AU2011341844A2 - Electro-recovery of gold and silver from leaching solutions by means of simultaneous cathodic and anodic deposition - Google Patents
Electro-recovery of gold and silver from leaching solutions by means of simultaneous cathodic and anodic deposition Download PDFInfo
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- AU2011341844A2 AU2011341844A2 AU2011341844A AU2011341844A AU2011341844A2 AU 2011341844 A2 AU2011341844 A2 AU 2011341844A2 AU 2011341844 A AU2011341844 A AU 2011341844A AU 2011341844 A AU2011341844 A AU 2011341844A AU 2011341844 A2 AU2011341844 A2 AU 2011341844A2
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- silver
- gold
- leaching
- anode
- thiosulfate
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- Abandoned
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- 229910052709 silver Inorganic materials 0.000 title claims abstract description 43
- 239000004332 silver Substances 0.000 title claims abstract description 43
- 239000010931 gold Substances 0.000 title claims abstract description 21
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 title claims abstract description 20
- 229910052737 gold Inorganic materials 0.000 title claims abstract description 20
- 238000002386 leaching Methods 0.000 title claims description 21
- 238000011084 recovery Methods 0.000 title claims description 4
- 230000008021 deposition Effects 0.000 title 1
- UMGDCJDMYOKAJW-UHFFFAOYSA-N thiourea Chemical compound NC(N)=S UMGDCJDMYOKAJW-UHFFFAOYSA-N 0.000 claims abstract description 16
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Natural products NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims abstract description 8
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 8
- 239000003446 ligand Substances 0.000 claims abstract description 4
- 230000003647 oxidation Effects 0.000 claims abstract description 3
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 3
- 230000009467 reduction Effects 0.000 claims abstract description 3
- DHCDFWKWKRSZHF-UHFFFAOYSA-N sulfurothioic S-acid Chemical compound OS(O)(=O)=S DHCDFWKWKRSZHF-UHFFFAOYSA-N 0.000 claims abstract 2
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims description 35
- 238000006722 reduction reaction Methods 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 15
- 229910052500 inorganic mineral Inorganic materials 0.000 abstract description 7
- 239000011707 mineral Substances 0.000 abstract description 7
- 238000005065 mining Methods 0.000 abstract description 4
- 238000011282 treatment Methods 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000000463 material Substances 0.000 abstract description 2
- 238000001465 metallisation Methods 0.000 abstract 1
- 238000004070 electrodeposition Methods 0.000 description 16
- DHCDFWKWKRSZHF-UHFFFAOYSA-L thiosulfate(2-) Chemical compound [O-]S([S-])(=O)=O DHCDFWKWKRSZHF-UHFFFAOYSA-L 0.000 description 14
- 229940048910 thiosulfate Drugs 0.000 description 13
- 238000010586 diagram Methods 0.000 description 8
- 230000008569 process Effects 0.000 description 7
- 239000010949 copper Substances 0.000 description 6
- 229910052751 metal Inorganic materials 0.000 description 5
- 239000002184 metal Substances 0.000 description 5
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 4
- 230000008859 change Effects 0.000 description 4
- 229910052802 copper Inorganic materials 0.000 description 4
- 238000009854 hydrometallurgy Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000002441 X-ray diffraction Methods 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- -1 silver metals Chemical class 0.000 description 3
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 239000008139 complexing agent Substances 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 150000002739 metals Chemical group 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000010936 titanium Substances 0.000 description 2
- 229910052719 titanium Inorganic materials 0.000 description 2
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- PTFCDOFLOPIGGS-UHFFFAOYSA-N Zinc dication Chemical compound [Zn+2] PTFCDOFLOPIGGS-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- GJLUFTKZCBBYMV-UHFFFAOYSA-N carbamimidoylsulfanyl carbamimidothioate Chemical compound NC(=N)SSC(N)=N GJLUFTKZCBBYMV-UHFFFAOYSA-N 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000008367 deionised water Substances 0.000 description 1
- 229910021641 deionized water Inorganic materials 0.000 description 1
- 230000000368 destabilizing effect Effects 0.000 description 1
- 229910000388 diammonium phosphate Inorganic materials 0.000 description 1
- 229940075933 dithionate Drugs 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000005188 flotation Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 229910001739 silver mineral Inorganic materials 0.000 description 1
- OYNOOANKSLJSCV-UHFFFAOYSA-N silver;thiourea Chemical compound [Ag].NC(N)=S OYNOOANKSLJSCV-UHFFFAOYSA-N 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
- C25C1/20—Electrolytic production, recovery or refining of metals by electrolysis of solutions of noble metals
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
- C25C1/22—Electrolytic production, recovery or refining of metals by electrolysis of solutions of metals not provided for in groups C25C1/02 - C25C1/20
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
- C25C7/06—Operating or servicing
- C25C7/08—Separating of deposited metals from the cathode
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Electrolytic Production Of Metals (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention relates to the mining industry, for the treatment of minerals and materials containing gold and silver. The invention specifically relates to a method for recovering gold and silver from thiosulfate and thiourea solutions, by means of an electrolysis method with simultaneous metal deposition on the cathode and anode. The advantages of the invention compared to prior art are that the method is faster and the energy consumption is lower than that observed in conventional cells. The electrolysis is carried out in the potential zones that enable the reduction of the silver and gold on the cathode and the oxidation of the ligand on the anode.
Description
ELECTRORECOVERY OF GOLD AND SILVER FROM LEACHING SOLUTIONS BY SIMULTANEOUS CATHODIC AND ANODIC DEPOSITS 5 FIELD OF THE INVENTION The present invention is related to the mining industry for treat ment of minerals and materials which contain gold and silver. 10 Specifically, it is related to a process to recover gold and silver, from leaching solutions with a simultaneous anodic and cathodic electrodeposition process, after which the poor solution is recy cled back to the leaching stage. 15 BACKGROUND OF THE INVENTION The recovery of gold and silver from their minerals has been performed by various methods; among the most employed are 20 pyrometallurgical treatments, in which upon the addition of a considerable amount of energy, part of the mineral is oxidized, in this manner liberating the precious metals. This great amount of energy is the principal inconvenience of the process, which in the end reflects on the operation costs. 25 On the other hand, the hydrometallurgical methods are charac terized for their high selectivity and relatively low reagent and 2 REPLACEMENT SHEET UNDER ARTICLE 19 energy costs. Gold and silver has been obtained by one such method for over 100 years, using cyanide and oxygen as a com plexing agent and an oxidant, respectively. Despite the high ef ficiency of this system, the treatment of complex minerals, as 5 well as environmental restrictions, has encouraged research on other leaching systems that could compete with cyanide, without its disadvantages. Thiosulfate, in the presence of copper, and the combination of 10 thiourea with formamidine disulfide (Poisot-Diaz, M.E., Gon zilez, I. and Lapidus, G.T. (2008), " Effect of Copper, Iron and Zinc Ions on the Selective Electrodeposition of Doree from Acid ic thiourea Solutions", Hydrometallurgy 2008, Eds. C.A. Young, P.R. Taylor, C.G. Anderson y Y. Choi, Society for Mining, Metal 15 lurgy and Exploration, Inc. (SME), Littleton, Colorado, U.S.A., ISBN: 978-0-87335-266-6, pp. 843-848 and Alonso-G6mez, A.R. and Lapidus, G.T. (2008), "Pretreatment for Refractory Gold and Silver Minerals before Leaching with Ammoniacal Copper Thi osulfate", Hydrometallurgy 2008, Eds. C.A. Young, P.R. Taylor, 20 C.G. Anderson y Y. Choi, Society for Mining, Metallurgy and Ex ploration, Inc. (SME), Littleton, Colorado, U.S.A., ISBN: 978-0 87335-266-6, pp. 817-822.) are two chemical systems that leach gold and silver from minerals for which cyanidation has proved to be inefficient. In this same manner, it was shown possible to 25 recover gold and silver metals in both systems using direct elec trodeposition (A. Alonso. G.T. Lapidus and 1. Gonzelez, A strat- 3 REPLACEMENT SHEET UNDER ARTICLE 19 egy to determine the potential interval for selective silver elec trodeposition from ammoniacal thiosulfate solutions Hydrometal lurgy, Volume 85, Issues 2-4, March 2007, Pages 144-153); However, this recovery was accomplished in geometrically com 5 plex reactors (F.C. Walsh, C. Ponce de Leon and C.T. Low, The rotating cylinder electrode (RCE) an its application to the elec trodeposition of metals, Australian Journal of Chemistry, 58, (4), 246-262 and A. Alonso, G.T. Lapidus and I. Gonzalez, Selective silver electroseparation from ammoniacal thiosulfate solutions 10 using a rotating cylinder electrode reactor (RCE), Hydrometal lurgy, Volume 92, Issues 3-4, June 2008, Pages 115-123), with an energy consumption that renders un attractive from an eco nomic and financial standpoint. 15 At this point, it is important to mention a characteristic of the thiourea and thiosulfate systems: both complexing agents can oxidize at potentials near the reduction potential of silver (Fig ures 1 and 2). The diagrams of both ligands with gold are simi lar. This originates the formation of a narrow potential region 20 where Ag(l) and Au(l) ions are soluble and because of this, both the leaching as well as the electroseparation conditions should be controlled with precision. This could imply a great disadvan tage with respect to other systems and has motivated the use of membrane reactors, in order to avoid contact of these solutions 25 with the anode.
4 REPLACEMENT SHEET UNDER ARTICLE 19 OBJECTIVES OF THE INVENTION 5 One objective of the present invention is to provide a method to separate gold and silver from thiosulfate or thiourea solutions by simultaneous anodic and cathodic electrodeposition, increasing in this manner the velocity of the process. Another is to accom plish this with a minimum affectation of the solution composi 10 tion, so that it may be recirculated back to the leaching stage. Yet another is to promote efficient energy use. Other objectives and advantages that apply the principles and are derived from the present invention may be apparent from the 15 study of the following description and diagrams that are included here for illustrative and not limitative purposes. BRIEF DESCRIPTION OF THE INVENTION 20 The present invention is intended to solve the problem of gold ans silver separation from thiosulfate and thiourea leaching so lutions, providing an improvement over the traditional electro chemical reactors now in use. This improvement is characterizes 25 by a novel process to simultaneously deposit metals in on the 5 REPLACEMENT SHEET UNDER ARTICLE 19 anode and cathode in a one compartment reactor, using a com mercial copper sheet as the anode and a titanium sheet as the cathode. The conditions which permit this technique to operate were cho 5 sen from the analysis of Figure 1, where a region of the soluble complex Ag(S203)2 3 - is observed within the metallic silver stabil ity zone. When the potential is decreased below -110 mV, the Ag(l) species is reduced to Ag 0 , in a typical electrolytic process. However, the most interesting aspect of this diagram is when the 10 potential is less negative than -50 mV, where part of the thiosul fate oxidizes, destabilizing the soluble complex and forming me tallic silver. The present invention takes advantage of this phe nomenon and has not been previously reported for this or other ligands. 15 The application of the simultaneous anodic-cathodic electrode position of gold and silver allows more efficient use of the elec trical energy in electrochemical reactors of simple geometry without a membrane; additionally, the separation process occurs 20 in less time than that required in conventional electrochemical reactors. In order to better understand the characteristics of the inven tion, the following description is accompanied by diagrams and 25 figures, which form an integral part of the same and are meant to be illustrative but not limitative and are described in the fol- 6 REPLACEMENT SHEET UNDER ARTICLE 19 lowing section. BRIEF DESCRIPTION OF THE DRAWINGS 5 Figure 1 is a Pourbaix-type diagram in which the predominance zones for the soluble species Ag(S203)2 3 - (thiosulfate-silver complex) and metallic silver AgO are shown. 10 Figure 2 is a Pourbaix-type diagram in which the predominance zones for the soluble species AgTu3+ (thiourea-silver complex) and metallic silver Ag 0 are shown. Figure 3 shows a leaching-electrodeposition scheme for obtain 15 ing gold and silver which utilizes the present invention. Figure 4 is a diagram showing a recirculation system which in cludes the electrochemical reactor. 20 Figure 5 is a schematic diagram of the electrochemical cell in which the simultaneous anodic and cathodic deposits are achieved. Figure 6 is a graphic representation of the change in silver con 25 centration with leaching time.
H \dI\lninmoenNRPonbl\DCC\DXI.\53515 I1_) DOC-26M/20 13 7 Figure 7 is a graphic representation of the change in silver concentration with electrolysis time where there is simultaneous anodic and cathodic electrodeposition. 5 Figure 8 is a graph that compares the change in silver concentration for leaches 1, 2 and 3 with the same solution. Figure 9 shows the comparison of the silver concentration during electrolysis 1, 2 and 3 with the same solution. 10 Figure 10 shows a comparison of XRD spectra for the anodic deposit obtained after the electrolysis and for pure metallic silver. DETAILED DESCRIPTION OF THE INVENTION 15 The simultaneous electrodeposition process, referred to in the present invention, is illustrated in Figure 3. . A thiosulfate or thiourea solution, rich in gold and silver ions, 20 originating from the leaching stage (100) and after having been filtered (200), is introduced into the electrochemical reactor (300). * Once the electrodeposition has finalized, the cathode (312, Figure 5) and the anode (313, Figure 5) are removed from the reactor 25 and mechanically abraded to remove the gold and silver metals. The solution is then recirculated back to the leaching 8 REPLACEMENT SHEET UNDER ARTICLE 19 stage (301). The electrodeposition is performed in a recirculation scheme, illustrated in Figure 4, in which the solution is charged to the 5 reservoir (320) from which it is pumped (330) to the electro chemical reactor (310) and then returned by gravity to the reser voir. EXAMPLES 10 EXAMPLE 1 To better understand the invention, one of the many experiments is detailed as an example, which employs a system such as that 15 schematized in Figures 3 to 5. A 60 cm 2 (exposed geometrical area) titanium plate was used as the cathode and a copper plate with the same exposed area was the anode. As shown in Figure 3, the first stage is gold and silver leaching from the mineral or concentrate, using a thiosulfate solution, in 20 this case, whose composition is presented in Table 1. The pH was adjusted to 10.0 with NH 4 0H. Table 1. Composition of the leaching solution Component Composition (mol/L) (NH4)28203 0.2 9 REPLACEMENT SHEET UNDER ARTICLE 19 CuSO 4 0.05 EDTA 0.025 (NH4)2HP04 0.1 The solutions were prepared with reagent grade chemicals using deionized water (lx1OIC MQcm- 1 ). 500 mL of this solution was placed in contact with 3.75 g of a flotation concentrate, with a 5 particle size less than 10 pm, containing 21 kg/ton of silver. Af ter six hours in continuous agitation, the solution was separated from the solid by filtration and placed in a reactor such as that represented in Figures 4 and 5. 10 During the electrodeposition, a flow of 1.1 L/min was used with a cell voltage of 100 mV; with this voltage, the potential at the cathode was -260 mV versus the normal hydrogen electrode (NHE), which is adequate to obtain a selective silver deposit on this electrode 15 Figure 6 shows a graphic representation of the silver concentra tion with respect to the leaching time. A maximum value was at tained in 120 minutes, after which time the concentration re mained relatively constant. 20 The change in silver concentration during the electrolysis is shown in Figure 7. Within the first 15 minutes a sharp descent is 10 REPLACEMENT SHEET UNDER ARTICLE 19 observed, which then gradually decreases to values below 10 mg/L. The current registered throughout the experiment was 0.01 A, which together with the cell voltage translates to 0.004 W-h, Considering that the deposited mass of silver was 0.065 g, the 5 energy consumption was 0.062 W-h per g of deposited silver. After finalizing the electrodeposition, the solution was recycled back to the leaching stage, where it was contacted with fresh unleached concentrate, under the same conditions as described 10 previously. The entire procedure was repeated until three full cycles were completed. Figure 8 shows a graphic representation of the leaching results for all three cycles; an increase in the leaching velocity and the 15 maximum silver concentration may be observed in the second and third leach, relative to the first, possibly due to the stabili zation of the equilibria between the thiosulfate and the Cu(IlI) and Cu(l) ions. 20 On the other hand, the second and third electrolyses (the dashed and dotted lines of Figure 9) show similar tendencies to that of the first (solid line), only differentiable by the initial val ue, which depends on the previous leaching stage. In all three cases, the values reached below 10 mg/L in approximately 4 25 hours.
HU ixl~nmoen\o~cn RPonbl\DCC\DXL\535151 I DOC-26A7/2ol0 11 These results clearly show that the thiosulfate solution can be recirculated after the electrodeposition stage, back to the leaching stage, at least three times without reconditioning or make-up. Additionally, during the three electrolyses, the current maintained a 5 constant value of 0.01 A, conserving the same energy expenditure as the first cycle. Anode consumption was negligible after three electrodeposition cycles. Finally, it is important to mention that X-ray diffraction analysis of 10 both the anodic and the cathodic deposits showed that they consisted exclusively of metallic silver. Figure 10 compares the XRD spectra for the deposit obtained from the anode, at the end of the electrolysis and the corresponding 15 spectra for pure metallic silver. As can be- observed, the anodic deposit corresponds to metallic silver; indicating that oxidation of thiosulfate is forming only soluble species, such as tetrathionate, dithionate or even sulfate, and is not contaminating the deposit.
Claims (1)
1. Electrolysis for the silver recovery from thiosulfate or thio urea leaching solutions characterized by accomplishing metallic deposits simultaneously on the anode and cathode surfaces, by 10 operating in the potential zones that permit silver or gold reduc tion at the cathode and ligand oxidation at the anode. 15 20 25
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| MXMX/A/2010/013717 | 2010-12-13 | ||
| MX2010013717A MX2010013717A (en) | 2010-12-13 | 2010-12-13 | Electro-recovery of gold and silver from leaching solutions by means of simultaneous cathodic and anodic deposition. |
| PCT/MX2011/000151 WO2012081952A2 (en) | 2010-12-13 | 2011-12-09 | Electro-recovery of gold and silver from leaching solutions by means of simultaneous cathodic and anodic deposition |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2016200327 Division | 2011-12-09 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| AU2011341844A1 AU2011341844A1 (en) | 2013-08-01 |
| AU2011341844A2 true AU2011341844A2 (en) | 2013-10-17 |
Family
ID=45558362
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2011341844A Abandoned AU2011341844A1 (en) | 2010-12-13 | 2011-12-09 | Electro-recovery of gold and silver from leaching solutions by means of simultaneous cathodic and anodic deposition |
Country Status (12)
| Country | Link |
|---|---|
| US (1) | US20140076735A1 (en) |
| EP (1) | EP2653590A2 (en) |
| JP (1) | JP2014505788A (en) |
| CN (1) | CN103380234A (en) |
| AU (1) | AU2011341844A1 (en) |
| BR (1) | BR112013014874A2 (en) |
| CA (1) | CA2821421A1 (en) |
| CO (1) | CO6801793A2 (en) |
| MX (1) | MX2010013717A (en) |
| PE (1) | PE20140494A1 (en) |
| RU (1) | RU2013132451A (en) |
| WO (1) | WO2012081952A2 (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2016018409A1 (en) * | 2014-07-31 | 2016-02-04 | Hewlett-Packard Development Company, L.P. | Process image according to mat characteristic |
| MX2019006790A (en) * | 2016-12-08 | 2019-11-12 | Metoxs Pte Ltd | Recovery of gold and silver from precious metals-containing solids. |
| US10807085B2 (en) * | 2017-11-17 | 2020-10-20 | University Of Massachusetts | Silver recovery as Ag0nanoparticles from ion-exchange regenerant solution |
| CN113621995B (en) * | 2021-07-16 | 2023-12-26 | 武汉理工大学 | Method for recycling noble metals in thiosulfate leaching solution based on electrochemical combined catalysis technology |
| CN113652554B (en) * | 2021-07-16 | 2022-12-27 | 武汉理工大学 | Method for recovering noble metal in solution based on capacitive deionization technology |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3616332A (en) * | 1969-12-17 | 1971-10-26 | Texas Instruments Inc | Process for recovering silver from scrap materials and electrolyte composition for use therein |
| US4280884A (en) * | 1980-04-07 | 1981-07-28 | Demco, Inc. | Method and apparatus for recovery of silver employing an electrolytic cell having improved solution movement |
| CN85103707B (en) * | 1985-05-13 | 1987-05-06 | 华东化工学院 | Technology to extract gold, silver and copper from gold ore |
| GB8927964D0 (en) * | 1989-12-11 | 1990-02-14 | Kodak Ltd | Method and apparatus for recovering silver from a photographic fixing solution |
| JP3816241B2 (en) * | 1998-07-14 | 2006-08-30 | 株式会社大和化成研究所 | Aqueous solution for reducing and precipitating metals |
| JP2001192878A (en) * | 2000-01-11 | 2001-07-17 | Yuken Industry Co Ltd | Method for recovering noble metal from metallic composition |
| US8025859B2 (en) * | 2007-05-18 | 2011-09-27 | Cesl Limited | Process for gold and silver recovery from a sulphide concentrate |
| MX2008003602A (en) * | 2008-03-14 | 2009-02-25 | Univ Autonoma Metropolitana | Process for the lixiviation and recovery of silver and gold with copper ammonia thiosulfate solutions. |
| MX2008008671A (en) * | 2008-07-02 | 2010-01-04 | Univ Autonoma Metropolitana | Electrochemical reactor of the press filter-type for the recovery of gold (au) and silver (ag) in powder. |
-
2010
- 2010-12-13 MX MX2010013717A patent/MX2010013717A/en active IP Right Grant
-
2011
- 2011-12-09 US US13/993,247 patent/US20140076735A1/en not_active Abandoned
- 2011-12-09 CA CA2821421A patent/CA2821421A1/en not_active Abandoned
- 2011-12-09 PE PE2013001408A patent/PE20140494A1/en not_active Application Discontinuation
- 2011-12-09 CN CN2011800674437A patent/CN103380234A/en active Pending
- 2011-12-09 AU AU2011341844A patent/AU2011341844A1/en not_active Abandoned
- 2011-12-09 WO PCT/MX2011/000151 patent/WO2012081952A2/en active Application Filing
- 2011-12-09 EP EP11813915.3A patent/EP2653590A2/en not_active Withdrawn
- 2011-12-09 JP JP2013544412A patent/JP2014505788A/en active Pending
- 2011-12-09 BR BR112013014874A patent/BR112013014874A2/en not_active IP Right Cessation
- 2011-12-09 RU RU2013132451/02A patent/RU2013132451A/en not_active Application Discontinuation
-
2013
- 2013-07-10 CO CO13164020A patent/CO6801793A2/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| WO2012081952A4 (en) | 2013-01-24 |
| CA2821421A1 (en) | 2012-06-21 |
| JP2014505788A (en) | 2014-03-06 |
| PE20140494A1 (en) | 2014-04-30 |
| AU2011341844A1 (en) | 2013-08-01 |
| CO6801793A2 (en) | 2013-11-29 |
| US20140076735A1 (en) | 2014-03-20 |
| RU2013132451A (en) | 2015-01-20 |
| BR112013014874A2 (en) | 2016-10-18 |
| WO2012081952A3 (en) | 2012-12-06 |
| CN103380234A (en) | 2013-10-30 |
| WO2012081952A2 (en) | 2012-06-21 |
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| MX2010013717A (en) | 2012-06-13 |
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