CN111910075A - Method for leaching nickel and cobalt from rough nickel and cobalt hydroxide in two stages - Google Patents
Method for leaching nickel and cobalt from rough nickel and cobalt hydroxide in two stages Download PDFInfo
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- CN111910075A CN111910075A CN202010804257.8A CN202010804257A CN111910075A CN 111910075 A CN111910075 A CN 111910075A CN 202010804257 A CN202010804257 A CN 202010804257A CN 111910075 A CN111910075 A CN 111910075A
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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
- C22B3/04—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
- C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
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- 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
- C22B23/0407—Leaching processes
- C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
- C22B23/043—Sulfurated acids or salts thereof
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Abstract
A method for leaching nickel and cobalt from rough nickel and cobalt hydroxide by two stages belongs to the technical field of hydrometallurgy and comprises the following steps: a, circularly washing magnesium: mixing and stirring the rough nickel cobalt hydroxide and water, washing, and carrying out filter pressing after washing. Leaching in the first stage of B: after washing magnesium, the filter cake is pulped, leached by sulfuric acid and then subjected to solid-liquid separation. C, second-stage leaching: and (3) using the first-stage leaching residue as a raw material for second-stage leaching, adding part of sulfuric acid, performing second-stage leaching, then performing solid-liquid separation, and washing the second-stage leaching residue. D, refluxing the second-stage leachate and washing water: and C, mixing the second-stage leachate obtained in the step C with washing water, returning to the first-stage leaching in the step B, and slurrying the second-stage leachate with a second-stage magnesium washing filter cake in a stirring tank. The method ensures that the rough nickel cobalt hydroxide efficiently leaches the nickel cobalt only by sulfuric acid leaching without adding other reducing agents, simultaneously can reduce the leaching of manganese element, and has the advantages of easy operation, production cost saving, high nickel cobalt leaching rate and the like.
Description
Technical Field
The invention belongs to the technical field of hydrometallurgy, and relates to a method for leaching nickel and cobalt from rough nickel and cobalt hydroxide in two stages.
Background
The nickel sulfate is widely applied to the industries of electroplating, storage battery materials, catalysts, pigments and the like. In recent years, with the development of aluminum profile surface treatment process and the updating of battery products, the application field of nickel sulfate is continuously widened. The nickel sulfate is used as one of the main raw materials of the ternary battery, and the market demand is increased year by year.
Nickel hydroxide cobalt, one of the intermediate products of laterite-nickel ores, has now become one of the main nickel raw materials for electrolytic nickel and nickel salts. Generally, in a sulfuric acid system, crude nickel hydroxide cobalt prepared from nickel sulfide concentrate is used as a raw material, and nickel sulfate is produced by processes of acid dissolution, extraction impurity removal, cooling crystallization and the like, and the process is relatively mature and reliable. In the acid dissolving process, sulfuric acid is generally adopted for dissolving and leaching, and reducing agents such as sodium metabisulfite, hydrogen peroxide and the like are added for auxiliary leaching, so that the leaching rate of nickel and cobalt can be improved, but meanwhile, a large amount of impurities such as manganese and the like can be leached into the solution, and pressure is brought to subsequent extraction and impurity removal. People urgently need a new method for leaching nickel and cobalt from rough nickel and cobalt hydroxide (MHP), which can reduce the leaching of other impurity elements and reduce the pressure of impurity removal process while ensuring the leaching rate of nickel and cobalt. The inventor of the invention provides a method for leaching nickel and cobalt from rough nickel and cobalt hydroxide by two stages through continuous exploration, only sulfuric acid is used for leaching, no reducing agent and the like are added in the leaching process, nickel and cobalt elements can be efficiently leached by two stages of leaching, so that less manganese elements enter a solution, the acid consumption is less, and the manganese content of the final leaching slag can reach more than 50 percent and can be used as a raw material for producing manganese.
Disclosure of Invention
The invention aims to provide a method for leaching nickel and cobalt from nickel and cobalt hydroxide (MHP) in two stages, which is used for preparing nickel sulfate and cobalt sulfate by using crude nickel and cobalt hydroxide as a raw material through sulfuric acid leaching. Under the conditions of no addition of any reducing agent, no increase of acid consumption and lower cost, the method can efficiently leach nickel and cobalt elements through two-stage leaching, simultaneously less manganese elements can enter a solution, the manganese content of the final leaching slag reaches over 50 percent, and the final leaching slag can be used as a raw material for producing manganese. The purpose of the invention is realized by the following technical scheme.
A method for leaching nickel and cobalt from crude nickel and cobalt hydroxide in two stages comprises the following steps:
a, circularly washing magnesium: mixing, stirring and washing the rough nickel cobalt hydroxide and water, and carrying out filter pressing after washing to obtain a first-stage magnesium washing filter cake and a first-stage magnesium washing filtrate; mixing, stirring and washing the first-stage magnesium washing filter cake and water, and carrying out filter pressing after washing to obtain a second-stage magnesium washing filter cake and a second-stage magnesium washing filtrate; returning part of the second-stage magnesium washing filtrate to the first-stage washing to be mixed with the rough nickel cobalt hydroxide and water, and opening the circuit of the rest of the second-stage magnesium washing filtrate;
leaching in the first stage of B: slurrying the second-stage magnesium washing filter cake in a stirring tank, then carrying out sulfuric acid leaching, and carrying out filter pressing on the leached slurry to obtain a first-stage leachate and a first-stage leached residue; the first-stage leaching solution is a crude nickel and cobalt sulfate solution, and nickel sulfate and cobalt sulfate are prepared by a subsequent impurity removal process;
c, second-stage leaching: using the first-stage leaching residue as a raw material for second-stage leaching, adding sulfuric acid for second-stage leaching, and then carrying out solid-liquid separation to obtain a second-stage leaching solution and second-stage leaching residue; washing the second-stage leaching residue to obtain washing water and manganese residue;
d, refluxing the second-stage leachate and washing water: and C, mixing the second-stage leachate obtained in the step C with washing water, returning to the first-stage leaching in the step B, and slurrying the second-stage leachate with a second-stage magnesium washing filter cake in a stirring tank.
Further, the liquid-solid ratio (mass ratio of liquid to solid) in the stirring and washing in the step A is 2: 1 to 5: 1, and the total washing time is 0.5 to 2 hours.
And further, the first-stage magnesium washing filtrate in the step A is sent to back extraction for replenishing water, 20-40% of second-stage magnesium washing filtrate returns to the first-stage washing, and the rest of the second-stage magnesium washing filtrate is opened.
Further, the specific conditions of the first stage leaching in the step B are as follows: the slurry liquid-solid ratio is 3: 1-4: 1, the leaching temperature is 50-80 ℃, the pH value is 1.5-2.5, and the leaching time is 1-2 h.
Further, the specific conditions of the second stage leaching in the step C are as follows: the liquid-solid ratio is 10: 1-5: 1, the leaching time is 1-2 h, the leaching temperature is 50-80 ℃, and the addition amount of sulfuric acid is 50-70% of the dosage of the first-stage leaching sulfuric acid.
The innovation of the invention is that: 1) adding a circulating magnesium washing link to remove most of magnesium element before entering a leaching link; 2) the nickel cobalt can be efficiently leached under the condition of no addition of a reducing agent through two-stage leaching; 3) the second-stage leaching solution returns to the first-stage leaching process, and the washing water part of the second-stage leaching slag returns to the first-stage leaching process, so that the effective utilization rate of acid can be increased, the waste of water is reduced, and the cost is reduced; 4) the final leached slag can be used as a raw material for extracting manganese.
Based on the technical scheme, the invention has the beneficial effects that:
1. in the process of circularly washing magnesium, the washing rate of the magnesium element can reach more than 55 percent.
2. The method comprises two-stage leaching without adding any reducing agent, wherein the leaching rate of nickel is more than or equal to 99.8 percent, the leaching rate of Ni in the leaching solution is more than or equal to 90g/L, the leaching rate of cobalt is more than or equal to 98 percent, the leaching solution of Co is more than or equal to 8g/L, the total slag rate is less than or equal to 5.5 percent, the content of manganese in slag is more than or equal to 55 percent, the content of cobalt is less than or equal to 0.3 percent, and the content of nickel is.
3. In the invention, the second-stage leaching solution returns to the first-stage leaching process, and the washing water part of the second-stage leaching slag returns to the first-stage leaching, so that the sulfuric acid consumption and the water consumption in the subsequent sulfuric acid leaching can be reduced, and the leaching cost is reduced;
4. the content of the manganese element in the final leaching slag can reach more than 55 percent, and the manganese element can be used as manganese ore to extract manganese, thereby achieving the effect of high-efficiency utilization of resources.
Drawings
FIG. 1 is a process flow diagram of two-stage leaching of nickel cobalt from crude nickel cobalt hydroxide (MHP) according to the present invention.
Detailed Description
The invention will be described in further detail below with reference to the drawings and examples, which are intended to facilitate the understanding of the invention without limiting it in any way.
The crude nickel hydroxide cobalt used in the following examples was purchased from an external source and the typical composition is shown in table 1.
Typical composition (wt.%) of the crude nickel cobalt hydroxide used in Table 1
| Element(s) | Ni | Co | Fe | Zn | Cu |
| Content (wt.) | 40.85 | 3.92 | 0.08 | 0.73 | 0.10 |
| Element(s) | Al | Mg | Mn | Ca | Cr |
| Content% | 0.24 | 1.46 | 5.25 | 0.15 | 0.02 |
Example 1
A, circularly washing magnesium: and (3) circularly washing magnesium according to the liquid-solid ratio of 3.5: 1, adding 1/3 of the second-stage magnesium washing liquid into the first-stage magnesium washing liquid, and leaching for 0.5h at room temperature, wherein the washing rate of magnesium element is 60.5%.
Leaching in the first stage of B: and slurrying the washed filter cake at a liquid-solid ratio of 3.8 to 1, adding sulfuric acid to adjust the pH value of the solution to be kept at about 2.0 when the leaching temperature is 70 ℃, leaching for 1.5h, wherein the acid-mineral ratio is 0.68, carrying out filter pressing on the leached slurry after the completion of leaching, and carrying out solid-liquid separation to obtain a first-stage leaching solution and a first-stage leaching residue, wherein the leaching rates of nickel and cobalt elements in the first stage are 97.8% and 83.3% respectively, and the first-stage residue rate is 10%.
C, second-stage leaching: the first-stage leaching slag is used as a raw material for second-stage leaching, 50% of first-stage acid consumption is added according to a liquid-solid ratio of 10: 1 at a leaching temperature of 70 ℃, leaching is carried out for 1h, the slag rate of the first-stage leaching slag is 5.5%, the leaching rates of nickel and cobalt are 100% and 98.9% respectively, the manganese content of the generated slag is 55%, and the slag can be used as manganese concentrate.
D, refluxing the second-stage leachate and washing water: and B, mixing the filter cake after magnesium washing with washing water of the second-stage leaching solution and the second-stage leaching slag according to the liquid-solid ratio of 3.8 to 1, supplementing 50% of sulfuric acid under the same condition as that in the step B, adjusting the pH value of the solution to be kept at about 2.0, and performing solid-liquid separation after leaching to obtain a crude nickel-cobalt sulfate solution with the nickel element concentration of 90g/L and the cobalt element concentration of 8 g/L.
Example 2
A, circularly washing magnesium: and (3) circularly washing magnesium according to the liquid-solid ratio of 3.5: 1, adding 1/3 of the second-stage magnesium washing liquid into the first-stage magnesium washing liquid, and leaching for 1h at room temperature, wherein the washing rate of magnesium element is 61%.
Leaching in the first stage of B: and slurrying the washed filter cake at a liquid-solid ratio of 4: 1, adding sulfuric acid to adjust the pH value of the solution to be kept at about 1.5 when the leaching temperature is 75 ℃, leaching for 2 hours, wherein the acid-mineral ratio is 0.7, carrying out filter pressing on the leached slurry after the completion of the leaching, and carrying out solid-liquid separation to obtain a first-stage leaching solution and a first-stage leaching residue, wherein the leaching rates of nickel and cobalt elements in the first stage are respectively 98.2% and 85.5%, and the first-stage residue rate is 10%.
C, second-stage leaching: the first-stage leaching residue is used as a raw material for second-stage leaching, 60% of first-stage acid consumption is added according to a liquid-solid ratio of 9: 1 at a leaching temperature of 70 ℃, leaching is carried out for 1h, the residue rate of the first-stage leaching residue is 5%, the leaching rates of nickel and cobalt are 100% and 99% respectively, the manganese content of the generated residue is 57%, and the manganese can be used as manganese concentrate.
D, refluxing the second-stage leachate and washing water: and B, mixing the filter cake after magnesium washing with washing water of the second-stage leaching solution and the second-stage leaching slag according to the liquid-solid ratio of 3.5 to 1, supplementing 40% of sulfuric acid under the same condition as that in the step B, adjusting the pH value of the solution to be kept at about 1.5, and performing solid-liquid separation after leaching to obtain a crude nickel-cobalt sulfate solution with the nickel element concentration of 91g/L and the cobalt element concentration of 8.3 g/L.
Example 3
A, circularly washing magnesium: and (3) circularly washing magnesium according to a liquid-solid ratio of 4: 1, adding 1/3 of a second-stage magnesium washing liquid into the first-stage magnesium washing liquid, and leaching for 1h at room temperature, wherein the washing rate of magnesium element is 62%.
Leaching in the first stage of B: and slurrying the washed filter cake at a liquid-solid ratio of 4: 1, adding sulfuric acid to adjust the pH value of the solution to be kept at about 2.5 when the leaching temperature is 75 ℃, leaching for 1.5h, wherein the acid-mineral ratio is 0.69, filter-pressing the leached slurry after the completion of the leaching, and carrying out solid-liquid separation to obtain a first-stage leaching solution and a first-stage leaching residue, wherein the leaching rates of nickel and cobalt in the first stage are 97% and 83% respectively, and the rate of the first-stage residue is 10%.
C, second-stage leaching: the first-stage leaching residue is used as a raw material for second-stage leaching, 70% of first-stage acid consumption is added according to the liquid-solid ratio of 9: 1 at the leaching temperature of 70 ℃, leaching is carried out for 1h, the residue rate of the first-stage leaching residue is 5%, the leaching rates of nickel and cobalt are 100% and 99% respectively, the manganese content of the generated residue is 55%, and the manganese can be used as manganese concentrate.
D, refluxing the second-stage leachate and washing water: and B, mixing the filter cake after magnesium washing with washing water of the second-stage leaching solution and the second-stage leaching slag according to the liquid-solid ratio of 4 to 1, supplementing 30% of sulfuric acid under the same condition as that in the step B, adjusting the pH value of the solution to be kept at about 2.5, and performing solid-liquid separation after leaching to obtain a crude nickel-cobalt sulfate solution with the nickel element concentration of 93g/L and the cobalt element concentration of 8.4 g/L.
Claims (5)
1. A method for leaching nickel and cobalt from rough nickel and cobalt hydroxide in two stages is characterized by comprising the following steps:
a, circularly washing magnesium: mixing, stirring and washing the rough nickel cobalt hydroxide and water, and carrying out filter pressing after washing to obtain a first-stage magnesium washing filter cake and a first-stage magnesium washing filtrate; mixing, stirring and washing the first-stage magnesium washing filter cake and water, and carrying out filter pressing after washing to obtain a second-stage magnesium washing filter cake and a second-stage magnesium washing filtrate; returning part of the second-stage magnesium washing filtrate to the first-stage washing to be mixed with the rough nickel cobalt hydroxide and water, and opening the circuit of the rest of the second-stage magnesium washing filtrate;
leaching in the first stage of B: slurrying the second-stage magnesium washing filter cake in a stirring tank, then carrying out sulfuric acid leaching, and carrying out filter pressing on the leached slurry to obtain a first-stage leachate and a first-stage leached residue; the first-stage leaching solution is a crude nickel and cobalt sulfate solution, and nickel sulfate and cobalt sulfate are prepared by a subsequent impurity removal process;
c, second-stage leaching: using the first-stage leaching residue as a raw material for second-stage leaching, adding sulfuric acid for second-stage leaching, and then carrying out solid-liquid separation to obtain a second-stage leaching solution and second-stage leaching residue; washing the second-stage leaching residue to obtain washing water and manganese residue;
d, refluxing the second-stage leachate and washing water: and C, mixing the second-stage leachate obtained in the step C with washing water, returning to the first-stage leaching in the step B, and slurrying the second-stage leachate with a second-stage magnesium washing filter cake in a stirring tank.
2. The method according to claim 1, wherein the liquid-solid ratio during stirring and washing in the step A is 2: 1-5: 1, and the total washing time is 0.5-2 h.
3. The method according to claim 1, wherein in the step A, the first-stage magnesium washing filtrate is sent to strip water, 20-40% of the second-stage magnesium washing filtrate is returned to the first-stage washing, and the rest of the second-stage magnesium washing filtrate is opened.
4. The method as claimed in claim 1, wherein the specific conditions of the stage of leaching in the step B are as follows: the slurry liquid-solid ratio is 3: 1-4: 1, the leaching temperature is 50-80 ℃, the pH value is 1.5-2.5, and the leaching time is 1-2 h.
5. The method as claimed in claim 1, wherein the specific conditions of the second leaching in step C are as follows: the liquid-solid ratio is 10: 1-5: 1, the leaching time is 1-2 h, the leaching temperature is 50-80 ℃, and the addition amount of sulfuric acid is 50-70% of the dosage of the first-stage leaching sulfuric acid.
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| CN202010804257.8A CN111910075A (en) | 2020-08-12 | 2020-08-12 | Method for leaching nickel and cobalt from rough nickel and cobalt hydroxide in two stages |
| CN202011238500.0A CN112095005A (en) | 2020-08-12 | 2020-11-09 | Method for leaching nickel and cobalt from rough nickel and cobalt hydroxide in two stages |
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| CN112553478A (en) * | 2020-12-02 | 2021-03-26 | 金川集团镍盐有限公司 | Method for quickly leaching nickel hydroxide cobalt sulfuric acid system |
| CN114427037A (en) * | 2022-01-06 | 2022-05-03 | 中国恩菲工程技术有限公司 | Method for continuously enriching nickel and cobalt from low-concentration nickel and cobalt solution |
| CN114457245A (en) * | 2020-11-10 | 2022-05-10 | 北京博萃循环科技有限公司 | Method for preparing nickel sulfate and cobalt sulfate from nickel hydroxide cobalt |
| JP7099592B1 (en) | 2021-06-25 | 2022-07-12 | 住友金属鉱山株式会社 | Manufacturing method of cobalt sulfate |
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Family Cites Families (6)
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| AU2007271672A1 (en) * | 2006-07-03 | 2008-01-10 | Curlook Enterprises Inc. | Metal recovery system as applied to the high pressure leaching of limonitic nickel laterite ores |
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| CN104310495B (en) * | 2014-10-17 | 2016-05-04 | 金川集团股份有限公司 | A kind of Leaching in Hydrochloric Acid nickel hydroxide cobalt is produced the method for nickel chloride solution |
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2020
- 2020-08-12 CN CN202010804257.8A patent/CN111910075A/en active Pending
- 2020-11-09 CN CN202011238500.0A patent/CN112095005A/en active Pending
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| CN116121556A (en) * | 2022-12-23 | 2023-05-16 | 中国恩菲工程技术有限公司 | Nickel cobalt hydroxide intermediate product quality improving method and hydrometallurgical treatment method |
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Application publication date: 20201110 |