CN110616322A - Non-saponification extraction method for extracting and separating cobalt, nickel and manganese by using acidic extracting agent - Google Patents
Non-saponification extraction method for extracting and separating cobalt, nickel and manganese by using acidic extracting agent Download PDFInfo
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- 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
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
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- 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
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
- C22B3/38—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds containing phosphorus
- C22B3/384—Pentavalent phosphorus oxyacids, esters thereof
- C22B3/3842—Phosphinic acid, e.g. H2P(O)(OH)
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- 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
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
- C22B3/38—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds containing phosphorus
- C22B3/384—Pentavalent phosphorus oxyacids, esters thereof
- C22B3/3846—Phosphoric acid, e.g. (O)P(OH)3
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Abstract
The invention belongs to the technical field of metal extraction and separation, and particularly relates to a non-saponification extraction method for extracting and separating cobalt, nickel and manganese by using an acidic extraction agent. The method does not need to saponify an acidic extractant, does not need to repeatedly adjust the pH value of a water phase by using acid and alkali in the extraction process, only needs to add a certain weak acid into a feed liquid before extraction and adjust the acidity of the feed liquid to the range of pH 4.00-6.00 by using alkali, can extract and separate cobalt, nickel and manganese by adopting unsaponifiable P204, Cyanex272 or P507, achieves an ideal extraction and separation effect, and solves the technical problem that the operation is time-consuming and tedious because the acidic extractant is saponified when the acidic extractant is used for extracting and separating the cobalt, nickel and manganese in the prior art.
Description
Technical Field
The invention belongs to the technical field of metal extraction and separation, and particularly relates to a non-saponification extraction method for extracting and separating cobalt, nickel and manganese by using an acidic extraction agent.
Background
At present, a solvent extraction method is widely adopted to separate cobalt, nickel and manganese. Commonly used extractants are acidic organophosphorus extractants, such as P204, Cyanex272 and P507. During the extraction process, H in the extractant molecule+Exchange with metal ions in the aqueous phase, resulting in a decrease in the pH of the aqueous phase and a consequent decrease in extraction efficiency. To avoid this phenomenon, saponification techniques are commonly used in which the extractant is treated with alkali before extraction, part of the extractant is converted into sodium or ammonium salts, and then the sodium or ammonium salts are converted into the desired formExtracting, wherein the extraction reaction is changed from (1) to (2):
extracting with saponified extractant containing Na+Exchange with metal ions in the water phase, so that the pH value of the water phase is not reduced any more in the extraction process, and the extraction efficiency of the metal ions is effectively improved.
However, when extraction is carried out with saponified extractants, Na is present in the extractant+In addition to exchange with metal ions in the aqueous phase, the metal ions also exchange with H in the aqueous phase+The exchange is carried out, so that the pH value of the water phase is increased, the co-extraction of coexisting metal ions is further caused, and the separation effect of the metal ions is reduced. In order to avoid the phenomenon of the reagent to be extracted containing various metal ions, such as cobalt, nickel and manganese, the pH value of the feed liquid must be monitored in the extraction process, and a certain amount of acid or alkali is added to adjust the pH value of the water phase within a proper range.
The prior saponification extraction technology has the following defects: (1) before extraction, alkali and an extracting agent are required to carry out saponification reaction, and after the reaction is finished, the extraction solution is kept stand until the extraction solution is clarified and can be used, so that the time is wasted, and the operation is complicated; (2) during the extraction process, the pH value of the aqueous phase still needs to be monitored and adjusted. Moreover, the pH change of the aqueous phase in the extraction process is a dynamic process, the pH value of the aqueous phase needs to be repeatedly adjusted, and the operation is very inconvenient.
Disclosure of Invention
Aiming at the defects or the improvement requirements of the prior art, the invention provides a non-saponification extraction method for extracting and separating cobalt, nickel and manganese by using an acidic extraction agent, which does not need to saponify the acidic extraction agent, does not need to repeatedly adjust the pH value of a water phase by using acid and alkali in the extraction process, only needs to add a certain weak acid into a feed liquid before extraction, and adjusts the acidity of the feed liquid to be within the range of 4.00-6.00 by using alkali, namely, can extract and separate cobalt, nickel and manganese by using non-saponification P204, Cyanex272 or P507, so as to achieve an ideal extraction and separation effect, thereby solving the technical problem that the operation is time-consuming and complicated because the acidic extraction agent is saponified when the cobalt, nickel and manganese are extracted and separated by using the acidic extraction agent in the prior art.
In order to achieve the above object, according to one aspect of the present invention, there is provided a non-saponification extraction method for extracting and separating cobalt, nickel and manganese by using an acidic extractant, comprising the steps of:
(1) mixing a feed liquid to be extracted containing cobalt, nickel and manganese with a buffer solution to obtain a mixed feed liquid, adjusting the pH of the mixed feed liquid to 4.00-4.60, and extracting manganese in the feed liquid by using a non-saponified first acidic extracting agent to obtain a raffinate after manganese extraction; the buffer solution comprises a weak acid and its conjugate base, wherein the molar ratio of weak acid to the first acidic extractant is not less than 5: 1;
(2) adjusting the pH value of the raffinate obtained after manganese extraction in the step (1) to 5.00-5.50, and separating cobalt and nickel by using a non-saponified second acidic extracting agent, wherein the molar ratio of the weak acid to the second acidic extracting agent is 6-15: 1.
Preferably, the weak acid is acetic acid or lactic acid.
Preferably, the weak acid is acetic acid.
Preferably, the molar concentration of the weak acid in the buffer solution is 2-4 mol/L.
Preferably, the molar ratio of the weak acid to the first acidic extracting agent in the step (1) is 5-15: 1.
Preferably, the first acidic extractant is P204; the second acidic extracting agent is Cyanex272 or P507.
Preferably, in the step (1), the pH of the mixed feed liquid is adjusted to 4.00-4.60 by alkali and/or acid; and (2) adjusting the pH of the raffinate after manganese extraction to 5.00-5.50 by using alkali and/or acid.
Preferably, the pH of the mixed feed liquid is adjusted to 4.30 in the step (1); and (2) adjusting the pH value of the mixed material liquid to 5.40.
In general, compared with the prior art, the above technical solution contemplated by the present invention can achieve the following beneficial effects:
the invention provides a non-saponification extraction method for extracting and separating cobalt, nickel and manganese by using an acidic extraction agent, which establishes the non-saponification extraction method for extracting and separating cobalt, nickel and manganese by using an acidic organic phosphorus extraction agent, can completely replace a saponification extraction separation method, greatly simplifies the cobalt, nickel and manganese extraction and separation process, and greatly improves the work efficiency.
According to the method, the extraction agent is not required to be saponified in advance, the pH value of a water phase is not required to be repeatedly adjusted by acid and alkali in the extraction process, the acidity of the feed liquid is adjusted to be within the range of pH 4.00-6.00 by alkali after a certain weak acid is added into the feed liquid before extraction, and the cobalt, nickel and manganese can be extracted and separated by adopting unsaponifiable P204, Cyanex272 or P507, so that an ideal extraction and separation effect is achieved.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail with reference to the following embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention. In addition, the technical features involved in the embodiments of the present invention described below may be combined with each other as long as they do not conflict with each other.
The invention provides a non-saponification extraction method for extracting and separating cobalt, nickel and manganese by using an acidic extraction agent, which is characterized by comprising the following steps of:
(1) mixing a feed liquid to be extracted containing cobalt, nickel and manganese with a buffer solution to obtain a mixed feed liquid, adjusting the pH of the mixed feed liquid to 4.00-4.60, and extracting manganese in the feed liquid by using a non-saponified first acidic extracting agent to obtain a raffinate after manganese extraction; the buffer solution comprises a weak acid and its conjugate base, wherein the molar ratio of weak acid to the first acidic extractant is not less than 5: 1;
(2) adjusting the pH value of the raffinate obtained after manganese extraction in the step (1) to 5.00-5.50, and extracting and separating cobalt and nickel by using a non-saponified second acidic extraction agent, wherein the molar ratio of the weak acid to the second acidic extraction agent is 6-15: 1.
In some embodiments, the weak acid is acetic acid or lactic acid, preferably acetic acid.
In some embodiments, the weak acid has a molar concentration of 2 to 4 mol/L.
In some embodiments, the first acidic extractant is P204; the second acidic extracting agent is Cyanex272 or P507.
In some embodiments, the molar ratio of weak acid to the first acidic extractant is greater than 5: 1.
In some embodiments, the pH of the mixed feed liquid is adjusted to 4.00-4.60 by alkali and/or acid in the step (1); and (2) adjusting the pH of the raffinate after manganese extraction to 5.00-5.50 by using alkali and/or acid.
In some embodiments, step (1) adjusts the pH of the mixed liquor to 4.30, corresponding to the optimal pH for extracting manganese from P204; and (2) adjusting the pH of the mixed feed liquid to 5.40, wherein the pH corresponds to the optimum pH for extracting and separating cobalt and nickel by using Cyanex272 or P507.
In the prior art, when the saponified extractant is used for extracting and separating manganese, cobalt and nickel, Na in the extractant is generated by the exchange reaction of sodium ions and metal ions in the extractant in the extraction process+In addition to exchange with metal ions in the aqueous phase, the metal ions also exchange with H in the aqueous phase+Exchange is carried out to cause the pH value of the water phase to rise, and weak acid is added in the extraction process to fundamentally inhibit the pH value of the feed liquid from rising; the invention adopts non-saponification extracting agent to extract and separate cobalt, nickel and manganese, which is characterized in that hydrogen ions in the extracting agent and metal ions are subjected to exchange reaction to generate hydrogen ions to reduce the pH value of the feed liquid, and weak acid is added into the feed liquid to form buffer solution, so that the reduction of the pH value is actually inhibited, although the pH value of the feed liquid in the extracting process is stabilized, the pH value of the feed liquid is fundamentally different from the pH value of the feed liquid in the extracting process in the control principle.
The invention adopts non-saponification extracting agent to extract and separate cobalt, nickel and manganese, and weak acid is added into the feed liquid, and the weak acid and conjugate base thereof form buffer solution to stabilize the pH value of the feed liquid. Wherein, the concentration and dosage of weak acid can affect the buffer effect of the buffer solution, and the concentration of the extracting agent, the concentration of metal ions in the feed liquid, the extraction ratio and the like can affect the pH of the feed liquid before and after extraction.
Because the dosage of the weak acid in the feed liquid has obvious influence on the extraction efficiency of cobalt, nickel and manganese, and the extraction of manganese from P204 and the separation of cobalt and nickel from Cyanex272 or P507 are two continuous and uninterrupted processes, the key point of the invention is that the dosage of the weak acid needs to be controlled, so that the dosage of the weak acid can simultaneously take two extraction and separation processes into consideration, and the pH in the two extraction processes can be kept stable and stabilized in respective better pH ranges.
In some embodiments of the present invention, under other conditions, the difference between the pH values of the feed solution before and after the P204 extraction gradually decreases with the increase of the acetic acid concentration, and the extraction rate of manganese is substantially unchanged. Experiments show that 2-4 mol/L of acetic acid basically can well control the pH value of the feed liquid.
The extractant P204 adopted by the invention is a non-saponified extractant, namely, the extractant P204 is not converted into salt by adding alkali, but is a non-saponified acidic extractant, and the suitable concentration range is 0.20 mol/L-0.40 mol/L. Correspondingly, the ratio of the acetic acid amount to the non-saponified extractant amount is suitably: n (acetic acid): n (P204) is more than 5:1, preferably 5-15: 1. Similarly, under the condition of 2-4 mol/L acetic acid, the pH value of the feed liquid can be well controlled to be basically unchanged, and a higher cobalt-nickel separation effect can be obtained. Determining the proportion relation of the acetic acid dosage and the non-saponification extracting agent Cyanex272 dosage: n (acetic acid): n (Cyanex272) is 6-15: 1, wherein the concentration of the non-saponified extractant Cyanex272 is 0.20-0.50 mol/L.
In some embodiments, the concentration of manganese ions in the initial feed solution to be extracted ranges from 2g/L to 4 g/L. The concentration range of the cobalt ions is 2 g/L-4 g/L. The concentration range of the nickel ions is 2 g/L-4 g/L.
In some embodiments, the ratio of manganese extracted is 1:2 to 1: 8. The ratio of the extracted cobalt to nickel is 1: 1-1: 4.
In the experiment, the pH value of the cobalt, nickel and manganese separated by non-saponification extraction is within the pH range of 3.80-5.50, and the pH change of the feed liquid before and after extraction is not more than 0.15; the extraction rates of manganese and cobalt both increase with increasing initial pH of the feed solution. In order to obtain the best manganese and cobalt separation effect, the pH value of the extracted manganese is best 4.30. And in the pH range of 4.80-5.60, the pH value after extraction is basically kept unchanged, the extraction rate of cobalt and nickel is increased along with the increase of the initial pH value of the feed liquid, and the optimal extraction pH value for separating cobalt and nickel is 5.40.
The invention belongs to the field of metal extraction and separation, and particularly relates to extraction and separation of manganese from acidic organic phosphorus extractant P204 and cobalt and nickel from Cyanex 272/P507. The method is not limited to the separation of cobalt, nickel and manganese in the waste lithium ion anode material, and is also suitable for other feed liquid containing cobalt, nickel and manganese.
The chemical name of P204 is di (2-ethylhexyl) phosphate, Cyanex272 is di (2, 4, 4) -trimethylpentylphosphinic acid, and P507 is 2-ethylhexyl phosphonic acid-2-ethylhexyl ester.
The saponification of the extractant in the prior art mentioned in the invention means that the acidic extractant is treated by alkali, so that part of the extractant is converted into sodium salt or ammonium salt, and the extraction efficiency of the extractant on metal ions is improved.
The following are examples:
example 1
P204 is adopted to extract manganese in the ternary cathode material of the 111 type lithium ion battery.
The separation method of the embodiment comprises the following steps:
1. leaching of cobalt, nickel and manganese in battery anode material
Weighing 10g of battery anode material powder, and selecting H2SO4+H2O2The leaching agent is obtained by refluxing and leaching by a constant-temperature heating magnetic stirrer. Wherein, the liquid-solid ratio is 10: 1, H2SO4Concentration 2.5mol/L, 2.0mL H2O2The leaching temperature is 85 ℃, and the leaching time is 120 min. Adjusting the pH value of the leached feed liquid to 4.5-5.0, filtering and precipitating, and fixing the volume to 250 mL. The contents of the elements in the leaching solution are respectively as follows through the determination of an atomic absorption spectrometry: co: 6.646 g/L; ni: 7.124 g/L; mn: 6.880 g/L.
2. P204 extraction of manganese
Transferring 17.20mL of glacial acetic acid, adding a proper amount of distilled water for dilution, adjusting the pH of the solution to be slightly more than 4.30 by using solid sodium hydroxide, adding 50mL of the leaching solution, adjusting the pH of the mixed solution to be about 4.30 by using a sodium hydroxide solution and a sulfuric acid solution, and fixing the volume to be 100 mL. The contents of acetic acid, cobalt, nickel and manganese in the feed liquid are respectively as follows: 3.0mol/L acetic acid, 3.323g/L LCo, 3.562g/L Ni, 3.440g/L Mn. Extracting with 0.40mol/L P204 at O/A ratio of 1:2, 1:4, and 1:8 for 15min at 25 deg.C. In the first stage of extraction, the molar ratio of acetic acid to extractant is n (HAc) to n (P204) is 15: 1. As a control, manganese was extracted under the same conditions using P204 having a saponification rate of 50% at 0.40mol/L, and the extraction results are shown in Table 1.
TABLE 1 comparison of the results of manganese extraction of unsaponifiable P204 with saponified P204
After four-stage extraction by using the non-saponified P204, the pH value of the feed liquid is averagely reduced by 0.15, and the change amplitude is small, which shows that the pH change in the extraction process can be well controlled by adding acetic acid into the feed liquid before extraction. Extracting with unsaponifiable P204, wherein the removal rate of manganese reaches 99.80%, and the manganese content in raffinate is only 0.007 g/L; the co-extraction of cobalt and nickel into the organic phase was 47.34%, 18.24%, respectively. The above extraction results are substantially identical to the extraction results of saponified P204.
Example 2
Cobalt and nickel in the ternary cathode material of the 111 type lithium ion battery are extracted and separated by adopting Cyanex 272.
The raffinate from manganese extraction in example 1 was adjusted to pH 5.40 with solid NaOH, and extracted twice with 0.60mol/L Cyanex272 at 25 ℃ for 15min at O/A ratios of 1:2 and 1:4, respectively. In the first stage of extraction, the molar ratio of acetic acid to extractant is n (HAc) to n (C272) is 10: 1. As a control, extraction was carried out under the same conditions using Cyanex272 having a saponification rate of 70% at 0.60mol/L, and the extraction results are shown in Table 2.
TABLE 2 comparison of the results of the extraction separation of cobalt and nickel by unsaponifiable Cyanex272 and saponified Cyanex272
After the two-stage extraction by adopting the non-saponified Cyanex272, the pH value of the feed liquid is averagely reduced by 0.06, which shows that the acetic acid in the raffinate can still maintain the pH value of the feed liquid basically unchanged. The extraction separation effect of the unsaponified Cyanex272 and the extraction separation effect of the saponified Cyanex272 are basically the same. The cobalt and nickel contents in the raffinate are respectively as follows: co: 0.008 g/L; ni: 2.754g/L, the extraction rate of cobalt reaches 99.57 percent, and the co-extraction rate of nickel is only 5.43 percent.
Example 3
P507 extraction separation of cobalt and nickel in the ternary anode material of the 111 type lithium ion battery:
the pH of the raffinate after manganese extraction is adjusted to about 5.40 by solid sodium hydroxide, and the raffinate is extracted twice by 0.50mol/L P507 according to the O/A ratio of 1:2 and 1:4 respectively at the temperature of 25 ℃ for 15 min. In the first stage of extraction, the molar ratio of acetic acid to extractant is n (HAc) to n (P507) is 12: 1. As a control, extraction was carried out under the same conditions using P507 having a saponification rate of 70% at 0.50mol/L, and the extraction results are shown in Table 3.
TABLE 3 comparison of the results of the cobalt-nickel separation by extraction of unsaponifiable P507 with saponified P507
After the non-saponification P507 is adopted for two-stage extraction, the pH value of the feed liquid is averagely reduced by 0.13, which shows that the pH value of the feed liquid can still be maintained to be basically unchanged by an acetic acid system in the raffinate. The extraction separation effect of the unsaponifiable P507 is basically consistent with that of the saponified P507. The cobalt and nickel contents in the raffinate are respectively as follows: co: 0.034 g/L; ni: 2.275g/L, the extraction rate of cobalt is 98.08%, and the co-extraction rate of nickel is 21.89%.
It will be understood by those skilled in the art that the foregoing is only a preferred embodiment of the present invention, and is not intended to limit the invention, and that any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the scope of the present invention.
Claims (7)
1. A non-saponification extraction method for extracting and separating cobalt, nickel and manganese by using an acidic extractant is characterized by comprising the following steps of:
(1) mixing a feed liquid to be extracted containing cobalt, nickel and manganese with a buffer solution to obtain a mixed feed liquid, adjusting the pH of the mixed feed liquid to 4.00-4.60, and extracting manganese in the feed liquid by using a non-saponified first acidic extracting agent to obtain a raffinate after manganese extraction; the buffer solution comprises a weak acid and its conjugate base, wherein the molar ratio of weak acid to the first acidic extractant is not less than 5: 1;
(2) adjusting the pH value of the raffinate obtained after manganese extraction in the step (1) to 5.00-5.50, and separating cobalt and nickel by using a non-saponified second acidic extracting agent, wherein the molar ratio of the weak acid to the second acidic extracting agent is 6-15: 1.
2. The extraction process of claim 1, wherein the weak acid is acetic acid or lactic acid.
3. The extraction process of claim 1, wherein the weak acid is acetic acid.
4. The extraction process according to claim 2, wherein the molar concentration of the weak acid in the buffer solution is 2 to 4 mol/L.
5. The extraction process of claim 1, wherein the molar ratio of the weak acid to the first acidic extractant in step (1) is from 5 to 15: 1.
6. The extraction process of claim 1, wherein the first acidic extractant is P204; the second acidic extracting agent is Cyanex272 or P507.
7. The extraction process of claim 1, wherein step (1) adjusts the pH of the mixed liquor to 4.30; and (2) adjusting the pH value of the mixed material liquid to 5.40.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112662878A (en) * | 2020-12-02 | 2021-04-16 | 桂林理工大学 | Method for preparing high-purity cobalt sulfate from electrolytic manganese sulfide slag |
| CN113073208A (en) * | 2021-03-29 | 2021-07-06 | 华中科技大学 | Pretreatment method of extracting agent for cobalt-nickel separation and corresponding extraction method |
| CN113174485A (en) * | 2021-04-29 | 2021-07-27 | 金川集团镍盐有限公司 | Method for deeply removing calcium and manganese in cobalt sulfate solution |
| CN113355512A (en) * | 2021-06-03 | 2021-09-07 | 华中科技大学 | Pretreatment method and extraction method of di (2-ethylhexyl) phosphate extractant |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1814828A (en) * | 2006-02-17 | 2006-08-09 | 昆明理工大学 | Method for increasing metal-extracting efficiency of 1,, (2-ethyl-hexyl) phosphate |
| CN101871048A (en) * | 2010-06-25 | 2010-10-27 | 浙江华友钴业股份有限公司 | Method for recovering cobalt, nickel and manganese from waste lithium cells |
| CN102010999A (en) * | 2010-12-24 | 2011-04-13 | 湖南邦普循环科技有限公司 | Method for separating impurities from cobalt and/or nickel solution by non-saponifiable extraction |
| EP2572007A1 (en) * | 2010-05-20 | 2013-03-27 | CESL Limited | Solvent extraction process for separating cobalt from nickel in aqueous solution |
-
2019
- 2019-09-20 CN CN201910891711.5A patent/CN110616322A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1814828A (en) * | 2006-02-17 | 2006-08-09 | 昆明理工大学 | Method for increasing metal-extracting efficiency of 1,, (2-ethyl-hexyl) phosphate |
| EP2572007A1 (en) * | 2010-05-20 | 2013-03-27 | CESL Limited | Solvent extraction process for separating cobalt from nickel in aqueous solution |
| CN101871048A (en) * | 2010-06-25 | 2010-10-27 | 浙江华友钴业股份有限公司 | Method for recovering cobalt, nickel and manganese from waste lithium cells |
| CN102010999A (en) * | 2010-12-24 | 2011-04-13 | 湖南邦普循环科技有限公司 | Method for separating impurities from cobalt and/or nickel solution by non-saponifiable extraction |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112662878A (en) * | 2020-12-02 | 2021-04-16 | 桂林理工大学 | Method for preparing high-purity cobalt sulfate from electrolytic manganese sulfide slag |
| CN113073208A (en) * | 2021-03-29 | 2021-07-06 | 华中科技大学 | Pretreatment method of extracting agent for cobalt-nickel separation and corresponding extraction method |
| CN113174485A (en) * | 2021-04-29 | 2021-07-27 | 金川集团镍盐有限公司 | Method for deeply removing calcium and manganese in cobalt sulfate solution |
| CN113355512A (en) * | 2021-06-03 | 2021-09-07 | 华中科技大学 | Pretreatment method and extraction method of di (2-ethylhexyl) phosphate extractant |
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