CA2396972A1 - Processing of nickel bearing solutions - Google Patents
Processing of nickel bearing solutions Download PDFInfo
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- CA2396972A1 CA2396972A1 CA 2396972 CA2396972A CA2396972A1 CA 2396972 A1 CA2396972 A1 CA 2396972A1 CA 2396972 CA2396972 CA 2396972 CA 2396972 A CA2396972 A CA 2396972A CA 2396972 A1 CA2396972 A1 CA 2396972A1
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Abstract
Disclosed is a process for recovering a nickel constituent from a solution containing iron, cobalt and manganese, comprising the steps of:
a) removing the iron from the solution using an oxidation and partial neutralization step;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of said nickel constituent in solution; and c) recovering the nickel constituent from solution.
a) removing the iron from the solution using an oxidation and partial neutralization step;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of said nickel constituent in solution; and c) recovering the nickel constituent from solution.
Description
REFERENCE TO CO-PENDING APPLICATION
The subject matter of each of the following applications is incorporated herein by reference:
- U.S. Patent Application 09/275,932, filed on March 24, 1999 entitled METHODS
OF
PURIFYING COBALT;
- U.S. Patent Application 09/306,311, filed on May 6, 1999 entitled BASE METAL
RECOVERY; and - PCT Patent Application PCT/CA00/00352, filed April 5, 2000 entitled PURIFICATION OF ZINC MATERIALS
BACKGROUND OF THE INVENTION
1. FIELD OF THE INVENTION
The present invention relates to techniques for the processing of nickel bearing solutions.
The subject matter of each of the following applications is incorporated herein by reference:
- U.S. Patent Application 09/275,932, filed on March 24, 1999 entitled METHODS
OF
PURIFYING COBALT;
- U.S. Patent Application 09/306,311, filed on May 6, 1999 entitled BASE METAL
RECOVERY; and - PCT Patent Application PCT/CA00/00352, filed April 5, 2000 entitled PURIFICATION OF ZINC MATERIALS
BACKGROUND OF THE INVENTION
1. FIELD OF THE INVENTION
The present invention relates to techniques for the processing of nickel bearing solutions.
2. DESCRIPTION OF THE RELATED ART
Typical nickel solutions include cobalt and impurities such as iron and manganese. There are several ways in which nickel has been recovered from these solutions.
These are widely known and generally involve removal of iron, followed by:
a) solvent extraction of cobalt, manganese and zinc using the well known (a trademark) solvent, followed by a nickel solvent extraction using VERSATIC
10 (a trademark), then cobalt sulphide precipitation from the CYANEX 272 raffinate, followed by a cobalt sulphide pressure leach, purification and cobalt recovery.
b) precipitation of cobalt and nickel using Mg0 or CaO, with the cobalt and nickel being re-leached in NH3 for separation and recovery.
c) precipitation of cobalt and nickel sulphides which are later subjected to a pressure leach, followed by a cobalt solvent extraction and a nickel precipitation using Hz.
The processes b) and c) therefore remove iron in the first step, then cobalt and nickel are precipitated from the rest of the impurities, in particular manganese, and then cobalt is separated from nickel. Therefore, to recover nickel, which is generally the most valuable element, nickel and cobalt must usually be separated from manganese and then the nickel recovered from the cobalt.
It is an object of the present invention to provide a novel method for processing nickel bearing solutions.
SUMMARY OF THE INVENTION
Briefly stated, the invention involves a process for recovering a nickel constituent from a solution containing iron, cobalt and manganese, comprising the steps of:
a) removing the iron from the solution using an oxidation and partial neutralization step;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of the nickel constituent in solution; and c) recovering the nickel constituent from solution.
In one embodiment, the solution is reacted, in step (b), with hypochlorite to precipitate both the cobalt and manganese, preferably at a pH from about 3.0 to about 3.5.
In another embodiment, the solution, in step (b), is reacted with a mixture of sulphur dioxide and oxygen to precipitate both the cobalt and manganese, again at a pH
from about 3.0 to about 3.5.
In another aspect, the present invention provides a method of processing a nickel bearing solution containing iron, cobalt and manganese constituents, comprising the steps of:
a) removing the iron constituent from the solution using an oxidation and partial neutralization step; and b) removing cobalt and manganese constituents together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of the nickel constituent in solution.
In one embodiment, the method further comprises the step of:
c) recovering the nickel constituent from solution.
In still another of its aspects, the present invention provides a method of processing a laterite leach solution, comprising the steps of a) providing a laterite leach solution including 1 to 10 g/L nickel, 10 to 1000 mg/L cobalt, and 50 to 1500 mg/L manganese;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of the nickel in solution.
Typical nickel solutions include cobalt and impurities such as iron and manganese. There are several ways in which nickel has been recovered from these solutions.
These are widely known and generally involve removal of iron, followed by:
a) solvent extraction of cobalt, manganese and zinc using the well known (a trademark) solvent, followed by a nickel solvent extraction using VERSATIC
10 (a trademark), then cobalt sulphide precipitation from the CYANEX 272 raffinate, followed by a cobalt sulphide pressure leach, purification and cobalt recovery.
b) precipitation of cobalt and nickel using Mg0 or CaO, with the cobalt and nickel being re-leached in NH3 for separation and recovery.
c) precipitation of cobalt and nickel sulphides which are later subjected to a pressure leach, followed by a cobalt solvent extraction and a nickel precipitation using Hz.
The processes b) and c) therefore remove iron in the first step, then cobalt and nickel are precipitated from the rest of the impurities, in particular manganese, and then cobalt is separated from nickel. Therefore, to recover nickel, which is generally the most valuable element, nickel and cobalt must usually be separated from manganese and then the nickel recovered from the cobalt.
It is an object of the present invention to provide a novel method for processing nickel bearing solutions.
SUMMARY OF THE INVENTION
Briefly stated, the invention involves a process for recovering a nickel constituent from a solution containing iron, cobalt and manganese, comprising the steps of:
a) removing the iron from the solution using an oxidation and partial neutralization step;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of the nickel constituent in solution; and c) recovering the nickel constituent from solution.
In one embodiment, the solution is reacted, in step (b), with hypochlorite to precipitate both the cobalt and manganese, preferably at a pH from about 3.0 to about 3.5.
In another embodiment, the solution, in step (b), is reacted with a mixture of sulphur dioxide and oxygen to precipitate both the cobalt and manganese, again at a pH
from about 3.0 to about 3.5.
In another aspect, the present invention provides a method of processing a nickel bearing solution containing iron, cobalt and manganese constituents, comprising the steps of:
a) removing the iron constituent from the solution using an oxidation and partial neutralization step; and b) removing cobalt and manganese constituents together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of the nickel constituent in solution.
In one embodiment, the method further comprises the step of:
c) recovering the nickel constituent from solution.
In still another of its aspects, the present invention provides a method of processing a laterite leach solution, comprising the steps of a) providing a laterite leach solution including 1 to 10 g/L nickel, 10 to 1000 mg/L cobalt, and 50 to 1500 mg/L manganese;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of the nickel in solution.
In one embodiment, the solution of step a) includes 0 to 2000 mg/L iron, the method further comprising, before step b), the step of:
c) removing the iron from the solution using an oxidation and partial neutralization step.
In another embodiment, the method includes the step of:
d) recovering the nickel from solution.
In still another embodiment, the method further comprises the steps of:
e) re-leaching the cobalt and manganese from step b) into an intermediate leach solution;
and f) recovering the cobalt from the intermediate leach solution.
In still another embodiment, the method may further comprise the steps of:
e) re-leaching the cobalt and manganese from step b) into an intermediate leach solution;
and f) recovering the manganese from the intermediate leach solution.
In one embodiment, the solution includes at least one of the following impurities: 0 to 50 g/L chloride, 2 to 15 g/L magnesium and 300 to 600 mg/L calcium, further comprising the step of:
d) recovering the nickel from solution, while leaving the impurities in solution.
c) removing the iron from the solution using an oxidation and partial neutralization step.
In another embodiment, the method includes the step of:
d) recovering the nickel from solution.
In still another embodiment, the method further comprises the steps of:
e) re-leaching the cobalt and manganese from step b) into an intermediate leach solution;
and f) recovering the cobalt from the intermediate leach solution.
In still another embodiment, the method may further comprise the steps of:
e) re-leaching the cobalt and manganese from step b) into an intermediate leach solution;
and f) recovering the manganese from the intermediate leach solution.
In one embodiment, the solution includes at least one of the following impurities: 0 to 50 g/L chloride, 2 to 15 g/L magnesium and 300 to 600 mg/L calcium, further comprising the step of:
d) recovering the nickel from solution, while leaving the impurities in solution.
In yet another of its aspects, there is provided a method of processing a laterite leach solution, comprising the steps of a) providing a laterite leach solution including 1 to 10 g/L nickel, 10 to 1000 mg/L cobalt, 50 to 1500 mg/L manganese, and at least one of the following impurities: 0 to 50 g/L
chloride, 2 to 15 g/L magnesium and 300 to 600 mg/L calcium;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of the nickel and the impurities in the solution.
In one embodiment, the solution of step a) includes 0 to 2000 mg/L iron, the method further comprising, before step b), the step of:
c) removing the iron from the solution using an oxidation and partial neutralization step.
It will be understood by those skilled in the art that the steps of a hydrometallurgy process to 'remove' or 'recover' an impurity or a metal of value will often not be absolute. Rather, trace elements will sometimes remain, the amount of which will vary depending on the selected process parameters, such as pH, temperature and the like. Therefore, terms used herein such as 'remove' or 'recover' are intended to take this into account.
Thus, in one embodiment, the present invention provides a method of recovering either nickel or cobalt, or both, from a leach solution containing impurities such as iron, manganese and others.
chloride, 2 to 15 g/L magnesium and 300 to 600 mg/L calcium;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of the nickel and the impurities in the solution.
In one embodiment, the solution of step a) includes 0 to 2000 mg/L iron, the method further comprising, before step b), the step of:
c) removing the iron from the solution using an oxidation and partial neutralization step.
It will be understood by those skilled in the art that the steps of a hydrometallurgy process to 'remove' or 'recover' an impurity or a metal of value will often not be absolute. Rather, trace elements will sometimes remain, the amount of which will vary depending on the selected process parameters, such as pH, temperature and the like. Therefore, terms used herein such as 'remove' or 'recover' are intended to take this into account.
Thus, in one embodiment, the present invention provides a method of recovering either nickel or cobalt, or both, from a leach solution containing impurities such as iron, manganese and others.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
An embodiment of the present invention is illustrated in figure 1, this case employing a laterite leach solution. It will, of course, be understood that the present process may be used on any other leach solutions.
As shown, at step 10, the leach solution is first subjected to an oxidation and partial neutralization step to remove iron (as is known to those skilled in the art), which leaves as a solid phase residue as shown in the separation step 12. The solution is then exposed to a suitable oxidant at step 14, (at a pH ranging from about 1 to about 4, more preferably from about 3 to about 3.5, for example at 3.5 as illustrated in the example herein below) to oxidize cobalt and manganese together. The cobalt and manganese oxides are then removed in a later separation step 16, while the nickel bearing solution is directed to a nickel recovery step, not shown (but which is known to those skilled in the art).
The cobalt and manganese oxides are re-leached in a re-leach step 18 and the resulting leach solution is directed to a cobalt manganese separation step as shown in figure 2.
As figure 2 illustrates, some trace amounts of nickel will, in some cases, be present in the cobalt manganese leach solution. However, the presence of nickel is only an economic issue and should not otherwise impair the removal of cobalt and manganese. The former is removed by subjecting the leach solution, for example by solvent extraction or precipitation, the latter using complexants such as NaSH or others (as is known to those skilled in the art), at step 20, to form a cobalt sulphide, which is then recovered in a separation step 22, with the manganese bearing leach solution advancing to a later recovery step (as is known to those skilled in the art) not shown.
The present process is advantageous in that cobalt, manganese and nickel may be recovered from the solution using well known process steps.
An embodiment of the present invention is illustrated in figure 1, this case employing a laterite leach solution. It will, of course, be understood that the present process may be used on any other leach solutions.
As shown, at step 10, the leach solution is first subjected to an oxidation and partial neutralization step to remove iron (as is known to those skilled in the art), which leaves as a solid phase residue as shown in the separation step 12. The solution is then exposed to a suitable oxidant at step 14, (at a pH ranging from about 1 to about 4, more preferably from about 3 to about 3.5, for example at 3.5 as illustrated in the example herein below) to oxidize cobalt and manganese together. The cobalt and manganese oxides are then removed in a later separation step 16, while the nickel bearing solution is directed to a nickel recovery step, not shown (but which is known to those skilled in the art).
The cobalt and manganese oxides are re-leached in a re-leach step 18 and the resulting leach solution is directed to a cobalt manganese separation step as shown in figure 2.
As figure 2 illustrates, some trace amounts of nickel will, in some cases, be present in the cobalt manganese leach solution. However, the presence of nickel is only an economic issue and should not otherwise impair the removal of cobalt and manganese. The former is removed by subjecting the leach solution, for example by solvent extraction or precipitation, the latter using complexants such as NaSH or others (as is known to those skilled in the art), at step 20, to form a cobalt sulphide, which is then recovered in a separation step 22, with the manganese bearing leach solution advancing to a later recovery step (as is known to those skilled in the art) not shown.
The present process is advantageous in that cobalt, manganese and nickel may be recovered from the solution using well known process steps.
Feed solutions, for example, may include laterite leach solutions having the following:
- 1 to 10 g/L, more preferably 1 to 5 g/L Ni - 10 to 1000 mg/L Co, - 50 to 1500 mg/L, more preferably 60 to 1000 mg/L Mn -Oto50g/LCl - 2 to 15 g/L Mg;
- 0 to 200 mg/L Fe;
- 300 to 600 mg/L Ca;
- Cu, Cr, Zn or other trace elements, each not usually exceeding 100 mg/L.
The oxidation steps may involve hypochlorite or other oxidants such as mixtures of SOZ
and OZ (and others as known to those skilled in the art) at temperatures ranging, for example, from 25 to 80 degrees Celsius, more preferably 50 to 70 degrees Celsius.
Typical reactions involve an excess of oxidant ranging from 1 to 20 percent of the stoichiometric amount.
IS
Thus, the nickel constituent can be removed by using the VERSATIC 10 solvent.
The cobalt constituent can be upgraded by precipitation and recovery in a side stream. The present process thus enables the selective precipitation of Co and Mn by oxidation to Co 3+, Mn 4+
without oxidizing Ni z'.
The oxidation steps herein may include, for example, SOZ/OZ at lower pH's or NaClO.
Other oxidants include C12, Os, and Caro's acid. Preferably, the Co-Mn re-leach step is carried out using reductive leaching (for example using metabisulphite or SOZ).
Co Mn separation can also be carried out in several ways, such as by a sulphide precipitation of CoS leaving Mn behind, and a re-leach CoS in an autoclave, or selective oxidation of Mn and selective precipitation of MnOx, using SOZ/OZ , then recovering the cobalt as metal (by solvent extraction or electrowinning ), or by recovering the cobalt in other forms such as a carbonate or a hydroxide.
_7_ If desired, the iron constituent may, in some cases, be removed together with the cobalt and manganese from the nickel bearing leach solution, for example, by reacting the solution with an appropriate oxidant such as hypochlorite. However, this may complicate, to some extent, the subsequent recovery of cobalt from the precipitate.
Embodiments of the present invention will be described with reference to the following examples which are presented for illustrative purposes only and are not intended to limit the scope of the invention.
EXAMPLE:
1. Feed Solution An example of the present process was conducted on a laterite feed solution, having the following composition:
Ni: 1.9 g/L
Co: 60 mg/L
Mn: 410 mg/L
Cl: 28 g/L
Mg: 12 g/L
Fe: <5 mg/L
+ Cu, Cr, Zn: < 100 mg/L each 2. Oxidation-precipitation of Co + Mn Following a conventional oxidation of Fe, the oxidation and precipitation of Co and Mn proceeded under the following conditions:
_g_ 2.1. Conditions Temperature: 68°C
pH = 3.5 Duration: 120 min.
Oxidant: sodium hypochlorite 2.2. Results The results are shown in the table below indicating that the process was very selective for the recovery/removal of Co (95.4%) and Mn (99.9%) while removing a relatively small amount of Ni (2%).
Stream Ni Co Mn PLS (mg/L) 1930 62 414 Final Solution (mg/L)1800 2.9 0.3 Co/Mn precip (%) 3.45 5.75 33.5 Recovery in Precipitate2.0 95.4 99.9 3. Re-dissolution of Co + Mn precipitate The Co Mn precipitate was re-dissolved under the following conditions:
3.1. Conditions Reductive leach: sodium metabisulphite pH = 1.5 Temperature = 50°C
Time = 15 minutes 3.2. Results:
The sample was completely re-dissolved with a 100 percent recovery of Co, Ni and Mn, resulting in the leach solution having the following composition:
Leach solution:
2.9 g/L Ni 3.0 g/L Co 21.2 g/L Mn
- 1 to 10 g/L, more preferably 1 to 5 g/L Ni - 10 to 1000 mg/L Co, - 50 to 1500 mg/L, more preferably 60 to 1000 mg/L Mn -Oto50g/LCl - 2 to 15 g/L Mg;
- 0 to 200 mg/L Fe;
- 300 to 600 mg/L Ca;
- Cu, Cr, Zn or other trace elements, each not usually exceeding 100 mg/L.
The oxidation steps may involve hypochlorite or other oxidants such as mixtures of SOZ
and OZ (and others as known to those skilled in the art) at temperatures ranging, for example, from 25 to 80 degrees Celsius, more preferably 50 to 70 degrees Celsius.
Typical reactions involve an excess of oxidant ranging from 1 to 20 percent of the stoichiometric amount.
IS
Thus, the nickel constituent can be removed by using the VERSATIC 10 solvent.
The cobalt constituent can be upgraded by precipitation and recovery in a side stream. The present process thus enables the selective precipitation of Co and Mn by oxidation to Co 3+, Mn 4+
without oxidizing Ni z'.
The oxidation steps herein may include, for example, SOZ/OZ at lower pH's or NaClO.
Other oxidants include C12, Os, and Caro's acid. Preferably, the Co-Mn re-leach step is carried out using reductive leaching (for example using metabisulphite or SOZ).
Co Mn separation can also be carried out in several ways, such as by a sulphide precipitation of CoS leaving Mn behind, and a re-leach CoS in an autoclave, or selective oxidation of Mn and selective precipitation of MnOx, using SOZ/OZ , then recovering the cobalt as metal (by solvent extraction or electrowinning ), or by recovering the cobalt in other forms such as a carbonate or a hydroxide.
_7_ If desired, the iron constituent may, in some cases, be removed together with the cobalt and manganese from the nickel bearing leach solution, for example, by reacting the solution with an appropriate oxidant such as hypochlorite. However, this may complicate, to some extent, the subsequent recovery of cobalt from the precipitate.
Embodiments of the present invention will be described with reference to the following examples which are presented for illustrative purposes only and are not intended to limit the scope of the invention.
EXAMPLE:
1. Feed Solution An example of the present process was conducted on a laterite feed solution, having the following composition:
Ni: 1.9 g/L
Co: 60 mg/L
Mn: 410 mg/L
Cl: 28 g/L
Mg: 12 g/L
Fe: <5 mg/L
+ Cu, Cr, Zn: < 100 mg/L each 2. Oxidation-precipitation of Co + Mn Following a conventional oxidation of Fe, the oxidation and precipitation of Co and Mn proceeded under the following conditions:
_g_ 2.1. Conditions Temperature: 68°C
pH = 3.5 Duration: 120 min.
Oxidant: sodium hypochlorite 2.2. Results The results are shown in the table below indicating that the process was very selective for the recovery/removal of Co (95.4%) and Mn (99.9%) while removing a relatively small amount of Ni (2%).
Stream Ni Co Mn PLS (mg/L) 1930 62 414 Final Solution (mg/L)1800 2.9 0.3 Co/Mn precip (%) 3.45 5.75 33.5 Recovery in Precipitate2.0 95.4 99.9 3. Re-dissolution of Co + Mn precipitate The Co Mn precipitate was re-dissolved under the following conditions:
3.1. Conditions Reductive leach: sodium metabisulphite pH = 1.5 Temperature = 50°C
Time = 15 minutes 3.2. Results:
The sample was completely re-dissolved with a 100 percent recovery of Co, Ni and Mn, resulting in the leach solution having the following composition:
Leach solution:
2.9 g/L Ni 3.0 g/L Co 21.2 g/L Mn
Claims (23)
1. A process for recovering a nickel constituent from a solution containing iron, cobalt and manganese, comprising the steps of:
a) removing the iron from the solution using an oxidation and partial neutralization step;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of said nickel constituent in solution; and c) recovering the nickel constituent from solution.
a) removing the iron from the solution using an oxidation and partial neutralization step;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of said nickel constituent in solution; and c) recovering the nickel constituent from solution.
2. A process as defined in claim 1 wherein, in step b), the solution is reacted with hypochlorite to precipitate both the cobalt and manganese.
3. A process as defined in claim 2 wherein step b) is conducted at a pH from about 3.0 to about 3.5.
4. A process as defined in claim 1 wherein, in step b), the solution is reacted with a mixture of sulphur dioxide and oxygen to precipitate both the cobalt and manganese.
5. A process as defined in claim 4 wherein step b) is conducted at a pH from about 3.0 to about 3.5.
6. A method of processing a nickel bearing solution containing iron, cobalt and manganese constituents, comprising the steps of:
a) removing the iron constituent from the solution using an oxidation and partial neutralization step; and b) removing cobalt and manganese constituents together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of said nickel constituent in solution.
a) removing the iron constituent from the solution using an oxidation and partial neutralization step; and b) removing cobalt and manganese constituents together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of said nickel constituent in solution.
7. A method as defined in claim 6, further comprising the step of:
c) recovering the nickel constituent from solution.
c) recovering the nickel constituent from solution.
8. A process as defined in claim 6 wherein, in step b), the solution is reacted with hypochlorite to precipitate both the cobalt and manganese constituents.
9. A process as defined in claim 8 wherein step b) is conducted at a pH from about 3.0 to about 3.5.
10. A process as defined in claim 6 wherein, in step b), the solution is reacted with a mixture of sulphur dioxide and oxygen to precipitate both the cobalt and manganese constituents.
11. A process as defined in claim 10 wherein step b) is conducted at a pH from about 3.0 to about 3.5.
12. A method of processing a laterite leach solution, comprising the steps of:
a) providing a laterite leach solution including 1 to 10 g/L nickel, 10 to 1000 mg/L cobalt, and 50 to 1500 mg/L manganese;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of said nickel in solution.
a) providing a laterite leach solution including 1 to 10 g/L nickel, 10 to 1000 mg/L cobalt, and 50 to 1500 mg/L manganese;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of said nickel in solution.
13. A method as defined in claim 12, wherein the solution of step a) includes 0 to 2000 mg/L
iron, the method further comprising, before step b), the step of:
c) removing the iron from solution using an oxidation and partial neutralization step.
iron, the method further comprising, before step b), the step of:
c) removing the iron from solution using an oxidation and partial neutralization step.
14. A method as defined in claim 12, further comprising the step of:
d) recovering the nickel from solution.
d) recovering the nickel from solution.
15. A method as defined in claim 12, further comprising the steps of:
e) re-leaching the cobalt and manganese from step b) into an intermediate leach solution;
and f) recovering the cobalt from the intermediate leach solution.
e) re-leaching the cobalt and manganese from step b) into an intermediate leach solution;
and f) recovering the cobalt from the intermediate leach solution.
16. A method as defined in claim 12, further comprising the steps of:
e) re-leaching the cobalt and manganese from step b) into an intermediate leach solution;
and f) recovering the manganese from the intermediate leach solution.
e) re-leaching the cobalt and manganese from step b) into an intermediate leach solution;
and f) recovering the manganese from the intermediate leach solution.
17. A process as defined in claim 12 wherein the solution includes at least one of the following impurities: 0 to 50 g/L chloride, 2 to 15 g/L magnesium and 300 to 600 mg/L
calcium, further comprising the step of:
d) recovering the nickel from solution, while leaving the one or more impurities in solution.
calcium, further comprising the step of:
d) recovering the nickel from solution, while leaving the one or more impurities in solution.
18. A process as defined in claim 14 wherein, in step a), the solution is reacted with hypochlorite to precipitate both the cobalt and manganese.
19. A process as defined in claim 18 wherein step a) is conducted at a pH from about 3.0 to about 3.5.
20. A process as defined in claim 14 wherein, in step a), the solution is reacted with a mixture of sulphur dioxide and oxygen to precipitate both the cobalt and manganese.
21. A process as defined in claim 20 wherein step a) is conducted at a pH from about 3.0 to about 3.5.
22. A method of processing a laterite leach solution, comprising the steps of:
a) providing a laterite leach solution including 1 to 10 g/L nickel, 10 to 1000 mg/L cobalt, 50 to 1500 mg/L manganese, and at least one of the following impurities: 0 to 50 g/L
chloride, 2 to 15 g/L magnesium and 300 to 600 mg/L calcium;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of said nickel and the one or more impurities in solution.
a) providing a laterite leach solution including 1 to 10 g/L nickel, 10 to 1000 mg/L cobalt, 50 to 1500 mg/L manganese, and at least one of the following impurities: 0 to 50 g/L
chloride, 2 to 15 g/L magnesium and 300 to 600 mg/L calcium;
b) removing cobalt and manganese together from the solution using an oxidation step at a pH ranging from about 1 to about 4, to leave substantially all of said nickel and the one or more impurities in solution.
23. A method as defined in claim 22, wherein the solution of step a) includes 0 to 2000 mg/L
iron, the method further comprising, before step b), the step of:
c) removing the iron from solution using an oxidation and partial neutralization step.
iron, the method further comprising, before step b), the step of:
c) removing the iron from solution using an oxidation and partial neutralization step.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US31109201P | 2001-08-10 | 2001-08-10 | |
| US60/311,092 | 2001-08-10 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2396972A1 true CA2396972A1 (en) | 2003-02-10 |
Family
ID=23205366
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA 2396972 Abandoned CA2396972A1 (en) | 2001-08-10 | 2002-08-07 | Processing of nickel bearing solutions |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA2396972A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3638819A4 (en) * | 2017-06-14 | 2021-01-27 | Urban Mining Pty Ltd | Method for the production of cobalt and associated oxides from various feed materials |
-
2002
- 2002-08-07 CA CA 2396972 patent/CA2396972A1/en not_active Abandoned
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3638819A4 (en) * | 2017-06-14 | 2021-01-27 | Urban Mining Pty Ltd | Method for the production of cobalt and associated oxides from various feed materials |
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