CN108913883B - Method for producing nickel cobalt hydroxide by laterite-nickel ore hydrometallurgy - Google Patents
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Abstract
The method for producing the nickel cobalt hydroxide by the laterite-nickel ore hydrometallurgy is characterized by comprising the following steps: s1, pressure leaching or atmospheric pressure leaching the laterite-nickel ore to obtain leached ore pulp; s2, performing pre-neutralization treatment on the leached ore pulp, and controlling the pH value of the end point to be 1.1-1.8; s3, removing iron and aluminum from the ore pulp subjected to the preneutralization treatment, controlling the pH value of the end point to be 3.5-4.2, and introducing compressed air in the process; s4, washing the ore pulp subjected to de-ironing by CCD; s5, deeply removing impurities from the overflow washed by the CCD, controlling the pH value of the end point to be 4.8-5.2, and introducing compressed air in the process; and S6, precipitating the overflow subjected to deep impurity removal by using lime milk to obtain a gypsum-nickel hydroxide cobalt mixture, and separating the gypsum-nickel hydroxide cobalt mixture to obtain a nickel cobalt hydroxide product. The method omits the press filtration process of the deironing aluminum slag before the deironing aluminum is placed in the CCD for washing; and the gypsum and the nickel cobalt hydroxide have obvious granularity difference, and are easy to separate by a solid-solid grading device, so that the production cost is reduced.
Description
Technical Field
The invention belongs to the field of nickel and cobalt hydrometallurgy, and particularly relates to a method for producing nickel and cobalt hydroxide by laterite nickel ore hydrometallurgy.
Background
Currently, the precipitation of nickel and cobalt in the hydrometallurgical process of laterite nickel ores generally comprises the following steps: firstly, carrying out acid leaching on laterite-nickel ore; then carrying out preneutralization, CCD washing, first-stage iron and aluminum removal and deep impurity removal; finally, precipitating nickel and cobalt in the acid leaching solution by using sodium hydroxide as a precipitator to form nickel and cobalt precipitation solution; and then carrying out thickening treatment on the nickel cobalt precipitation solution to obtain nickel hydroxide cobalt precipitate (nickel hydroxide and cobalt hydroxide).
However, the first stage of iron and aluminum removal is arranged behind the CCD, a filter pressing workshop needs to be built to separately process iron and aluminum slag, the investment is high, and the later stage operation cost is high; when sodium hydroxide is used as a precipitator, on one hand, the cost is high, and on the other hand, due to strong alkalinity, partial over-alkali is easily formed in feeding in the industrial practical operation process, so that the precipitation granularity is small, the sedimentation energy is poor, the separation speed in the concentration separation process is slow, the concentration of the concentration underflow is low, and the later separation is not facilitated. In addition, sodium hydroxide is adopted as a precipitator, and the obtained nickel cobalt hydroxide filter cake has high water content and is not beneficial to subsequent treatment.
Disclosure of Invention
In order to solve the defects, the invention provides a method for producing nickel cobalt hydroxide by laterite nickel ore hydrometallurgy.
The method for producing the nickel cobalt hydroxide by the laterite-nickel ore hydrometallurgy comprises the following steps: s1, pressure leaching or atmospheric pressure leaching the laterite-nickel ore to obtain leached ore pulp; s2, performing pre-neutralization treatment on the leached ore pulp, and controlling the pH value of the end point to be 1.1-1.8; s3, removing iron and aluminum from the ore pulp subjected to the preneutralization treatment, controlling the pH value of the end point to be 3.5-4.2, and introducing compressed air in the process; s4, washing the ore pulp subjected to de-ironing by CCD; s5, deeply removing impurities from the overflow washed by the CCD, controlling the pH value of the end point to be 4.8-5.2, and introducing compressed air in the process; and S6, precipitating the overflow subjected to deep impurity removal by using lime milk to obtain a gypsum-nickel hydroxide cobalt mixture, and separating the gypsum-nickel hydroxide cobalt mixture to obtain a nickel cobalt hydroxide product.
According to an embodiment of the invention, the lateritic nickel ore is limonite type lateritic nickel ore, eluvial ore type lateritic nickel ore, or a mixture of two minerals.
According to another embodiment of the invention, in the step S1, the leaching temperature is 98-260 ℃, the leaching time is 0.5-4h, and the end-point acidity value is controlled to be 20-60 g/L.
According to another embodiment of the present invention, in the step S2, the neutralizing agent used in the pre-neutralization treatment is selected from one or more of limestone, lime milk, magnesite pulp, magnesia pulp, and sodium hydroxide, and sodium sulfate is further added in the pre-neutralization treatment.
According to another embodiment of the present invention, in the step S3, the neutralizing agent for removing iron and aluminum is selected from one or more of limestone, lime milk, magnesite pulp, magnesia powder pulp, magnesium oxide and sodium hydroxide.
According to another embodiment of the present invention, in the step S4, the CCD washing stages are 4 to 7 stages, and the washing ratio is 2 to 4; and the bottom flow after the CCD washing is neutralized by lime milk, the pH value of the end point is controlled to be 8.5-9.0, and compressed air is introduced in the process.
According to another embodiment of the present invention, in the step S5, the neutralizing agent for deep impurity removal is selected from one or more of limestone, lime cream, magnesite pulp, magnesia powder pulp, magnesium oxide and sodium hydroxide; and the underflow after the deep impurity removal is returned to be mixed with the leached ore pulp for reaction.
According to another embodiment of the invention, in the step S6, after the lime milk performs a first-stage nickel and cobalt precipitation on the overflow subjected to deep impurity removal, part of the underflow returns to the first-stage nickel and cobalt precipitation, and part of the underflow is separated by the solid-solid separation device.
According to another embodiment of the present invention, the solid-solid separation device is a fluidized solid-solid separation device, the overflow after the first stage of nickel and cobalt precipitation is used to dilute the part of the underflow before entering the separation device, the diluted underflow is pumped into the separation device for separation, the overflow is subjected to concentration filtration to obtain the nickel and cobalt hydroxide product, and the underflow is returned to be mixed with the leached ore pulp.
According to another embodiment of the invention, the lime milk is used for carrying out secondary nickel and cobalt precipitation on the overflow after the overflow subjected to deep impurity removal is precipitated, one or more of lime milk, sodium hydroxide and magnesium oxide is used as a precipitator, the end point pH value is controlled to be 8.5-9.0, the underflow after reaction is returned to be mixed with the leached ore pulp, and the overflow is used for washing the CCD.
According to another embodiment of the invention, the concentration of the lime milk is controlled to be 15-25 wt.%, and the mass ratio of the lime milk to Ni in the overflow from the deep impurity removal is CaO to Ni which is 1.6-2.5.
The method omits the press filtration process of the deironing aluminum slag before the deironing aluminum is placed in the CCD for washing; and the gypsum and the nickel cobalt hydroxide have obvious granularity difference, and are easy to separate by a solid-solid grading device, so that the production cost is reduced. The whole process of the invention is compact and reasonable, and the new technology is well embedded into the process flow of the laterite-nickel ore hydrometallurgy.
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The above and other features and advantages of the present invention will become more apparent by describing in detail exemplary embodiments thereof with reference to the attached drawings.
FIG. 1 is a flow chart of a method of making an embodiment of the present invention.
FIG. 2 is a flow chart of a method of making an embodiment of the present invention.
Detailed Description
The present invention will be described in detail with reference to the following embodiments.
The invention provides a method for producing nickel cobalt hydroxide by laterite nickel ore hydrometallurgy. The method comprises the steps of leaching laterite-nickel ore under pressure or atmospheric pressure, precipitating nickel and cobalt by lime milk after leachate is subjected to preneutralization, aluminum removal, CCD washing and deep impurity removal, separating a precipitated gypsum-nickel hydroxide cobalt mixture by a solid-solid separation device to obtain a nickel and cobalt hydroxide product, and recovering nickel and cobalt by a preneutralization process after gypsum containing a small amount of nickel and cobalt returns to leaching.
Specifically, as shown in fig. 1, the method for producing nickel cobalt hydroxide by hydrometallurgical smelting of lateritic nickel ore of the present invention includes the following steps: s1, pressure leaching or atmospheric pressure leaching the laterite-nickel ore to obtain leached ore pulp; s2, performing pre-neutralization treatment on the leached ore pulp, and controlling the pH value of the end point to be 1.1-1.8; s3, removing iron and aluminum from the ore pulp subjected to the preneutralization treatment, controlling the pH value of the end point to be 3.5-4.2, and introducing compressed air in the process; s4, washing the ore pulp subjected to de-ironing by CCD; s5, deeply removing impurities from the overflow washed by the CCD, controlling the pH value of the end point to be 4.8-5.2, and introducing compressed air in the process; and S6, precipitating the overflow subjected to deep impurity removal by using lime milk to obtain a gypsum-nickel hydroxide cobalt mixture, and separating the gypsum-nickel hydroxide cobalt mixture to obtain nickel cobalt hydroxide.
In detail, referring to fig. 2, in the step S1, the laterite-nickel ore is limonite type laterite-nickel ore, residual ore type laterite-nickel ore or a mixture of two minerals, the leaching temperature is 98-260 ℃, the leaching time is 0.5-4h, and the final acidity value is controlled at 20-60 g/L.
In step S2, the neutralizing agent used in the pre-neutralization treatment is one or more selected from limestone, lime milk, magnesite pulp, magnesia powder pulp, magnesium oxide and sodium hydroxide, and the pH value of the end point is controlled to be 1.1-1.8. Sodium sulfate was also added to the pre-neutralization treatment to provide sodium ions to remove ferric iron.
In step S3, the neutralizing agent used for removing iron and aluminum is one or more selected from limestone, lime milk, magnesite pulp, magnesia powder pulp, magnesium oxide and sodium hydroxide, and the pH value of the end point is controlled to be 3.5-4.2.
In the step S4, CCD washing is performed in a washing stage number of 4 to 7 and a washing ratio of 2 to 4. Bottom flow after washing the CCD is neutralized by lime milk, the pH value of the end point is controlled to be 8.5-9.0, and compressed air is introduced in the process. The nickel and cobalt in the liquid phase can be washed by CCD washing, and the overall recovery rate is improved. And neutralizing part of bottom flow and tailings after washing by the CCD and then discharging.
In the step S5, the neutralizing agent used for deep impurity removal is selected from one or more of limestone, lime milk, magnesite pulp, magnesia powder pulp, magnesium oxide and sodium hydroxide, and the pH value of the end point is controlled to be 4.8-5.2. And the underflow after deep impurity removal is returned to be mixed with the leached ore pulp for reaction. Removing iron, aluminum and chromium ions by deep impurity removal.
In the step S6, lime milk is used as a precipitator, the overflow subjected to deep impurity removal is subjected to first-stage nickel and cobalt precipitation, the precipitation reaction is followed by thickening, partial bottom flow of the first-stage nickel and cobalt precipitation is returned to be mixed with the lime milk, and partial bottom flow is treated by a fluidization separation device. The concentration of lime milk is controlled to be 15-25 wt.%, and the mass ratio of the amount of the lime milk to Ni in the overflow from deep impurity removal is 1.6-2.5. The mixing time is 1-10min, and the volume for mixing is 1-6 times of the volume of the filter pressing removal. The separation device is a fluidized solid-solid separation device, underflow ore pulp is diluted and pumped into the separation device, a certain amount of water is introduced, the separation device utilizes different settling speeds to concentrate and filter overflow and obtain a nickel cobalt hydroxide product, and underflow is calcium sulfate. The underflow contains a small amount of nickel and cobalt, and the underflow returns to be mixed with the leached ore pulp to react to recover the nickel and cobalt. And diluting the underflow ore pulp by adopting the first-stage nickel-cobalt-deposited dense overflow, wherein the dilution volume multiple of the underflow ore pulp is 2-4 times. After entering the separation device, the introduced water is concentrated and overflowed after the first-stage nickel and cobalt precipitation, and the volume of the introduced water is 0.4-1.2 times of that of the ore pulp. After the first-stage nickel and cobalt precipitation, the dense overflow is subjected to second-stage nickel and cobalt precipitation, the precipitator adopts lime milk, sodium hydroxide, magnesium oxide and the like, the pH value of the end point is controlled to be 8.5-9.0, the ore pulp is concentrated after the reaction, and the dense underflow returns to be mixed with the leached ore pulp for reaction to recover the nickel and cobalt. And part of overflow after the second-stage nickel-cobalt precipitation is used for washing the CCD, and part of overflow is neutralized with tailings.
Example 1
The limonite type laterite-nickel ore has the nickel content of 1.4 wt.%, the acid-ore ratio of 350kg/t ore and the leaching temperature of 240 ℃. After the leached ore pulp dissolves the mixture of the returned second-stage nickel-cobalt precipitation concentrated underflow ore pulp, the deep impurity removal precipitation concentrated ore pulp and the gypsum ore pulp after the first-stage nickel-cobalt precipitation separation, the magnesium oxide ore pulp with the concentration of 20 percent is added, and 5kg/m of the magnesium oxide ore pulp is added3Sodium sulfate in mineral slurry to pH 1.8. Adding the magnesia pulp continuously, introducing compressed air, adjusting the pH value to 3.8, then washing by a 6-grade CCD (charge coupled device), wherein the washing water is 2 times that of the magnesia pulp, neutralizing the underflow by lime milk, adding the magnesia pulp in the overflow, introducing the compressed air, adjusting the pH value to 5.0, and then thickening. The underflow returns to leaching, the overflow is used for precipitating nickel and cobalt, 20 percent lime milk is adopted for precipitation, CaO/Ni is 1.9, and the lime milk is mixed with 3 times of the first-stage nickel and cobalt precipitation dense underflow for 5 min. Then adding the nickel and cobalt precipitated in the liquid after deep impurity removal, diluting the bottom flow part to 3 times of the original volume after precipitation, entering a separator, and introducing water of which the volume is 0.8 times of the volume after dilution for separationAfter separation, overflow filtration is carried out, underflow gypsum is returned to be mixed with the leaching solution, the solution after the first-stage nickel and cobalt precipitation enters into second-stage nickel and cobalt precipitation, lime milk is adopted for precipitation, the underflow is mixed with the leaching solution after precipitation, and CCD washing and tailing neutralization are carried out on overflow.
The quality of the nickel hydroxide cobalt product obtained by the process is as follows:
34 wt.% of Ni, 3 wt.% of Ca, 1.2 wt.% of Mg, 5.6 wt.% of Mn and 58% of water content after filter pressing.
Example 2
The limonite type laterite-nickel ore and the residual ore type laterite-nickel ore have the mass ratio of 4:1, the nickel content is 1.6 wt.%, the acid-ore ratio is 480kg/t ore, and the leaching temperature is 240 ℃. After the leached ore pulp dissolves the mixture of the returned second-stage nickel-cobalt precipitation concentrated underflow ore pulp, the deep impurity removal precipitation concentrated ore pulp and the gypsum ore pulp after the first-stage nickel-cobalt precipitation separation, the magnesium oxide ore pulp with the concentration of 20 percent is added, and 5kg/m of the magnesium oxide ore pulp is added3Sodium sulfate in mineral slurry to pH 1.8. Adding the magnesia pulp continuously, introducing compressed air, adjusting the pH value to 3.8, then washing by a 6-grade CCD (charge coupled device), wherein the washing water is 2 times that of the magnesia pulp, neutralizing the underflow by lime milk, adding the magnesia pulp in the overflow, introducing the compressed air, adjusting the pH value to 5.0, and then thickening. The underflow returns to leaching, the overflow is used for precipitating nickel and cobalt, 20 percent lime milk is adopted for precipitation, CaO/Ni is 1.9, and the lime milk is mixed with 3 times of the first-stage nickel and cobalt precipitation dense underflow for 5 min. Then adding the solution after deep impurity removal to precipitate nickel and cobalt, diluting the underflow part to 3 times of the original volume after precipitation, entering a separator, introducing water which is 0.8 times of the volume of the diluted solution for separation, overflowing and filtering after separation, returning underflow gypsum to be mixed with the leaching solution, entering the solution after nickel and cobalt precipitation in the first stage into nickel and cobalt precipitation in the second stage, adopting lime milk for precipitation, mixing the underflow and the leaching solution after precipitation, overflowing to perform CCD washing and tailing neutralization.
The quality of the nickel hydroxide cobalt product obtained by the process is as follows:
34 wt.% of Ni, 3 wt.% of Ca, 1.2 wt.% of Mg, 5.6 wt.% of Mn and 58% of water content after filter pressing.
Example 3
The limonite type laterite-nickel ore has nickel content of 1.4 wt%, acid-ore ratio of 350kg/t ore and leaching temperature ofAt 240 ℃. After the leached ore pulp dissolves the mixture of the returned second-stage nickel-cobalt precipitation concentrated underflow ore pulp, the deep impurity removal precipitation concentrated ore pulp and the gypsum ore pulp after the first-stage nickel-cobalt precipitation separation, the magnesium oxide ore pulp with the concentration of 20 percent is added, and 5kg/m of the magnesium oxide ore pulp is added3Sodium sulfate in mineral slurry to pH 1.8. Adding the magnesia pulp continuously, introducing compressed air, adjusting the pH value to 3.8, then washing by a 6-grade CCD (charge coupled device), wherein the washing water is 2 times that of the magnesia pulp, neutralizing the underflow by lime milk, adding the magnesia pulp in the overflow, introducing the compressed air, adjusting the pH value to 5.0, and then thickening. The underflow returns to leaching, the overflow is used for precipitating nickel and cobalt, 20 percent lime milk is adopted for precipitation, CaO/Ni is 1.9, and the lime milk is mixed with the dense underflow of 3 times of the first-stage nickel and cobalt precipitation for 3 min. Then adding the solution after deep impurity removal to precipitate nickel and cobalt, diluting the underflow part to 3 times of the original volume after precipitation, entering a separator, introducing water which is 0.8 times of the volume of the diluted solution for separation, overflowing and filtering after separation, returning underflow gypsum to be mixed with the leaching solution, entering the solution after nickel and cobalt precipitation in the first stage into nickel and cobalt precipitation in the second stage, adopting lime milk for precipitation, mixing the underflow and the leaching solution after precipitation, overflowing to perform CCD washing and tailing neutralization.
The quality of the nickel hydroxide cobalt product obtained by the process is as follows:
35 wt.% of Ni, 3.5 wt.% of Ca, 0.8 wt.% of Mg and 5.3 wt.% of Mn, and the water content is 61% after filter pressing.
By adopting the method, the water content of the product is reduced by nearly 20 percent compared with the water content (up to 75 percent) of the product obtained by precipitating nickel and cobalt by adopting sodium hydroxide, the efficiency of equipment is greatly improved, and the freight cost is greatly saved.
The present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof, and it should be understood that various changes and modifications can be effected therein by one skilled in the art without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (9)
1. A method for producing nickel cobalt hydroxide by laterite-nickel ore hydrometallurgy is characterized by comprising the following steps:
s1, pressure leaching or atmospheric pressure leaching the laterite-nickel ore to obtain leached ore pulp;
s2, performing pre-neutralization treatment on the leached ore pulp, and controlling the pH value of the end point to be 1.1-1.8;
s3, removing iron and aluminum from the ore pulp subjected to the preneutralization treatment, controlling the pH value of the end point to be 3.5-4.2, and introducing compressed air in the process;
s4, carrying out CCD washing on the ore pulp subjected to aluminum removal, wherein the number of CCD washing stages is 4-7, and the washing ratio is 2-4; the bottom flow after the CCD washing is neutralized by lime milk, the pH value of the end point is controlled to be 8.5-9.0, and compressed air is introduced in the process;
s5, deeply removing impurities from the overflow washed by the CCD, controlling the pH value of the end point to be 4.8-5.2, and introducing compressed air in the process; and
s6, lime milk is adopted to carry out primary nickel and cobalt precipitation on overflow subjected to deep impurity removal, the concentration of the lime milk is controlled to be 15-25 wt%, the mass ratio of the lime milk to Ni in the overflow subjected to deep impurity removal is CaO to Ni is 1.6-2.5, partial underflow of the primary precipitated nickel and cobalt returns to be mixed with the lime milk, partial underflow of the primary precipitated nickel and cobalt returns to a separation device to obtain a gypsum-nickel and cobalt hydroxide mixture, and the gypsum-nickel and cobalt hydroxide mixture is separated to obtain a nickel and cobalt hydroxide product; after nickel and cobalt are precipitated at the first stage, carrying out secondary nickel and cobalt precipitation on the concentrated overflow, controlling the pH value of the end point to be 8.5-9.0, carrying out concentration on the ore pulp after reaction, and returning the concentrated underflow to be mixed with the leached ore pulp for reaction to recover the nickel and cobalt; and part of overflow after the two-stage nickel-cobalt precipitation is used for washing the CCD, and part of overflow is neutralized with tailings.
2. The method according to the claim 1, characterized in that the lateritic nickel ores are limonite type lateritic nickel ores, alluvial ore type lateritic nickel ores, or mixtures of both minerals.
3. The method as claimed in claim 1, wherein in the step of S1, the leaching temperature is 98-260 ℃, the leaching time is 0.5-4h, and the end-point acidity value is controlled at 20-60 g/L.
4. The method as claimed in claim 1, wherein in the step S2, the neutralizing agent used in the pre-neutralization treatment is selected from one or more of limestone, lime milk, magnesite pulp, magnesia pulp, and sodium hydroxide, and sodium sulfate is added in the pre-neutralization treatment.
5. The method as claimed in claim 1, wherein in the step S3, the neutralizing agent for removing iron and aluminum is selected from one or more of limestone, lime milk, magnesite pulp, magnesia powder pulp, magnesium oxide and sodium hydroxide.
6. The method as claimed in claim 1, wherein in the step S5, the neutralizing agent for deep impurity removal is selected from one or more of limestone, lime milk, magnesite pulp, magnesia powder pulp, magnesium oxide and sodium hydroxide; and the underflow after the deep impurity removal is returned to be mixed with the leached ore pulp for reaction.
7. The method of claim 1, wherein in the step S6, after the lime milk is used for carrying out primary nickel and cobalt precipitation on the overflow subjected to deep impurity removal, part of underflow is returned to the primary nickel and cobalt precipitation, and part of underflow is separated by a solid-solid separation device.
8. The method of claim 7, wherein the solid-solid separation device is a fluidized solid-solid separation device, the overflow of the primary precipitated nickel and cobalt is used to dilute the partial underflow before entering the separation device, the diluted underflow is pumped into the separation device for separation, the overflow is subjected to concentration filtration to obtain the nickel and cobalt hydroxide product, and the underflow is returned to be mixed with the leached ore pulp.
9. The method as claimed in claim 7, characterized in that the lime milk is used for secondary nickel cobalt precipitation of the overflow after precipitation of the overflow subjected to deep impurity removal, the precipitator is one or more of lime milk, sodium hydroxide and magnesium oxide, the end point pH value is controlled to be 8.5-9.0, the underflow after reaction is returned to be mixed with the leached ore pulp, and the overflow is used for washing the CCD.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201811045949.8A CN108913883B (en) | 2018-09-07 | 2018-09-07 | Method for producing nickel cobalt hydroxide by laterite-nickel ore hydrometallurgy |
| AU2019222853A AU2019222853B2 (en) | 2018-09-07 | 2019-08-28 | Method of nickel-cobalt hydroxide hydrometallurgical extraction from laterite-nickel ore |
| PH12019000335A PH12019000335A1 (en) | 2018-09-07 | 2019-09-02 | Method of nickel-cobalt hydroxide hydromettallurgical extraction from laterite-nickel ore |
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| CN201811045949.8A CN108913883B (en) | 2018-09-07 | 2018-09-07 | Method for producing nickel cobalt hydroxide by laterite-nickel ore hydrometallurgy |
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| CN110541081A (en) * | 2019-09-02 | 2019-12-06 | 中国恩菲工程技术有限公司 | method for treating laterite-nickel ore |
| CN114427037B (en) * | 2022-01-06 | 2023-09-29 | 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 |
| CN115074527B (en) * | 2022-05-27 | 2024-07-09 | 中国恩菲工程技术有限公司 | Treatment method of copper-zinc mixed ore |
| CN114854987B (en) * | 2022-07-11 | 2022-09-20 | 中国恩菲工程技术有限公司 | Nickel-cobalt precipitation method for removing iron-aluminum solution by acid leaching of laterite-nickel ore |
| CN115340132A (en) * | 2022-09-19 | 2022-11-15 | 北方矿业有限责任公司 | Industrial crude cobalt hydroxide pulping and washing method |
| CN116770065A (en) * | 2023-06-25 | 2023-09-19 | 四川顺应动力电池材料有限公司 | Method for recycling laterite-nickel ore acid leaching residues |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101619400A (en) * | 2009-08-05 | 2010-01-06 | 江西稀有稀土金属钨业集团有限公司 | Method for extracting cobalt and nickel from nickel laterite |
| CN107400788A (en) * | 2017-07-18 | 2017-11-28 | 中国恩菲工程技术有限公司 | The method that nickel cobalt is precipitated in laterite nickel ore hydrometallurgical |
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| US6261527B1 (en) * | 1999-11-03 | 2001-07-17 | Bhp Minerals International Inc. | Atmospheric leach process for the recovery of nickel and cobalt from limonite and saprolite ores |
| AUPR207200A0 (en) * | 2000-12-13 | 2001-01-11 | QNI Limited | Hydroxide solids enrichment by slurry contact |
| US7387767B2 (en) * | 2005-04-07 | 2008-06-17 | Dynatec Corporation | Recovery of nickel, cobalt, iron, silica, zinc and copper from laterite ore by sulfuric acid leaching |
| US8147782B2 (en) * | 2007-09-28 | 2012-04-03 | Vale Inco Limited | Producing nickel hydroxide suitable for pelletization with iron-containing ore and for stainless steel manufacture |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101619400A (en) * | 2009-08-05 | 2010-01-06 | 江西稀有稀土金属钨业集团有限公司 | Method for extracting cobalt and nickel from nickel laterite |
| CN107400788A (en) * | 2017-07-18 | 2017-11-28 | 中国恩菲工程技术有限公司 | The method that nickel cobalt is precipitated in laterite nickel ore hydrometallurgical |
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| CN108913883A (en) | 2018-11-30 |
| AU2019222853B2 (en) | 2021-03-18 |
| AU2019222853A1 (en) | 2020-03-26 |
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