Patent Application
20240002251
Embodiments of the present invention relates to a method for preparing a cobalt sulfate salt. More particularly, the present invention relates to a method for preparing a cobalt sulfate salt which includes a purification process.
Secondary batteries which can be charged and discharged repeatedly have been developed and employed as power source for mobile electronic-communication devices including camcorders, mobile phones, laptop computers, and the like and for vehicles including hybrid vehicles and electric vehicles. Lithium secondary batteries in particular are being actively developed due to their high operational voltage and energy density per unit weight, high charging rate, and compact dimensions.
Lithium metal oxide is often used as a cathode active material for lithium secondary batteries which may also use other metals such as cobalt, and transition metals such as nickel, manganese, and the like.
As the above-mentioned high-cost valuable metals are used for the cathode active material, 20% or more of a production cost is required for manufacturing the cathode material. Additionally, as environment protection issues have recently been highlighted, a recycling method of the cathode active material is being researched.
For example, cobalt may be recovered in the form of cobalt sulfate by leaching a waste cathode active material in a strong acid, and a cathode active material may be prepared again using the recovered cobalt sulfate.
However, another transition metal such as manganese may be included as impurities in the recovered cobalt sulfate. Therefore, an improved process for obtaining a high-purity cobalt compound without excessively reducing a cobalt yield is required.
According to an aspect of the present invention, there is provided a method for preparing a cobalt sulfate salt characterized in that it provides improved purity and yield.
According to a first aspect of the present invention, a method for preparing a cobalt sulfate salt is provided. The method includes preparing a feeding solution containing cobalt sulfate and an aqueous solution of sulfuric acid. The feeding solution may be prepared by adding an aqueous solution of sulfuric acid and cobalt wherein the cobalt reacts with the sulfuric acid to form cobalt sulfate and hydrogen gas. A first solution is then produced by subjecting the feeding solution to evaporation crystallization.
According to the evaporation crystallization operation, the feeding solution is concentrated by removing the solvent via evaporation until the cobalt sulfate begins to crystallize and forms first crystals of the cobalt sulfate. The first solution is then filtered together with a first purging of the remaining solvent to obtain the first cobalt sulfate salt. An aqueous solution containing the first cobalt sulfate salt is formed. A second solution is produced by a cooling crystallization of an aqueous solution containing the first cobalt sulfate salt. The aqueous solution containing the first cobalt sulfate salt may be formed by adding water into the recovered cobalt sulfate from the following the first filtration and purging. During the cooling crystallization the cobalt sulfate solute is again crystallized by gradually lowering the temperature causing the cobalt sulfate to come out of solution and form second crystals. The second solution is filtered together with a second purging to produce a second cobalt sulfate salt.
In some embodiments, a temperature of the evaporation crystallization may be from 60 to 80° C.
In some embodiments, a temperature of the cooling crystallization may be from 10 to 20° C.
In some embodiments, a ratio of a removed solution by the first purging may be 5 wt % or less based on a weight of the first solution.
In some embodiments, a ratio of a removed solution by the first purging may be from 1 to 5 wt % based on a weight of the first solution.
In some embodiments, a ratio of a removed solution by the second purging may be from 5 to 20 wt % based on a weight of the second solution.
In some embodiments, a ratio of a removed solution by the second purging may be from 5 to 10 wt % based on a weight of the second solution.
In some embodiments, a ratio of a removed solution from a weight of the second solution by the second purging may be greater than or equal to a ratio of a removed solution from a weight of the first solution by the first purging.
In some embodiments, the feeding solution may further include manganese impurities.
In some embodiments, an amount of manganese impurities removed in the cooling crystallization may be greater than an amount of manganese impurities removed in the evaporation crystallization.
In some embodiments, the first cobalt sulfate salt may include cobalt sulfate monohydrate (CoSO4·H2O), and the second cobalt sulfate salt may include cobalt sulfate heptahydrate (CoSO4·7H2O).
In some embodiments, filtering the first solution together with the first purging or filtering the second solution together with the second purging may include recycling a liquid phase separated by the filtration to the feeding solution.
According to the embodiments as described above, an evaporation crystallization and a cooling crystallization may be sequentially performed on a feeding solution containing cobalt sulfate to obtain a cobalt sulfate salt with high purity.
In various embodiments, a first purging may be performed between the evaporation crystallization and the cooling crystallization to reduce a concentration of a sulfuric acid in the solution, thereby promoting a crystallization of the cobalt sulfate salt. Additionally, a second purging may be performed after the cooling crystallization to reduce an amount of a liquid phase, so that an amount of manganese remaining in the feeding solution may be reduced.
In various embodiments, yield and purity of the recovered cobalt sulfate salt may both be improved by adjusting a purging amount of each of the first purging and the second purging.
Embodiments of the present invention provide a high-purity, high-yield method for preparing a cobalt sulfate salt from a cathode active material of a lithium secondary battery.
However, embodiments of the present invention are not limited to a recovery process from the lithium secondary battery, and may be used in various manufacturing and producing processes involving a purification process of a cobalt sulfate salt.
Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawing. However, the embodiments are merely examples and the present invention is not limited to the specific embodiments.
Referring to
The feeding solution may include cobalt sulfate (CoSO4). In some embodiments, cobalt sulfate may be obtained from a cathode active material of a waste lithium secondary battery or a used lithium secondary battery.
For example, a cathode may be separated from the waste lithium secondary battery to recover the waste cathode. The waste cathode may include a cathode current collector (e.g., aluminum (Al)) and a cathode active material layer, and the cathode active material layer may include, e.g., a nickel-cobalt-manganese (NCM)-based lithium transition metal oxide (e.g., Li(NCM)O2).
An active material solution may be formed by separating the cathode active material layer from the waste cathode to collect an active material mixture, and then treating the active material mixture with sulfuric acid together with a reducing agent such as hydrogen peroxide (H2O2).
In some embodiments, a precipitation using an alkali, a filtration, a centrifugation, a washing, etc., may be further performed to reduce components of the current collector, a conductive material and/or a binder remaining in the active material mixture.
A transition metal extractant may be added to the active material solution, so that, e.g., nickel sulfate (NiSO4), cobalt sulfate (CoSO4) and manganese sulfate (MnSO4) may be generated and collected from Ni, Co, and Mn, respectively. For example, the transition metal extractant may include a phosphoric acid-based compound.
In some embodiments, the transition metal extraction may be performed while increasing a pH stepwise. For example, Mn, Co and Ni may be sequentially extracted while increasing the pH.
For example, manganese sulfate (MnSO4), cobalt sulfate (CoSO4) and nickel sulfate (NiSO4) may be sequentially extracted while stepwise increasing the pH of the active material solution.
The feeding solution including cobalt sulfate collected as described above may be prepared. The feeding solution may include cobalt sulfate contained in an aqueous sulfuric acid solution, and unextracted residual manganese sulfate may be included as an impurity. As will be described below, a crystallization process may be performed to obtain high-purity cobalt sulfate.
For example, an evaporation crystallization of the feeding solution may be performed in, e.g., a process of S20.
The evaporative crystallization may include a vacuum evaporation process. For example, the evaporative crystallization may be performed at a temperature ranging from about 60 to 80° C. As shown in
Thereafter, a first cobalt sulfate salt may be obtained through a first filtration process of the first solution in, e.g., processes of S30 and S40.
The first filtration process may include, e.g., a solid phase-liquid phase separation (solid/liquid separation) process using a filter press or a centrifugal dehydration process. The liquid phase may be at least partially removed and separated by the first filtration process, so that the solid phase of the first cobalt sulfate salt may be extracted.
In some embodiments, a portion of the liquid phase separated by the first filtration process may be recycled to the feeding solution (e.g., a first recycle C1). Accordingly, cobalt that is not recovered through the evaporation crystallization may be circulated again to increase cobalt recovery.
In some embodiments, the first cobalt sulfate salt may include cobalt sulfate monohydrate (CoSO4·H2O).
In example embodiments, a first purging of the first solution may be performed. In some embodiments, as shown in
A predetermined fraction of the first solution introduced into the first filtration process may be removed by the first purging. Accordingly, a concentration of sulfuric acid may become lowered during the first filtration process, so that solid/liquid separation efficiency in the first filtration process may be enhanced. Thus, collection efficiency and yield of the first cobalt sulfate salt may be increased.
In
A cooling crystallization may be further performed on the collected first cobalt sulfate salt in, e.g., a process of S50. For example, an aqueous solution may be formed by adding a distilled water to the first cobalt sulfate salt. A temperature of the distilled water may be from about 60 to 80° C. for a dissolution efficiency. Thereafter, the aqueous solution may be cooled to a temperature of about 10 to 20° C. to obtain a second solution.
Thereafter, a second cobalt sulfate salt may be obtained by a second filtration process for the second solution cooled in, e.g., the processes of S50 and S60.
The second filtration process may include a solid phase-liquid phase separation (solid/liquid separation) process through, e.g., a filter press or a centrifugal dehydration process. The liquid phase of the second solution may be at least partially removed and separated by the second filtration process, so that the solid second cobalt sulfate salt may be extracted.
In some embodiments, the second cobalt sulfate salt may include cobalt sulfate heptahydrate (CoSO4·7H2O).
In some embodiments, a portion of the liquid phase separated by the second filtration process may be recycled back to the feeding solution (e.g., a second recycling C2). Accordingly, cobalt that is not recovered by the cooling crystallization may be circulated again to increase the cobalt recovery.
In various embodiments, a second purging of the second solution may be performed. In some embodiments, as shown in
A predetermined fraction of the second solution introduced into the second filtration process may be removed by the second purging. An amount of manganese that remains and is not separated by the cooling crystallization may be reduced by the second purging. Accordingly, manganese removal and manganese separation efficiency may be increased by the second filtration. Thus, purity of the second cobalt sulfate salt collected in the process of S70 may be increased.
In
In some embodiments, a purging ratio in the second purging may be greater than or equal to a purging ratio in the first purging.
In an embodiment, a ratio of the solution removed in the first purging (the first purging ratio) may be about 5 wt % or less, preferably from about 1 to 5 wt % based on a weight of the first solution. Within the first purging ratio range, a separation efficiency of the first cobalt sulfate salt may be enhanced without excessive degradation of an overall yield.
In an embodiment, a ratio of the solution removed in the second purging (the second purging ratio) may be from about 5 to 20 wt %, preferably from about 5 to 15 wt %, more preferably from about 5 to 10 wt % based on a weight of the second solution. Within the second purging ratio range, manganese impurities may be sufficiently removed while preventing an excessive reduction of the overall yield of the cobalt sulfate salt.
As described above, in an embodiment, the second purging ratio may be adjusted to be greater than or equal to the first purging ratio or greater than the first purging ratio. Accordingly, a removal efficiency of the manganese impurities in the cooling crystallization may be increased while relatively increasing the crystallization efficiency of the entire sulfate salt in the evaporative crystallization.
For example, the liquid phase separation may be performed from the feeding solution through the evaporative crystallization, and the production efficiency of the solid salt may be improved through the first purging. A relatively large amount of the manganese impurities may be included in the first solution formed after the evaporative crystallization, and the manganese impurities may be removed through the cooling crystallization.
Accordingly, an amount of manganese removed through the cooling crystallization may be greater than an amount of manganese removed through the evaporative crystallization. The cooling crystallization may be combined with the second purging, so that the removal efficiency of manganese impurities may be further improved, and a high-purity cobalt sulfate salt may be obtained.
Hereinafter, specific experimental examples are presented to enhance understanding of the present invention, but these are merely examples of the present invention and do not limit the scope of the appended claims. It is apparent to those skilled in the art that various changes and modifications are possible, and these changes and modifications fall within the scope of the appended claims.
3 kg of CoSO4 containing 800 ppm of MnSO4 and 5-6% of H2SO4 was used as a feeding solution.
The feeding solution was evaporated under reduced pressure for 8 hours at 70° C. and a pressure of 200 to 500 mbar to produce a first solution. The first solution was filtered through a vacuum pump while maintaining a first purging ratio of 5 wt % to obtain cobalt sulfate monohydrate (CoSO4·H2O) as a first cobalt sulfate salt.
0.6 kg of distilled water (70° C.) was added to the obtained first cobalt sulfate salt, and cooled at 15° C. for 2 hours to produce a second solution. The second solution was filtered through a vacuum pump while maintaining a second purging ratio of 5 wt % to obtain cobalt sulfate heptahydrate (CoSO4·7H2O) as a second cobalt sulfate salt.
Cobalt sulfate heptahydrate (CoSO4·7H2O) was obtained by the same process as that in Example 1, except that the first purging ratio and the second purging ratio was adjusted as shown in Table 1.
Cobalt sulfate heptahydrate (CoSO4·7H2O) was obtained by the same process as that in Example 1, except that the second purging was not performed in the cooling crystallization.
Cobalt sulfate heptahydrate (CoSO4·7H2O) was obtained by the same method as that in Example 1, except that the first purging was not performed in the evaporation crystallization.
For each product obtained in the above-described Examples and Comparative Examples, an amount of recovered cobalt (recovery ratio (%)) relative to that in the feeding solution, a content of manganese, and a purity of the cobalt sulfate salt were measured. The purity was calculated by a weight of cobalt sulfate heptahydrate relative to a total weight of the obtained product, and the weight of cobalt sulfate heptahydrate was measured using an ICP-AES (Inductively Coupled Plasma Atomic Emission Spectroscopy) analysis.
The evaluation results are shown together in Table 1 below.
Referring to Table 1, according to Examples, the first purging and the second purging were combined to reduce the amount of manganese impurities and achieve the cobalt recovery ratio of 85% or more.
In Comparative Example 1 or Comparative Example 2 where the first purging or the second purging was omitted, the purity of the cobalt salt decreased as an amount of residual manganese increased or as an amount of sulfuric acid was not sufficiently removed to be concentrated.
While the present invention has been described with respect to the specific embodiments, it will be apparent to those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention as defined in the following claims. Furthermore, the embodiments may be combined to form additional embodiments.
| Number | Date | Country | Kind |
|---|---|---|---|
| 10-2021-0034110 | Mar 2021 | KR | national |
This application is a bypass continuation application of PCT/KR2022/003504 filed on Mar. 14, 2022, which claims priority to KR 10-2021-0034110 filed on Mar. 16, 2021. The disclosure of each of the foregoing applications is incorporated herein by reference in its entirety.
| Number | Date | Country | |
|---|---|---|---|
| Parent | PCT/KR2022/003504 | Mar 2022 | US |
| Child | 18467728 | US |
