A method for leaching and purifying nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore

Abstract

The present application belongs to the field of non-ferrous hydrometallurgy, and particularly relates to a method for leaching and purifying nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore. The method for leaching and purifying nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore provided by the present application comprises the following steps: (1) adding nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore into a sulfuric acid solution for acid leaching to obtain an acid leaching mixture; (2) mixing and ball-milling the nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore with water to prepare a slurry; (3) adding the slurry obtained in step (2) into the acid leaching mixture obtained in step (1) to adjust the pH, and then filtering to obtain a leaching solution and a leaching residue after reaction; and (4) adding an alkaline solution into the leaching solution obtained in step (3) to adjust the pH, and then filtering to obtain a solution after removing iron and aluminum and an iron and aluminum residue after reaction. The method has high yield of valuable metals, reduces the consumption of acid and alkali, reduces the processing cost, and has simple process operation and low loss of materials in the turnover process.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of non-ferrous hydrometallurgy, and particularly relates to a method for leaching and purifying a nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore. BACKGROUND

[0002] With the rapid development of the new energy vehicle industry and the integration of vehicle platform functions, future new energy vehicles will continue to develop towards higher energy density and longer driving range, and the development trend of high-nickel ternary lithium batteries is increasingly obvious. According to SMM Shanghai Nonferrous Metals Network data, in 2021, domestic ternary cathode materials were still dominated by high-voltage nickel 5 series products, accounting for 46%, followed by nickel 8 series high-nickel products accounting for 36%, and nickel 6 series products accounting for 16%.

[0003] From the perspective of energy density, after using super-high nickel positive electrode material, the energy density of the battery cell has reached 300-400 Wh / kg, widening the gap with the lithium iron phosphate battery cell, and better meeting the development requirements of new energy vehicles for lightweight and intelligentization. From the market side, many multinational vehicle enterprises choose high-nickel power battery technology route as a commercial solution to realize high-end application and high driving range, accelerating the promotion and popularization of high-nickel power battery technology route.

[0004] Nickel element ratio of 60% and above is called high-nickel ternary material, and nickel as the main element in high-nickel ternary material plays a crucial role in improving the performance of ternary material. Nickel resources generally exist in nickel sulfide ore and laterite nickel ore, and laterite nickel ore reserves are abundant in the world, especially in Indonesia and other places. Laterite nickel ore is considered to be the main developed nickel resource in the future. The wet metallurgical process of laterite nickel ore mainly includes pressure acid leaching, atmospheric leaching and heap leaching, etc. Among them, the pressure acid leaching needs ore sample selection, pressure acid leaching, continuous countercurrent washing, alkali neutralization and precipitation impurity removal and nickel and cobalt precipitation steps. The high pressure kettle has high maintenance cost, difficult debugging and easy corrosion of equipment during pressure leaching, resulting in high production cost. The atmospheric leaching process uses a reducing agent to reduce leaching under acidic conditions, and sodium carbonate is added to the leaching solution for neutralization and hydrolysis to remove impurities. This method has high sodium content and large auxiliary material consumption. The heap leaching process has low metal salt solution concentration and high iron and aluminum impurities in the leaching solution. With the trend of many enterprises' battery technology route towards high-nickel batteries, there is a strong demand for high-nickel batteries, and it is urgent to explore the technology for extracting nickel and cobalt from laterite nickel ore nickel-cobalt-manganese hydroxide intermediate product. SUMMARY

[0005] The present application is made based on the inventors' discovery and understanding of the following facts and problems:

[0006] The prior art technology for extracting nickel and cobalt from nickel-cobalt-manganese hydroxide intermediate product (MHP) of laterite nickel ore mainly adopts a hydrometallurgical process, that is, MHP is mixed with concentrated sulfuric acid and water to prepare a slurry, then hydrogen peroxide and sodium pyrosulfite are added for reduction leaching, the leaching slurry (containing nickel, cobalt, manganese, iron, aluminum, silicon, etc.) is adjusted to pH 4.0-5.0 by adding nickel carbonate and sodium carbonate to remove iron and aluminum, the slurry after removal of iron and aluminum is filtered under pressure, and silicon, iron and aluminum are separated from nickel, cobalt and manganese metal ions in the form of precipitates, and the nickel-cobalt-manganese sulfate solution is subjected to P204 manganese extraction and P507 cobalt extraction to obtain cobalt sulfate and nickel sulfate solutions, the P204 manganese extraction solution is subjected to organic dilute acid back extraction to obtain a back manganese solution, the back manganese solution is subjected to calcium removal by fluorination, and then is subjected to P204 full extraction and full back extraction to remove fluorine again to obtain a high-purity manganese sulfate solution.

[0007] However, the above method has the following problems: 1. The method uses hydrogen peroxide and sodium pyrosulfite for leaching, which increases the cost of extracting nickel and cobalt, and the addition of sodium pyrosulfite introduces a large amount of sodium ions, resulting in high sodium content in the leaching solution, high treatment cost, and product sodium content exceeding the standard; 2. The method leaches all the manganese in MHP into the solution, increasing the consumption of acid and alkali and greatly increasing the treatment cost; 3. Silicon is removed during the removal of iron and aluminum, and due to the high adsorption of silicon, the loss of valuable metals such as nickel and cobalt increases during the removal of iron and aluminum, and the direct recovery rate of nickel and cobalt decreases.

[0008] The present application aims to at least solve one of the technical problems in the related art. To this end, an embodiment of the present application proposes a method for leaching and purifying nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore, which has high valuable metal yield, reduces the consumption of acid and alkali, reduces the treatment cost, and has simple process operation and reduces the loss of materials in the turnover process.

[0009] The method for leaching and purifying nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore according to an embodiment of the present application comprises the following steps:

[0010] (1) adding nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore into a sulfuric acid solution for acid leaching to obtain an acid leaching mixture;

[0011] (2) mixing the nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore with water to prepare a slurry by ball milling to obtain a slurry;

[0012] (3) adding the slurry obtained in step (2) into the acid leaching mixture obtained in step (1) to adjust the pH, and filtering after reaction to obtain a leaching solution and a leaching residue;

[0013] (4) adding an alkaline solution to the leaching solution obtained in step (3) to adjust the pH, and filtering after reaction to obtain a solution after removal of iron and aluminum and an iron and aluminum residue.

[0014] The method for leaching and purifying the nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore has the following advantages and technical effects: 1. The method reduces the content of nickel and cobalt in the leaching residue by high-acid leaching, so that the yield of valuable metal leaching and purification is high; 2. The method prevents high-valence manganese in the nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore from being leached, avoids the need for subsequent separation and treatment of manganese and nickel-cobalt (extraction), cancels the use of sodium pyrosulfite and hydrogen peroxide, shortens the treatment process, avoids the introduction of sodium, and reduces the consumption of neutralizing agent and the treatment cost; 3. The method uses high-acid leaching to convert the difficult-to-filter silica gel into silica with good filterability, which is left in the leaching residue, reduces the amount of iron and aluminum slag generated in the subsequent iron and aluminum removal process, and effectively reduces the loss of nickel and cobalt in the leaching residue; 4. The method simplifies the process operation, has low input cost, reduces the material turnover process, reduces the material loss in the turnover process, and is suitable for large-scale industrial production.

[0015] In some embodiments, the pH of the acid leaching in step (1) is less than 0.5.

[0016] In some embodiments, the temperature of the acid leaching in step (1) is 75-95 DEG C, the acid leaching time is 2-3 h, and the stirring speed is 400-600 rpm / min.

[0017] In some embodiments, the liquid-solid ratio of the nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore to water in step (2) is 1-2:1.

[0018] In some embodiments, the pH is adjusted to 1-3 in step (3), the reaction temperature is 70-85 DEG C, and the reaction time is 1.5-2.5 h.

[0019] In some embodiments, the alkaline solution in step (4) includes at least one of sodium hydroxide solution, sodium carbonate solution, sodium bicarbonate solution, and ammonium carbonate solution; and / or, the pH is adjusted to 4.0-5.0, the reaction temperature is 75-95 DEG C, and the reaction time is 2-4 h.

[0020] In some embodiments, the method further comprises adding the slurry obtained in step (2) to the leaching solution obtained in step (3), adjusting the pH to 3.5-4.5, and reacting at 75-95 DEG C for 2-3 h.

[0021] In some embodiments, the method further comprises adding a sulfuric acid solution to the leaching residue obtained in step (3) for pickling, and filtering to obtain pickling residue and pickling solution.

[0022] In some embodiments, the temperature of the acid washing is 50-60℃, the pH of the acid washing is less than 1.0, the time of the acid washing is 0.5-2h, and the acid washing solution is returned to the acid leaching process of step (1).

[0023] In some embodiments, the acid washing residue is subjected to water washing treatment, the temperature of the water washing is 50-60℃, the time of the water washing is 0.5-2h, and the water washing solution is returned to the acid washing treatment process. BRIEF DESCRIPTION OF DRAWINGS

[0024] Figure 1 is a process flow diagram of a method for leaching and purifying a nickel-cobalt-manganese hydroxide intermediate product of a laterite nickel ore according to an embodiment of the present application;

[0025] Figure 2 is a process flow diagram of a method for leaching and purifying a nickel-cobalt-manganese hydroxide intermediate product of a laterite nickel ore according to embodiment 1. DETAILED DESCRIPTION

[0026] Embodiments of the present application are described in detail below, examples of which are shown in the accompanying drawings. The embodiments described below with reference to the accompanying drawings are exemplary and are intended to explain the present application, and cannot be understood as limiting the present application.

[0027] As shown in Figure 1 , a method for leaching and purifying a nickel-cobalt-manganese hydroxide intermediate product (MHP) of a laterite nickel ore according to an embodiment of the present application includes the following steps:

[0028] (1) adding MHP to a sulfuric acid solution for acid leaching to obtain an acid leaching mixture;

[0029] (2) mixing and ball-milling MHP with water to obtain a slurry;

[0030] (3) adding the slurry obtained in step (2) to the acid leaching mixture obtained in step (1) to adjust the pH, and after reaction, filtering to obtain a leaching solution and a leaching residue;

[0031] (4) adding an alkaline solution to the leaching solution obtained in step (3) to adjust the pH, and after reaction, filtering to obtain a post-iron and aluminum removal solution and an iron and aluminum residue.

[0032] The method for MHP leaching purification in the embodiment of the application reduces the content of nickel and cobalt in the leaching residue through high-acid leaching, so that the yield of valuable metals in leaching purification is high; in order to prevent the leaching of high-valence manganese in the nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore, avoid the need for separation of manganese from nickel and cobalt (extraction) in the subsequent process, cancel the use of sodium pyrosulfite and hydrogen peroxide, not only shorten the processing flow, but also avoid the introduction of sodium, in addition, reduce the consumption of neutralizing agent, reduce the processing cost; the method of high-acid leaching can transform the silica gel which is difficult to filter into silicic acid which has good filterability and remains in the leaching residue, reduce the amount of iron and aluminum slag generated in the subsequent iron and aluminum removal process, in addition, the silica gel can easily adsorb nickel and cobalt, and converting the silica gel into silicic acid which does not adsorb nickel and cobalt can effectively reduce the loss of nickel and cobalt in the leaching residue; the process operation is simplified, the input cost is low, the material turnover process is reduced, the material loss in the turnover process is reduced, and it is suitable for large-scale industrial production.

[0033] In some embodiments, preferably, in the step (1), the pH of the acid leaching is less than 0.5. Further preferably, in the step (1), the temperature of the acid leaching is 75-95℃, the acid leaching time is 2-3h, and the stirring speed is 400-600rpm / min. More preferably, in the step (1), the concentration of the sulfuric acid solution is 93-98%.

[0034] In the embodiment of the application, in the step (1), the pH in the acid leaching process is preferably controlled in the range of 0-0.5, and under the condition of high acid, high-valence nickel can oxidize manganese ions to become high-valence manganese which cannot be leached by acid leaching, thereby reducing the content of manganese in the leaching solution and further reducing the subsequent processing pressure, while nickel ions enter the leaching solution to improve the yield thereof; if the pH is controlled too low, more MHP slurry is needed for subsequent pH adjustment, and if the pH is controlled too high, the MHP leaching effect is poor and the yield of nickel and cobalt valuable metals cannot be improved.

[0035] In some embodiments, preferably, in the step (2), the liquid-solid ratio of the MHP to water is 1-2:1.

[0036] In some embodiments, preferably, in the step (3), the pH is adjusted to 1-3, the reaction temperature is 70-85℃, and the reaction time is 1.5-2.5h. Further preferably, the pH is adjusted to 1.65-1.75.

[0037] In the embodiment of the application, in the step (3), the pH is controlled in the range of 1-3, which can better selectively leach nickel and cobalt and retain high-valence manganese in the leaching residue, thereby reducing the leaching rate of metallic manganese, reducing the amount of metallic manganese extracted in the subsequent extraction system, reducing the consumption of acid and alkali, greatly reducing the cost, and reducing the leaching of other impurities such as silicon and iron.

[0038] In some embodiments, preferably, in step (4), the alkaline solution includes at least one of sodium hydroxide solution, sodium carbonate solution, sodium bicarbonate solution, and ammonium carbonate solution; and / or, the pH is adjusted to 4.0–5.0, the reaction temperature is 75–95°C, and the reaction time is 2–4 h. More preferably, the concentration of the alkaline solution is 10–20 wt%.

[0039] In this embodiment of the invention, in step (4), the pH of iron and aluminum removal is controlled within the range of 4.0 to 5.0, which is beneficial for the effective removal of iron and aluminum. If the pH is too low, the removal of iron and aluminum will be incomplete and the effect of removing iron and aluminum will be poor. If the pH is too high, it will increase the loss of nickel and cobalt, thereby reducing the yield of nickel and cobalt.

[0040] In some embodiments, preferably, the process further includes adding the slurry obtained in step (2) to the leachate obtained in step (3), adjusting the pH to 3.5 to 4.5, and reacting at 75 to 95°C for 2 to 3 hours.

[0041] In this embodiment of the invention, slurry is added to the high-acid leachate first, which can pre-neutralize the pH of the high-acid leachate and reduce the consumption of alkali solution during subsequent iron and aluminum removal.

[0042] In some embodiments, preferably, the process further includes adding sulfuric acid solution to the leaching residue obtained in step (3) for acid washing, and filtering to obtain acid-washed residue and acid-washing solution. More preferably, the acid washing temperature is 50–60°C, the pH of the acid washing is less than 1.0, the acid washing time is 0.5–2 hours, and the acid-washing solution is returned to the acid leaching process in step (1). More preferably, the acid-washed residue is subjected to water washing at a temperature of 50–60°C for 0.5–2 hours, and the water washing solution is returned to the acid washing process.

[0043] In this embodiment of the invention, the pH is controlled below 1.0 during the acid washing process of the leaching residue. If the pH is too high, only a small amount of nickel in the leaching residue will dissolve in the solution, resulting in incomplete cleaning and increased nickel loss. After acid washing and water washing, the nickel content in the manganese slag can be effectively controlled below 0.5%, thereby improving the nickel yield.

[0044] The technical solution of the present invention will be described in detail below with reference to the embodiments and accompanying drawings.

[0045] Example 1

[0046] like Figure 2 As shown, the leaching and purification method for laterite nickel-cobalt-manganese hydroxide intermediate (MHP) in this embodiment includes the following steps:

[0047] (1) Take 660 g of MHP, the elemental content of which is shown in Table 1, add 150 mL of water, then uniformly add 170 mL of 93% sulfuric acid to adjust the pH to 0.2, and react at 75°C and a stirring speed of 400 rpm / min for 3 h to obtain an acid leaching mixture;

[0048] (2) Ball mill 280 g of MHP and 280 mL of water to obtain a slurry; add the slurry to the acid leaching mixture obtained after step (1), adjust the pH to 1.71, and react at 75°C and a stirring speed of 400 rpm / min for 1.5 h; stop stirring, and naturally settle at 55°C for 60 min to obtain an overflow supernatant and a bottom thick slurry; filter the bottom thick slurry to obtain a leaching residue, and the analysis results of the leaching residue are shown in Table 2; the filtrate is a bottom thick slurry leaching filtrate; and mix the bottom thick slurry leaching filtrate and the overflow supernatant to obtain a high-acid leaching solution;

[0049] (3) Add the slurry to the high-acid leaching solution to adjust the pH to 3.98, then add 100 mL of 10% sodium carbonate solution to the high-acid leaching solution to adjust the pH to 4.97, and filter after reacting at 75°C and a stirring speed of 400 rpm / min for 2 h to obtain an iron and aluminum removed solution and an iron and aluminum residue, and the analysis results of the iron and aluminum removed solution are shown in Table 3;

[0050] (4) Add concentrated sulfuric acid and water to the obtained leaching residue to perform pickling, the solid-liquid ratio of the leaching residue and water is 1:1, the pH is controlled to be 0.1, the temperature is 55°C, and the pickling is performed for 1 h to obtain a pickling residue; add a certain amount of water to the pickling residue to perform water washing, the solid-liquid ratio of the pickling residue and water is 1:1, the temperature is 55°C, and the water washing is performed for 1 h to obtain a manganese residue, and the analysis results of the manganese residue are shown in Table 4.

[0051] After calculation, the yield of nickel in this embodiment is 99.95%, the yield of cobalt is 99.43%, the leaching rate of manganese is 56.28%, and the leaching rate of silicon is 39.15%.

[0052] Example 2

[0053] (1) Take 670 g of MHP, the elemental content of which is shown in Table 1, add 150 mL of water, then uniformly add 175 mL of 93% sulfuric acid to adjust the pH to 0.16, and react at 75°C and a stirring speed of 400 rpm / min for 3 h to obtain an acid leaching mixture;

[0054] (3) adding the slurry into the high acid leaching solution, adjusting pH to 4.0, adding 100 mL of 10% sodium carbonate solution into the high acid leaching solution to adjust pH to 5.0, and then filtering after reacting at 75°C and with stirring speed of 400 rpm / min for 2 h to obtain the post-iron and aluminum removal solution and iron and aluminum residue, and the analysis results of the post-iron and aluminum removal solution are shown in Table 3;

[0055] (3) adding the slurry into the high acid leaching solution, adjusting pH to 4.0, adding 100 mL of 10% sodium carbonate solution into the high acid leaching solution to adjust pH to 5.0, and then filtering after reacting at 75°C and with stirring speed of 400 rpm / min for 2 h to obtain the post-iron and aluminum removal solution and iron and aluminum residue, and the analysis results of the post-iron and aluminum removal solution are shown in Table 3;

[0056] (4) adding concentrated sulfuric acid and water into the obtained leaching residue to perform acid washing, the solid-liquid ratio of the leaching residue and water is 1:1, pH is controlled to be 0.4, the temperature is 55°C, and the acid washing is performed for 1 h to obtain an acid washing residue, a certain amount of water is added into the acid washing residue to perform water washing, the solid-liquid ratio of the acid washing residue and water is 1:1, the temperature is 55°C, and the water washing is performed for 1 h to obtain a manganese residue, and the analysis results of the manganese residue are shown in Table 4.

[0057] After calculation, the yield of nickel is 99.96%, the yield of cobalt is 99.45%, the leaching rate of manganese is 56.7%, and the leaching rate of silicon is 39.32% in this embodiment.

[0058] Example 3

[0059] (1) adding 600 g of MHP into 150 mL of water, the element content of the MHP is shown in Table 1, and then adding 160 mL of 93% sulfuric acid to adjust pH to 0.21, and then reacting at 75°C and with stirring speed of 400 rpm / min for 3 h to obtain an acid leaching mixture;

[0060] (2) adding 300 g of MHP and 300 mL of water to perform ball milling to obtain a slurry; adding the slurry into the acid leaching mixture obtained after the acid leaching in step (1), adjusting pH to 1.75, and then reacting at 75°C and with stirring speed of 400 rpm / min for 1.5 h; stopping stirring, and then naturally settling at 55°C for 60 min to obtain overflow supernatant and underflow thick slurry; filtering the underflow thick slurry to obtain a leaching residue, and the analysis results of the leaching residue are shown in Table 2, the filtrate is a leaching filtrate of the underflow thick slurry, and the leaching filtrate of the underflow thick slurry is mixed with the overflow supernatant to obtain a high acid leaching solution;

[0061] (3) The slurry was added to the high-acid leaching solution to adjust the pH to 4.0, and 95 mL of 10% sodium carbonate solution was added to the high-acid leaching solution to adjust the pH to 5.0. After reaction at 75°C and a stirring speed of 400 rpm / min for 2 h, filtration was performed to obtain the iron and aluminum removed solution and iron and aluminum residue. The analysis results of the iron and aluminum removed solution are shown in Table 3.

[0062] (4) Concentrated sulfuric acid was added to the obtained leaching residue for pickling, and the solid-liquid ratio of the leaching residue to water was 1:1. The pH was controlled at 0.7, the temperature was 55°C, and the pickling was performed for 1 h. The pickling residue was filtered, and a certain amount of water was added to the pickling residue for water washing. The solid-liquid ratio of the pickling residue to water was 1:1, the temperature was 55°C, and the water washing was performed for 1 h. The manganese residue was filtered, and the analysis results of the manganese residue are shown in Table 4.

[0063] After calculation, the yield of nickel in this embodiment was 99.93%, the yield of cobalt was 99.41%, the leaching rate of manganese was 56.23%, and the leaching rate of silicon was 39.11%.

[0064] Example 4

[0065] The treatment method of this embodiment was the same as that of Example 1, except that in step (1), the pH of the acid leaching system was adjusted to 1.

[0066] After calculation, the yield of nickel in this embodiment was 99.56%, the yield of cobalt was 99.22%, the leaching rate of manganese was 54.18%, and the leaching rate of silicon was 37.82%.

[0067] Example 5

[0068] The treatment method of this embodiment was the same as that of Example 1, except that in step (2), after the addition of the slurry, the pH of the acid leaching mixture was adjusted to 3.5.

[0069] After calculation, the yield of nickel in this embodiment was 95.10%, the yield of cobalt was 96.34%, the leaching rate of manganese was 50.25%, and the leaching rate of silicon was 33.60%.

[0070] Table 1 Element analysis table of nickel-cobalt-manganese hydroxide intermediate product from laterite nickel ore in Examples 1-5

[0071] Ni Co Mn Ca Mg Fe Cu Zn Na Cr Al Si Example 1 15.660 1.390 2.190 0.057 0.880 0.042 0.041 0.330 0.052 0.0095 0.072 0.098 Example 2 15.610 1.470 2.170 0.060 0.870 0.044 0.040 0.350 0.055 0.0094 0.077 0.090 Example 3 15.560 1.361 2.210 0.055 0.870 0.051 0.041 0.350 0.054 0.010 0.070 0.098 Example 4 15.561 1.384 2.185 0.053 0.883 0.046 0.041 0.340 0.051 0.0097 0.075 0.096 Example 5 15.625 1.388 2.197 0.055 0.879 0.042 0.041 0.350 0.052 0.089 0.071 0.093

[0072] Table 2 Element analysis table of leaching residue in Examples 1-5

[0073] Ni Co Mn Ca Mg Fe Cu Zn Al Si Example 1 9.21 1.15 27.61 0.018 0.58 0.74 0.12 0.22 0.073 1.27 Example 2 9.54 1.05 20.23 0.27 0.48 1.52 0.051 0.19 0.083 2.24 Example 3 8.89 0.89 35.15 0.035 0.53 2.18 0.047 0.49 0.062 2.53 Example 4 11.95 1.10 35.20 0.022 0.39 2.53 0.19 0.34 0.074 2.12 Example 5 13.35 1.49 34.25 0.029 0.51 3.35 0.062 0.25 0.382 2.02

[0074] Table 3 Composition analysis table of iron and aluminum removed solution obtained in Examples 1-5 g / L

[0075] Ni Co Mn Ca Mg Cu Zn Na Si Example 1 113.56 13.37 6.13 0.039 4.13 0.098 2.08 2.23 0.05 Example 2 105.46 8.12 4.83 0.30 6.56 0.017 1.44 2.13 0.05 Example 3 99.03 7.90 4.74 0.26 6.00 0.014 1.42 1.96 0.049 Example 4 101.91 11.88 7.50 0.24 4.27 0.072 2.09 1.10 0.034 Example 5 98.10 14.65 4.32 0.044 2.41 0.071 3.12 0.58 0.046

[0076] Table 4 Elemental analysis of manganese slag in Examples 1-5

[0077] Ni Co Mn Ca Mg Fe Cu Zn Al Si Example 1 0.36 0.33 52.87 0.010 0.012 2.55 0.032 0.044 0.021 1.25 Example 2 0.39 0.43 48.15 0.013 0.020 2.16 0.037 0.038 0.020 1.34 Example 3 0.45 0.48 47.25 0.019 0.015 2.95 0.049 0.054 0.029 1.19 Example 4 0.77 0.60 44.84 0.021 0.026 2.34 0.046 0.038 0.019 1.98 Example 5 0.97 0.92 48.10 0.032 0.035 2.87 0.059 0.036 0.036 2.11

[0078] In this disclosure, the terms "one embodiment", "some embodiments", "an example", "a specific example", or "some examples" mean that a particular feature, structure, material, or characteristic is included in at least one embodiment or example of the present application. The illustrative appearances of the above-mentioned terms in various places in the specification are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics can be combined in any suitable manner in one or more embodiments or examples. Moreover, the terms "first", "second", "third", etc. are used herein merely as identifiers for different elements, regions, layers, or sections, and are not intended to denote a spatial or chronological priority or sequence.

[0079] Although the above-mentioned embodiments have been shown and described, it is to be understood that these embodiments are exemplary only, and that changes, modifications, substitutions and variations can be made thereto without departing from the scope of the present application.

Claims

1. A process for leaching purification of nickel cobalt manganese hydroxide intermediate product of laterite nickel ore, characterized by, The method comprises the following steps: (1) adding the nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore into a sulfuric acid solution for acid leaching to obtain an acid leaching mixture; the pH of the acid leaching is less than 0.5; (2) mixing and ball-milling the nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore with water to prepare a slurry; the liquid-solid ratio of the nickel-cobalt-manganese hydroxide intermediate product of laterite nickel ore to water is 1:1; (3) adding the slurry obtained in step (2) into the acid leaching mixture obtained in step (1) to adjust the pH, and then filtering to obtain a leaching solution and a leaching residue after reaction; (4) adding an alkaline solution to the leaching solution obtained in step (3) to adjust the pH, and then filtering to obtain a solution after removing iron and aluminum and an iron and aluminum residue after reaction.

2. The process for leaching and cleaning of nickel-cobalt-manganese hydroxide intermediate from laterite nickel ore according to claim 1, characterized in that, In step (1), the temperature of the acid leaching is 75-95℃, the acid leaching time is 2-3h, and the stirring speed is 400-600rpm / min.

3. The process for leaching and cleaning of nickel-cobalt-manganese hydroxide intermediate from laterite nickel ore according to claim 1, characterized in that, In step (3), the pH is adjusted to 1-3, the reaction temperature is 70-85℃, and the reaction time is 1.5-2.5h.

4. The process for leaching and cleaning of nickel-cobalt-manganese hydroxide intermediate from laterite nickel ore according to claim 1, characterized in that, In step (4), the alkaline solution comprises at least one of a sodium hydroxide solution, a sodium carbonate solution, a sodium bicarbonate solution, and an ammonium carbonate solution; and / or, the pH is adjusted to 4.0-5.0, the reaction temperature is 75-95℃, and the reaction time is 2-4h.

5. The process for leaching and cleaning of nickel-cobalt-manganese hydroxide intermediate from laterite nickel ore according to claim 1, characterized in that, Further comprising adding the slurry obtained in step (2) to the leaching solution obtained in step (3), adjusting the pH to 3.5-4.5, and reacting at 75-95℃ for 2-3h.

6. The process for leaching and cleaning of nickel-cobalt-manganese hydroxide intermediate product of nickel laterite ores according to claim 1 or 5, characterized in that, Further comprising adding a sulfuric acid solution to the leaching residue obtained in step (3) for pickling treatment, and filtering to obtain a pickling residue and a pickling solution.

7. The process for leaching and cleaning of nickel-cobalt-manganese hydroxide intermediate from laterite nickel ore according to claim 6, characterized in that, The pickling temperature is 50-60℃, the pickling pH is less than 1.0, the pickling time is 0.5-2h, and the pickling solution is returned to the acid leaching process in step (1).

8. The process for leaching and cleaning of nickel-cobalt-manganese hydroxide intermediate from laterite nickel ore according to claim 6, characterized in that, The pickling residue is subjected to water washing treatment, the water washing temperature is 50-60℃, the water washing time is 0.5-2h, and the water washing solution is returned to the pickling treatment process.

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