WO2007092994A1 - Processing of laterite ore - Google Patents

Processing of laterite ore Download PDF

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Publication number
WO2007092994A1
WO2007092994A1 PCT/AU2007/000149 AU2007000149W WO2007092994A1 WO 2007092994 A1 WO2007092994 A1 WO 2007092994A1 AU 2007000149 W AU2007000149 W AU 2007000149W WO 2007092994 A1 WO2007092994 A1 WO 2007092994A1
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WO
WIPO (PCT)
Prior art keywords
per cent
ore
range
nickel
manganese
Prior art date
Application number
PCT/AU2007/000149
Other languages
French (fr)
Inventor
John Joseph Andreazza
Original Assignee
Andreazza Consulting Pty Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from AU2006900739A external-priority patent/AU2006900739A0/en
Application filed by Andreazza Consulting Pty Ltd filed Critical Andreazza Consulting Pty Ltd
Priority to US12/279,292 priority Critical patent/US20090217786A1/en
Priority to AU2007215378A priority patent/AU2007215378A1/en
Priority to CA002640550A priority patent/CA2640550A1/en
Publication of WO2007092994A1 publication Critical patent/WO2007092994A1/en

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Classifications

    • 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
    • C22B23/0407—Leaching processes
    • C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
    • C22B23/043—Sulfurated acids or salts thereof
    • 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
    • C22B47/00—Obtaining manganese
    • C22B47/0018—Treating ocean floor nodules
    • C22B47/0045—Treating ocean floor nodules by wet processes
    • C22B47/0054—Treating ocean floor nodules by wet processes leaching processes
    • C22B47/0063—Treating ocean floor nodules by wet processes leaching processes with acids or salt solutions

Definitions

  • the present invention relates the processing of laterite ore.
  • HPAL high-pressure acid leaching
  • the processing of nickel laterites by the above method is complex, costly, time consuming and involves high energy consumption.
  • the present invention attempts to overcome at least in part the aforementioned disadvantages
  • Naturally occurring nickel laterites are derived from peridotite rocks containing olivine
  • These laterite deposits can be divided into three zones at increasing depth from the surface.
  • the three zones are the limonite zone, the serpentinite zone, and the garnierite zone.
  • the zone of interest in this invention is the limonite zone.
  • Limonite zones are typically
  • Asbolane has the general formula:
  • the present invention proposes that highly oxidised laterite ores, preferably containing asbolane, are treated by the reduction of the mineral species by a sulfur reducing agent in an aqueous acidic medium.
  • the present invention is envisaged to be used where the asbolane ore is preferably made up of between 0.1-10 per cent cobalt by weight, 40-80 per cent manganese oxide by weight and 0.1-20 per cent nickel by weight. More preferably the asbolane ore is made up of between 2-5 per cent cobalt by weight, 50-70 per cent manganese oxide by weight and 5-15 per cent nickel by weight.
  • the ore may preferably be ground to a particle size in the range of 50 to 600 mesh, more
  • This ground ore is admixed with, such as by being added to, an
  • aqueous medium Preferably the aqueous medium may be a dilute solution of mineral
  • the medium has a low pH, more preferably a pH less than 2.0.
  • the sulfur reducing agent may be added directly to the medium in the form of gaseous sulfur dioxide, or an aqueous solution thereof.
  • the amount of sulfur dioxide is preferably
  • the sulfur dioxide may be added incrementally or all at once.
  • the sulfur reducing agent is generated in situ by the reduction of an alkali metal sulfite salt, preferably sodium sulfite through the reaction:
  • the amount of sulfite salt may preferably be in the range of 10 to 40 per cent by weight of the ore.
  • the sulfite salt may be added to the medium containing the asbolane ore either incrementally or all at once.
  • the nickel, cobalt and manganese in the ore are solubilised in the aqueous medium as a result of a reduction of the mineral components by the sulfur reducing agent.
  • the treatment time may be in the range of 20 minutes to 20 hours, preferably in the range of 30 minutes to 10 hours.
  • the treatment temperature may preferably be in the range of 20 to 5O 0 C.
  • the pressure is less than 2 atmospheres, more preferably the pressure is ambient.
  • the process of the present invention may be performed in sealed reactors designed to contain sulphur dioxide or any other off gases from venting to atmosphere.
  • the reactors preferably contain a stirring mechanism to maintain the slurry in suspension.
  • the reactors may contain baffles to reduce bypass or short circuiting' the reactor residence volume.
  • the nickel, cobalt and manganese can then be recovered by known processes.
  • the soluble metal salts may be recovered by ionic exchange to produce nickel sulphate hexahydrate, cobalt suylphate hexahydrate and manganese sulphate.
  • the sulfur reducing agent may preferably be generated in situ by the reduction of an alkali metal metabisulfite salt, preferably sodium metabisulfite through the reaction: S 2 O 5 2" + 2H + 2SO 2 + H 2 O
  • the amount of metabisulfite salt may preferably be in the range of 5 to 30 per cent by
  • the metabisulfite salt may be added to the medium containing the
  • the ore used had the following composition of elements of interest.
  • the percentage of cobalt, manganese, nickel and iron in the highly oxidised laterite ore sample was 0.688, 4.35, 0.996 and 38.1 per cent by weight respectively.
  • Example 1 This example illustrates the rate of leaching over a 24 hour period. 50 g of asbolane ore
  • the optimal contact time is under 10 hours.
  • This example illustrates the effect of increasing temperature and decreasing amounts of Na 2 SO 3 in the reaction with respect to Example 1.
  • 5O g of asbolane ore was admixed with 50OmL of 0.2M sulfuric acid and 1O g OfNa 2 SO 3 added incrementally. The experiment was conducted at 4O 0 C and ambient pressure. Samples were taken at 0, 3, 6, 9 and 24 hours and analysed for their cobalt, nickel, iron and manganese concentrations.
  • Example 2 The amount of iron however was 1.4 per cent in Example 1 compared with 2.2 per cent in Example 2.
  • Example 3 It may be seen from Example 3 that a selective recovery of nickel, manganese and cobalt may be achieved by leaching with sulfur dioxide in an acid medium. The efficiency of the leaching increased with the increasing concentration of sulfur dioxide. The quantities of
  • This example illustrates the effect of adding Na 2 SO 3 all at once at the start of the reaction rather than incrementally during the reaction, as performed in Example 1.
  • 50 g of asbolane ore was admixed with 500 mL of 0.2M sulfuric acid and 1O g OfNa 2 SO 3 , adding all the Na 2 SO 3 at the start of the reaction.
  • the experiment was conducted at 25 0 C and ambient pressure. Samples were taken at 0, 30, 60, 110, 150, and 190 minutes and
  • Example 5 This examples illustrates the effect that the particle size of the ore has on the efficiency of
  • Samples of the asbolane ore were crushed and separated into sizes ranges, namely 75- 104 ⁇ , 104 - 152 ⁇ , 152 - 21 l ⁇ , 211 - 295 ⁇ , 295 - 422 ⁇ , 422 - 599 ⁇ . Samples of the ore from each size fraction were then admixed with 500 niL of 0.2M

Abstract

A process for the leaching of metals from highly oxidised laterite ores. The ore is admixed with an acidic aqueous medium, preferably a solution of sulfuric acid and the resulting mixture is treated with a sulfur reducing agent so as to reduce mineral species containing cobalt, nickel or manganese. The sulfur reducing agent may be an aqueous solution of sulfur dioxide or more preferably the sulfur dioxide is generated in situ by the reduction of alkali metal sulfite salt. The process is conducted at ambient temperature and pressure with the reduced mineral species being dissolved and subsequently recovered.

Description

TITLE
"PROCESSING OF LATERITE ORE"
The present invention relates the processing of laterite ore.
BACKGROUND TO THE INVENTION
Processing of nickel laterite ore is complicated due to the mineralogically and chemically complex nature of the ore. A technique called high-pressure acid leaching (HPAL) is usually used. The process involves the preparation of the ore into a slurry. The slurry is then contacted with sulfuric acid at temperatures of 25O0C - 28O0C and under high pressure for 60 minutes. This process leaches the nickel, cobalt and iron into solution. The resultant nickel cobalt liquor is recovered and processed by solvent extraction to produce separate nickel and cobalt products.
The processing of nickel laterites by the above method is complex, costly, time consuming and involves high energy consumption. The present invention attempts to overcome at least in part the aforementioned disadvantages
SUMMARY OF THE INVENTION
According to one aspect of the present invention there is provided a process for the
leaching of metals from highly oxidised laterite ores by admixing the ore and an acidic aqueous medium and treating the resulting mixture with a sulfur reducing agent at ambient temperature and pressure so as to reduce mineral species containing cobalt, nickel or manganese, the reduced mineral species being dissolved and subsequently recovered. DETAILED DESCRIPTION OF THE INVENTION
Naturally occurring nickel laterites are derived from peridotite rocks containing olivine
and serpentine. Under favorable conditions and with abundant rainfall various acids, such
as humic and others, are produced as a result of decaying organic matter. These acids
leach out the magnesium and silica values, while enriching the residue with iron and nickel.
These laterite deposits can be divided into three zones at increasing depth from the surface. The three zones are the limonite zone, the serpentinite zone, and the garnierite zone.
The zone of interest in this invention is the limonite zone. Limonite zones are typically
highly oxidised and preferably contain asbolite type materials such as asbolane. Asbolane has the general formula:
(Co,Ni)l-y(MnO2)2-x(OH)2-2y+2x-n(H2O).
The present invention proposes that highly oxidised laterite ores, preferably containing asbolane, are treated by the reduction of the mineral species by a sulfur reducing agent in an aqueous acidic medium. The present invention is envisaged to be used where the asbolane ore is preferably made up of between 0.1-10 per cent cobalt by weight, 40-80 per cent manganese oxide by weight and 0.1-20 per cent nickel by weight. More preferably the asbolane ore is made up of between 2-5 per cent cobalt by weight, 50-70 per cent manganese oxide by weight and 5-15 per cent nickel by weight.
The ore may preferably be ground to a particle size in the range of 50 to 600 mesh, more
preferably 100 mesh. This ground ore is admixed with, such as by being added to, an
aqueous medium. Preferably the aqueous medium may be a dilute solution of mineral
acid, more preferably a dilute solution of sulfuric acid. Preferably the medium has a low pH, more preferably a pH less than 2.0.
The sulfur reducing agent may be added directly to the medium in the form of gaseous sulfur dioxide, or an aqueous solution thereof. The amount of sulfur dioxide is preferably
in the range of 0.8 to 3.2 mol SO2/ kg of ore. The sulfur dioxide may be added incrementally or all at once.
More preferably the sulfur reducing agent is generated in situ by the reduction of an alkali metal sulfite salt, preferably sodium sulfite through the reaction:
SO, 2*- + 2H+ SO2 + H2O
The amount of sulfite salt may preferably be in the range of 10 to 40 per cent by weight of the ore. The sulfite salt may be added to the medium containing the asbolane ore either incrementally or all at once.
The nickel, cobalt and manganese in the ore are solubilised in the aqueous medium as a result of a reduction of the mineral components by the sulfur reducing agent. Copper, iron
and aluminium may not be leached to an appreciable level and remain in the solid residue.
The treatment time may be in the range of 20 minutes to 20 hours, preferably in the range of 30 minutes to 10 hours. The treatment temperature may preferably be in the range of 20 to 5O0C. Preferably the pressure is less than 2 atmospheres, more preferably the pressure is ambient.
The process of the present invention may be performed in sealed reactors designed to contain sulphur dioxide or any other off gases from venting to atmosphere. The reactors preferably contain a stirring mechanism to maintain the slurry in suspension. Also, the reactors may contain baffles to reduce bypass or short circuiting' the reactor residence volume.
The nickel, cobalt and manganese can then be recovered by known processes. For example, the soluble metal salts may be recovered by ionic exchange to produce nickel sulphate hexahydrate, cobalt suylphate hexahydrate and manganese sulphate.
In an alternative embodiment of the present invention the sulfur reducing agent may preferably be generated in situ by the reduction of an alkali metal metabisulfite salt, preferably sodium metabisulfite through the reaction: S2O5 2" + 2H+ 2SO2 + H2O
The amount of metabisulfite salt may preferably be in the range of 5 to 30 per cent by
weight of the ore. The metabisulfite salt may be added to the medium containing the
asbolane ore either incrementally or all at once.
The present invention will now be described with reference to the following examples.
In the following examples the ore used had the following composition of elements of interest. The percentage of cobalt, manganese, nickel and iron in the highly oxidised laterite ore sample was 0.688, 4.35, 0.996 and 38.1 per cent by weight respectively.
Example 1 This example illustrates the rate of leaching over a 24 hour period. 50 g of asbolane ore
was admixed with 500 mL of 0.2 M sulfuric acid and 15 g of Na2SO3 added
incrementally. The experiment was conducted at 250C and ambient pressure. Samples were taken at 0, 6, 9 and 24 hours and analysed for their cobalt, nickel, iron and manganese concentrations.
An analysis of the samples taken at six hours showed that 76.7 per cent of the cobalt, 67.4 per cent of the manganese, 43.2 per cent of the nickel and 0.8 per cent of the iron had been recovered. An analysis of the samples taken at nine hours showed that 79.9 per cent of the cobalt, 70.5 per cent of the manganese, 45.2 per cent of the nickel and 0.9 per cent
of the iron had been recovered. An analysis of the samples taken at twenty four hours
showed that 83.0 per cent of the cobalt, 72.6 per cent of the manganese, 47.4 per cent of
the nickel and 1.4 per cent of the iron had been recovered.
From the data it may be seen that the optimal contact time is under 10 hours.
Example 2
This example illustrates the effect of increasing temperature and decreasing amounts of Na2SO3 in the reaction with respect to Example 1. 5O g of asbolane ore was admixed with 50OmL of 0.2M sulfuric acid and 1O g OfNa2SO3 added incrementally. The experiment was conducted at 4O0C and ambient pressure. Samples were taken at 0, 3, 6, 9 and 24 hours and analysed for their cobalt, nickel, iron and manganese concentrations.
An analysis of the samples taken at three hours showed that 62.9 per cent of the cobalt, 50.1 per cent of the manganese, 35.1 per cent of the nickel and 0.7 per cent of the iron had been recovered. An analysis of the samples taken at 6 hours showed that 74.8 per cent of the cobalt, 65.6 per cent of the manganese, 43.0 per cent of the nickel and 1.0 per cent of the iron had been recovered. An analysis of the samples taken at nine hours
showed that 81.1 per cent of the cobalt, 69.7 per cent of the manganese, 47.8 per cent of the nickel and 1.5 per cent of the iron had been recovered. An analysis of the samples taken at twenty four hours showed that 80.8 per cent of the cobalt, 69.6 per cent of the manganese, 47.3 per cent of the nickel and 2.2 per cent of the iron had been recovered. From this data it may be seen that the optimal contact time for extraction of the metal values is around 10 hours.
After twenty four hours the recovery rates for cobalt and nickel were greater in Example
1 than in Example 2. In the same period the amount of nickel recovered was very similar.
The amount of iron however was 1.4 per cent in Example 1 compared with 2.2 per cent in Example 2.
Example 3
This example illustrates the effect of the concentration of reducing agent on the extraction efficiency. 25 g samples of asbolane ore were admixed with 500 mL of 0.2M sulfuric acid. These samples were then treated with differing concentrations of sulfur dioxide, namely approximately 1.8, 7.2, 10.8, 12.6 and 14.4 mmol/g. The samples were leached for 45 minutes at 250C and ambient pressure. At the completion of the leaching
period the pulps were filtered dried and analysed.
An analysis of the sample treated with 1.8 mmol/g SO2 showed that 16.2 per cent manganese, 8.0 per cent nickel, 16.0 per cent cobalt and 4.0 per cent iron by weight had
been recovered from the ore. An analysis of the sample treated with 7.2 mmol/g SO2 showed that 62.6 per cent manganese, 48.6 per cent nickel, 25.0 per cent cobalt and 4.0 per cent iron by weight had been recovered from the ore. An analysis of the sample treated with 10.8 mmol/g SO2 showed that 82.1 per cent manganese, 76.6 per cent nickel, 30.0 per cent cobalt and 5.8 per cent iron by weight had been recovered from the ore. An analysis of the sample treated with 12.6 mmol/g SO2 showed that 88.6 per cent manganese, 88.6 per cent nickel, 52.1 per cent cobalt and 5.8 per cent iron by weight had
been recovered from the ore. An analysis of the sample treated with 14.4 mmol/g SO2
showed that 92.6 per cent manganese, 92.0 per cent nickel, 88.0 per cent cobalt and 5.8 per cent iron by weight had been recovered from the ore.
It may be seen from Example 3 that a selective recovery of nickel, manganese and cobalt may be achieved by leaching with sulfur dioxide in an acid medium. The efficiency of the leaching increased with the increasing concentration of sulfur dioxide. The quantities of
iron leached were minimal and appeared independent of the concentration of sulfur dioxide when leached in this way.
Example 4.
This example illustrates the effect of adding Na2SO3 all at once at the start of the reaction rather than incrementally during the reaction, as performed in Example 1. 50 g of asbolane ore was admixed with 500 mL of 0.2M sulfuric acid and 1O g OfNa2SO3, adding all the Na2SO3 at the start of the reaction. The experiment was conducted at 250C and ambient pressure. Samples were taken at 0, 30, 60, 110, 150, and 190 minutes and
analysed for their cobalt, nickel, iron and manganese concentrations.
An analysis of the samples taken at thirty minutes showed that 59.6 per cent of the cobalt, 61.4 per cent of the manganese, 28.2 per cent of the nickel and 0.4 per cent of the iron had been recovered. An analysis of the samples taken at sixty minutes showed that 67.3 per cent of the cobalt, 71.3 per cent of the manganese, 33.3 per cent of the nickel and 0.5 per cent of the iron had been recovered. An analysis of the samples taken at one hundred and ten minutes showed that 72.3 per cent of the cobalt, 76.0 per cent of the manganese,
37.1 per cent of the nickel and 0.5 per cent of the iron had been recovered. An analysis of
the samples taken at one hundred and fifty minutes showed that 73.7 per cent of the cobalt, 78.6 per cent of the manganese, 37.7 per cent of the nickel and 0.5 per cent of the
iron had been recovered. An analysis of the samples taken at one hundred and ninety
minutes showed that 74.2 per cent of the cobalt,78.5 per cent of the manganese, 39.1 per cent of the nickel and 0.6 per cent of the iron had been recovered.
It is evident from the data in Example 4 that the optimal contact time is approximately 1 hour when the Na2SO3 is added all at once at the start of the reaction. This reaction time is significantly lower than times used in examples 1 and 2, however the
recoveries achieved in this example were slightly lower.
Example 5 This examples illustrates the effect that the particle size of the ore has on the efficiency of
the leaching process. Samples of the asbolane ore were crushed and separated into sizes ranges, namely 75- 104μ, 104 - 152 μ, 152 - 21 lμ , 211 - 295μ, 295 - 422μ, 422 - 599μ. Samples of the ore from each size fraction were then admixed with 500 niL of 0.2M
sulfuric acid and 1O g OfNa2SO3, The samples were then leached for 45 minutes at 25°C and ambient pressure. At the completion of the leaching period the pulps were filtered dried and analysed.
An analysis of the 75 - 104μ ore fraction showed that 75.3 per cent nickel, 85.6 per cent cobalt, 88.0 per cent manganese and 5.8 per cent by weight of iron had been recovered. An analysis of the 104 - 152μ ore fraction showed that 70.9 per cent nickel, 80.1 per cent
cobalt, 86.0 per cent manganese and 5.8 per cent by weight of iron had been recovered.
An analysis of the 152 - 211 μ ore fraction showed that 68.1 per cent nickel, 76.4 per cent cobalt, 84.7 per cent manganese and 5.9 per cent by weight of iron had been recovered.
An analysis of the 211 - 295μ ore fraction showed that 59.0 per cent nickel, 69.4 per cent
cobalt, 76.2 per cent manganese and 7.6 per cent by weight of iron had been recovered.
An analysis of the 295 - 422μ ore fraction showed that 53.2 per cent nickel, 59.8 per cent
cobalt, 60.6 per cent manganese and 5.9 per cent by weight of iron had been recovered. An analysis of the 422 - 599μ ore fraction showed that 47.9 per cent nickel, 55.6 per cent cobalt, 60.2 per cent manganese and 5.7 per cent by weight of iron had been recovered.
It may be seen from this example that the efficiency of the leaching process decreased with the increase in size fraction of the ore. The quantities of iron leached were minimal and appeared independent of the particle size of the ore when leached in this way.
Modifications and variations as would be apparent to a skilled addressee are deemed to be within the scope of the present invention

Claims

The claims defining the invention are as follows:
5 1. A process for the leaching of metals from highly oxidised laterite ores by admixing
the ore and an acidic aqueous medium and treating the resulting mixture with a sulfur reducing agent at ambient temperature and pressure so as to reduce mineral species containing cobalt, nickel or manganese, the reduced mineral species being dissolved and subsequently recovered.
0
2. A process as defined in claim 1, wherein the highly oxidised laterite ore contains
asbolane.
3. A process as defined in claim 2, wherein the highly oxidised laterite ore comprises
5 cobalt in the range of 0.1 to 10 per cent by weight, manganese in the range of 40 to 80 per cent by weight and nickel in the range of 0.1 to 20 per cent by weight.
4. A process as defined in claim 3, wherein the highly oxidised laterite ore comprises
cobalt in the range of 2 to 5 per cent by weight, manganese in the range of 50 to 70
:0 per cent by weight and nickel in the range of 5 to 15 per cent by weight.
5. A process as defined in any one of claims 1 to 4, wherein the sulfur reducing agent
is provided in the form of an aqueous solution of sulfur dioxide
6. A process as defined in any one of claims 1 to 5, wherein the sulfur dioxide is generated in situ by the reduction of an alkali metal sulfite.
7. A process as defined in claim 6, wherein the sulfur dioxide is generated in situ by the reduction of sodium sulfite.
8. A process as defined in any one of claims 5 to 7, wherein the amount of sulfur
reducing agent added provided is in the range of 0.8 to 3.2 mol SO2/ kg of the ore.
9. A process as defined in any one of the preceding claims, wherein the pH of the aqueous medium is less than 2.0.
10. A process as defined in claim 9, wherein the source of acid is a mineral acid.
11. A process as defined in claim 10, wherein the mineral acid is sulfuric acid.
12. A process as defined in any one of the preceding claims, wherein the treatment
temperature is in the range of 2O0C to 5O0C.
13. A process as defined in any one of the preceding claims, wherein the treatment
pressure is less than 2 atmospheres.
14. A process as defined in any one of the preceding claims, wherein the ore is
crushed to a size in the range of 50 to 600 mesh.
15. A process as defined in claim 14, wherein the ore is crushed to a size in the range
of 90 to 110 mesh
PCT/AU2007/000149 2006-02-15 2007-02-14 Processing of laterite ore WO2007092994A1 (en)

Priority Applications (3)

Application Number Priority Date Filing Date Title
US12/279,292 US20090217786A1 (en) 2006-02-15 2007-02-14 Processing of laterite ore
AU2007215378A AU2007215378A1 (en) 2006-02-15 2007-02-14 Processing of laterite ore
CA002640550A CA2640550A1 (en) 2006-02-15 2007-02-14 Processing of laterite ore

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2006900739A AU2006900739A0 (en) 2006-02-15 Processing of nickel laterite ore
AU2006900739 2006-02-15

Publications (1)

Publication Number Publication Date
WO2007092994A1 true WO2007092994A1 (en) 2007-08-23

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Cited By (3)

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WO2009079715A1 (en) * 2007-12-24 2009-07-02 Bhp Billiton Ssm Development Pty Ltd Selectively leaching cobalt from lateritic ores
WO2011018550A1 (en) * 2009-08-11 2011-02-17 Outotec Oyj Method for leaching of ore containing copper and cobalt
WO2014000023A1 (en) * 2012-06-29 2014-01-03 Metaleach Limited Method for recovering cobalt from cobalt-containing ores

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CN112823027A (en) * 2018-07-24 2021-05-18 青春生命科学公司 Use of liposomes for delivering proteins and genes encoding said proteins to living cells

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Publication number Priority date Publication date Assignee Title
WO2009079715A1 (en) * 2007-12-24 2009-07-02 Bhp Billiton Ssm Development Pty Ltd Selectively leaching cobalt from lateritic ores
US7988938B2 (en) 2007-12-24 2011-08-02 Bhp Billiton Ssm Development Pty Ltd. Selectively leaching cobalt from lateritic ores
WO2011018550A1 (en) * 2009-08-11 2011-02-17 Outotec Oyj Method for leaching of ore containing copper and cobalt
WO2014000023A1 (en) * 2012-06-29 2014-01-03 Metaleach Limited Method for recovering cobalt from cobalt-containing ores
AU2013202009B2 (en) * 2012-06-29 2015-03-19 CAPSA Metals Pty Ltd Method For Recovering Cobalt from Cobalt-Containing Ores

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