxides, and the metal refers to Co, Mn, Cu, Ni, Ca, Mg, Fe and Al, which are added as alkaline substances, thereby avoiding the problem of introducing sodium ions or potassium ions by adding alkaline auxiliary materials in the traditional crude cobalt hydroxide selective leaching process, thereby avoiding the problem of increasing the number of extraction treatments and extending the extraction time to reduce production efficiency in the future, and avoiding the problem of adding wastewater treatment processes due to the need to treat the sodium in the P507 raffinate in the future, that is, reducing the production process, thereby improving production efficiency, and reducing labor intensity; and since no impurities are introduced into the first-stage leaching solution, the quality of subsequent cobalt products is improved, for example: the national standard for the sodium content of superior cobalt sulfate is less than or equal to 0.001%, and the sodium content of the first-class product is less than or equal to 0.002%.
  • the first-stage leachate is stored in the first-stage leachate storage mechanism, and the second-stage reduction leachate obtained by the subsequent second-stage reduction leaching of the acid leaching residue is stored in an independent mechanism, thereby avoiding the problem that the first-stage leachate with higher purity is affected by the second-stage reduction leachate with lower purity, thereby ensuring the purity of the first-stage leachate, and since the acid leaching residue is less, the acid leaching residue is subsequently processed in batches to improve production efficiency.
  • the acidic solution leach the divalent cobalt ions, trivalent iron ions, aluminum ions, copper ions and impurity ions in the crude cobalt hydroxide slurry to obtain a preliminary leachate, and then the added crude cobalt hydroxide slurry is gradually dissolved in the acidic solution to gradually increase the pH value until the pH value is within a range where the divalent cobalt ions do not precipitate and most of the impurity ions precipitate, so that the divalent cobalt ions exist in the form of ions and most of the impurities exist in the precipitate, thereby separating the divalent cobalt ions from most of the impurities in the solid-liquid state, and thus achieving the selective leaching of crude cobalt hydroxide.
  • the first-stage leaching solution not only avoids the problem of introducing sodium ions by adding a reducing agent into the leaching solution, introducing sodium ions or tetravalent manganese ions by adding an oxidant, and introducing sodium ions or potassium ions by adding an alkaline auxiliary material in the traditional crude cobalt hydroxide selective leaching process, but also simplifies the subsequent treatment process for sodium ions, tetravalent manganese ions and potassium ions, thereby improving production efficiency, and reduces the concentrations of sodium ions, tetravalent manganese ions and potassium ions, ensuring the quality of the cobalt products produced subsequently.
  • the crude cobalt hydroxide slurry and the acidic solution are added to the slurry dissolving component at the same time, thereby avoiding the problem of low production efficiency caused by first adding the slurry and heating it before adding sulfuric acid in the traditional crude cobalt hydroxide selective leaching process, thereby improving production efficiency.
  • the traditional selective leaching process for crude cobalt hydroxide transfers the divalent cobalt leaching solution and the trivalent cobalt reduction leaching solution to the transfer tank for iron removal.
  • the divalent cobalt leaching solution has a higher purity.
  • the trivalent cobalt reduction leaching solution introduces sodium ions and manganese ions respectively because the reducing agent is first added to the trivalent cobalt reduction leaching solution for reduction reaction and then the oxidant is added for oxidation reaction.
  • the sodium ions are difficult to hydrolyze and precipitate.
  • the precipitation pH of manganese ions is higher than the precipitation pH of divalent cobalt. It is also difficult to precipitate manganese ions under the condition that divalent cobalt is not precipitated.
  • the trivalent cobalt reduction leaching solution reduces the purity of the divalent cobalt leaching solution, thereby reducing the subsequent purification quality of the divalent cobalt leaching solution.
  • the crude cobalt hydroxide selective leaching process in this article treats the divalent cobalt leaching solution and the acid leaching residue separately, and the divalent cobalt leaching solution does not add reducing agents, oxidants and alkaline auxiliary materials, thereby ensuring the subsequent The quality of the cobalt product obtained.
  • the selective leaching process of crude cobalt hydroxide in this article treats the divalent cobalt leaching solution and the acid leaching residue separately, and collects and batch processes the acid leaching residue.
  • the step of preparing crude cobalt hydroxide slurry is specifically: crude cobalt hydroxide and water are prepared in a mass ratio of 1:(2.5-4) to prepare crude cobalt hydroxide slurry.
  • the step of preparing crude cobalt hydroxide slurry by mixing crude cobalt hydroxide and water in a mass ratio of 1:(2.5-4) is specifically as follows: preparing crude cobalt hydroxide slurry by mixing crude cobalt hydroxide and water in a mass ratio of 1:(2.5-4) and stirring.
  • the acidic solution is at least one of sulfuric acid or hydrochloric acid.
  • the pH of the preliminary leaching solution is 2.0 to 2.5. It can be understood that when the preliminary leaching solution is obtained, the crude cobalt hydroxide slurry is fully dissolved in the acidic solution, that is, a solution in which a large amount of divalent cobalt ions are leached is obtained.
  • a portion of the crude cobalt hydroxide slurry and the acidic solution are mixed under heating conditions until the crude cobalt hydroxide slurry is dissolved in the acidic solution to obtain a primary leaching solution.
  • another portion of the crude cobalt hydroxide slurry is added to the preliminary leachate under heating conditions for mixing to obtain an adjusted leachate.
  • a portion of the crude cobalt hydroxide slurry and the acidic solution are mixed at 60°C to 70°C until the crude cobalt hydroxide slurry is dissolved in the acidic solution to obtain a preliminary leaching solution.
  • the increase in temperature can activate the reaction, accelerate the movement between particles, and promote the reaction of sulfuric acid and the material powder liquid in contact with each other.
  • the increase in temperature increases the internal energy of the reactants, increases the collision chance between the two, and increases the leaching rate and leaching reaction rate of cobalt, shortening the time required for the leaching to reach the equilibrium point.
  • another portion of the crude cobalt hydroxide slurry is added to the preliminary leaching solution at 60°C to 70°C for mixing to obtain an adjusted leaching solution.
  • the increase in temperature can activate the reaction, accelerate the movement between particles, and promote the reaction of sulfuric acid and the material powder liquid in contact with each other.
  • the increase in temperature increases the internal energy of the reactants, increases the collision chance between the two, and increases the leaching rate and leaching reaction rate of cobalt, shortening the time required for the leaching to reach the equilibrium point.
  • a portion of the crude cobalt hydroxide slurry and the acidic solution are mixed until the crude cobalt hydroxide slurry is dissolved in the acidic solution, and the total time of the steps of obtaining the preliminary leachate is 0.8h to 1.2h.
  • a portion of the crude cobalt hydroxide slurry and the acidic solution are mixed until the crude cobalt hydroxide slurry is dissolved in the acidic solution, and the total time of the steps of obtaining the preliminary leachate is 1h.
  • a portion of the crude cobalt hydroxide slurry and the acidic solution are mixed until the crude cobalt hydroxide slurry is dissolved in the acidic solution to obtain a preliminary leachate.
  • the specific step is: a portion of the crude cobalt hydroxide slurry and the acidic solution are mixed and stirred for leaching at least twice to obtain a preliminary leachate. It can be understood that the crude cobalt hydroxide slurry is fully dissolved in the acidic solution, thereby obtaining a relatively fully leached divalent cobalt ion.
  • the steps of performing at least two mixing and stirring leaching operations on a portion of the crude cobalt hydroxide slurry and the acidic solution to obtain a preliminary leachate are specifically as follows:
  • the secondary leaching solution is subjected to a third leaching operation to obtain a preliminary leaching solution.
  • the pH of the primary leachate is 1.0 to 1.5. In this embodiment, the pH of the primary leachate is 1.2.
  • the pH of the secondary leaching solution is 1.5 to 2.0. In this embodiment, the pH of the secondary leaching solution is 1.8.
  • the pH of the preliminary leaching solution is 2.0 to 2.5. In this embodiment, the pH of the preliminary leaching solution is 2.3.
  • the sum of the time of adding another portion of the crude cobalt hydroxide slurry to the preliminary leachate to obtain the adjusted leachate and the time of performing a selective precipitation operation on the adjusted leachate to form a precipitate and a selective leachate is 0.8h to 1.2h.
  • the sum of the time of adding another portion of the crude cobalt hydroxide slurry to the preliminary leachate to obtain the adjusted leachate and the time of performing a selective precipitation operation on the adjusted leachate to form a precipitate and a selective leachate is 1h.
  • the steps of performing a selective precipitation operation on the adjusted leachate to form a precipitate and a selective leachate are specifically:
  • the adjusted leachate is subjected to at least one selective precipitation operation to form a precipitate and a selective leachate.
  • the steps of performing a selective precipitation operation on the adjusted leachate to form a precipitate and a selective leachate are specifically:
  • the adjusted leachate contains divalent cobalt ions, iron ions, aluminum ions, copper ions and impurity ions.
  • the easily precipitated iron ions are first hydrolyzed and precipitated, that is, the precipitate in this step is iron hydroxide, and the primary selective leachate is the adjusted leachate from which most of the iron ions have been removed.
  • the precipitate added in this step is aluminum hydroxide and a trace amount of iron hydroxide
  • the secondary selective leaching solution is an adjusted leaching solution with iron ions and aluminum ions removed.
  • the secondary selective leaching solution is subjected to a third selective precipitation operation to obtain a selective leaching solution and a precipitate.
  • the secondary selective leaching solution is a regulated leaching solution from which iron ions, aluminum ions and part of copper ions have been removed.
  • the pH of the primary selective leaching solution is 3.5 to 4.0. It can be understood that the reaction between the crude cobalt hydroxide slurry and the acidic solution reduces the pH of the mixed solution. When the pH is greater than 3.5, the iron ions are easily completely hydrolyzed and precipitated.
  • the pH of the secondary selective leaching solution is 4.0 to 4.5. It can be understood that the reaction between the crude cobalt hydroxide slurry and the acidic solution reduces the pH of the mixed solution, and when the pH is 4.0 to 4.5, most of the aluminum ions are hydrolyzed and precipitated.
  • the pH of the selective leaching solution is 5.0 to 5.5. It can be understood that the reaction of the crude cobalt hydroxide slurry with the acidic solution reduces the pH of the mixed solution. When the pH is 5.0 to 5.5, a small amount of aluminum ions and part of the copper ions are hydrolyzed and precipitated, thereby reducing the impurity ions in the selective leaching solution and achieving copper enrichment.
  • the pH of the primary selective leaching solution is 3.2-3.4. It can be understood that when the pH of the primary selective leaching solution is 3.2-3.4, the iron ions are fully hydrolyzed and precipitated, and the aluminum ions have not begun to hydrolyze and precipitate, that is, the first precipitate obtained is mainly ferric hydroxide precipitate, which has a higher grade and a higher recovery value. For example, it can be used to make pigments, medicines, and arsenic antidotes, and can also be treated with a reducing agent at high temperature to become ferroferric oxide.
  • the pH of the secondary selective leachate is 4.7. It can be understood that when the pH of the secondary selective leachate is 4.7, the iron ions have been fully precipitated in the previous step, the aluminum ions are fully hydrolyzed and precipitated in this step, and the copper ions have not begun to hydrolyze and precipitate, that is, the second precipitate obtained in this step is mainly aluminum hydroxide precipitate, which has a higher grade and a higher recovery value. For example, it can be used to prepare antacids, treat stomach pain, hyperacidity, heartburn, and gastric acid, and it can also be used to reduce the phosphate level of people with kidney problems.
  • the pH of the selective leaching solution is 5.0-6.7. It can be understood that when the pH of the selective leaching solution is 5.0-6.7, the iron ions and aluminum ions have been fully precipitated in the previous step, and the divalent cobalt ions have not begun to hydrolyze and precipitate, that is, the third precipitate obtained in this step is mainly copper hydroxide precipitate, which has a high grade and a high recovery value.
  • the third precipitate obtained in this step is mainly copper hydroxide precipitate, which has a high grade and a high recovery value.
  • it can be used to prepare mordants, catalysts, fungicides and pigments, and used for dyeing paper, etc., as an analytical reagent; a raw material for making copper salts, a mordant, and as a component of a fungicide and antifouling paint for the bottom of a ship.
  • the pH of the selective leaching solution is 6.7. It can be understood that when the pH of the selective leaching solution is 5.0-6.7, the copper ions are fully hydrolyzed and precipitated, and the divalent cobalt ions do not begin to hydrolyze and precipitate, that is, the sedimentation rate of the copper ions can be increased while reducing the loss of divalent cobalt ions, and the enrichment and recovery of copper can be more fully achieved.
  • the conventional selective leaching process for crude cobalt hydroxide simultaneously leaches iron hydroxide, aluminum hydroxide and copper hydroxide, that is, a precipitate containing iron hydroxide, aluminum hydroxide and copper hydroxide is obtained.
  • iron, aluminum and copper need to be separated to be recovered, which reduces production efficiency and increases production costs.
  • the pH of the primary selective leaching solution is 3.2-3.4
  • the pH of the secondary selective leaching solution is 4.7
  • the pH of the selective leaching solution is 5.0-6.7.
  • the content of iron hydroxide in the first precipitate is higher, the content of aluminum hydroxide in the second precipitate is higher, and the content of copper hydroxide in the third precipitate is higher, so that iron hydroxide, aluminum hydroxide and copper hydroxide can be recovered separately, and the production convenience and production efficiency of the subsequent recovery process are improved, and the production cost is reduced.
  • the step of mixing a portion of the crude cobalt hydroxide slurry and the acidic solution is specifically: adding a portion of the crude cobalt hydroxide slurry and the acidic solution at the same time and mixing them. It can be understood that adding a portion of the crude cobalt hydroxide slurry and the acidic solution at the same time and mixing them alleviates the problem of long production time caused by the traditional method of first adding the crude cobalt hydroxide slurry and then adding the acidic solution, thereby improving production efficiency.
  • This article also provides a cobalt product production process.
  • the above cobalt product production process includes performing at least the following steps on a first-stage leaching solution obtained by any of the above embodiments:
  • the primary leachate prepared by the above-mentioned continuous selective leaching process of crude cobalt hydroxide is adopted, that is, the primary leachate is not added with a reducing agent, an oxidizing agent and an alkaline auxiliary material, thereby avoiding the problem of sodium ions, sulfides, tetravalent manganese ions and potassium ions introduced into the traditional primary leachate due to the addition of reducing agents, oxidizing agents and alkaline auxiliary materials.
  • the first stage leachate has hydrolyzed and precipitated iron ions, aluminum ions and part of copper ions
  • the first stage leachate still includes impurity ions, specifically tetravalent manganese ions, nickel ions, calcium ions, magnesium ions and part of copper ions, which need to be removed by extraction treatment.
  • concentration of the impurity ions after treatment is inversely proportional to the quality of the cobalt product obtained subsequently.
  • the conventional selective leaching process of crude cobalt hydroxide introduces sodium ions or sulfides by adding a reducing agent, introduces sodium ions or tetravalent manganese ions by adding an oxidant, and introduces sodium ions or potassium ions by adding an alkaline auxiliary material. Therefore, extraction treatment and other treatments are required to remove impurity ions, and there are the following problems:
  • the concentration of tetravalent manganese ions is higher, which requires more extractants to remove the tetravalent manganese ions, increases the number of extractions, and prolongs the extraction time, thereby reducing the production efficiency.
  • the above-mentioned cobalt product production process adopts the first-stage leachate prepared by the above-mentioned crude cobalt hydroxide continuous selective leaching process, which avoids the problem of sodium ions, sulfides, tetravalent manganese ions and potassium ions introduced into the traditional first-stage leachate, reduces the number of extraction treatments and shortens the extraction time, thereby improving production efficiency; and because the first-stage leachate does not introduce impurities, the quality of subsequent cobalt products is improved.
  • the national standard for the sodium content of superior cobalt sulfate is less than or equal to 0.001%, and the sodium content of first-class products is less than or equal to 0.002%. Because the first-stage leachate does not introduce sodium ions, the subsequent cobalt products are easy to reach the level of superior cobalt sulfate, that is, the quality of the cobalt products is ensured.
  • the present invention also provides a continuous selective leaching device for crude cobalt hydroxide, which uses the continuous selective leaching process for crude cobalt hydroxide of any of the above embodiments to perform leaching operations, and the crude cobalt hydroxide
  • the continuous selective leaching device includes:
  • the leaching mechanism includes at least a dissolving slurry component, a slurry replenishing component and a selective precipitation component.
  • the dissolving slurry component is provided with a first overflow port, the first overflow port is connected to the slurry replenishing component, the slurry replenishing component is provided with a second overflow port, the second overflow port is connected to the selective precipitation component, and the selective precipitation component is provided with a third overflow port;
  • the transfer mechanism is connected to the third overflow port, and is used to be connected to the primary leachate storage mechanism and the leachate residue pulping device respectively.
  • the slurry component is used to hold the crude cobalt hydroxide slurry and the acidic solution.
  • the acidic solution leach the divalent cobalt ions, trivalent iron ions, aluminum ions and copper ions in the crude cobalt hydroxide slurry in the slurry component to obtain a leachate, and then the leachate overflows to the slurry replenishment component through the first overflow port.
  • the slurry replenishment component is used to hold the leachate and the added crude cobalt hydroxide slurry.
  • the added crude cobalt hydroxide slurry is gradually dissolved in the acidic solution to gradually increase the pH value of the liquid in the slurry replenishment component and the selective precipitation component until the pH value is within the range where the divalent cobalt ions do not precipitate and most of the impurity ions are precipitated, so that the divalent cobalt ions exist in the form of ions and most of the impurities exist in the precipitate, thereby separating the divalent cobalt ions from most of the impurities in solid and liquid, and realizing the selective leaching of crude cobalt hydroxide.
  • the first-stage leachate and precipitate obtained by selective leaching of the selective precipitation component overflow to the transfer mechanism through the third overflow port, and then the first-stage leachate flows to the first-stage leachate storage mechanism, and the precipitate is transported to the leaching residue slurry making device;
  • the first-stage leachate not only avoids the problem of introducing impurities caused by adding reducing agents and oxidizing agents to the leachate in the traditional crude cobalt hydroxide selective leaching process, but also avoids the problem of introducing impurities caused by adding alkaline auxiliary materials by using crude cobalt hydroxide slurry as a regulator for increasing pH, thereby ensuring the purity of the first-stage leachate, that is, improving the purification quality of cobalt.
  • the above-mentioned crude cobalt hydroxide continuous selective leaching device adds the crude cobalt hydroxide slurry and the acidic solution into the slurry dissolving component at the same time, thereby avoiding the problem of low production efficiency caused by first adding the slurry and heating it before adding sulfuric acid in the traditional crude cobalt hydroxide selective leaching process, thereby improving production efficiency.
  • the crude cobalt hydroxide slurry and the acidic solution overflow from the dissolving slurry component to the slurry replenishing component through the first overflow port, then overflow from the slurry replenishing component to the selective precipitation component through the second overflow port, and then overflow from the selective precipitation component to the transfer mechanism through the third overflow port, thereby reducing the use of machine pumps, ensuring the automation of the crude cobalt hydroxide continuous selective leaching device, simplifying the operating process, and avoiding the problem that the traditional crude cobalt hydroxide selective leaching process also needs to transfer the leaching solution to the transfer tank, thereby reducing the labor intensity.
  • the divalent cobalt leaching solution and the trivalent cobalt reduction leaching solution are successively transferred to the transfer tank for iron removal.
  • the divalent cobalt leaching solution has a higher purity. Since the trivalent cobalt reduction leaching solution first adds a reducing agent for reduction reaction and then adds an oxidant for oxidation reaction, sodium ions and manganese ions are introduced respectively, and the sodium ions are difficult to hydrolyze and precipitate.
  • the precipitation pH of manganese ions is higher than the precipitation pH of divalent cobalt, and it is also difficult to precipitate manganese ions under the condition of ensuring that divalent cobalt is not precipitated, that is, the impurity ions introduced by the reducing agent and the oxidant are difficult to remove. Therefore, the trivalent cobalt reduction leaching solution reduces the purity of the divalent cobalt leaching solution, thereby reducing the subsequent purification quality of the divalent cobalt leaching solution.
  • the content of divalent cobalt is relatively high, while the content of trivalent cobalt is relatively low and requires the addition of a reducing agent for leaching.
  • the divalent cobalt is leached, it is transferred to a transfer tank for iron removal. It is necessary to wait for the trivalent cobalt to be reduced and leached before being transferred to a transfer tank for iron removal, which reduces production efficiency.
  • the selective precipitation module is connected to the slurry dissolving module.
  • the dissolving component is provided with a first overflow port
  • the first overflow port is connected to the slurry replenishing component
  • the slurry replenishing component is provided with a second overflow port
  • the second overflow port is connected to the selective precipitation component
  • the selective precipitation component is connected to the dissolving component, that is, the dissolving component, the slurry replenishing component and the selective precipitation component form a loop connection
  • the selective precipitation component is not limited to being used only for selective precipitation, but can also be used for dissolving slurry or replenishing slurry.
  • the dissolving slurry component is not limited to being used only for dissolving slurry, but can also be used for selective precipitation or replenishing slurry.
  • the replenishing slurry component is not limited to being used only for replenishing slurry, but can also be used for selective precipitation or dissolving slurry; therefore, when the slurry in the selective precipitation component is not fully dissolved, the selective precipitation component with more slurry accumulation in this round can be used as the dissolving slurry component of the next round, and other components are also adjusted in coordination so that the slurry that is not fully dissolved accumulated in this round can be dissolved again in the next round, thereby improving the full utilization of the crude cobalt hydroxide slurry, and reducing the problem of high labor intensity caused by manual cleaning and transfer of the slurry, and saving time for cleaning and transferring the slurry, thereby improving production efficiency.
  • the transfer mechanism is used to be connected to a leachate storage mechanism and a leach residue slurry making device respectively. It can be understood that the transfer mechanism performs solid-liquid separation on the divalent cobalt leachate and the precipitate.
  • the divalent cobalt leachate is a first-stage leachate, and the first-stage leachate flows to a first-stage leachate storage mechanism.
  • the first-stage leachate storage mechanism is only used to store a first-stage leachate, and is not used to store the trivalent cobalt leachate of the subsequent precipitation reduction leaching, thereby ensuring the purity of the first-stage leachate; and because the amount of precipitate is small, the precipitate will be concentrated in batches for leaching later, and the batch processing of precipitate saves energy, reduces the use of the leaching residue pulping device, thereby reducing the damage and maintenance of the leaching residue pulping device, thereby increasing the service life of the leaching residue pulping device, and greatly improving the production efficiency; and because the traditional crude cobalt hydroxide selective leaching process is avoided to transfer the divalent cobalt to the transfer tank for iron removal after leaching, and the problem of waiting for the trivalent cobalt reduction leachate to be iron removed together is avoided, thereby reducing the phenomenon of equipment being occupied but not used, that is, ensuring the utilization rate of the equipment, thereby reducing the equipment footprint.
  • the transfer mechanism is used to be connected to a leachate storage mechanism and a leach residue slurry making device respectively. It can be understood that the transfer mechanism performs solid-liquid separation on the divalent cobalt leachate and the precipitate.
  • the divalent cobalt leachate is a first-stage leachate, and the first-stage leachate flows to a first-stage leachate storage mechanism.
  • the first-stage leachate storage mechanism is only used to store a first-stage leachate, and is not used to store the trivalent cobalt leachate of the subsequent precipitation reduction leaching, thereby ensuring the purity of the first-stage leachate; and because the amount of precipitate is small, the precipitate will be concentrated in batches for leaching later, and the batch processing of precipitate saves energy, reduces the use of the leaching residue pulping device, thereby reducing the damage and maintenance of the leaching residue pulping device, thereby increasing the service life of the leaching residue pulping device, and greatly improving the production efficiency; and because the traditional crude cobalt hydroxide selective leaching process is avoided to transfer the divalent cobalt to the transfer tank for iron removal after leaching, and the problem of waiting for the trivalent cobalt reduction leachate to be iron removed together is avoided, thereby reducing the phenomenon of equipment being occupied but not used, that is, ensuring the utilization rate of the equipment, thereby reducing the equipment footprint.
  • the slurry dissolving component includes at least a primary slurry dissolving kettle and a secondary slurry dissolving kettle connected to each other, and the first overflow port is formed in the secondary slurry dissolving kettle.
  • the crude cobalt hydroxide slurry is more fully dissolved in the acidic solution, that is, the divalent cobalt in the crude cobalt hydroxide is more fully leached, thereby ensuring the leaching rate of divalent cobalt in the crude cobalt hydroxide.
  • the slurry dissolving component further comprises an intermediate slurry dissolving kettle, which is connected to the primary slurry dissolving kettle and the secondary slurry dissolving kettle respectively. It takes time for the liquid to fill up the primary dissolving kettle from the time it is just added to the primary dissolving kettle. Similarly, it takes time for the liquid to overflow from the primary dissolving kettle to the intermediate dissolving kettle. Similarly, it takes time for the liquid to overflow from the intermediate dissolving kettle to the secondary dissolving kettle.
  • the crude cobalt hydroxide slurry is more fully dissolved in the acidic solution, so that the divalent cobalt in the crude cobalt hydroxide is more fully leached, thereby ensuring the leaching rate of divalent cobalt in the crude cobalt hydroxide.
  • the selective precipitation component at least includes a first hydrolysis precipitation tank and a second hydrolysis precipitation tank that are connected, and the third overflow port is formed in the second hydrolysis precipitation tank. It can be understood that the added crude cobalt hydroxide slurry takes a certain amount of time to dissolve.
  • the added crude cobalt hydroxide slurry is more fully dissolved, and the acidic solution is gradually consumed, so that the pH gradually increases, and then the trivalent iron ions, aluminum ions and copper ions are gradually hydrolyzed and precipitated, thereby achieving continuous selective leaching of crude cobalt hydroxide and ensuring the leaching effect, that is, ensuring the purification effect of divalent cobalt.
  • the selective precipitation component is connected to the slurry dissolving component.
  • the slurry dissolving component is provided with a first overflow port, the first overflow port is connected to the slurry replenishing component, the slurry replenishing component is provided with a second overflow port, the second overflow port is connected to the selective precipitation component, and the selective precipitation component is connected to the slurry dissolving component, that is, the slurry dissolving component, the slurry replenishing component and the selective precipitation component form a loop connection; and the selective precipitation component is not limited to being used only for selective precipitation, but can also be used for slurry dissolving or slurry replenishing, similarly, the slurry dissolving component is not limited to being used only for slurry dissolving, but can also be used for selective precipitation or slurry replenishing, similarly, the slurry replenishing component is not limited to being used only for slurry replenishing, but can also be used for selective Selective precipitation or dissolution
  • the selective precipitation component is connected to the slurry dissolving component, and the slurry replenishing component is connected to the transfer component.
  • the slurry dissolving component is provided with a first overflow port, the first overflow port is connected to the slurry replenishing component, the slurry replenishing component is provided with a second overflow port, the second overflow port is connected to the selective precipitation component, and the selective precipitation component is connected to the slurry dissolving component, that is, the slurry dissolving component, the slurry replenishing component and the selective precipitation component form a circular connection;
  • the selective precipitation component is not limited to being used only for selective precipitation, but can also be used for slurry dissolving or slurry replenishing, similarly, the slurry dissolving component is not limited to being used only for slurry dissolving, but can also be used for selective precipitation or slurry replenishing, similarly, the slurry replenishing component is not limited to being used only for slurry replenishing
  • the selective precipitation component with more slurry accumulation in this round can be used as the dissolving component in the next round
  • the dissolving component in this round can be used as the slurry replenishing component in the next round of production
  • the slurry replenishing component in this round can be used as the selective precipitation component in the next round of production. Then, the selective leaching liquid obtained by processing the slurry replenishing component in this round in the next round of production flows to the transfer component.
  • the selective precipitation component is connected to the slurry dissolving component, and the slurry dissolving component is connected to the transfer component.
  • the slurry dissolving component is provided with a first overflow port, the first overflow port is connected to the slurry replenishing component, the slurry replenishing component is provided with a second overflow port, the second overflow port is connected to the selective precipitation component, and the selective precipitation component is connected to the slurry dissolving component, that is, the slurry dissolving component, the slurry replenishing component and the selective precipitation component form a circular connection;
  • the selective precipitation component is not limited to being used only for selective precipitation, but can also be used for slurry dissolving or slurry replenishing, similarly, the slurry dissolving component is not limited to being used only for slurry dissolving, but can also be used for selective precipitation or slurry replenishing, similarly, the slurry replenishing component is not limited to being used only for slurry replenish
  • the slurry replenishment component with more slurry accumulation in this round can be used as the slurry dissolving component in the next round
  • the slurry dissolving component in this round can be used as the selective precipitation component in the next round
  • the selective precipitation component in this round can be used as the slurry replenishment component in the next round. Then, the selective leaching liquid obtained by processing the slurry replenishment component in this round in the next round of production flows to the transfer component.
  • the third overflow port is connected to the primary slurry kettle, and the primary slurry kettle, the intermediate slurry kettle, the secondary slurry kettle, the slurry replenishing assembly, the first hydrolysis precipitation kettle and the second hydrolysis precipitation kettle are respectively connected to the transfer assembly.
  • the primary slurry kettle, the primary slurry kettle, the secondary slurry kettle, the slurry replenishing assembly, the first hydrolysis precipitation kettle and the second hydrolysis precipitation kettle form a loop connection; and the selective precipitation assembly is not limited to being used only for selective precipitation, but can also be used for slurry dissolution or slurry replenishment.
  • the slurry dissolution assembly is not limited to being used only for slurry dissolution, but can also be used for selective precipitation or slurry replenishment.
  • the slurry replenishing assembly is not limited to being used only for slurry replenishment, but can also be used for selective precipitation or slurry dissolution. Therefore, when the leaching mechanism fails or other reasons occur, for example, there is a large amount of undissolved crude cobalt hydroxide slurry accumulated in the second hydrolysis precipitation kettle, there is no need to transfer the slurry, nor to move the position of the leaching mechanism, so that the second hydrolysis precipitation kettle of this round is used as the primary slurry kettle of the next round.
  • the primary dissolving kettle of this round serves as the intermediate dissolving kettle of the next round
  • the intermediate dissolving kettle of this round serves as the secondary dissolving kettle of the next round
  • the secondary dissolving kettle of this round serves as the slurry replenishing component of the next round
  • the slurry replenishing component of this round serves as the first hydrolysis precipitation kettle of the next round
  • the first hydrolysis precipitation kettle of this round serves as the second hydrolysis precipitation kettle of the next round
  • the selective leaching liquid obtained by the first hydrolysis precipitation kettle of this round in the next round of production flows to the transfer component, so that the incompletely dissolved slurry accumulated in this round can be dissolved again in the next round, thereby improving the full utilization of the crude cobalt hydroxide slurry, reducing the need for manual cleaning and transfer of the slurry, which causes a high labor intensity, and saving the time for cleaning and transfer of the slurry, thereby improving production efficiency.
  • the traditional leaching process is carried out in a reactor.
  • the leaching mechanism includes a primary slurry kettle, an intermediate slurry kettle, a secondary slurry kettle, a slurry replenishing component, a first hydrolysis precipitation kettle, and a second hydrolysis precipitation kettle that are connected in sequence.
  • the crude cobalt hydroxide used in this article is a cobalt intermediate, which includes 34.7% Co, 1.75% Mn, 1.83% Cu, 0.08% Ni, 0.88% Ca, 5.3% Mg, 1.22% Fe, 0.23% Al and 15% moisture.
  • the amount of precipitate obtained in each step of the process is predictable, and the amount, color and morphology of the precipitate can be used to observe whether there are any problems in the production of each step, and when problems are found in the process, corresponding adjustments and improvements are made quickly to ensure normal production, thereby ensuring production efficiency, and improving the quality of the leachate and the quality of subsequent cobalt products; and after it is observed that a problem occurs in a certain link in the process, the intermediate product before this step can be saved and wait for adjustment and improvement to continue to be put into production; and for the link with problems and the subsequent links, targeted adjustments are made, and the intermediate products that cannot be adjusted are discarded to avoid the subsequent cobalt products being unqualified due to unqualified intermediate products. causing greater losses.
  • the crude cobalt hydroxide continuous selective leaching device further includes a filter press mechanism, which is connected to the transfer mechanism and used to be connected to the leaching residue slurry making device.
  • the leaching mechanism further includes a heating component, and an active end of the heating component acts on the slurry component.
  • the heating component is a steam heating component
  • the steam heating component is provided with a steam output end, and the steam output end is connected to the slurry dissolving component.
  • the slurry component is provided with a first pH measurement component.
  • the grouting component is provided with a second pH measuring component.
  • the selective precipitation component is provided with a third pH measurement component.
  • the leaching mechanism further includes at least a first stirring component, and a stirring end of the first stirring component is disposed in the slurry component.
  • the slurry dissolving component is formed with a slurry inlet groove and a slurry inlet port which are connected to each other, and the slurry inlet groove is connected to the first overflow port.
  • the leaching mechanism further includes a first slurry supply component, and the first slurry supply component is connected to the dissolving slurry component.
  • the first slurry supply component includes a first pH meter, a first flow rate monitor, a first movable baffle and a first slurry supply tank body, the first slurry supply tank body is connected to the slurry dissolving component, the first movable baffle is arranged at the connection between the first slurry supply tank body and the slurry dissolving component, the detection end of the first pH meter is arranged in the slurry dissolving component, and the action end of the first flow rate monitor is arranged at the first overflow port.
  • the first pH meter is used to add an acidic solution to the slurry dissolving component and monitor the pH of the mixed body in the slurry dissolving component, and adjust the addition rate of the acidic solution according to the pH
  • the first flow rate monitor is used to monitor the flow rate of the mixed body, and change the opening of the first movable baffle according to the flow rate, thereby changing the flow rate of the crude cobalt hydroxide slurry, ensuring the leaching effect of the crude cobalt hydroxide slurry in the acidic solution, that is, ensuring the leaching rate of divalent cobalt ions.
  • the first slurry supply assembly is used to set the flow rate of the crude cobalt hydroxide slurry to 1 m 3 /h to 3 m 3 /h.
  • the slurry replenishment component is provided with a slurry storage tank and a feeding port which are connected to each other, and the slurry storage tank is connected to the first overflow port and the selective precipitation component respectively.
  • the leaching mechanism further includes a second slurry supply component, and the second slurry supply component is connected to the slurry replenishment component.
  • the second slurry supply component includes a second pH meter, a second flow rate monitor, a second movable partition and a second slurry supply tank body, the second slurry supply tank body is connected to the slurry dissolving component, the second movable partition is arranged at the connection point between the second slurry supply tank body and the slurry dissolving component, the detection end of the second pH meter is arranged in the slurry dissolving component, and the active end of the second flow rate monitor is arranged at the second overflow port.
  • the present invention also provides a two-stage leaching device for crude cobalt hydroxide, comprising a first-stage leaching solution storage mechanism, a leaching residue slurry making device and a crude cobalt hydroxide continuous selective leaching device of any of the above-mentioned embodiments, wherein the filter press mechanism is respectively connected to the first-stage leaching solution storage mechanism and the leaching residue slurry making device.
  • the above-mentioned crude cobalt hydroxide two-stage leaching equipment collects and leaches the precipitates in batches, saves energy for batch processing of precipitates, reduces the use of leaching slag pulping devices, and thus reduces the damage and maintenance of the leaching slag pulping devices, thereby increasing the service life of the leaching slag pulping devices and greatly improving the production efficiency; and because it avoids the problem of transferring the divalent cobalt to the transfer tank for iron removal after leaching in the traditional crude cobalt hydroxide selective leaching process, and waiting for the trivalent cobalt reduction leaching solution to remove iron together, it reduces the phenomenon of equipment being occupied but not used, that is, ensures the utilization rate of the equipment, and thereby reduces the equipment footprint.
  • the leached residue pulping device includes a two-stage leaching mechanism and a two-stage leaching liquid storage mechanism connected to each other, and the two-stage leaching mechanism is connected to the filter press mechanism.
  • the second-stage reduction leaching liquid is stored in the second-stage leaching liquid storage mechanism, that is, it is stored in a different storage mechanism from the first-stage leaching liquid.
  • the present invention also provides a cobalt product production system, comprising a first-stage leachate treatment device, a second-stage leachate treatment device and a crude cobalt hydroxide second-stage leaching device of any of the above embodiments, wherein the first-stage leachate treatment device is connected to a first-stage leachate storage mechanism, and the second-stage leachate treatment device is connected to the second-stage leachate storage device.
  • the first-stage leachate treatment equipment is used to treat the first-stage leachate
  • the second-stage leachate treatment equipment is used to treat the second-stage reduction leachate, that is, the first-stage leachate and the second-stage reduction leachate are treated separately, which ensures the quality of the cobalt product obtained from the first-stage leachate, simplifies the process of treating the first-stage leachate, and improves production convenience and production efficiency.
  • Crude cobalt hydroxide is a cobalt intermediate product, which includes 34.7% Co, 1.75% Mn, 1.83% Cu, 0.08% Ni, 0.88% Ca, 5.3% Mg, 1.22% Fe, 0.23% Al and 15% moisture.
  • the remaining 0.15 tons of crude cobalt hydroxide slurry is gradually added to the preliminary leaching solution to obtain an adjusted leaching solution; then the adjusted leaching solution is subjected to a selective precipitation operation for 1 hour to obtain a first precipitate and a primary selective leaching solution with a pH of 3.5 to 4.0, a second precipitate and a secondary selective leaching solution with a pH of 4.0 to 4.5, and a third precipitate and a selective leaching solution with a pH of 5.0 to 5.5;
  • a filter press was used to perform solid-liquid separation operations, and a section of leaching liquid and 0.19 tons of solid matter were obtained respectively;
  • the first-stage leaching solution was subjected to an extraction treatment using P204 for 30 minutes to obtain a P204 raffinate.
  • the P204 raffinate is subjected to one extraction treatment with P507, each extraction treatment time being 20 minutes, to obtain a cobalt-containing organic phase and a P507 raffinate;
  • the solid matter is collected and waits for batch secondary reduction leaching treatment.
  • Crude cobalt hydroxide is a cobalt intermediate product, which includes 34.7% Co, 1.75% Mn, 1.83% Cu, 0.08% Ni, 0.88% Ca, 5.3% Mg, 1.22% Fe, 0.23% Al and 15% moisture.
  • 0.16 tons of crude cobalt hydroxide slurry is gradually added to the preliminary leaching solution to obtain an adjusted leaching solution; then the adjusted leaching solution is subjected to a 1-hour selective precipitation operation to obtain a first precipitate and a primary selective leaching solution with a pH of 3.5 to 4.0, a second precipitate and a secondary selective leaching solution with a pH of 4.0 to 4.5, and a third precipitate and a selective leaching solution with a pH of 5.0 to 5.5;
  • a filter press was used to perform solid-liquid separation operations, and a section of leaching liquid and 0.21 tons of solid matter were obtained respectively;
  • the first-stage leaching solution was subjected to an extraction treatment using P204 for 30 minutes to obtain a P204 raffinate.
  • the P204 raffinate is subjected to one extraction treatment with P507, each extraction treatment time being 20 minutes, to obtain a cobalt-containing organic phase and a P507 raffinate;
  • the solid matter is collected and waits for batch secondary reduction leaching treatment.
  • Crude cobalt hydroxide is a cobalt intermediate product, which includes 34.7% Co, 1.75% Mn, 1.83% Cu, 0.08% Ni, 0.88% Ca, 5.3% Mg, 1.22% Fe, 0.23% Al and 15% moisture.
  • 0.11 tons of crude cobalt hydroxide slurry is gradually added to the preliminary leaching solution to obtain an adjusted leaching solution; then the adjusted leaching solution is subjected to a selective precipitation operation for 1 hour to obtain a first precipitate and a primary selective leaching solution with a pH of 3.5 to 4.0, a second precipitate and a secondary selective leaching solution with a pH of 4.0 to 4.5, and a third precipitate and a selective leaching solution with a pH of 5.0 to 5.5;
  • a filter press was used to perform solid-liquid separation operations, and a section of leaching liquid and 0.18 tons of acid leaching residue were obtained respectively;
  • the first-stage leaching solution was subjected to an extraction treatment using P204 for 30 minutes to obtain a P204 raffinate.
  • the P204 raffinate is subjected to one extraction treatment with P507, each extraction treatment time being 20 minutes, to obtain a cobalt-containing organic phase and a P507 raffinate;
  • the solid matter is collected and waits for batch secondary reduction leaching treatment.
  • Crude cobalt hydroxide is a cobalt intermediate product, which includes 34.7% Co, 1.75% Mn, 1.83% Cu, 0.08% Ni, 0.88% Ca, 5.3% Mg, 1.22% Fe, 0.23% Al and 15% moisture.
  • the remaining 0.13 tons of crude cobalt hydroxide slurry is gradually added to the preliminary leaching solution to obtain an adjusted leaching solution; then the adjusted leaching solution is subjected to a 1-hour selective precipitation operation to obtain a first precipitate and a primary selective leaching solution with a pH of 3.2 to 3.4, a second precipitate and a secondary selective leaching solution with a pH of 4.7, and a third precipitate and a selective leaching solution with a pH of 5.0 to 5.5;
  • a filter press was used to perform solid-liquid separation operations, and a first-stage leaching solution and 0.16 tons of acid leaching residue, 27.82 kg of the first precipitate, 7.06 kg of the second precipitate, and 13.86 kg of the third precipitate were obtained respectively;
  • the first-stage leaching solution was subjected to an extraction treatment using P204 for 30 minutes to obtain a P204 raffinate.
  • the P204 raffinate is subjected to one extraction treatment with P507, each extraction treatment time being 20 minutes, to obtain a cobalt-containing organic phase and a P507 raffinate;
  • the acid leaching residue is collected and waits for batch secondary reduction leaching treatment.
  • Crude cobalt hydroxide is a cobalt intermediate product, which includes 34.7% Co, 1.75% Mn, 1.83% Cu, 0.08% Ni, 0.88% Ca, 5.3% Mg, 1.22% Fe, 0.23% Al and 15% moisture.
  • Pre-oxidation after the treatment in step 2), manganese dioxide ore is added to oxidize Fe 2+ to Fe 3+ .
  • the obtained second-stage reduction leaching solution is transferred to the transfer tank for iron removal to obtain a mixture of the first-stage leaching solution and the second-stage reduction leaching solution;
  • the mixed solution is subjected to selective precipitation treatment to obtain a leachate and a precipitate; and the concentration of tetravalent manganese ions in Comparative Example 1 is higher than that in Examples 1 to 4;
  • the leaching solution was subjected to an extraction treatment using P204 for 30 min to obtain a P204 raffinate.
  • the P204 raffinate is subjected to two extraction treatments with P507, each extraction treatment time being 30 min, to obtain a cobalt-containing organic phase and a P507 raffinate;
  • the sodium ions in the P507 raffinate are treated.
  • Crude cobalt hydroxide is a cobalt intermediate product, which includes 34.7% Co, 1.75% Mn, 1.83% Cu, 0.08% Ni, 0.88% Ca, 5.3% Mg, 1.22% Fe, 0.23% Al and 15% moisture.
  • Pre-oxidation after the treatment in step 2), sodium chlorate is added to oxidize Fe 2+ to Fe 3+ .
  • the obtained second-stage reduction leaching solution is transferred to a transfer tank for iron removal to obtain a mixture of the first-stage leaching solution and the second-stage reduction leaching solution.
  • the mixed solution is subjected to selective precipitation treatment to obtain a leachate and a precipitate; and the concentration of tetravalent manganese ions in Comparative Example 1 is higher than that in Examples 1 to 4;
  • the leaching solution was subjected to an extraction treatment using P204 for 30 min to obtain a P204 raffinate.
  • the P204 raffinate is subjected to two extraction treatments with P507, each extraction treatment time being 30 min, to obtain a cobalt-containing organic phase and a P507 raffinate;
  • the sodium ions in the P507 raffinate are treated.
  • Example 1 Since the amount of crude cobalt hydroxide added in Examples 1 to 4 and Comparative Examples 1 to 2 is the same, but the amount of water added is different, the amount of 3 tons of water added in Example 1 is used as the standard to convert the metal ion content in Examples 1 to 4 and Comparative Examples 1 to 2 to obtain Table 2.
  • the content of tetravalent manganese ions is significantly lower than that of Comparative Example 1. Therefore, in the subsequent extraction treatment, the number of extraction treatments and the time of each extraction treatment are less than those of Comparative Examples 1 to 2, thereby improving the production efficiency and saving the use of the extraction agent.
  • Example 4 27.82 kg of the first precipitate obtained in Example 4 was dissolved with 100 L of dilute hydrochloric acid to obtain a first dissolving solution and 5.27 kg of acid leaching residue, and the concentration of iron ions in the first dissolving solution was determined to be 2.085 mol/L. It can be seen that the mass proportion of iron hydroxide in the first precipitate is 80.2%, and the proportion of iron hydroxide in the soluble matter is 98.9%, which shows that the recovery value of the first precipitate is high;
  • the acidic solution leach the divalent cobalt ions, trivalent iron ions, aluminum ions, copper ions and impurity ions in the crude cobalt hydroxide slurry to obtain a preliminary leachate, and then the added crude cobalt hydroxide slurry is gradually dissolved in the acidic solution to gradually increase the pH value until the pH value is within a range where the divalent cobalt ions do not precipitate and most of the impurity ions precipitate, so that the divalent cobalt ions exist in the form of ions and most of the impurities exist in the precipitate, thereby separating the divalent cobalt ions from most of the impurities in the solid-liquid state, and thus realizing the selective leaching of crude cobalt hydroxide.
  • the continuous selective leaching process for crude cobalt hydroxide in this article not only avoids the problem of introducing sodium ions by adding a reducing agent, introducing sodium ions or tetravalent manganese ions by adding an oxidant, and introducing sodium ions or potassium ions by adding an alkaline auxiliary material in the conventional crude cobalt hydroxide selective leaching process, but also simplifies the subsequent treatment process for sodium ions, tetravalent manganese ions and potassium ions, thereby improving production efficiency, and reduces the concentrations of sodium ions, tetravalent manganese ions and potassium ions, ensuring the quality of the cobalt products produced subsequently.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Manufacturing & Machinery (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Inorganic Chemistry (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

本文提供一种粗制氢氧化钴连续选择性浸出工艺，包括如下步骤：制备粗制氢氧化钴浆料；对一部分粗制氢氧化钴浆料和酸性溶液进行混合操作，直至粗制氢氧化钴浆料溶解于酸性溶液，得到初步浸出液；将另一部分粗制氢氧化钴浆料加入到初步浸出液进行混合，得到调节浸出液；对调节浸出液进行选择性沉淀操作，以形成有沉淀物及选择性浸出液；对沉淀物与选择性浸出液进行固液分离操作，分别得到一段浸出液及酸浸渣。

Description

粗制氢氧化钴连续选择性浸出工艺、浸出装置及二段浸出设备、钴产品生产工艺及生产系统 技术领域
本文涉及一种粗制氢氧化钴连续选择性浸出工艺、浸出装置及二段浸出设备、钴产品生产工艺及生产系统。
背景技术
有色金属是国民经济发展的基础性材料，随着我国经济的快速发展，有色金属需求量日益增长，有色金属提取冶金技术也应随着科技发展不断创新。
由于钴与镍、铁、锰、铜的化学性质比较相似，在天然矿物中经常伴生在一起，矿物中常常同时含有这些元素；含钴的矿物原料多种多样，提取钴的方法繁多且流程各异，可以按照不同的矿物类型进行分类，主要有氧化型矿物、砷化型矿物和硫化型矿物，通常采用火法富集-湿法冶炼的工艺进行处理，目前的全湿法工艺的研究和应用正在发展。
湿法冶金是冶金领域的重要技术手段，它是将矿石、经选矿富集的精矿或其它原料通过浸出剂转入液相，从而实现金属分离、富集和提取的科学技术，湿法冶金包括浸出、金属富集、溶液净化等流程。浸出是湿法冶金的重要工序，在浸出工艺中，不同的浸出剂有其独特的应用。氰化浸出是提取金银的最古老的方法，直接溶于水的硫酸铜等金属用水直接浸出。铜、镍、钴、锌、磷的氧化物可采用硫酸浸出，黄铜矿可采用盐酸浸出，铌、钽可采用氢氟酸浸出，白钨矿、铀矿可采用碳酸钠浸出，铜、镍、钴的硫化物可采用氨水浸出，铜、钴、锰等金属还可采用细菌浸出剂浸出。
粗制氢氧化钴为钴中间品，其包括Co、Mn、Cu、Ni、Ca、Mg、Fe、Al和水分，可以将粗制氢氧化钴中的钴进行选择性浸出。
传统的选择性浸出工艺，存在以下问题：采用二段浸出，不仅浸出二价钴，还采用还原剂浸出三价钴，还原剂的加入引入了较多杂质，进而影响钴的提纯品质。且还原剂会将铁离子还原为亚铁离子，难以在较低的pH下沉淀，因此在还原浸出后，还需要加入氧化剂，将亚铁离子氧化为铁离子；氧化剂的加入进一步引入了较多杂质。还原剂为焦亚硫酸钠、亚硫酸钠、二氧化硫和硫中的至少一种；氧化剂为氯酸钠、二氧化锰中的至少一种。
例如，专利公开号CN112359225A的中国专利提出了一种粗制氢氧化钴矿的选择性浸出工艺，其包括以下步骤：原矿按矿:水＝1:3进行搅拌浆化，浆化后升温至60℃～70℃，加入浓硫酸使料浆pH为0.45～0.5，进行一段浸出，将二价钴和三价铁优先溶解，搅拌5min～10min进行过滤；酸浸液直接进中转槽待除铁，酸浸渣按酸浸渣:水＝1:2进行二次浆化；酸浸渣二次浆化后升温至50℃～60℃，加入焦亚硫酸钠进行二段还原浸出，并维持料浆pH为1.0～1.5，直至还原电位低于240mV。经过上述处理后的料浆加入二氧化锰矿进行预氧化处理，二氧化锰将Fe2+氧化成Fe3+，当浆料中的Fe2+含量低于0.05g/L，浆料转入中转槽待除铁。还原剂为焦亚硫酸钠，即Na2S2O5，还原剂的加入引入了钠离子，同样地，氧化剂为二氧化锰，即MnO2，氧化剂的加入引入了锰离子，降低了选择性浸出的溶液的纯度，即影响了钴的提纯品质。
发明内容
基于此，有必要提供一种对二价钴离子的提纯效果较好的粗制氢氧化钴连续选择性浸出工艺、浸出装置及二段浸出设备、钴产品生产工艺及生产系统。
一种粗制氢氧化钴连续选择性浸出工艺，包括如下步骤：
制备粗制氢氧化钴浆料；
对一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液；
将另一部分所述粗制氢氧化钴浆料加入到所述初步浸出液进行混合，得到调节浸出液；
对所述调节浸出液进行选择性沉淀操作，以形成有沉淀物及选择性浸出液；
对所述沉淀物与选择性浸出液进行固液分离操作，分别得到一段浸出液及酸浸渣。
在其中一个实施例中，所述制备粗制氢氧化钴浆料的步骤具体为：将粗制氢氧化钴与水按质量比1:(2.5～4)制成所述粗制氢氧化钴浆料。
在其中一个实施例中，所述将粗制氢氧化钴与水按质量比1:(2.5～4)制成所述粗制氢氧化钴浆料的步骤具体为：在搅拌下，将粗制氢氧化钴与水按质量比1:(2.5～4)制成所述粗制氢氧化钴浆料。
在其中一个实施例中，所述酸性溶液为硫酸或盐酸中的至少一种。
在其中一个实施例中，所述初步浸出液的pH为2.0～2.5。
在其中一个实施例中，在加热条件下，对一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液。
在其中一个实施例中，在加热条件下，将另一部分所述粗制氢氧化钴浆料加入到所述初步浸出液进行混合，得到调节浸出液。
在其中一个实施例中，在60℃～70℃的条件下，对一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液。
在其中一个实施例中，在60℃～70℃的条件下，将另一部分所述粗制氢氧化钴浆料加入到所述初步浸出液进行混合，得到调节浸出液。
在其中一个实施例中，所述将一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液的步骤的时间为之和为0.8h～1.2h。
在其中一个实施例中，所述将一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液的步骤的时间为之和为1h。
在其中一个实施例中，所述将一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液的步骤具体为：
对一部分所述粗制氢氧化钴浆料和酸性溶液进行至少两次混合搅拌浸出操作，得到所述初步浸出液。
在其中一个实施例中，所述对一部分所述粗制氢氧化钴浆料和酸性溶液进行至少两次混合搅拌浸出操作，得到所述初步浸出液的步骤具体为：
对一部分所述粗制氢氧化钴浆料和酸性溶液进行第一次浸出操作，得到一次浸出液；
对所述一次浸出液进行第二次浸出操作，得到二次浸出液；
将二次浸出液进行第三次浸出操作，得到初步浸出液。
在其中一个实施例中，所述一次浸出液的pH的pH为1.0～1.5。
在其中一个实施例中，所述二次浸出液的pH为1.5～2.0。
在其中一个实施例中，所述初步浸出液的pH为2.0～2.5。
在其中一个实施例中，所述将另一部分所述粗制氢氧化钴浆料加入到所述初步浸出液中，得到调节浸出液的步骤与所述对所述调节浸出液进行选择性沉淀操作，以形成有沉淀物及选择性浸出液的步骤的时间之和为0.8h～1.2h。
在其中一个实施例中，所述将另一部分所述粗制氢氧化钴浆料加入到所述初步浸出液中，得到调节浸出液的步骤与所述对所述调节浸出液进行选择性沉淀操作，以形成有沉淀物及选择性浸出液的步骤的时间之和为1h。
在其中一个实施例中，所述对所述调节浸出液进行选择性沉淀操作，以形成有沉淀物及选择性浸出液的步骤具体为：
对所述调节浸出液进行至少一次选择性沉淀操作，以形成有沉淀物及选择性浸出液。
在其中一个实施例中，所述对所述调节浸出液进行选择性沉淀操作，以形成有沉淀物及选择性浸出液的步骤具体为：
对调节浸出液进行第一次选择性沉淀操作，得到一次选择性浸出液及第一沉淀物；
对所述一次选择性浸出液进行第二次选择性沉淀操作，得到二次选择性浸出液及第二沉淀物；
对所述二次选择性浸出液进行第三次选择性沉淀操作，得到选择性浸出液及第三沉淀物。
在其中一个实施例中，所述一次选择性浸出液的pH为3.5～4.0。
在其中一个实施例中，所述二次选择性浸出液的pH为4.0～4.5。
在其中一个实施例中，所述选择性浸出液的pH为5.0～5.5。
在其中一个实施例中，所述一次选择性浸出液的pH为3.2～3.4。
在其中一个实施例中，所述二次选择性浸出液的pH为4.7。
在其中一个实施例中，所述选择性浸出液的pH为5.0～6.7。
在其中一个实施例中，所述对一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作的步骤具体为：
同时加入一部分所述粗制氢氧化钴浆料和酸性溶液并进行混合操作。
在其中一个实施例中，所述对一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作的步骤具体为：所述一部分所述粗制氢氧化钴浆料与所述酸性溶液的体积比为14～16。
在其中一个实施例中，所述将另一部分所述粗制氢氧化钴浆料加入到所述初步浸出液中，得到调节浸出液的步骤具体为：所述一部分所述粗制氢氧化钴浆料与所述酸性溶液的体积比为15。
一种钴产品生产工艺，包括对采用上述任一实施例得到的所述一段浸出液进行至少如下步骤：
获取一段浸出液；
对所述一段浸出液进行萃取处理；
对经过所述萃取处理的所述一段浸出液进行加工处理，得到一段浸出钴产品。
一种粗制氢氧化钴的连续选择性浸出装置，采用上述任一实施例所述的粗制氢氧化钴连续选择性浸出工艺进行浸出操作，所述粗制氢氧化钴连 续选择性浸出装置包括：
浸出机构，所述浸出机构至少包括溶浆组件、补浆组件和选择性沉淀组件，所述溶浆组件开设有所述第一溢流口，所述第一溢流口连通于所述补浆组件，所述补浆组件开设有所述第二溢流口，所述第二溢流口连通于所述选择性沉淀组件，所述选择性沉淀组件开设有所述第三溢流口；
中转机构，所述中转机构连通于所述第三溢流口，所述中转机构用于分别连通于一级浸出液存储机构和浸出渣制浆装置。
在其中一个实施例中，所述选择性沉淀组件连通于所述溶浆组件。
在其中一个实施例中，所述溶浆组件连通于所述中转组件。
在其中一个实施例中，所述补浆组件连通于所述中转组件。
在其中一个实施例中，所述溶浆组件至少包括相连通的一次溶浆釜和二次溶浆釜，所述第一溢流口形成于所述二次溶浆釜。
在其中一个实施例中，所述溶浆组件还包括中间溶浆釜，所述中间溶浆釜分别连通于所述一次溶浆釜和所述二次溶浆釜。
在其中一个实施例中，所述选择性沉淀组件至少包括相连通的第一水解沉淀釜和第二水解沉淀釜，所述第三溢流口形成于所述第二水解沉淀釜。
在其中一个实施例中，所述粗制氢氧化钴连续选择性浸出装置还包括压滤机构，所述压滤机构连通于所述中转机构，所述压滤机构用于连通于所述浸出渣制浆装置。
在其中一个实施例中，所述浸出机构还包括加热组件，所述加热组件的作用端作用于所述溶浆组件。
在其中一个实施例中，所述加热组件为蒸汽加热组件，所述蒸汽加热组件设有蒸汽输出端，所述蒸汽输出端连通于所述溶浆组件。
在其中一个实施例中，所述溶浆组件设置有第一pH测量组件。
在其中一个实施例中，所述补浆组件设置有第二pH测量组件。
在其中一个实施例中，所述选择性沉淀组件设置有第三pH测量组件。
在其中一个实施例中，所述浸出机构至少还包括有第一搅拌组件，所述第一搅拌组件的搅拌端设置于所述溶浆组件内。
在其中一个实施例中，所述溶浆组件形成有相连通的进浆槽和进浆口，所述进浆槽连通于所述第一溢流口。
在其中一个实施例中，所述浸出机构还包括第一供浆组件，所述第一供浆组件连通于所述溶浆组件。
在其中一个实施例中，所述第一供浆组件包括第一pH仪表、第一流速监测器、第一活动隔板和第一供浆槽体，所述第一供浆槽体连通于所述溶浆组件，所述第一活动隔板设置于所述第一供浆槽体与所述溶浆组件的连通处，所述第一pH仪表的探测端设置于所述溶浆组件内，所述第一流速监测器的作用端设置于所述第一溢流口。
在其中一个实施例中，所述第一供浆组件用于将所述粗制氢氧化钴浆料的流量设置为1m3/h～3m3/h。
在其中一个实施例中，所述补浆组件开设有相连通的盛浆槽和补料口，所述盛浆槽分别连通于所述第一溢流口及所述选择性沉淀组件。
在其中一个实施例中，所述浸出机构还包括第二供浆组件，所述第二供浆组件连通于所述补浆组件。
在其中一个实施例中，所述第二供浆组件
本文还提供一种粗制氢氧化钴二段浸出设备，包括一段浸出液存储机构、浸出渣制浆装置和上述任一实施例所述的粗制氢氧化钴连续选择性浸出装置，所述压滤机构分别连通于所述一段浸出液存储机构和所述浸出渣制浆装置。
在其中一个实施例中，所述浸出渣制浆装置包括相连通的二段浸出机构和二段浸出液存储机构。
一种钴产品生产系统，包括一段浸出液处理设备、二段浸出液处理设备和上述任一实施例所述的粗制氢氧化钴二段浸出设备，所述一段液处理设备连通于所述一段浸出液存储机构，所述二段浸出液处理设备连通于所述二段浸出液存储设备。
本文的一个或多个实施例的细节在下面的附图和描述中提出。与现有技术相比，本文至少具有以下优点：
1)本文的粗制氢氧化钴连续选择性浸出工艺，酸性溶液将粗制氢氧化钴浆料中的二价钴离子、三价铁离子、铝离子和铜离子和杂质离子浸出，以得到初步浸出液，然后补加的粗制氢氧化钴浆料逐渐溶解于酸性溶液，以逐渐提高pH值，直至pH值处于使二价钴离子不发生沉淀且使大部分杂质离子沉淀的范围，使二价钴离子以离子形态存在且大部分杂质存在于沉淀中，进而使二价钴离子与大部分杂质固液分离，进而实现粗制氢氧化钴的选择性浸出。
2)本文的粗制氢氧化钴连续选择性浸出工艺，一段浸出液不仅避免了因传统的粗制氢氧化钴选择性浸出工艺在浸出液中加入还原剂而引入钠离子、加入氧化剂而引入钠离子或四价锰离子以及加入碱性辅料而引入钠离子或钾离子的问题，进而简化了后续对于钠离子、四价锰离子和钾离子的处理工艺，进而提升生产效率，且降低了钠离子、四价锰离子和钾离子的浓度，确保了后续生产得到的钴产品的品质。
附图说明
为了更清楚地说明本文实施例或现有技术中的技术方案，下面将对实施例或现有技术描述中所可以使用的附图作简单地介绍。
图1为一实施例的粗制氢氧化钴连续选择性浸出工艺的方法步骤流程图；
图2为一实施例的钴产品生产工艺的方法步骤流程图。
具体实施方式
为了便于理解本文，下面将参照相关附图对本文进行更全面的描述。附图中给出了本文的可选实施方式。但是，本文可以以许多不同的形式来实现，并不限于本文所描述的实施方式。相反地，提供这些实施方式的目的是使对本文的公开内容理解的更加透彻全面。当元件被称为“固定于”另一个元件，它可以直接在另一个元件上或者也可以存在居中的元件。当一个元件被认为是“连接”另一个元件，它可以是直接连接到另一个元件或者可能同时存在居中元件。本文所使用的术语“垂直的”、“水平的”、“左”、“右”以及类似的表述只是为了说明的目的，并不表示是唯一的实施方式。除非另有定义，本文所使用的所有的技术和科学术语与属于本文的技术领域的技术人员通常理解的含义相同。本文中在本文的说明书中所使用的术语只是为了描述具体的实施方式的目的，不是旨在于限制本文。本文所使用的术语“及/或”包括一个或多个相关的所列项目的任意的和所有的组合。
本文提供一种粗制氢氧化钴连续选择性浸出工艺。为了更好地理解本文的粗制氢氧化钴连续选择性浸出工艺，以下对本文的粗制氢氧化钴连续选择性浸出工艺做进一步的解释说明：
如图1所示，进一步地，粗制氢氧化钴连续选择性浸出工艺包括以下步骤的部分或全部：
S100，制备粗制氢氧化钴浆料。
可以理解，称取粗制氢氧化钴和水，进行混合搅拌操作，得到粗制氢氧化钴浆料。
S200，对一部分粗制氢氧化钴浆料和酸性溶液进行混合操作，直至粗制氢氧化钴浆料溶解于酸性溶液，得到初步浸出液。
其中，粗制氢氧化钴浆料和酸性溶液同时加入，酸性溶液可以为硫酸或盐酸，减轻了传统的粗制氢氧化钴选择性浸出工艺先加入粗制氢氧化钴浆料后加入酸性溶液造成的加料时间较长而降低生产效率的问题。在其他实施例中，氢氧化钴浆料和酸性溶液不仅限于同时加入，即氢氧化钴浆料和酸性溶液分别加入。
S300，将另一部分粗制氢氧化钴浆料加入到初步浸出液进行混合，得到调节浸出液。
可以理解，粗制氢氧化钴浆料包括金属氢氧化物和金属氧化物，金属指Co、Mn、Cu、Ni、Ca、Mg、Fe和Al，作为碱性物质加入，避免了传统的粗制氢氧化钴选择性浸出工艺加入碱性辅料而引入钠离子或钾离子的问题，进而避免后续还需要增加萃取处理次数并延长萃取时间进而降低生产效率的问题，且避免了后续还需要对P507萃余液中的钠进行处理而造成增加废水处理工序的问题，即减少了生产工序，进而提高生产效率，且降低人工劳动强度；且由于一段浸出液未引入杂质，提高了后续的钴产品的品质，例如：国家标准对于硫酸钴优等品钠的含量为小于等于0.001％，一等品钠含量为小于等于0.002％，由于一段浸出液未引入钠离子，使得后续的钴产品容易达到硫酸钴优等品的等级，即确保了钴产品的品质。
S400，对调节浸出液进行选择性沉淀操作，以形成有沉淀物及选择性浸出液。
可以理解，由于粗制氢氧化钴浆料逐渐溶解，在溶解过程中pH逐渐升高，使得沉淀pH较低的杂质离子逐渐析出为沉淀物，同时确保二价钴离子以离子形态存在于选择性浸出液中，即得到包含二价钴离子的选择性浸出液。
S500，对沉淀物与选择性浸出液进行固液分离操作，分别得到一段浸出液及酸浸渣。
可以理解，一段浸出液存储于一段浸出液存储机构中，与后续对酸浸渣进行二段还原浸出得到的二段还原浸出液各自存储于独立的机构中，避免纯度较高的一段浸出液受到纯度较低的二段还原浸出液的影响的问题，进而确保一段浸出液的纯度，且由于酸浸渣较少，后续对酸浸渣进行批量处理，提高生产效率。
上述的粗制氢氧化钴连续选择性浸出工艺，酸性溶液将粗制氢氧化钴浆料中的二价钴离子、三价铁离子、铝离子和铜离子和杂质离子浸出，以得到初步浸出液，然后补加的粗制氢氧化钴浆料逐渐溶解于酸性溶液，以逐渐提高pH值，直至pH值处于使二价钴离子不发生沉淀且使大部分杂质离子沉淀的范围，使二价钴离子以离子形态存在且大部分杂质存在于沉淀中，进而使二价钴离子与大部分杂质固液分离，进而实现粗制氢氧化钴的选择性浸出。
进一步地，上述的粗制氢氧化钴连续选择性浸出工艺，由于无需加入还原剂进行浸出，节省了还原反应的时间，提高了生产效率。
进一步地，一段浸出液不仅避免了因传统的粗制氢氧化钴选择性浸出工艺在浸出液中加入还原剂而引入钠离子、加入氧化剂而引入钠离子或四价锰离子以及加入碱性辅料而引入钠离子或钾离子的问题，进而简化了后续对于钠离子、四价锰离子和钾离子的处理工艺，进而提升生产效率，且降低了钠离子、四价锰离子和钾离子的浓度，确保了后续生产得到的钴产品的品质。
进一步地，将粗制氢氧化钴浆料与酸性溶液同时加入到溶浆组件中，避免了传统的粗制氢氧化钴选择性浸出工艺因先加入浆料并加热再加入硫酸造成的生产效率较低的问题，进而提高生产效率。
进一步地，传统的粗制氢氧化钴选择性浸出工艺将二价钴的浸出液与三价钴的还原浸出液先后转入至中转槽待除铁，二价钴的浸出液的纯度较高，三价钴的还原浸出液由于先加入了还原剂发生还原反应且后加入氧化剂进行氧化反应分别引入了钠离子和锰离子，且钠离子难以水解沉淀，相同温度下，锰离子的沉淀pH高于二价钴的沉淀pH，也难以在确保二价钴不沉淀的条件下对锰离子进行沉淀，即还原剂与氧化剂引入的杂质离子难以去除，因此三价钴的还原浸出液降低了二价钴浸出液的纯度，进而降低了二价钴浸出液后续的提纯品质。为了提高后续得到的钴产品的品质，本文的粗制氢氧化钴选择性浸出工艺将二价钴的浸出液与酸浸渣分开进行处理，且二价钴浸出液不加入还原剂、氧化剂和碱性辅料，进而确保了后续 得到的钴产品的品质。
进一步地，粗制氢氧化钴中，二价钴的含量较高，三价钴的含量较低，且三价钴需要还原剂的加入才能浸出，二价钴浸出后转移至中转槽待除铁，需要等待三价钴还原浸出，再转移至中转槽一同除铁，因此，传统的粗制氢氧化钴选择性浸出工艺降低了生产效率。为了提高后续得到的钴产品的品质，同时进一步提高生产效率，本文的粗制氢氧化钴选择性浸出工艺将二价钴的浸出液与酸浸渣分开进行处理，并对酸浸渣进行收集并进行批量处理。
在其中一个实施例中，制备粗制氢氧化钴浆料的步骤具体为：将粗制氢氧化钴与水按质量比1:(2.5～4)制成粗制氢氧化钴浆料。
在其中一个实施例中，将粗制氢氧化钴与水按质量比1:(2.5～4)制成粗制氢氧化钴浆料的步骤具体为：将粗制氢氧化钴与水按质量比1:(2.5～4)并搅拌混合制成粗制氢氧化钴浆料。
在其中一个实施例中，酸性溶液为硫酸或盐酸中的至少一种。
在其中一个实施例中，初步浸出液的pH为2.0～2.5。可以理解，得到初步浸出液时，粗制氢氧化钴浆料较充分地溶解于酸性溶液，即得到浸出了大量二价钴离子的溶液。
在其中一个实施例中，在加热条件下，对一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液。
在其中一个实施例中，在加热条件下，将另一部分所述粗制氢氧化钴浆料加入到所述初步浸出液进行混合，得到调节浸出液。
在其中一个实施例中，在60℃～70℃的条件下，对一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液。可以理解，温度升高可以活化反应、加速颗粒间的运动，促进硫酸与物料粉末液两相接触的反应。温度的升高增加了反应物内部能量，加大了两者的碰撞机会而提高了钴的浸出率和浸出反应速率，缩短了浸出达到平衡点所需要的时间。
在其中一个实施例中，在60℃～70℃的条件下，将另一部分所述粗制氢氧化钴浆料加入到所述初步浸出液进行混合，得到调节浸出液。可以理解，温度升高可以活化反应、加速颗粒间的运动，促进硫酸与物料粉末液两相接触的反应。温度的升高增加了反应物内部能量，加大了两者的碰撞机会而提高了钴的浸出率和浸出反应速率，缩短了浸出达到平衡点所需要的时间。
在其中一个实施例中，将一部分粗制氢氧化钴浆料和酸性溶液进行混合操作，直至粗制氢氧化钴浆料溶解于酸性溶液，得到初步浸出液的步骤的时间为之和为0.8h～1.2h。在本实施例中，将一部分粗制氢氧化钴浆料和酸性溶液进行混合操作，直至粗制氢氧化钴浆料溶解于酸性溶液，得到初步浸出液的步骤的时间为之和为1h。
在其中一个实施例中，将一部分粗制氢氧化钴浆料和酸性溶液进行混合操作，直至粗制氢氧化钴浆料溶解于酸性溶液，得到初步浸出液的步骤具体为：对一部分粗制氢氧化钴浆料和酸性溶液进行至少两次混合搅拌浸出操作，得到初步浸出液。可以理解，使粗制氢氧化钴浆料充分溶解于酸性溶液，进而得到较充分浸出的二价钴离子。
在其中一个实施例中，对一部分粗制氢氧化钴浆料和酸性溶液进行至少两次混合搅拌浸出操作，得到初步浸出液的步骤具体为：
对一部分粗制氢氧化钴浆料和酸性溶液进行第一次浸出操作，得到一次浸出液；
对一次浸出液进行第二次浸出操作，得到二次浸出液；
将二次浸出液进行第三次浸出操作，得到初步浸出液。
在其中一个实施例中，一次浸出液的pH为1.0～1.5。在本实施例中，一次浸出液的pH为1.2。
在其中一个实施例中，二次浸出液的pH为1.5～2.0。在本实施例中，二次浸出液的pH为1.8。
在其中一个实施例中，初步浸出液的pH为2.0～2.5。在本实施例中，初步浸出液的pH为2.3。
在其中一个实施例中，将另一部分粗制氢氧化钴浆料加入到初步浸出液中，得到调节浸出液的步骤与对调节浸出液进行选择性沉淀操作，以形成有沉淀物及选择性浸出液的步骤的时间之和为0.8h～1.2h。在本实施例中，将另一部分粗制氢氧化钴浆料加入到初步浸出液中，得到调节浸出液的步骤与对调节浸出液进行选择性沉淀操作，以形成有沉淀物及选择性浸出液的步骤的时间之和为1h。
在其中一个实施例中，对调节浸出液进行选择性沉淀操作，以形成有沉淀物及选择性浸出液的步骤具体为：
对调节浸出液进行至少一次选择性沉淀操作，以形成有沉淀物及选择性浸出液。
在其中一个实施例中，对调节浸出液进行选择性沉淀操作，以形成有沉淀物及选择性浸出液的步骤具体为：
对调节浸出液进行第一次选择性沉淀操作，得到一次选择性浸出液及沉淀物；
可以理解，调节浸出液中含有二价钴离子、铁离子、铝离子、铜离子和杂质离子，随着pH的升高，易于沉淀的铁离子首先被水解沉淀，即此步骤中的沉淀物为氢氧化铁，一次选择性浸出液为去除了大部分铁离子的调节浸出液。
对一次选择性浸出液进行第二次选择性沉淀操作，得到二次选择性浸出液及沉淀物；
可以理解，随着pH的进一步升高，铝离子被水解沉淀，即此步骤增加的沉淀物为氢氧化铝和微量的氢氧化铁，二次选择性浸出液为去除了铁离子和铝离子的调节浸出液。
对二次选择性浸出液进行第三次选择性沉淀操作，得到选择性浸出液及沉淀物。
可以理解，随着pH的进一步升高，铜离子被水解沉淀，即此步骤增加的沉淀物为氢氧化铜、少量的氢氧化铝和微量的氢氧化铁，实现了铜的富 集，二次选择性浸出液为去除了铁离子、铝离子和部分铜离子的调节浸出液。
在其中一个实施例中，一次选择性浸出液的pH为3.5～4.0。可以理解，粗制氢氧化钴浆料与酸性溶液的反应，降低了混合液的pH，当pH大于3.5时，铁离子容易完全水解沉淀。
在其中一个实施例中，二次选择性浸出液的pH为4.0～4.5。可以理解，粗制氢氧化钴浆料与酸性溶液的反应，降低了混合液的pH，当pH为4.0～4.5时，大部分铝离子水解沉淀。
在其中一个实施例中，选择性浸出液的pH为5.0～5.5。可以理解，粗制氢氧化钴浆料与酸性溶液的反应，降低了混合液的pH，当pH为5.0～5.5时，少量铝离子和部分铜离子水解沉淀，进而减少了选择性浸出液中的杂质离子，且实现了铜的富集。
在其中一个实施例中，一次选择性浸出液的pH为3.2～3.4。可以理解，当一次选择性浸出液的pH为3.2～3.4时，铁离子充分水解沉淀，铝离子未开始水解沉淀，即得到的第一沉淀物主要为氢氧化铁沉淀，品位较高，具有较高的回收价值，例如可以用于制颜料、药物、制作砷的解毒药，也可加还原剂高温处理成四氧化三铁。
在其中一个实施例中，二次选择性浸出液的pH为4.7。可以理解，当二次选择性浸出液的pH为4.7时，铁离子已在前一步骤充分沉淀，铝离子在本步骤中充分水解沉淀，铜离子未开始水解沉淀，即本步骤得到的第二沉淀物主要为氢氧化铝沉淀，品位较高，具有较高的回收价值，例如可以用于制备抗酸剂，治疗胃痛、胃酸过多、胃灼热、胃酸，还可以使用它来降低患有肾脏问题的人的磷酸盐水平。
在其中一个实施例中，选择性浸出液的pH为5.0～6.7。可以理解，当选择性浸出液的pH为5.0～6.7时，铁离子和铝离子已在之前的步骤中充分沉淀，且二价钴离子未开始水解沉淀，即本步骤得到的第三沉淀物主要为氢氧化铜沉淀，品位较高，具有较高的回收价值，例如可以用于制备媒染剂、催化剂、杀菌剂和颜料，并用于染纸张等、用作分析试剂；制铜盐的原料、媒染剂，以及用作杀菌剂、船底防污漆的组分。
在其中一个实施例中，选择性浸出液的pH为6.7。可以理解，当选择性浸出液的pH为5.0～6.7时，铜离子充分水解沉淀，且二价钴离子未开始水解沉淀，即能够在减少二价钴离子损失的前提下提高铜离子的沉降率，较充分地实现对铜的富集和回收。
传统的粗制氢氧化钴选择性浸出工艺，同时浸出氢氧化铁、氢氧化铝和氢氧化铜，即得到同时包含氢氧化铁、氢氧化铝和氢氧化铜的沉淀物，在回收沉淀物时还需要将铁、铝和铜进行分离才能回收，降低了生产效率，且提高了生产成本。为了使氢氧化铁、氢氧化铝和氢氧化铜分别沉淀，在其中一个实施例中，一次选择性浸出液的pH为3.2～3.4，二次选择性浸出液的pH为4.7，选择性浸出液的pH为5.0～6.7。可以理解，使得第一沉淀物中氢氧化铁的含量较高，且第二沉淀物中氢氧化铝的含量较高，且第三沉淀物中氢氧化铜的含量较高，进而使氢氧化铁、氢氧化铝和氢氧化铜均能单独回收，且提高了后续的回收工序的生产便利性和生产效率，且降低了生产成本。
在其中一个实施例中，对一部分粗制氢氧化钴浆料和酸性溶液进行混合操作的步骤具体为：同时加入一部分粗制氢氧化钴浆料和酸性溶液并进行混合操作。可以理解，同时加入一部分粗制氢氧化钴浆料和酸性溶液并进行混合操作，减轻了传统的先加入粗制氢氧化钴浆料再加入酸性溶液而造成生产时间较长的问题，进而提高生产效率。
请一并参阅图1至图2，本文还提供一种钴产品生产工艺。上述的钴产品生产工艺包括对采用上述任一实施例得到的一段浸出液进行至少如下步骤：
S501、获取一段浸出液；
在本实施例中，采用了上述的粗制氢氧化钴连续选择性浸出工艺制备得到的一段浸出液，即一段浸出液中未加入还原剂、氧化剂和碱性辅料，进而避免了传统的一段浸出液由于加入还原剂、氧化剂和碱性辅料而引入的钠离子、硫化物、四价锰离子和钾离子的问题。
S600、对一段浸出液进行萃取处理；
在本实施例中，虽然一段浸出液已经对铁离子、铝离子和部分铜离子进行水解沉淀，但是一段浸出液中还包括杂质离子，杂质离子具体为四价锰离子、镍离子、钙离子、镁离子和部分铜离子，还需要通过萃取处理去除，经过处理后的杂质离子的浓度与后续得到的钴产品的质量成反比。
S700、对经过萃取处理的一段浸出液进行加工处理，得到一段浸出钴产品。
传统的粗制氢氧化钴选择性浸出工艺，由于加入还原剂而引入钠离子或硫化物，且加入氧化剂而引入钠离子或四价锰离子，且加入碱性辅料而引入钠离子或钾离子，因此需要通过萃取处理以及其它处理以去除杂质离子，且存在以下问题：
钠离子和钾离子会严重影响后续钴产品的品质，因此还需要通过后续的增加萃取处理次数并延长萃取时间才能使离子浓度降低至0.01g/L，达到除杂的目的，使得生产工序较为复杂，且降低了生产效率；同样地，处理硫化物需要采用气提、化学沉淀或氧化的方法，需要较多的化学药品及沉淀物处理，能耗较高，成本较高，且对环境不友好，尤其是气提，会产生大量含H2S的空气，因此后续需要对含H2S的空气进行处理，进一步使得生产工序较为复杂，且降低了生产效率；且由于氧化剂引入了四价锰离子，使得四价锰离子的浓度较高，进而使得去除四价锰离子需要用到的萃取剂较多，且萃取次数增多，同时延长了萃取时间，进而降低了生产效率。
上述的钴产品生产工艺，采用了上述的粗制氢氧化钴连续选择性浸出工艺制备得到的一段浸出液，避免了传统的一段浸出液引入钠离子、硫化物、四价锰离子和钾离子的问题，减少了萃取处理次数并缩短萃取时间，进而提高了生产效率；且由于一段浸出液未引入杂质，提高了后续的钴产品的品质，例如：国家标准对于硫酸钴优等品钠的含量为小于等于0.001％，一等品钠含量为小于等于0.002％，由于一段浸出液未引入钠离子，使得后续的钴产品容易达到硫酸钴优等品的等级，即确保了钴产品的品质。
本文还提供一种粗制氢氧化钴的连续选择性浸出装置，采用上述任一实施例的粗制氢氧化钴连续选择性浸出工艺进行浸出操作，粗制氢氧化钴 连续选择性浸出装置包括：
浸出机构，浸出机构至少包括溶浆组件、补浆组件和选择性沉淀组件，溶浆组件开设有第一溢流口，第一溢流口连通于补浆组件，补浆组件开设有第二溢流口，第二溢流口连通于选择性沉淀组件，选择性沉淀组件开设有第三溢流口；
中转机构，中转机构连通于第三溢流口，中转机构用于分别连通于一级浸出液存储机构和浸出渣制浆装置。
上述的粗制氢氧化钴连续选择性浸出装置，溶浆组件用于盛装粗制氢氧化钴浆料和酸性溶液，酸性溶液在溶浆组件内将粗制氢氧化钴浆料中的二价钴离子、三价铁离子、铝离子和铜离子浸出，以得到浸出液，然后浸出液通过第一溢流口溢出到补浆组件，补浆组件用于盛装浸出液和补加的粗制氢氧化钴浆料，补加的粗制氢氧化钴浆料逐渐溶解于酸性溶液，以逐渐提高补浆组件及选择性沉淀组件内液体的pH值，直至pH值处于使二价钴离子不发生沉淀且使大部分杂质离子沉淀的范围，使二价钴离子以离子形态存在且大部分杂质存在于沉淀中，进而使二价钴离子与大部分杂质固液分离，进而实现粗制氢氧化钴的选择性浸出。
进一步地，经过选择性沉淀组件选择性浸出得到的一段浸出液和沉淀均通过第三溢流口溢流至中转机构，然后一段浸出液流向一段浸出液存储机构，沉淀输送至浸出渣制浆装置；一段浸出液不仅避免了因传统的粗制氢氧化钴选择性浸出工艺在浸出液中加入还原剂和氧化剂而造成的引入杂质的问题，还通过以粗制氢氧化钴浆料为提高pH的调节剂避免了通过加入碱性辅料而造成的引入杂质的问题，进而确保一段浸出液的纯度，即提高钴的提纯品质。
进一步地，上述的粗制氢氧化钴连续选择性浸出装置，将粗制氢氧化钴浆料与酸性溶液同时加入到溶浆组件中，避免了传统的粗制氢氧化钴选择性浸出工艺因先加入浆料并加热再加入硫酸造成的生产效率较低的问题，进而提高生产效率。
进一步地，粗制氢氧化钴浆料和酸性溶液从溶浆组件通过第一溢流口溢流至补浆组件，再从补浆组件通过第二溢流口溢流至选择性沉淀组件，再从选择性沉淀组件通过第三溢流口溢流至中转机构，减少了机泵的使用，确保了粗制氢氧化钴连续选择性浸出装置的自动化，简化了操作流程，且避免了传统的粗制氢氧化钴选择性浸出工艺还需要改将浸出液转移至中转槽的问题，降低了人工劳动强度。
进一步地，传统的粗制氢氧化钴选择性浸出工艺将二价钴的浸出液与三价钴的还原浸出液先后转入至中转槽待除铁，二价钴的浸出液的纯度较高，三价钴的还原浸出液由于先加入了还原剂发生还原反应且后加入氧化剂进行氧化反应分别引入了钠离子和锰离子，且钠离子难以水解沉淀，相同温度下，锰离子的沉淀pH高于二价钴的沉淀pH，也难以在确保二价钴不沉淀的条件下对锰离子进行沉淀，即还原剂与氧化剂引入的杂质离子难以去除，因此三价钴的还原浸出液降低了二价钴浸出液的纯度，进而降低了二价钴浸出液后续的提纯品质。
进一步地，粗制氢氧化钴中，二价钴的含量较高，三价钴的含量较低且需要还原剂的加入才能浸出，二价钴浸出后转移至中转槽待除铁，需要等待三价钴还原浸出，再转移至中转槽一同除铁，降低了生产效率。
在其中一个实施例中，选择性沉淀组件连通于溶浆组件。可以理解，溶浆组件开设有第一溢流口，第一溢流口连通于补浆组件，补浆组件开设有第二溢流口，第二溢流口连通于选择性沉淀组件，选择性沉淀组件连通于溶浆组件，即溶浆组件、补浆组件和选择性沉淀组件形成循环连接；且选择性沉淀组件不局限于仅用于进行选择性沉淀，还可用于溶浆或补浆，同样地，溶浆组件不局限于仅用于溶浆，还可用于进行选择性沉淀或补浆，同样地，补浆组件不局限于仅用于补浆，还可用于进行选择性沉淀或溶浆；因此，当选择性沉淀组件中的浆料没有充分溶解时，可将本轮的浆料堆积较多的选择性沉淀组件作为下一轮的溶浆组件，且其他组件也配合进行调整，使本轮堆积的未充分溶解的浆料在下一轮中重新得以溶解，进而提高对粗制氢氧化钴浆料的充分利用，且减少了还需要人工清理并转移浆料而造成人工劳动强度较大的问题，且节约了清理及转移浆料的时间，进而提高了生产效率。
为了提高二价钴浸出液后续的提纯品质，同时提高生产效率，在其中一个实施例中，中转机构用于分别连通于一段浸出液存储机构和浸出渣制浆装置。可以理解，中转机构对二价钴的浸出液与沉淀进行固液分离，二价钴的浸出液即一段浸出液，一段浸出液流向一段浸出液存储机构，一段浸出液存储机构仅用于存储一段浸出液，而不用于存储后续沉淀还原浸出的三价钴浸出液，进而确保一段浸出液的纯度；且由于沉淀的量较少，后续将沉淀批量集中进行浸出，对沉淀的批量处理节省了能源，并减少了浸出渣制浆装置的使用，进而减少了浸出渣制浆装置的损坏和维修，进而提高浸出渣制浆装置的使用寿命，且较好地提高了生产效率；且由于避免了传统的粗制氢氧化钴选择性浸出工艺将二价钴浸出后转移至中转槽待除铁，需要等待三价钴还原浸出液一并进行除铁的问题，进而减少了设备占而不用的现象，即确保了设备的使用率，进而缩小了设备的占地面积。
为了提高二价钴浸出液后续的提纯品质，同时提高生产效率，在其中一个实施例中，中转机构用于分别连通于一段浸出液存储机构和浸出渣制浆装置。可以理解，中转机构对二价钴的浸出液与沉淀进行固液分离，二价钴的浸出液即一段浸出液，一段浸出液流向一段浸出液存储机构，一段浸出液存储机构仅用于存储一段浸出液，而不用于存储后续沉淀还原浸出的三价钴浸出液，进而确保一段浸出液的纯度；且由于沉淀的量较少，后续将沉淀批量集中进行浸出，对沉淀的批量处理节省了能源，并减少了浸出渣制浆装置的使用，进而减少了浸出渣制浆装置的损坏和维修，进而提高浸出渣制浆装置的使用寿命，且较好地提高了生产效率；且由于避免了传统的粗制氢氧化钴选择性浸出工艺将二价钴浸出后转移至中转槽待除铁，需要等待三价钴还原浸出液一并进行除铁的问题，进而减少了设备占而不用的现象，即确保了设备的使用率，进而缩小了设备的占地面积。
在其中一个实施例中，溶浆组件至少包括相连通的一次溶浆釜和二次溶浆釜，第一溢流口形成于二次溶浆釜。可以理解，粗制氢氧化钴浆料及酸性溶液从刚加入一次溶浆釜到装满一次溶浆釜为一个过程，需要时间，同样地，从一次溶浆釜溢流至二次溶浆釜也需要时间，在此期间，粗制氢氧化钴浆料较充分地溶解于酸性溶液，即使得粗制氢氧化钴中的二价钴较充分地浸出，进而确保粗制氢氧化钴中二价钴的浸出率。
在其中一个实施例中，溶浆组件还包括中间溶浆釜，中间溶浆釜分别连通于一次溶浆釜和二次溶浆釜。可以理解，粗制氢氧化钴浆料及酸性溶 液从刚加入一次溶浆釜到装满一次溶浆釜为一个过程，需要时间，同样地，从一次溶浆釜溢流至中间溶浆釜也需要时间，同样地，从中间溶浆釜溢流至二次溶浆釜也需要时间，在此期间，粗制氢氧化钴浆料较充分地溶解于酸性溶液，即使得粗制氢氧化钴中的二价钴较充分地浸出，进而确保粗制氢氧化钴中二价钴的浸出率。
在其中一个实施例中，选择性沉淀组件至少包括相连通的第一水解沉淀釜和第二水解沉淀釜，第三溢流口形成于第二水解沉淀釜。可以理解，补加的粗制氢氧化钴浆料需要一定时间溶解，从补浆组件依次流向第一水解沉淀釜和第二水解沉淀釜的过程中，补加的粗制氢氧化钴浆料较充分地溶解，且逐渐消耗酸性溶液，使pH逐渐升高，进而使三价铁离子、铝离子和铜离子逐渐水解沉淀析出，进而实现粗制氢氧化钴的连续选择性浸出，且确保了浸出效果，即确保了二价钴的提纯效果。
在其中一个实施例中，选择性沉淀组件连通于溶浆组件。可以理解，溶浆组件开设有第一溢流口，第一溢流口连通于补浆组件，补浆组件开设有第二溢流口，第二溢流口连通于选择性沉淀组件，选择性沉淀组件连通于溶浆组件，即溶浆组件、补浆组件和选择性沉淀组件形成循环连接；且选择性沉淀组件不局限于仅用于进行选择性沉淀，还可用于溶浆或补浆，同样地，溶浆组件不局限于仅用于溶浆，还可用于进行选择性沉淀或补浆，同样地，补浆组件不局限于仅用于补浆，还可用于进行选择性沉淀或溶浆；因此，当浸出机构出现故障或其它原因，使得选择性沉淀组件中的浆料没有充分溶解时，可将本轮的浆料堆积较多的选择性沉淀组件作为下一轮的溶浆组件，且其他组件也配合进行调整，使本轮堆积的未充分溶解的浆料在下一轮中重新得以溶解，进而提高对粗制氢氧化钴浆料的充分利用，且减少了还需要人工清理并转移浆料而造成人工劳动强度较大的问题，且节约了清理及转移浆料的时间，进而提高了生产效率。
在其中一个实施例中，选择性沉淀组件连通于溶浆组件，补浆组件连通于中转组件。可以理解，溶浆组件开设有第一溢流口，第一溢流口连通于补浆组件，补浆组件开设有第二溢流口，第二溢流口连通于选择性沉淀组件，选择性沉淀组件连通于溶浆组件，即溶浆组件、补浆组件和选择性沉淀组件形成循环连接；且选择性沉淀组件不局限于仅用于进行选择性沉淀，还可用于溶浆或补浆，同样地，溶浆组件不局限于仅用于溶浆，还可用于进行选择性沉淀或补浆，同样地，补浆组件不局限于仅用于补浆，还可用于进行选择性沉淀或溶浆；因此，当浸出机构出现故障或其它原因，使得选择性沉淀组件中的浆料没有充分溶解时，可将本轮的浆料堆积较多的选择性沉淀组件作为下一轮的溶浆组件，本轮的溶浆组件作为下一轮生产的补浆组件，本轮的补浆组件作为下一轮生产的选择性沉淀组件，然后经过本轮的补浆组件在下一轮生产中处理得到的选择性浸出液流向中转组件，无需转移浆料，也无需移动浸出机构的位置，即可使本轮堆积的未充分溶解的浆料在下一轮中重新得以溶解，进而提高对粗制氢氧化钴浆料的充分利用，且减少了还需要人工清理并转移浆料而造成人工劳动强度较大的问题，且节约了清理及转移浆料的时间，进而提高了生产效率。
在其中一个实施例中，选择性沉淀组件连通于溶浆组件，溶浆组件连通于中转组件。可以理解，溶浆组件开设有第一溢流口，第一溢流口连通于补浆组件，补浆组件开设有第二溢流口，第二溢流口连通于选择性沉淀组件，选择性沉淀组件连通于溶浆组件，即溶浆组件、补浆组件和选择性沉淀组件形成循环连接；且选择性沉淀组件不局限于仅用于进行选择性沉淀，还可用于溶浆或补浆，同样地，溶浆组件不局限于仅用于溶浆，还可用于进行选择性沉淀或补浆，同样地，补浆组件不局限于仅用于补浆，还可用于进行选择性沉淀或溶浆；因此，当浸出机构出现故障或其它原因，使得补浆组件中的浆料有较多未溶解时，可将本轮的浆料堆积较多的补浆组件作为下一轮的溶浆组件，本轮的溶浆组件作为下一轮的选择性沉淀组件，本轮的选择性沉淀组件作为下一轮的补浆组件，然后本轮的补浆组件在下一轮生产中处理得到的选择性浸出液流向中转组件，无需转移浆料，也无需移动浸出机构的位置，即可使本轮堆积的未充分溶解的浆料在下一轮中重新得以溶解，进而提高对粗制氢氧化钴浆料的充分利用，且减少了还需要人工清理并转移浆料而造成人工劳动强度较大的问题，且节约了清理及转移浆料的时间，进而提高了生产效率。
在其中一个实施例中，第三溢流口连通于一次溶浆釜，一次溶浆釜、中间溶浆釜、二次溶浆釜、补浆组件、第一水解沉淀釜和第二水解沉淀釜分别连通于中转组件。可以理解，一次溶浆釜，一次溶浆釜、二次溶浆釜、补浆组件、第一水解沉淀釜和第二水解沉淀釜形成循环连接；且选择性沉淀组件不局限于仅用于进行选择性沉淀，还可用于溶浆或补浆，同样地，溶浆组件不局限于仅用于溶浆，还可用于进行选择性沉淀或补浆，同样地，补浆组件不局限于仅用于补浆，还可用于进行选择性沉淀或溶浆；因此，当浸出机构出现故障或其它原因，例如第二水解沉淀釜内中堆积有较多未溶解的粗制氢氧化钴浆料时，无需转移浆料，也无需移动浸出机构的位置，使本轮的第二水解沉淀釜作为下一轮的一次溶浆釜，本轮的一次溶浆釜作为下一轮的中间溶浆釜，本轮的中间溶浆釜作为下一轮的二次溶浆釜，本轮的二次溶浆釜作为下一轮的补浆组件，本轮的补浆组件作为下一轮的第一水解沉淀釜，本轮的第一水解沉淀釜作为下一轮的第二水解沉淀釜，本轮的第一水解沉淀釜在下一轮生产中得到的选择性浸出液流向中转组件，即可使本轮堆积的未充分溶解的浆料在下一轮中重新得以溶解，进而提高对粗制氢氧化钴浆料的充分利用，且减少了还需要人工清理并转移浆料而造成人工劳动强度较大的问题，且节约了清理及转移浆料的时间，进而提高了生产效率。
传统的浸出工艺在一个反应釜内进行，当生产中出现问题时，难以分析是在哪一步出现了问题，且分析了也难以及时对应调整；且传统的浸出工艺还需要进行还原反应和氧化反应，即工艺较为复杂，使得反应釜的结构也较复杂，且占地面积较大。为了在使生产问题易于分析及调整的前提下，简化粗制氢氧化钴的连续选择性浸出装置的结构，在其中一个实施例中，浸出机构包括依次连通的一次溶浆釜、中间溶浆釜、二次溶浆釜、补浆组件、第一水解沉淀釜和第二水解沉淀釜。可以理解，本文采用的粗制氢氧化钴为钴中间品，其包括34.7％Co、1.75％Mn、1.83％Cu、0.08％Ni、0.88％Ca、5.3％Mg、1.22％Fe、0.23％Al和15％水分，因此工艺中的每一步骤得到的沉淀物的量是可预计的，且可根据沉淀物的量、颜色及形态观察每一步骤的生产是否出现问题，且在发现工艺中的环节出现问题时迅速对应调整和改进，确保生产正常进行，进而确保生产效率，且提高了浸出液的质量和后续的钴产品的质量；且观察到在工艺中的某个环节出现问题之后，可以将此步骤之前的中间品进行保存，并等待调整和改进后继续投入生产；而对于出现了问题的环节及之后的环节，针对性地进行调整，无法调整的中间品舍弃掉，避免因中间品不合格而造成后续的钴产品不合格而 造成更大损失的问题。
在其中一个实施例中，粗制氢氧化钴连续选择性浸出装置还包括压滤机构，压滤机构连通于中转机构，压滤机构用于连通于浸出渣制浆装置。
在其中一个实施例中，浸出机构还包括加热组件，加热组件的作用端作用于溶浆组件。
在其中一个实施例中，加热组件为蒸汽加热组件，蒸汽加热组件设有蒸汽输出端，蒸汽输出端连通于溶浆组件。
在其中一个实施例中，溶浆组件设置有第一pH测量组件。
在其中一个实施例中，补浆组件设置有第二pH测量组件。
在其中一个实施例中，选择性沉淀组件设置有第三pH测量组件。
在其中一个实施例中，浸出机构至少还包括有第一搅拌组件，第一搅拌组件的搅拌端设置于溶浆组件内。
在其中一个实施例中，溶浆组件形成有相连通的进浆槽和进浆口，进浆槽连通于第一溢流口。
在其中一个实施例中，浸出机构还包括第一供浆组件，第一供浆组件连通于溶浆组件。
在其中一个实施例中，第一供浆组件包括第一pH仪表、第一流速监测器、第一活动隔板和第一供浆槽体，第一供浆槽体连通于溶浆组件，第一活动隔板设置于第一供浆槽体与溶浆组件的连通处，第一pH仪表的探测端设置于溶浆组件内，第一流速监测器的作用端设置于第一溢流口。可以理解，第一pH仪表用于对溶浆组件加入酸性溶液，并监测溶浆组件内混合料体的pH，根据pH调整酸性溶液的加入速度，第一流速监测器用于监测混合料体的流速，根据流速大小改变第一活动隔板的开度，进而改变粗制氢氧化钴浆料的流速，确保了粗制氢氧化钴浆料在酸性溶液中的浸出效果，即确保了二价钴离子的浸出率。
在其中一个实施例中，第一供浆组件用于将粗制氢氧化钴浆料的流量设置为1m3/h～3m3/h。
在其中一个实施例中，补浆组件开设有相连通的盛浆槽和补料口，盛浆槽分别连通于第一溢流口及选择性沉淀组件。
在其中一个实施例中，浸出机构还包括第二供浆组件，第二供浆组件连通于补浆组件。
在其中一个实施例中，第二供浆组件包括第二pH仪表、第二流速监测器、第二活动隔板和第二供浆槽体，第二供浆槽体连通于溶浆组件，第二活动隔板设置于第二供浆槽体与溶浆组件的连通处，第二pH仪表的探测端设置于溶浆组件内，第二流速监测器的作用端设置于第二溢流口。
本文还提供一种粗制氢氧化钴二段浸出设备，包括一段浸出液存储机构、浸出渣制浆装置和上述任一实施例的粗制氢氧化钴连续选择性浸出装置，压滤机构分别连通于一段浸出液存储机构和浸出渣制浆装置。
上述的粗制氢氧化钴二段浸出设备，将收集的沉淀物批量集中进行浸出，对沉淀的批量处理节省了能源，并减少了浸出渣制浆装置的使用，进而减少了浸出渣制浆装置的损坏和维修，进而提高浸出渣制浆装置的使用寿命，且较好地提高了生产效率；且由于避免了传统的粗制氢氧化钴选择性浸出工艺将二价钴浸出后转移至中转槽待除铁，需要等待三价钴还原浸出液一并进行除铁的问题，进而减少了设备占而不用的现象，即确保了设备的使用率，进而缩小了设备的占地面积。
在其中一个实施例中，浸出渣制浆装置包括相连通的二段浸出机构和二段浸出液存储机构，二段浸出机构连通于压滤机构。可以理解，二段还原浸出液存储于二段浸出液存储机构，即与一段浸出液分别储存于不同的存储机构。
本文还提供一种钴产品生产系统，包括一段浸出液处理设备、二段浸出液处理设备和上述任一实施例的粗制氢氧化钴二段浸出设备，一段液处理设备连通于一段浸出液存储机构，二段浸出液处理设备连通于二段浸出液存储设备。
上述的钴产品生产系统，一段浸出液处理设备用于处理一段浸出液，二段浸出液处理设备用于处理二段还原浸出液，即一段浸出液和二段还原浸出液分别处理，确保了一段浸出液得到的钴产品的质量，以及简化了处理一段浸出液的工艺，提高了生产便利性和生产效率。
以下例举一些具体实施例，若提到％，均表示按重量百分比计。需注意的是，下列实施例并没有穷举所有可能的情况，并且下述实施例中所用的材料如无特殊说明，均可从商业途径得到。
实施例1
粗制氢氧化钴为钴中间品，其包括34.7％Co、1.75％Mn、1.83％Cu、0.08％Ni、0.88％Ca、5.3％Mg、1.22％Fe、0.23％Al和15％水分。
称取1吨的粗制氢氧化钴和3吨的水，进行混合搅拌浆化操作，得到4吨粗制氢氧化钴浆料，将浓硫酸和3.85吨粗制氢氧化钴浆料同时加入，进行混合搅拌操作，然后加热至60℃，以使粗制氢氧化钴浆料与浓硫酸的混合液的pH值为1.0，然后反应1h，得到pH为2.0～2.5的初步浸出液和酸浸渣；
将剩余的0.15吨粗制氢氧化钴浆料逐渐加入到初步浸出液中，得到调节浸出液；然后对调节浸出液进行1h选择性沉淀操作，依次得到第一沉淀物和pH为3.5～4.0的一次选择性浸出液、第二沉淀物和pH为4.0～4.5的二次选择性浸出液、第三沉淀物和pH为5.0～5.5的选择性浸出液；
采用压滤机进行固液分离操作，分别得到一段浸出液及0.19吨的固态物；
然后采用P204对一段浸出液进行1次萃取处理，萃取处理时间为30min，得到P204萃余液；
然后采用P507对P204萃余液进行1次萃取处理，每次萃取处理时间为20min，得到含钴有机相和P507萃余液；
然后再使用硫酸对含钴有机相进行反萃，得到硫酸钴溶液；
对硫酸钴溶液进行蒸发结晶操作，得到硫酸钴晶体；
对固态物进行收集并等待批量进行二段还原浸出处理。
实施例2
粗制氢氧化钴为钴中间品，其包括34.7％Co、1.75％Mn、1.83％Cu、0.08％Ni、0.88％Ca、5.3％Mg、1.22％Fe、0.23％Al和15％水分。
称取1吨的粗制氢氧化钴和4吨的水，进行混合搅拌浆化操作，得到5吨粗制氢氧化钴浆料，将浓硫酸和4.84吨粗制氢氧化钴浆料同时加入，进行混合搅拌操作，然后加热至65℃，以使粗制氢氧化钴浆料与浓硫酸的混合液的pH值为1.3，然后反应1h，得到pH为2.0～2.5的初步浸出液和酸浸渣；
将0.16吨粗制氢氧化钴浆料逐渐加入到初步浸出液中，得到调节浸出液；然后对调节浸出液进行1h选择性沉淀操作，依次得到第一沉淀物和pH为3.5～4.0的一次选择性浸出液、第二沉淀物和pH为4.0～4.5的二次选择性浸出液、第三沉淀物和pH为5.0～5.5的选择性浸出液；
采用压滤机进行固液分离操作，分别得到一段浸出液及0.21吨的固态物；
然后采用P204对一段浸出液进行1次萃取处理，萃取处理时间为30min，得到P204萃余液；
然后采用P507对P204萃余液进行1次萃取处理，每次萃取处理时间为20min，得到含钴有机相和P507萃余液；
然后再使用硫酸对含钴有机相进行反萃，得到硫酸钴溶液；
对硫酸钴溶液进行蒸发结晶操作，得到硫酸钴晶体；
对固态物进行收集并等待批量进行二段还原浸出处理。
实施例3
粗制氢氧化钴为钴中间品，其包括34.7％Co、1.75％Mn、1.83％Cu、0.08％Ni、0.88％Ca、5.3％Mg、1.22％Fe、0.23％Al和15％水分。
称取1吨的粗制氢氧化钴和2.5吨的水，进行混合搅拌浆化操作，得到3.5吨粗制氢氧化钴浆料，将3.39吨粗制氢氧化钴浆料和浓硫酸同时加入，进行混合搅拌操作，然后加热至70℃，以使粗制氢氧化钴浆料与浓硫酸的混合液的pH值为1.5，然后反应1h，得到pH为2.0～2.5的初步浸出液和酸浸渣；
将0.11吨粗制氢氧化钴浆料逐渐加入到初步浸出液中，得到调节浸出液；然后对调节浸出液进行1h选择性沉淀操作，依次得到第一沉淀物和pH为3.5～4.0的一次选择性浸出液、第二沉淀物和pH为4.0～4.5的二次选择性浸出液、第三沉淀物和pH为5.0～5.5的选择性浸出液；
采用压滤机进行固液分离操作，分别得到一段浸出液及0.18吨的酸浸渣；
然后采用P204对一段浸出液进行1次萃取处理，萃取处理时间为30min，得到P204萃余液；
然后采用P507对P204萃余液进行1次萃取处理，每次萃取处理时间为20min，得到含钴有机相和P507萃余液；
然后再使用硫酸对含钴有机相进行反萃，得到硫酸钴溶液；
对硫酸钴溶液进行蒸发结晶操作，得到硫酸钴晶体；
对固态物进行收集并等待批量进行二段还原浸出处理。
实施例4
粗制氢氧化钴为钴中间品，其包括34.7％Co、1.75％Mn、1.83％Cu、0.08％Ni、0.88％Ca、5.3％Mg、1.22％Fe、0.23％Al和15％水分。
称取1吨的粗制氢氧化钴和3吨的水，进行混合搅拌浆化操作，得到4吨粗制氢氧化钴浆料，将浓硫酸和3.87吨粗制氢氧化钴浆料同时加入，进行混合搅拌操作，然后加热至70℃，以使粗制氢氧化钴浆料与浓硫酸的混合液的pH值为1.0，然后反应1h，得到pH为2.0～2.5的初步浸出液和酸浸渣；
将剩余的0.13吨粗制氢氧化钴浆料逐渐加入到初步浸出液中，得到调节浸出液；然后对调节浸出液进行1h选择性沉淀操作，依次得到第一沉淀物和pH为3.2～3.4的一次选择性浸出液、第二沉淀物和pH为4.7的二次选择性浸出液、第三沉淀物和pH为5.0～5.5的选择性浸出液；
采用压滤机进行固液分离分离操作，分别得到一段浸出液及0.16吨的酸浸渣、27.82kg第一沉淀物、7.06kg第二沉淀物和13.86kg第三沉淀物；
然后采用P204对一段浸出液进行1次萃取处理，萃取处理时间为30min，得到P204萃余液；
然后采用P507对P204萃余液进行1次萃取处理，每次萃取处理时间为20min，得到含钴有机相和P507萃余液；
然后再使用硫酸对含钴有机相进行反萃，得到硫酸钴溶液；
对硫酸钴溶液进行蒸发结晶操作，得到硫酸钴晶体；
对酸浸渣进行收集并等待批量进行二段还原浸出处理。
对比例1
粗制氢氧化钴为钴中间品，其包括34.7％Co、1.75％Mn、1.83％Cu、0.08％Ni、0.88％Ca、5.3％Mg、1.22％Fe、0.23％Al和15％水分。
1)称取1吨的粗制氢氧化钴和3吨的水，进行混合搅拌浆化操作，加热至60℃～70℃，得到粗制氢氧化钴浆料，用将浓硫酸逐渐加入到粗制氢氧化钴浆料中，得到pH为0.45～0.5的粗制氢氧化钴浆料与浓硫酸的反应混合液，搅拌1h进行过滤；得到一段浸出液和0.20吨的酸浸渣；一段浸出液直接进中转槽待除铁；按0.20吨的酸浸渣和2倍的水进行二次浆化操作；
2)二段还原浸出：酸浸渣二次浆化后升温至50℃～60℃，加入焦亚硫酸钠，并维持料浆pH为1.0～1.5，直至还原电位低于240mV；
预氧化：经步骤2)处理后加入二氧化锰矿，将Fe2+氧化成Fe3+，当浆料中的Fe2+含量低于0.05g/L，得到的二段还原浸出液转入中转槽待除铁，得到一段浸出液和二段还原浸出液的混合液；
对混合液进行选择性沉淀处理，得到浸出液和沉淀物；且对比例1的四价锰离子的浓度高于实施例1～4的浓度；
然后采用P204对浸出液进行1次萃取处理，萃取处理时间为30min，得到P204萃余液；
然后采用P507对P204萃余液进行2次萃取处理，每次萃取处理时间为30min，得到含钴有机相和P507萃余液；
然后再使用硫酸对含钴有机相进行反萃，得到硫酸钴溶液；
对硫酸钴溶液进行蒸发结晶操作，得到硫酸钴晶体；
对P507萃余液中的钠离子进行处理。
对比例2
粗制氢氧化钴为钴中间品，其包括34.7％Co、1.75％Mn、1.83％Cu、0.08％Ni、0.88％Ca、5.3％Mg、1.22％Fe、0.23％Al和15％水分。
1)称取1吨的粗制氢氧化钴和3吨的水，进行混合搅拌浆化操作，加热至60℃～70℃，得到粗制氢氧化钴浆料，用将浓硫酸逐渐加入到粗制氢氧化钴浆料中，得到pH为0.45～0.5的粗制氢氧化钴浆料与浓硫酸的反应混合液，搅拌1h进行过滤；得到一段浸出液和0.20吨的酸浸渣；一段浸出液直接进中转槽待除铁；按0.20吨的酸浸渣和2倍的水进行二次浆化操作；
2)二段还原浸出：酸浸渣二次浆化后升温至50℃～60℃，加入二氧化硫，并维持料浆pH为1.0～1.5，直至还原电位低于240mV；
预氧化：经步骤2)处理后加入氯酸钠，将Fe2+氧化成Fe3+，当浆料中的Fe2+含量低于0.05g/L，得到的二段还原浸出液转入中转槽待除铁，得到一段浸出液和二段还原浸出液的混合液；
对混合液进行选择性沉淀处理，得到浸出液和沉淀物；且对比例1的四价锰离子的浓度高于实施例1～4的浓度；
然后采用P204对浸出液进行1次萃取处理，萃取处理时间为30min，得到P204萃余液；
然后采用P507对P204萃余液进行2次萃取处理，每次萃取处理时间为30min，得到含钴有机相和P507萃余液；
然后再使用硫酸对含钴有机相进行反萃，得到硫酸钴溶液；
对硫酸钴溶液进行蒸发结晶操作，得到硫酸钴晶体；
对P507萃余液中的钠离子进行处理。
以下分别测量实施例1至4的一段浸出液和对比例1至2中的浸出液中铁离子、铝离子、铜离子、四价锰离子、镍离子、钙离子、镁离子和钠离子的含量，结果如下表1所示：
表1：金属离子含量
由于实施例1至4及对比例1至2中加入的粗制氢氧化钴的量相同，但是加入的水量不同，因此以实施例1中加入3吨水的水量为标准，对实施例1至4及对比例1至2中的金属离子含量进行换算，得到表2。
表2：金属离子含量
以下分别测量实施例1至4得到的一段浸出钴产品中的钴、铁、铝、铜、锰、镍、钙、镁和钠的含量，以及对比例1至2得到的钴产品中的钴、铁、铝、铜、锰、镍、钙、镁和钠的含量，结果如下表3所示：
表3：钴产品中金属离子含量和硫的含量

1)由表2可以看出，实施例1至4的选择性浸出液中，四价锰离子的含量显著低于对比例1至2，实施例1至4的钠离子的含量等于0，对比例1的钠离子和四价锰离子的含量显著较高于实施例1至4，对比例2的钠离子的含量显著较高于实施例1至4。
2)由1)可知，实施例1至4的一段浸出液中，钠离子的含量等于0，因此，在后续的萃取处理中，萃取处理次数及每次萃取处理时间均小于对比例1至2，进而提高了生产效率，且节约了萃取剂的使用，且后续得到的P507萃余液不含钠离子，无需对P507萃余液进行去除钠离子的处理；
同样地，实施例1至4的一段浸出液中，四价锰离子的含量显著低于对比例1，因此，在后续的萃取处理中，萃取处理次数及每次萃取处理时间均小于对比例1至2，进而提高了生产效率，且节约了萃取剂的使用。
3)由表3可以看出，实施例1至4的一段浸出钴产品，符合硫酸钴优等品的国家标准；对比例1至2的钴产品，符合硫酸钴一等品的国家标准，即实施例1至4的一段浸出钴产品的品质显著高于对比例1至2的钴产品。
4)用100L稀盐酸对实施例4得到的27.82kg第一沉淀物进行溶解得到第一溶解液和5.27kg酸浸渣，并测定第一溶解液中铁离子的浓度为2.085mol/L，可知第一沉淀物中氢氧化铁的质量占比为80.2％，且可溶物中氢氧化铁的占比为98.9％，可知第一沉淀物的回收价值较高；
用100L稀盐酸对实施例4得到的7.06kg第二沉淀物进行溶解得到第二溶解液和0.99kg酸浸渣，并测定第二溶解液中铝离子的浓度为0.771mol/L，可知第二沉淀物中氢氧化铝的质量占比为85.1％，且可溶物中氢氧化铝的占比为99.01％，可知第二沉淀物的回收价值较高；
用100L稀盐酸对实施例4得到的13.86kg第三沉淀物进行溶解得到第三溶解液和0.04kg酸浸渣，并测定第三溶解液中铜离子的浓度为1.413mol/L，可知第三沉淀物中氢氧化铜的质量占比为99.42％，且可溶物中氢氧化铝的占比为99.71％，可知第三沉淀物的回收价值较高。
与现有技术相比，本文至少具有以下优点：
1)本文的粗制氢氧化钴连续选择性浸出工艺，酸性溶液将粗制氢氧化钴浆料中的二价钴离子、三价铁离子、铝离子和铜离子和杂质离子浸出，以得到初步浸出液，然后补加的粗制氢氧化钴浆料逐渐溶解于酸性溶液，以逐渐提高pH值，直至pH值处于使二价钴离子不发生沉淀且使大部分杂质离子沉淀的范围，使二价钴离子以离子形态存在且大部分杂质存在于沉淀中，进而使二价钴离子与大部分杂质固液分离，进而实现粗制氢氧化钴的选择性浸出。
2)本文的粗制氢氧化钴连续选择性浸出工艺，一段浸出液不仅避免了因传统的粗制氢氧化钴选择性浸出工艺在浸出液中加入还原剂而引入钠离子、加入氧化剂而引入钠离子或四价锰离子以及加入碱性辅料而引入钠离子或钾离子的问题，进而简化了后续对于钠离子、四价锰离子和钾离子的处理工艺，进而提升生产效率，且降低了钠离子、四价锰离子和钾离子的浓度，确保了后续生产得到的钴产品的品质。

Claims (41)

  1. 一种粗制氢氧化钴连续选择性浸出工艺，其特征在于，包括如下步骤：
    制备粗制氢氧化钴浆料；
    对一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液；
    将另一部分所述粗制氢氧化钴浆料加入到所述初步浸出液进行混合，得到调节浸出液；
    对所述调节浸出液进行选择性沉淀操作，以形成有沉淀物及选择性浸出液；
    对所述沉淀物与选择性浸出液进行固液分离操作，分别得到一段浸出液及酸浸渣。
  2. 根据权利要求1所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述制备粗制氢氧化钴浆料的步骤具体为：将粗制氢氧化钴与水按质量比1:(2.5～4)制成所述粗制氢氧化钴浆料。
  3. 根据权利要求1所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述将粗制氢氧化钴与水按质量比1:(2.5～4)制成所述粗制氢氧化钴浆料的步骤具体为：在搅拌下，将粗制氢氧化钴与水按质量比1:(2.5～4)制成所述粗制氢氧化钴浆料。
  4. 根据权利要求3所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述酸性溶液为硫酸或盐酸中的至少一种。
  5. 根据权利要求4所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述初步浸出液的pH为2.0～2.5。
  6. 根据权利要求1所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，在加热条件下，对一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液；及/或，
    在加热条件下，将另一部分所述粗制氢氧化钴浆料加入到所述初步浸出液进行混合，得到调节浸出液。
  7. 根据权利要求6所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，在60℃～70℃的条件下，对一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液；及/或，
    在60℃～70℃的条件下，将另一部分所述粗制氢氧化钴浆料加入到所述初步浸出液进行混合，得到调节浸出液。
  8. 根据权利要求1所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述将一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液的步骤的时间为之和为0.8h～1.2h。
  9. 根据权利要求8所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述将一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液的步骤的时间为之和为1h。
  10. 根据权利要求1所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述将一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作，直至所述粗制氢氧化钴浆料溶解于所述酸性溶液，得到初步浸出液的步骤具体为：
    对一部分所述粗制氢氧化钴浆料和酸性溶液进行至少两次混合搅拌浸出操作，得到所述初步浸出液。
  11. 根据权利要求10所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述对一部分所述粗制氢氧化钴浆料和酸性溶液进行至少两次混合搅拌浸出操作，得到所述初步浸出液的步骤具体为：
    对一部分所述粗制氢氧化钴浆料和酸性溶液进行第一次浸出操作，得到一次浸出液；
    对所述一次浸出液进行第二次浸出操作，得到二次浸出液；
    将二次浸出液进行第三次浸出操作，得到初步浸出液。
  12. 根据权利要求11所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述一次浸出液的pH的pH为1.0～1.5。
  13. 根据权利要求11所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述二次浸出液的pH为1.5～2.0。
  14. 根据权利要求11所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述初步浸出液的pH为2.0～2.5。
  15. 根据权利要求1所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述将另一部分所述粗制氢氧化钴浆料加入到所述初步浸出液进行混合的时间与所述对所述调节浸出液进行选择性沉淀操作的时间之和为0.8h～1.2h。
  16. 根据权利要求1所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述对所述调节浸出液进行选择性沉淀操作的步骤具体为：
    对所述调节浸出液进行至少一次选择性沉淀操作，以形成有沉淀物及选择性浸出液。
  17. 根据权利要求1所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述对所述调节浸出液进行选择性沉淀操作的步骤包括：
    对调节浸出液进行第一次选择性沉淀操作，得到一次选择性浸出液及第一沉淀物；
    对所述一次选择性浸出液进行第二次选择性沉淀操作，得到二次选择性浸出液及第二沉淀物；
    对所述二次选择性浸出液进行第三次选择性沉淀操作，得到选择性浸出液及第三沉淀物。
  18. 根据权利要求17所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述一次选择性浸出液的pH为3.5～4.0；及/或，
    所述二次选择性浸出液的pH为4.0～4.5；及/或，
    所述选择性浸出液的pH为5.0～5.5。
  19. 根据权利要求17所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述一次选择性浸出液的pH为3.2～3.4；及/或，
    所述二次选择性浸出液的pH为4.7；及/或，
    所述选择性浸出液的pH为5.0～6.7。
  20. 根据权利要求17所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述对一部分所述粗制氢氧化钴浆料和酸性溶液进行混合操作的步骤具体为：
    同时加入一部分所述粗制氢氧化钴浆料和酸性溶液并进行混合操作。
  21. 根据权利要求1所述的粗制氢氧化钴连续选择性浸出工艺，其特征在于，所述一部分所述粗制氢氧化钴浆料与所述酸性溶液的体积比为14～16。
  22. 一种钴产品生产工艺，其特征在于，包括如下步骤：
    采用权利要求1至22所述的粗制氢氧化钴连续选择性浸出工艺得到的所述一段浸出液；对所述一段浸出液进行萃取处理；
    对经过所述萃取处理的所述一段浸出液进行加工处理，得到一段浸出钴产品。
  23. 一种粗制氢氧化钴的连续选择性浸出装置，其特征在于，采用权利要求1至23任一项所述的粗制氢氧化钴连续选择性浸出工艺进行浸出操作，所述粗制氢氧化钴连续选择性浸出装置包括：
    浸出机构，所述浸出机构至少包括溶浆组件、补浆组件和选择性沉淀组件，所述溶浆组件开设有所述第一溢流口，所述第一溢流口连通于所述补浆组件，所述补浆组件开设有所述第二溢流口，所述第二溢流口连通于所述选择性沉淀组件，所述选择性沉淀组件开设有所述第三溢流口；
    中转机构，所述中转机构连通于所述第三溢流口，所述中转机构用于分别连通于一级浸出液存储机构和浸出渣制浆装置。
  24. 根据权利要求23所述的粗制氢氧化钴的连续选择性浸出装置，其特征在于，所述选择性沉淀组件连通于所述溶浆组件。
  25. 根据权利要求24所述的粗制氢氧化钴的连续选择性浸出装置，其特征在于，所述溶浆组件连通于所述中转组件；及/或，
    所述补浆组件连通于所述中转组件。
  26. 根据权利要求23所述的粗制氢氧化钴的连续选择性浸出装置，其特征在于，所述溶浆组件至少包括相连通的一次溶浆釜和二次溶浆釜，所述第一溢流口形成于所述二次溶浆釜。
  27. 根据权利要求26所述的粗制氢氧化钴的连续选择性浸出装置，其特征在于，所述溶浆组件还包括中间溶浆釜，所述中间溶浆釜分别连通于所述一次溶浆釜和所述二次溶浆釜。
  28. 根据权利要求23所述的粗制氢氧化钴的连续选择性浸出装置，其特征在于，所述粗制氢氧化钴连续选择性浸出装置还包括压滤机构，所述压滤机构连通于所述中转机构，所述压滤机构用于连通于所述浸出渣制浆装置。
  29. 根据权利要求23所述的粗制氢氧化钴的连续选择性浸出装置，其特征在于，所述选择性沉淀组件至少包括相连通的第一水解沉淀釜和第二水解沉淀釜，所述第三溢流口形成于所述第二水解沉淀釜。
  30. 根据权利要求23所述的粗制氢氧化钴的连续选择性浸出装置，其特征在于，所述浸出机构还包括加热组件，所述加热组件的作用端作用于所述溶浆组件。
  31. 根据权利要求30所述的粗制氢氧化钴连续选择性浸出装置，其特征在于，所述加热组件为蒸汽加热组件，所述蒸汽加热组件设有蒸汽输出端，所述蒸汽输出端连通于所述溶浆组件。
  32. 根据权利要求23所述的粗制氢氧化钴连续选择性浸出装置，其特征在于，所述溶浆组件设置有第一pH测量组件；及/或，
    所述补浆组件设置有第二pH测量组件；及/或，
    所述选择性沉淀组件设置有第三pH测量组件。
  33. 根据权利要求23所述的粗制氢氧化钴连续选择性浸出装置，其特征在于，所述浸出机构至少还包括有第一搅拌组件，所述第一搅拌组件的搅拌端设置于所述溶浆组件内；及/或，
    所述溶浆组件形成有相连通的进浆槽和进浆口，所述进浆槽连通于所述第一溢流口。
  34. 根据权利要求23所述的粗制氢氧化钴连续选择性浸出装置，其特征在于，所述浸出机构还包括第一供浆组件，所述第一供浆组件连通于所述溶浆组件。
  35. 根据权利要求23所述的粗制氢氧化钴连续选择性浸出装置，其特征在于，所述第一供浆组件包括第一pH仪表、第一流速监测器、第一活动隔板和第一供浆槽体，所述第一供浆槽体连通于所述溶浆组件，所述第一活动隔板设置于所述第一供浆槽体与所述溶浆组件的连通处，所述第一pH仪表的探测端设置于所述溶浆组件内，所述第一流速监测器的作用端设置于所述第一溢流口；及/或，
    所述第一供浆组件用于将所述粗制氢氧化钴浆料的流量设置为1m3/h～3m3/h。
  36. 根据权利要求23所述的粗制氢氧化钴连续选择性浸出装置，其特征在于，所述补浆组件开设有相连通的盛浆槽和补料口，所述盛浆槽分别连通于所述第一溢流口及所述选择性沉淀组件。
  37. 根据权利要求23所述的粗制氢氧化钴连续选择性浸出装置，其特征在于，所述浸出机构还包括第二供浆组件，所述第二供浆组件连通于所述补浆组件。
  38. 根据权利要求37所述的粗制氢氧化钴连续选择性浸出装置，其特征在于，所述第二供浆组件包括第二pH仪表、第二流速监测器、第二活动隔板和第二供浆槽体，所述第二供浆槽体连通于所述溶浆组件，所述第二活动隔板设置于所述第二供浆槽体与所述溶浆组件的连通处，所述第二pH仪表的探测端设置于所述溶浆组件内，所述第二流速监测器的作用端设置于所述第二溢流口。
  39. 一种粗制氢氧化钴二段浸出设备，其特征在于，包括一段浸出液存储机构、浸出渣制浆装置和权利要求23～38中任一项所述的粗制氢氧化钴连续选择性浸出装置，所述压滤机构分别连通于所述一段浸出液存储机构和所述浸出渣制浆装置。
  40. 根据权利要求39所述的粗制氢氧化钴二段浸出设备，其特征在于，所述浸出渣制浆装置包括相连通的二段浸出机构和二段浸出液存储机构，所述二段浸出机构连通于所述压滤机构。
  41. 一种钴产品生产系统，其特征在于，包括一段浸出液处理设备、二段浸出液处理设备和权利要求39～40中任一项所述的粗制氢氧化钴二段浸出设备，所述一段液处理设备连通于所述一段浸出液存储机构，所述二段浸出液处理设备连通于所述二段浸出液存储设备。
PCT/CN2023/096095 2023-05-24 2023-05-24 粗制氢氧化钴连续选择性浸出工艺、浸出装置及二段浸出设备、钴产品生产工艺及生产系统 Ceased WO2024239283A1 (zh)

Priority Applications (2)

Application Number Priority Date Filing Date Title
CN202380009229.9A CN116964232A (zh) 2023-05-24 2023-05-24 粗制氢氧化钴连续选择性浸出工艺、浸出装置及二段浸出设备、钴产品生产工艺及生产系统
PCT/CN2023/096095 WO2024239283A1 (zh) 2023-05-24 2023-05-24 粗制氢氧化钴连续选择性浸出工艺、浸出装置及二段浸出设备、钴产品生产工艺及生产系统

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/CN2023/096095 WO2024239283A1 (zh) 2023-05-24 2023-05-24 粗制氢氧化钴连续选择性浸出工艺、浸出装置及二段浸出设备、钴产品生产工艺及生产系统

Publications (1)

Publication Number Publication Date
WO2024239283A1 true WO2024239283A1 (zh) 2024-11-28

Family

ID=88447785

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2023/096095 Ceased WO2024239283A1 (zh) 2023-05-24 2023-05-24 粗制氢氧化钴连续选择性浸出工艺、浸出装置及二段浸出设备、钴产品生产工艺及生产系统

Country Status (2)

Country Link
CN (1) CN116964232A (zh)
WO (1) WO2024239283A1 (zh)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN121496170A (zh) * 2026-01-14 2026-02-10 中国恩菲工程技术有限公司 镍钴钪富集与分离的方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20110135547A1 (en) * 2009-02-04 2011-06-09 Sumitomo Metal Mining Co., Ltd. Method for recovering nickel from sulfuric acid aqueous solution
US20140262817A1 (en) * 2013-03-13 2014-09-18 Freeport-Mcmoran Corporation Systems and methods for selective proximity cobalt recovery
CN111910075A (zh) * 2020-08-12 2020-11-10 矿冶科技集团有限公司 一种粗制氢氧化镍钴两段浸出镍钴的方法
CN112359225A (zh) * 2020-11-12 2021-02-12 格林美（江苏）钴业股份有限公司 一种粗制氢氧化钴矿的选择性浸出工艺
CN113474069A (zh) * 2019-03-26 2021-10-01 住友金属矿山株式会社 从含镍和钴的氢氧化物制造含镍和钴的溶液的制造方法
CN114427037A (zh) * 2022-01-06 2022-05-03 中国恩菲工程技术有限公司 从低浓度镍钴溶液中连续化富集镍钴的方法
CN115057481A (zh) * 2022-06-09 2022-09-16 云南金浔资源股份有限公司 一种高性能锂离子动力电池使用硫酸钴生产方法

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20110135547A1 (en) * 2009-02-04 2011-06-09 Sumitomo Metal Mining Co., Ltd. Method for recovering nickel from sulfuric acid aqueous solution
US20140262817A1 (en) * 2013-03-13 2014-09-18 Freeport-Mcmoran Corporation Systems and methods for selective proximity cobalt recovery
CN113474069A (zh) * 2019-03-26 2021-10-01 住友金属矿山株式会社 从含镍和钴的氢氧化物制造含镍和钴的溶液的制造方法
CN111910075A (zh) * 2020-08-12 2020-11-10 矿冶科技集团有限公司 一种粗制氢氧化镍钴两段浸出镍钴的方法
CN112359225A (zh) * 2020-11-12 2021-02-12 格林美（江苏）钴业股份有限公司 一种粗制氢氧化钴矿的选择性浸出工艺
CN114427037A (zh) * 2022-01-06 2022-05-03 中国恩菲工程技术有限公司 从低浓度镍钴溶液中连续化富集镍钴的方法
CN115057481A (zh) * 2022-06-09 2022-09-16 云南金浔资源股份有限公司 一种高性能锂离子动力电池使用硫酸钴生产方法

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN121496170A (zh) * 2026-01-14 2026-02-10 中国恩菲工程技术有限公司 镍钴钪富集与分离的方法

Also Published As

Publication number Publication date
CN116964232A (zh) 2023-10-27

Similar Documents

Publication Publication Date Title
JPS60255938A (ja) 亜鉛と鉄とを含有する硫化物の浸出方法
CN107032417A (zh) 高纯度硫酸镍的制造方法
KR20230166088A (ko) 금속의 침전
CN108545706B (zh) 一种含碲废液的处理方法
EP1966401A1 (en) Method for recovering rare metals in a zinc leaching process
CN109797410A (zh) 一种硫化镍可溶阳极镍电解净化两段除杂工艺
WO2024178774A1 (zh) 一种废旧锂离子电池粉的浸出方法
CN102168181A (zh) 卧式加压浸出釜以及使用其的硫化锌精矿浸出方法
CN116463514B (zh) 一种铜冶炼含砷烟尘浸出渣的处理方法
FI64646B (fi) Hydrometallurgiskt foerfarande foer utvinning av vaerdemetaller ur metalliska legeringar
CN105695764A (zh) 一种含铅碱浸液氧化沉淀分离铅的方法
JP2013095988A (ja) 金属の硫化物沈殿方法
CN116287756A (zh) 从铜钴渣中提取铜和钴的方法及系统
CN100552059C (zh) 铟矿中直接浸取铟的方法
CA1110076A (en) Metal leaching from concentrates using nitrogen dioxide in acids
CN116964232A (zh) 粗制氢氧化钴连续选择性浸出工艺、浸出装置及二段浸出设备、钴产品生产工艺及生产系统
Matkarimov et al. Hydrometallurgical processing of copper-smelting dust
CN109809494A (zh) 一种稳定化处理砷碱渣制备臭葱石的固砷方法
Wu et al. Selective extraction of zinc from low-grade zinc oxide ores via NaOH leaching
Wen et al. Options to recover high-purity MnO2 from leach liquors of manganese dust containing Mn3O4 and iron and zinc oxide as minor impurities
JP7751301B2 (ja) 冶金残留物から有益な元素をリーチングするための方法
US6949232B2 (en) Producing cobalt (III) hexammine sulfate from nickel cobalt sulfides
CN115679117A (zh) 一种降低钴原料浸出液除铁尾料含钴的方法
CN222744368U (zh) 一种硫化镍钴渣协同三元电池黑粉回收系统
CA3240794C (en) A method for iron and copper removal from solution using metallic reagents

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 23937957

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE