WO1984000563A1 - Recovery of silver and gold from ores and concentrates - Google Patents
Recovery of silver and gold from ores and concentrates Download PDFInfo
- Publication number
- WO1984000563A1 WO1984000563A1 PCT/AU1983/000098 AU8300098W WO8400563A1 WO 1984000563 A1 WO1984000563 A1 WO 1984000563A1 AU 8300098 W AU8300098 W AU 8300098W WO 8400563 A1 WO8400563 A1 WO 8400563A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- process according
- silver
- gold
- solution
- mixture
- Prior art date
Links
- 229910052709 silver Inorganic materials 0.000 title claims abstract description 40
- 239000004332 silver Substances 0.000 title claims abstract description 40
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 239000010931 gold Substances 0.000 title claims abstract description 37
- 229910052737 gold Inorganic materials 0.000 title claims abstract description 36
- 239000012141 concentrate Substances 0.000 title claims abstract description 22
- 238000011084 recovery Methods 0.000 title claims description 15
- 238000000034 method Methods 0.000 claims abstract description 36
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000000460 chlorine Substances 0.000 claims abstract description 34
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 34
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims abstract description 8
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 7
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims abstract description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical group [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 18
- 239000000203 mixture Substances 0.000 claims description 18
- 230000003647 oxidation Effects 0.000 claims description 17
- 238000007254 oxidation reaction Methods 0.000 claims description 17
- 239000007789 gas Substances 0.000 claims description 9
- 229910052742 iron Inorganic materials 0.000 claims description 9
- 229910000831 Steel Inorganic materials 0.000 claims description 7
- 239000010959 steel Substances 0.000 claims description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- 239000003792 electrolyte Substances 0.000 claims description 5
- 239000001257 hydrogen Substances 0.000 claims description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- KKEBXNMGHUCPEZ-UHFFFAOYSA-N 4-phenyl-1-(2-sulfanylethyl)imidazolidin-2-one Chemical compound N1C(=O)N(CCS)CC1C1=CC=CC=C1 KKEBXNMGHUCPEZ-UHFFFAOYSA-N 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical group [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 238000009835 boiling Methods 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 239000007785 strong electrolyte Substances 0.000 claims description 4
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 claims description 2
- 229910052751 metal Inorganic materials 0.000 claims description 2
- 239000002184 metal Substances 0.000 claims description 2
- 238000001556 precipitation Methods 0.000 claims description 2
- 239000007787 solid Substances 0.000 abstract description 3
- 238000007664 blowing Methods 0.000 abstract description 2
- 238000004090 dissolution Methods 0.000 abstract 1
- 239000002244 precipitate Substances 0.000 abstract 1
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 26
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 11
- 238000002386 leaching Methods 0.000 description 6
- 239000011780 sodium chloride Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 4
- 229910052500 inorganic mineral Inorganic materials 0.000 description 4
- 239000011707 mineral Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000005660 chlorination reaction Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000001226 reprecipitation Methods 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 3
- 239000005708 Sodium hypochlorite Substances 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 238000005188 flotation Methods 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- 229910019093 NaOCl Inorganic materials 0.000 description 1
- 230000033558 biomineral tissue development Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 238000010908 decantation Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000009877 rendering Methods 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
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
- C22B11/00—Obtaining noble metals
- C22B11/06—Chloridising
-
- 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
- C22B11/00—Obtaining noble metals
- C22B11/04—Obtaining noble metals by wet processes
Definitions
- This invention relates to a hydrometallurgical method of recovering silver and/or gold from ores and concentrates. Particularly it applies to ores which are not easily treated by normal methods.
- the present invention relates to the treatment of minerals, where not only must a strong oxidant such as chlorine be used, but a high oxidation potential must be maintained in the solution to prevent reprecipitation of the Ag.
- a process for the recovery of silver and/ or gold from a silver and/or gold bearing ore or concentrate which includes
- a process for the recovery of silver and/or gold from a silver and/or gold bearing ore or concentrate which includes 1) forming a mixture of ore or concentrate and a strong electrolyte containing chloride ions, in an anolyte compartment of a cylindrical diaphragm cell, the cell also including an anode, a cathode and a catholyte compartment, 2) maintaining the mixture at a temperature up to the boiling point of the electrolyte whereby the silver and/ or gold is taken into solution,
- the oxidation potential (Eh) is maintained above about 850 m.v. It has been found by keeping the Eh above about 750 m.v. that reprecipitation of silver and/or gold is inhibited.
- a source of chlorine is usually chlorine gas or hypochlorite ion (e.g. sodium hypochlorite) .
- hypochlorite ion e.g. sodium hypochlorite
- an oxygen bearing gas is introduced into the mixture prior to introducing a source of chlorine. This reduces the amount of chlorine subsequently required. When chlorination does occur, it is preferably carried out at a pH of approximately 7.
- the resultant solution contains free chlorine.
- This free chlorine is recovered from the solution by blowing oxygen bearing gases through the solution prior to recovery of the silver and/or gold.
- the mixture of free chlorine and gas is conducted to another vessel containing fresh ore or concentrate, to effect a preliminary oxidation.
- the recovery of silver and/or gold is achieved by precipitation via contact of the solution with a reductant.
- the reductant may be a metal (iron or steel) having a potential above that of silver and/or gold in the electrochemical series.
- pH of the solution during treatment of the ore or concentrate it will be well known to those skilled in the art that same is normally set according to the type of ore or concentrate. For example it is preferable to treat carbonate containing ores or concentrates at a pH of about 7. At this level the material is stable. Similarly if the ore or concentrate contains sulphides, it is preferable to carry out the reaction at a pH of below 7. Typically when one is recovering gold a preferred pH is above 5 and more preferabl about 7. Thus it is to be understood that the present invention is not restricted to a pH of a particular range.
- An Ag bearing mineral was slurried with a strong chloride solution, 25% NaCl, and aerated for 1 to 2 hours at approximately 20 C to treat any easily oxidizable material present. This preliminary aeration can reduce the amount of chlorine required for the Ag leaching in the next step.
- chlorine was added to the slurry mixture in the form of sodium hypochlorite or preferably chlorine gas, and the oxidation potential (Eh) maintained above a value of 750 m.v.
- the chlorination was preferably carried out at a pH of approximately 7.0.
- Table I shows the leaching and reprecipitation of the Ag from solution when the Eh was allowed to fall below 750 m.v.
- Table II shows the leaching and high recovery of Ag from this particular mineral when the Eh was maintained above 850 m.v. throughout the test.
- Feed 260 ppm Feed 260 ppm Residue 250 ppm Residue 9 ppm
- the solution contained free chlorine.
- the solution pH was adjusted to approximately 2.5 to 3.0 and air was blown into the solution to remove free chlorine with the exit gases. These gases were conducted to another vessel con ⁇ taining a new batch of ore, to effect a preliminary oxidation.
- the chlorine free solution was passed to a vessel where it was contacted with a metallic iron reductant. Typically, this operation was effected by passage of the electrolyte down a column of vertical steel rods, for example 2 mm diameter. The Ag formed a powdery deposit on the surface of the iron. Periodically the column was either vibrated slightly or the solution flow adjusted to accomplish the removal of-Ag from the iron surface resulting in collection of the powder in the
- Chlorine was added to slurries of ore (300 g/1) in sodium chloride solution (300 g/1 NaCl) to maintain the Eh above 750 m.v.
- the pH was varied between pH 3.0 and 8.0.
- a cylindrical diaphragm cell was provided to achieve maximum anolyte volume for treatment of low grade ores with a small catholyte volume on the outside of the cylindrical diaphragm, in a cylindrical tank. Current was passed
- OMPI IPO between the anodes, for example graphite, and a high surface area cathode, for example copper, while the silver and/or gold bearing ore was agitated slowly in the anolyte compartment.
- Hydrogen may have been liberated at the cathode to form sodium hydroxide, and oxidized chlorine species may have been formed at the anode.
- Some mixing of the anolyte and the catholyte may have resulted in the formation of such compounds as NaOCl.
- the method and apparatus of the invention results in a greater than 20 times reduction in reagent costs.
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Electrolytic Production Of Metals (AREA)
Abstract
Process for the dissolution of silver and gold from ores and concentrates in a strong chloride solution where the Eh is maintained above a value of 750 m.v. and preferably above a value of 850 m.v. This process may include the additional step of removing excess chlorine from solution by blowing the solution with air and conducting the air and chlorine gas to another vessel where the chlorine is reacted with fresh incoming ore or concentrate. Subsequently the substantially chlorine free solution is contacted with a solid reductant to produce silver or gold precipitate. The above process is particularly suitable for operation in an electrochemical diaphragm cell.
Description
RECOVERY OF SILVER AND GOLD FROM ORES AND CONCENTRATES
FIELD OF THE INVENTION Background of the Invention This invention relates to a hydrometallurgical method of recovering silver and/or gold from ores and concentrates. Particularly it applies to ores which are not easily treated by normal methods.
Many silver and gold bearing ores and concentrates are treated by flotation and cyanidation. This can often lead to low recoveries due to the variety of mineralization which may be present. For example it is known that many ores containing appreciable quantities of manganese are treated with low recoveries.
Description of the Prior art
In Australian Patent Application 75848/81, "Recovery of Silver and Gold from Ores and Concentrates", there is described a process for the treatment of minerals that are not easily treated by traditional flotation and cyanidation processes. In this respect, it has been found possible to leach many Ag bearing materials by using a strong chloride solution. Typically strong chloride solutio may be used: a) without oxidation; b) with air oxidation; c) with air oxidation using a Cu catalyst; and d) oxidation using chlorine.
Further investigations have revealed that for some silver and/or gold ores or concentrates, the use of a strong oxidant is still not effective enough under normal process conditions.
OMPI
The Invention
The present invention relates to the treatment of minerals, where not only must a strong oxidant such as chlorine be used, but a high oxidation potential must be maintained in the solution to prevent reprecipitation of the Ag.
Preferred Aspects of the Invention
Accordingly, there is provided in one aspect of the invention, a process for the recovery of silver and/ or gold from a silver and/or gold bearing ore or concentrate which includes
1) forming a mixture of ore or concentrate and a strong electrolyte containing chloride ions,
2) maintaining the mixture at a temperature up to the boiling point of the electrolyte whereby the silver and/ or gold is taken into solution,
3) maintaining an oxidation potential of the solution above about 750 m.v. with reference to a hydrogen • e1ectrode, and 4) recovering silver and/or gold from the solution.
In another aspect of the invention, there is provided a process for the recovery of silver and/or gold from a silver and/or gold bearing ore or concentrate which includes 1) forming a mixture of ore or concentrate and a strong electrolyte containing chloride ions, in an anolyte compartment of a cylindrical diaphragm cell, the cell also including an anode, a cathode and a catholyte compartment, 2) maintaining the mixture at a temperature up to the boiling point of the electrolyte whereby the silver and/ or gold is taken into solution,
3) passing current between the anode and cathode to maintain an oxidation potential of the solution above about 750 m.v. with reference to a hydrogen electrode,
4) recovering silver and/or gold from the solution.
Λ
Preferably the oxidation potential (Eh) is maintained above about 850 m.v. It has been found by keeping the Eh above about 750 m.v. that reprecipitation of silver and/or gold is inhibited. To effect control of the Eh, it is convenient to add a source of chlorine. This source of chlorine is usually chlorine gas or hypochlorite ion (e.g. sodium hypochlorite) . Alternatively, it is possible to effect the control of Eh by passing a current through the mixture. Typically only intermittent passage of current will be necessary. As such it is possible to significantly reduce the chlorine requirement of the process.
Preferably prior to introducing a source of chlorine, an oxygen bearing gas is introduced into the mixture. This reduces the amount of chlorine subsequently required. When chlorination does occur, it is preferably carried out at a pH of approximately 7.
Where substantial amounts of chlorine are introduced, the resultant solution contains free chlorine. This free chlorine is recovered from the solution by blowing oxygen bearing gases through the solution prior to recovery of the silver and/or gold. To enhance the efficiency of process, the mixture of free chlorine and gas is conducted to another vessel containing fresh ore or concentrate, to effect a preliminary oxidation.
Desirably the recovery of silver and/or gold is achieved by precipitation via contact of the solution with a reductant. The reductant may be a metal (iron or steel) having a potential above that of silver and/or gold in the electrochemical series.
When iron or steel is employed, it is usual to form a column of elongated iron or steel members e.g. rods. Typically the solution is passed through the column and by contacting the surface of the members the silver and/or gold is precipitated. To ensure recovery of the precipitated silver and/or gold from the steel or iron members, it is desirable to either vibrate the column or
increase the volume of solution flowing therethrough. Thus the silver or gold powder will collect in the bottom of the column and be easily removed.
With regard to the pH of the solution during treatment of the ore or concentrate, it will be well known to those skilled in the art that same is normally set according to the type of ore or concentrate. For example it is preferable to treat carbonate containing ores or concentrates at a pH of about 7. At this level the material is stable. Similarly if the ore or concentrate contains sulphides, it is preferable to carry out the reaction at a pH of below 7. Typically when one is recovering gold a preferred pH is above 5 and more preferabl about 7. Thus it is to be understood that the present invention is not restricted to a pH of a particular range.
Examples
An Ag bearing mineral was slurried with a strong chloride solution, 25% NaCl, and aerated for 1 to 2 hours at approximately 20 C to treat any easily oxidizable material present. This preliminary aeration can reduce the amount of chlorine required for the Ag leaching in the next step. After the aeration, chlorine was added to the slurry mixture in the form of sodium hypochlorite or preferably chlorine gas, and the oxidation potential (Eh) maintained above a value of 750 m.v. The chlorination was preferably carried out at a pH of approximately 7.0. Table I shows the leaching and reprecipitation of the Ag from solution when the Eh was allowed to fall below 750 m.v. Table II shows the leaching and high recovery of Ag from this particular mineral when the Eh was maintained above 850 m.v. throughout the test.
OMPI
Leaching of Silver Ores
Slurry Density 300 g/1 - NaCl 250 g/1 - Temperature 30 C
Table I Table II
Eh(mv) Ag (ppm) Eh(mv) Ag (ppm) in soln. in soln.
780 25 850 55 765 26 855 59 725 23 866 66 740 16 893 69 726 11 892 73 440 3 865 74
Feed 260 ppm Feed 260 ppm Residue 250 ppm Residue 9 ppm
The solution was separated from the solids by
- filtration or counter-current decantation and because of the Eh requirement of greater than about 850 m.v. the solution contained free chlorine. The solution pH was adjusted to approximately 2.5 to 3.0 and air was blown into the solution to remove free chlorine with the exit gases. These gases were conducted to another vessel con¬ taining a new batch of ore, to effect a preliminary oxidation. When the chlorine removal step had been accomplished the new batch of ore then proceeded to the chlorination stage where the Eh was maintained above 850 m.v. The chlorine free solution was passed to a vessel where it was contacted with a metallic iron reductant. Typically, this operation was effected by passage of the electrolyte down a column of vertical steel rods, for example 2 mm diameter. The Ag formed a powdery deposit on the surface of the iron. Periodically the column was either vibrated slightly or the solution flow adjusted to accomplish the removal of-Ag from the iron surface resulting in collection of the powder in the
SRE
OMPI_ xfø IPO
'
bottom of the column.
It was found in many examples that large amounts of chlorine were required, rendering the process potentially uneconomic. The following example was one where the cost of chlorine was high.
Six kilos of ore assaying 160 ppm of silver were agitated in 20 litres of 25% NaCl in a 25 litre tank. Chlorine was admitted from a cylinder through a measuring apparatus to the sealed tank periodically to maintain the oxidation potential above 850 m.v. Over a 5 hour period the silver was liberated with a final Ag concentration in solution of 40 ppm Ag. The analysis of the residue showed 20 ppm Ag. The chlorine usage however was 35g for the 6 kilos. The cost of the chlorine was a large part of the value of the recovered silver.
The following examples illustrate the leaching of gold under these conditions.
Chlorine was added to slurries of ore (300 g/1) in sodium chloride solution (300 g/1 NaCl) to maintain the Eh above 750 m.v. The pH was varied between pH 3.0 and 8.0.
Sample Au Content (ppm)
Feed * 7.8
Residue from pH3 test 6.2
Residue from pH4 test 5.5 Residue from pH5 test 0.8
Residue from pH6.5 test " 0.5
Residue from pH8 test 0.3
These results showed the improved leaching of gold under these Eh conditions at a pH of over 5.0. The following example shows how electrochemical techniques can be used to overcome these high costs.
A cylindrical diaphragm cell was provided to achieve maximum anolyte volume for treatment of low grade ores with a small catholyte volume on the outside of the cylindrical diaphragm, in a cylindrical tank. Current was passed
OMPI IPO
between the anodes, for example graphite, and a high surface area cathode, for example copper, while the silver and/or gold bearing ore was agitated slowly in the anolyte compartment. Hydrogen may have been liberated at the cathode to form sodium hydroxide, and oxidized chlorine species may have been formed at the anode. Some mixing of the anolyte and the catholyte may have resulted in the formation of such compounds as NaOCl.
The following example illustrates the operation of an embodiment of this process, carried out, in a cylindrical diaphragm cell of the type illustrated and labelled in the accompanying drawing.
6 kilos of ore assaying 160 ppm of silver were agitated in 20 litres of 25% NaCl in a 25 litre cylindrical diaphragm cell. The current was turned on periodically to maintain the oxidation potential above 850 m.v. with reference to the saturated hydrogen electrode. Over a 4 hour period, current was passed at 2 amps, and 3.4 volts, for a total of 30 minutes. The theoretical amount of chlorine generated by this method would be 1.55 grams. The solution analysed 41 ppm Ag and the analysis of the solid residue showed a concentration of 16 ppm Ag. This resulted in a theoretical chlorine usage of 1.79 grams/ gram Ag. Although the example of the embodiment is described according to the liberation of chlorine at the anode, it will be appreciated that many different compounds can be generated.
The method and apparatus of the invention results in a greater than 20 times reduction in reagent costs.
Obviously, this is a significant improvement over previous proposals involved with the use of chlorine gas.
Claims
1. A process for the recovery of silver and/or gold from a silver and/or gold bearing ore or concentrate which includes
1) forming a mixture of ore or concentrate and a strong electrolyte containing chloride ions,
2) maintaining the mixture at a temperature up to the boiling point of the electrolyte whereby the silver and/ or gold is taken into solution,
3) maintaining an oxidation potential of the solution above about 750 m.v. with reference to a hydrogen electrode, and
4) recovering silver and/or gold from the solution.
2. A process according to Claim 1 wherein the oxidation potential of the solution is maintained above about 850 m.v.
3. A process according to either Claims 1 or 2 wherein an oxygen bearing gas is introduced into the mixture.
4. A process according to any one of Claims 1 to 3 wherein a source of chlorine is added to the mixture.
5. A process according to Claim 4 wherein the source of chlorine is chlorine gas or hypochlorite ion.
6. A process according to Claim 4 wherein the pH of the mixture is approximately 7.0.
7. A process according to Claim 1 wherein an oxygen bearing gas is blown through the solution prior to the recovery step (4) , to form a mixture of said gas and free chlorine.
8. A process according to Claim 7 wherein the mixture of said gas and free chlorine is admixed with fresh silver and/or gold bearing ore or concentrate.
9. A process according to any one of Claims 1 to 8 wherein the recovery includes contacting the solution with a reductant to precipitate silver and/or gold.
10. A process according to Claim 9 wherein the reductant is a metal having a potential above that of silver and/or gold in the electrochemical series.
11. A process according to Claim 9 wherein the reductant is iron or steel.
12. A process according to Claim 9 wherein the precipitation is carried out in a column containing a plurality of elongated iron and steel members.
13. A process according to Claim 12 wherein the column is vibrated.
14. A process according to Claim 12 wherein the solution is turbulent within the column.
15. A process for the recovery of silver and/or gold from a silver and/or gold bearing ore or concentrate which includes
1) forming a mixture of ore or concentrate and a strong electrolyte containing chloride ions, in an anolyte compartment of a cylindrical diaphragm cell, the cell also including an anode, a cathode and a catholyte compart¬ ment,
2) maintaining the mixture at a temperature up to the boiling point of the electrolyte whereby the silver and/ or gold is taken into solution,
3) passing current between the anode and cathode to maintain an oxidation potential of the solution above about 750 m.v. with reference to a hydrogen electrode,
4) recovering silver and/or gold from the solution.
16. A process according to Claim 15 wherein the oxidation potential of the solution is maintained above about 850 m.v.
17. A process according to Claim 15 wherein the catholyte compartment has a volume which is smaller than that of the anolyte compartment.
18. A process according to Claim 15 wherein said mixture is agitated in the anolyte compartment.
19. A process according to Claim 15 wherein the current is intermittently between the anode and cathode.
OMPI
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| BR8307472A BR8307472A (en) | 1982-08-05 | 1983-08-02 | SILVER AND GOLD RECOVERY PROCESS FROM MINES AND CONCENTRATES |
| FI841328A FI841328A0 (en) | 1982-08-05 | 1984-04-03 | AOTERVINNING AV SILVER OCH GULD FRAON MALMER OCH KONCENTRAT. |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AUPF522682 | 1982-08-05 | ||
| AUPF722482 | 1982-12-10 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| WO1984000563A1 true WO1984000563A1 (en) | 1984-02-16 |
Family
ID=25642566
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/AU1983/000098 WO1984000563A1 (en) | 1982-08-05 | 1983-08-02 | Recovery of silver and gold from ores and concentrates |
Country Status (8)
| Country | Link |
|---|---|
| EP (1) | EP0115500A4 (en) |
| JP (1) | JPS59501370A (en) |
| FI (1) | FI841328A0 (en) |
| IT (1) | IT1228590B (en) |
| NZ (1) | NZ205153A (en) |
| PH (1) | PH19799A (en) |
| WO (1) | WO1984000563A1 (en) |
| ZW (1) | ZW17483A1 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0220811A1 (en) * | 1985-08-29 | 1987-05-06 | 296388 B.C. Ltd. | Process and apparatus for removing precious metals from solutions |
| US4980134A (en) * | 1985-09-10 | 1990-12-25 | Action Gold Development Ltd. | Leaching process |
| CN100473732C (en) * | 2007-02-09 | 2009-04-01 | 上海大学 | Device for leaching gold mine by electrochemistry oxidation method |
| CN100485055C (en) * | 2007-02-09 | 2009-05-06 | 上海大学 | Method for leaching gold mine by electrochemistry oxidation method |
| US7858056B2 (en) | 2002-12-31 | 2010-12-28 | Intec, Ltd. | Recovering metals from sulfidic materials |
| WO2014053705A1 (en) * | 2012-10-03 | 2014-04-10 | Outotec Oyj | Method for recovery of silver from sulphur-containing zinc leach residues |
| US10400306B2 (en) | 2014-05-12 | 2019-09-03 | Summit Mining International Inc. | Brine leaching process for recovering valuable metals from oxide materials |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2794815B2 (en) * | 1989-08-31 | 1998-09-10 | 三菱マテリアル株式会社 | Gold electrolytic smelting equipment |
| PL2435590T3 (en) * | 2009-05-26 | 2018-11-30 | Metaleach Limited | Method of oxidative leaching of sulfide ores and/or concentrates |
| RU2476610C2 (en) * | 2010-12-28 | 2013-02-27 | Общество с ограниченной ответственностью "Научно-внедренческое предприятие "Флюидные Технологии и Экология" | Extraction method of metals from metal-containing mineral raw material |
| RU2497962C1 (en) * | 2012-05-17 | 2013-11-10 | Федеральное государственное бюджетное образовательное учреждение высшего профессионального образования "Забайкальский государственный университет" (ФГБОУ ВПО "ЗабГУ") | Method to extract dispersed gold from refractory ores |
| RU2510669C2 (en) * | 2012-08-14 | 2014-04-10 | Арье БАРБОЙ | Method of extracting noble metals from wastes |
| RU2655413C9 (en) * | 2015-02-12 | 2018-07-24 | БЕЛОЗЕРОВА Татьяна Алексеевна | Method for processing polymetallic raw materials (variants) and device for its leaching |
| JP6492970B2 (en) * | 2015-05-26 | 2019-04-03 | 住友金属鉱山株式会社 | Wet electrowinning method for gold and silver and wet electrowinning equipment for gold and silver |
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| US3639925A (en) * | 1968-05-15 | 1972-02-08 | Us Interior | Recovery of gold from carbonaceous ores |
| GB1277263A (en) * | 1968-06-07 | 1972-06-07 | Eastman Kodak Co | Recovery of noble metals |
| US3772003A (en) * | 1972-02-07 | 1973-11-13 | J Gordy | Process for the electrolytic recovery of lead, silver and zinc from their ore |
| AU5203873A (en) * | 1972-02-10 | 1974-08-15 | Australian Mineral Development Laboratories | ELECTROLYTIC OXIDATION AND REDUCTION OF Specification SULPHIDE CONCENTRATES |
| AU5465673A (en) * | 1972-04-21 | 1974-10-24 | Cyprus Metallurgical Processes Corporation | Process forthe recovery of metals from sulfide ores through electrolytic dissociation ofthe sulfides |
| US3957603A (en) * | 1974-06-14 | 1976-05-18 | Electromet, Inc. | Electrolytic gold recovery and separation process |
| WO1982001195A1 (en) * | 1980-09-29 | 1982-04-15 | Everett P | Recovery of silver and gold from ores and concentrates |
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| DE2734249A1 (en) * | 1977-07-29 | 1979-02-08 | Bayer Ag | THIGH NECK PROSTHESIS |
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1983
- 1983-07-29 IT IT8348784A patent/IT1228590B/en active
- 1983-07-29 ZW ZW174/83A patent/ZW17483A1/en unknown
- 1983-08-02 JP JP58502551A patent/JPS59501370A/en active Pending
- 1983-08-02 WO PCT/AU1983/000098 patent/WO1984000563A1/en not_active Application Discontinuation
- 1983-08-02 EP EP19830902420 patent/EP0115500A4/en not_active Withdrawn
- 1983-08-02 PH PH29340A patent/PH19799A/en unknown
- 1983-08-04 NZ NZ205153A patent/NZ205153A/en unknown
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1984
- 1984-04-03 FI FI841328A patent/FI841328A0/en not_active Application Discontinuation
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2835569A (en) * | 1956-04-19 | 1958-05-20 | Electro Chimie Metal | Process of extracting gold and other metals from ores, concentrates, residues and the like containing principally cobalt, nickel, iron, arsenic and gold |
| US3639925A (en) * | 1968-05-15 | 1972-02-08 | Us Interior | Recovery of gold from carbonaceous ores |
| GB1277263A (en) * | 1968-06-07 | 1972-06-07 | Eastman Kodak Co | Recovery of noble metals |
| US3772003A (en) * | 1972-02-07 | 1973-11-13 | J Gordy | Process for the electrolytic recovery of lead, silver and zinc from their ore |
| AU5203873A (en) * | 1972-02-10 | 1974-08-15 | Australian Mineral Development Laboratories | ELECTROLYTIC OXIDATION AND REDUCTION OF Specification SULPHIDE CONCENTRATES |
| AU5465673A (en) * | 1972-04-21 | 1974-10-24 | Cyprus Metallurgical Processes Corporation | Process forthe recovery of metals from sulfide ores through electrolytic dissociation ofthe sulfides |
| US3957603A (en) * | 1974-06-14 | 1976-05-18 | Electromet, Inc. | Electrolytic gold recovery and separation process |
| WO1982001195A1 (en) * | 1980-09-29 | 1982-04-15 | Everett P | Recovery of silver and gold from ores and concentrates |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0220811A1 (en) * | 1985-08-29 | 1987-05-06 | 296388 B.C. Ltd. | Process and apparatus for removing precious metals from solutions |
| US4980134A (en) * | 1985-09-10 | 1990-12-25 | Action Gold Development Ltd. | Leaching process |
| US7858056B2 (en) | 2002-12-31 | 2010-12-28 | Intec, Ltd. | Recovering metals from sulfidic materials |
| CN100473732C (en) * | 2007-02-09 | 2009-04-01 | 上海大学 | Device for leaching gold mine by electrochemistry oxidation method |
| CN100485055C (en) * | 2007-02-09 | 2009-05-06 | 上海大学 | Method for leaching gold mine by electrochemistry oxidation method |
| WO2014053705A1 (en) * | 2012-10-03 | 2014-04-10 | Outotec Oyj | Method for recovery of silver from sulphur-containing zinc leach residues |
| AU2013326361B2 (en) * | 2012-10-03 | 2016-06-16 | Outotec (Finland) Oy | Method for recovery of silver from sulphur-containing zinc leach residues |
| EA029249B1 (en) * | 2012-10-03 | 2018-02-28 | Оутотек (Финлэнд) Ой | Method for recovery of silver from sulphur-containing zinc leach residues |
| US10400306B2 (en) | 2014-05-12 | 2019-09-03 | Summit Mining International Inc. | Brine leaching process for recovering valuable metals from oxide materials |
Also Published As
| Publication number | Publication date |
|---|---|
| FI841328A (en) | 1984-04-03 |
| PH19799A (en) | 1986-07-02 |
| EP0115500A1 (en) | 1984-08-15 |
| IT8348784A0 (en) | 1983-07-29 |
| NZ205153A (en) | 1985-08-30 |
| JPS59501370A (en) | 1984-08-02 |
| ZW17483A1 (en) | 1983-10-26 |
| FI841328A0 (en) | 1984-04-03 |
| IT1228590B (en) | 1991-06-24 |
| EP0115500A4 (en) | 1984-11-23 |
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