US20140311896A1 - Electrorecovery of gold and silver from thiosulphate solutions - Google Patents
Electrorecovery of gold and silver from thiosulphate solutions Download PDFInfo
- Publication number
- US20140311896A1 US20140311896A1 US13/992,713 US201113992713A US2014311896A1 US 20140311896 A1 US20140311896 A1 US 20140311896A1 US 201113992713 A US201113992713 A US 201113992713A US 2014311896 A1 US2014311896 A1 US 2014311896A1
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- United States
- Prior art keywords
- silver
- leaching
- copper
- solution
- gold
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- 229910052709 silver Inorganic materials 0.000 title claims abstract description 58
- 239000004332 silver Substances 0.000 title claims abstract description 58
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 title claims abstract description 27
- 229910052737 gold Inorganic materials 0.000 title claims abstract description 27
- 239000010931 gold Substances 0.000 title claims abstract description 27
- DHCDFWKWKRSZHF-UHFFFAOYSA-L thiosulfate(2-) Chemical compound [O-]S([S-])(=O)=O DHCDFWKWKRSZHF-UHFFFAOYSA-L 0.000 title description 20
- 238000000034 method Methods 0.000 claims abstract description 40
- 238000002386 leaching Methods 0.000 claims abstract description 37
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims abstract description 24
- 229910052802 copper Inorganic materials 0.000 claims abstract description 22
- 239000010949 copper Substances 0.000 claims abstract description 22
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 20
- 239000003014 ion exchange membrane Substances 0.000 claims abstract description 5
- DHCDFWKWKRSZHF-UHFFFAOYSA-N sulfurothioic S-acid Chemical compound OS(O)(=O)=S DHCDFWKWKRSZHF-UHFFFAOYSA-N 0.000 claims abstract 4
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims description 52
- JPVYNHNXODAKFH-UHFFFAOYSA-N Cu2+ Chemical compound [Cu+2] JPVYNHNXODAKFH-UHFFFAOYSA-N 0.000 claims description 5
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 5
- 239000010936 titanium Substances 0.000 claims description 5
- 229910052719 titanium Inorganic materials 0.000 claims description 5
- 229910001431 copper ion Inorganic materials 0.000 claims description 4
- 239000002659 electrodeposit Substances 0.000 claims description 3
- 239000000463 material Substances 0.000 abstract description 10
- 229910052500 inorganic mineral Inorganic materials 0.000 abstract description 8
- 239000011707 mineral Substances 0.000 abstract description 8
- ANVWDQSUFNXVLB-UHFFFAOYSA-L copper;dioxido-oxo-sulfanylidene-$l^{6}-sulfane Chemical compound [Cu+2].[O-]S([O-])(=O)=S ANVWDQSUFNXVLB-UHFFFAOYSA-L 0.000 abstract description 4
- 238000005065 mining Methods 0.000 abstract description 2
- 238000004070 electrodeposition Methods 0.000 description 15
- 239000000203 mixture Substances 0.000 description 11
- 238000007254 oxidation reaction Methods 0.000 description 8
- 230000003647 oxidation Effects 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- -1 silver ions Chemical class 0.000 description 6
- 229910052751 metal Inorganic materials 0.000 description 5
- 239000002184 metal Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 4
- 239000003153 chemical reaction reagent Substances 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 230000002829 reductive effect Effects 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 3
- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 description 3
- 229910000366 copper(II) sulfate Inorganic materials 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000009854 hydrometallurgy Methods 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 229910021645 metal ion Inorganic materials 0.000 description 3
- AKHNMLFCWUSKQB-UHFFFAOYSA-L sodium thiosulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=S AKHNMLFCWUSKQB-UHFFFAOYSA-L 0.000 description 3
- 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 2
- 229910019142 PO4 Inorganic materials 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000010452 phosphate Substances 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- ZSILVJLXKHGNPL-UHFFFAOYSA-L S(=S)(=O)([O-])[O-].[Ag+2] Chemical compound S(=S)(=O)([O-])[O-].[Ag+2] ZSILVJLXKHGNPL-UHFFFAOYSA-L 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 239000010405 anode material Substances 0.000 description 1
- 238000001479 atomic absorption spectroscopy Methods 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000004020 conductor Substances 0.000 description 1
- 239000008367 deionised water Substances 0.000 description 1
- 229910021641 deionized water Inorganic materials 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 239000012633 leachable Substances 0.000 description 1
- 150000001455 metallic ions Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000006479 redox reaction Methods 0.000 description 1
- 229910001739 silver mineral Inorganic materials 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 230000007928 solubilization Effects 0.000 description 1
- 238000005063 solubilization Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
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
- C25C1/22—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
- 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
- C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Definitions
- the present invention is related to the mining industry and treatment of mineral and materials that contain gold and silver. Specifically, it is related to a process to recover gold and silver, from copper thiosulfate solutions with a autogenerated electrolysis process, in which the metallic values are recovered from the rich solution in the cathodic compartment. The barren solution is then used as the anolyte, re-establishing the copper concentration needed to be recycled back to the leaching stage.
- gold and silver are obtained from their minerals, concentrates and other materials, using different processes. These processes are in function of the nature of the gold and silver containing material, as well as their grade. Accordingly, if it is a high grade material, smelting is employed. On the other hand, if the material contains only small amounts of gold and silver, a hydrometallurgical treatment is usually selected (leaching).
- Direct electrodeposition used as a separation method, is a viable option, including from solutions with low concentrations of gold and silver, even when the copper ion concentration is more than 50 times greater than that of silver and over 100 times that of gold [Alonso-Gómez, A. R., Lapidus, G. T. and González, I., “Proceso de Lixivia Terms y Recuperaconstruconstru Plata y Oro con Soluations de Tiosulfato Amoniacales de Cobre, solicitud PCT/MX2009/000022, fecha 14 Mar. 2008 (WO20097113842, publicada 17 Sep. 2009)].
- a rotating cylinder electrode was employed in a reactor with separate anodic and cathodic compartments in order prevent the oxidation of the thiosulfate and the re-oxidation of the deposited gold and silver.
- deposits were obtained with less than 2% impurities [Alonso, A. R., Lapidus, G. T. and González, I. (2008), “Selective silver electroseparation from ammoniacal thiosulfate leaching solutions using a Rotating Cylinder Electrode reactor (RCE)”, Hydrometallurgy, 92 (3-4), 115-123].
- the separated anodic and cathodic compartments allow, on one hand, the election of the substrate upon which the metal is deposited (similar to a conventional electrolysis), eliminated the contamination of the deposit.
- the anode is in contact with a solution which is different from the one that contains the metallic ions to be deposited, it is also possible to tailor the anolyte composition according to the requirement of the process and in this manner modulate the reductive power of the system.
- One objective of the present invention is to provide a selective separation process for gold and silver from thiosulfate solutions, at an increased velocity compared with copper cementation, without the use of electrical current.
- Another objective is to accomplish the aforementioned task using the barren solution as the anolyte, conserving in this manner the level of soluble copper, in order to maintain the composition of the thiosulfate solution so that it can be recycled back to the leaching stage.
- the present invention is designed to solve the problem of gold and silver separation from copper thiosulfate leaching solutions, providing an improvement over the traditional separation methods (cementation and external current-driven electrolysis).
- This improvement is characterized by the use of a novel autogenerated electrolysis process, employing a commercial copper sheet as the anode and a titanium cathode, in a reactor with anodic and cathodic compartments separated by ion exchange membrane which prevents the contamination of the thiosulfate solution.
- the membrane achieves the purpose of separating the anodic and cathodic sections, to prevent the solutions used in each confinesto from mixing. This is important to avoid cementation of gold and silver on the copper surface, which slows the process and contaminates the product.
- the rich (pregnant) solution located in the cathodic compartment
- the copper concentration in this solution is kept low and for this reason the membrane plays a double role.
- FIG. 1 is a schematic diagram of the process for electrodepositing gold and silver in an electrochemical autogeneration cell.
- FIG. 2 shows a schematic diagram of the electrochemical autogeneration cell
- FIG. 3 corresponds to a graph indicating the change in the silver concentration during the electrolysis performed in Example 1.
- FIG. 4 is a diagram of the recirculation process of lots A and B of the leaching solution, used in Example 2.
- FIG. 5 shows a graphic representation of the silver concentration change during the first leach LA 1 , performed on lot A (solid lines and markers), as well as during the first autogenerated electrolysis Ca 1 (dotted line, hollow markers).
- FIG. 6 is a series of graphs that compare the quantity of silver remaining in solution throughout the electrolyses Ca 1 , Ca 3 and Ca 5 performed on lot A (markers ⁇ , ⁇ and ⁇ , respectively).
- FIG. 7 shows the lead concentration during the first leach LA 1 performed on lot A.
- FIG. 2 The operation of the electrochemical autogeneration reactor is represented in FIG. 2 :
- Composition of the solution used in the cathodic compartment of the autogeneration electrolytic reactor Component Composition (mol/L) Ag(I) 1 ⁇ 10 ⁇ 3 Na 2 S 2 O 3 0.2 CuSO 4 0.05 EDTA 4 ⁇ 0.025 (NH 4 ) 2 (HPO 4 ) 0.1 NH 3 0.6
- the solutions were prepared with analytical grade reagents and deionized water (1 ⁇ 10 10 M ⁇ cm ⁇ 1 ). Once the solutions were placed in their respective compartments, the electrodes were connected in short circuit. Stirring in both compartments was maintained during the electrodeposition process. Samples of the solution were taken every 20 minutes for four hours, after which time the test was detained. The samples were analyzed for silver and copper with atomic absorption spectrometry.
- FIG. 3 a graphic representation is shown of results of the electrodeposition process, performed in the reactor of FIG. 2 .
- the decrease in silver concentration is constant from the beginning of the electrolysis, attaining 50% of its initial value after only 60 minutes. Subsequently, the descent is slower, typical of first order reaction kinetics in a batch reactor, reaching 4% after 4 hours.
- the recirculation scheme used in the present invention employs two lots of the thiosulfate leaching solution, which are alternated in each one of the reactor compartments ( FIG. 2 ), as was mentioned in the Detailed Description section.
- the same reactor was used as in Example 1, with a copper sheet as the anode and a titanium sheet as the cathode, both with an exposed geometric area of 60 cm 2 .
- FIG. 4 a block diagram is shown ( FIG. 4 ), in which the passage through the process of lots A and B of the leaching solution are shown, without the solid streams.
- stream Al enters the first leach (LA 1 ), and after separating out and discarding the solid residue, stream A 2 (pregnant solution) enters the cathodic compartment (Ca 1 ) of the electrolytic reactor, where the silver electrodeposition takes place; only in this stage of the process is synthetic solution (Stream S 1 ) used in the anodic compartment (An 1 ).
- Stream A 3 stripped of its values, is placed in the anodic compartment of the reactor (An 2 ), where the first electrodeposit from the pregnant solution lot B (Ca 2 ) occurs.
- Stream A 4 is sent back to a new leaching stage (LA 2 ), where it is contacted with fresh mineral.
- the pregnant solution (A 5 ) is sent to the electrochemical reactor for silver recovery in the cathodic compartment (Ca 3 ).
- the anodic compartment is occupied by the solution of lot B originating from Ca 2 .
- stream A 7 is again introduced into the leaching stage with fresh mineral, obtaining a pregnant solution in stream A 8 .
- Table 3 shows the initial composition used in the leaching solutions for both lots; the volume of each one was 250 mL.
- FIG. 5 the silver concentration during the first leach is shown (solid lines and markers), as well as the electrodeposition process in the cathodic compartment Ca 1 (dashed line and hollow markers). It is important to consider that the silver content in this mineral is very high, explaining the reason for extractions above 200 ppm, a value close to the solubility limit for this metal ion in thiosulfate solutions. These high values of silver in solution are the reason that the silver concentration only decreases to 50% of its original value in the autogenerated electrolysis (Ca 1 ). Additionally, because of the high dissolved lead concentration (200 ppm), there is competition with the silver in the electrodeposition process. This could represent an enormous loss in the traditional cyanidation process; however, in this case, the thiosulfate solution is recycled back to the leaching stage, the gold and silver remaining in solution are separated in subsequent cycles.
- FIG. 6 a comparison of the change in silver concentration during the autogenerated electrolyses for lot A is shown in FIG. 6 .
- the electrolyses Ca 3 and Ca 5 present similar behavior to that registered for Ca 1 (first electrolysis of lot A).
- the quantity of silver that remains after the electrolyses Ca 2 and Ca 3 is similar, indicating that there is no accumulation of silver ions in the recycling process; in other words, the silver extracted in the leach is separated in the autogenerated electrolysis stage.
- the behavior of lot B during the electrolyses (data not shown here) is practically the same exhibited by lot A.
- the lead concentration is shown during the first leach of lot A, where it can be appreciated that the concentration of Pb(II) is similar to that of silver. Also, in the corresponding electrolysis, the lead concentration decreases approximately 35% during the first 20 minutes. This competition (inexistent in Example 1 with the synthetic solution) could be the cause that the silver recovery did not exceed 60%. Additionally, it must be considered that treating such high grade silver minerals would originate solubility problems during leaching, as well as electrode saturation in the electrodeposition stage. In these cases, it is possible to increase the thiosulfate concentration to increase the solubility of the Ag(S 2 O 3 ) 2 3 ⁇ complex, even though a larger electroactive area for the cathode would be required.
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- 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)
- Water Treatment By Electricity Or Magnetism (AREA)
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| MXMX/A/2010/013510 | 2010-12-09 | ||
| MX2010013510A MX2010013510A (es) | 2010-12-09 | 2010-12-09 | Electrorecuperacion de oro y plata a partir de soluciones de tiosulfato. |
| PCT/MX2011/000150 WO2012078019A2 (es) | 2010-12-09 | 2011-12-09 | Electrorecuperación de oro y plata a partir de soluciones de tiosulfato |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US20140311896A1 true US20140311896A1 (en) | 2014-10-23 |
Family
ID=45558361
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US13/992,713 Abandoned US20140311896A1 (en) | 2010-12-09 | 2011-12-09 | Electrorecovery of gold and silver from thiosulphate solutions |
Country Status (12)
| Country | Link |
|---|---|
| US (1) | US20140311896A1 (pt) |
| EP (1) | EP2650403A2 (pt) |
| JP (1) | JP2014501850A (pt) |
| CN (1) | CN103842557A (pt) |
| AU (1) | AU2011339119A1 (pt) |
| BR (1) | BR112013014261A2 (pt) |
| CA (1) | CA2821042A1 (pt) |
| CO (1) | CO6801690A2 (pt) |
| MX (1) | MX2010013510A (pt) |
| PE (1) | PE20140643A1 (pt) |
| RU (1) | RU2013131237A (pt) |
| WO (1) | WO2012078019A2 (pt) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9777346B2 (en) | 2015-09-03 | 2017-10-03 | Battelle Energy Alliance, Llc | Methods for recovering metals from electronic waste, and related systems |
| US10807085B2 (en) * | 2017-11-17 | 2020-10-20 | University Of Massachusetts | Silver recovery as Ag0nanoparticles from ion-exchange regenerant solution |
| CN114774686A (zh) * | 2022-05-06 | 2022-07-22 | 河南理工大学 | 一种在硫代硫酸盐浸金体系中置换回收金的装置及方法 |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101349305B1 (ko) * | 2013-05-24 | 2014-01-13 | 한국지질자원연구원 | 유로형 셀을 이용한 희유 금속의 전해 채취 장치, 및 그 방법 |
| PE20210787A1 (es) | 2014-05-12 | 2021-04-22 | Summit Mining Int Inc | Proceso de lixiviado de salmuera para la recuperacion de metales valiosos de materiales de oxido |
| CN104499003A (zh) * | 2014-11-13 | 2015-04-08 | 黄石市英柯有色金属有限公司 | 从水溶液中提取金属的方法 |
| US11408053B2 (en) | 2015-04-21 | 2022-08-09 | Excir Works Corp. | Methods for selective leaching and extraction of precious metals in organic solvents |
| CN104911351A (zh) * | 2015-06-07 | 2015-09-16 | 长春黄金研究院 | 一种生物浸出金及浸出液中金自发电回收方法 |
| CN108660314B (zh) * | 2018-05-02 | 2019-11-26 | 江南大学 | 一步法回收金属的方法 |
| CN108642091B (zh) * | 2018-05-02 | 2021-03-30 | 江南大学 | 一种同步回收金属与单质硫的方法 |
| CN108624912B (zh) * | 2018-05-25 | 2020-04-24 | 王勇 | 一种贵金属元素电化回收工艺及系统 |
| CN113621995B (zh) * | 2021-07-16 | 2023-12-26 | 武汉理工大学 | 一种基于电化学联合催化技术回收硫代硫酸盐浸出液中贵金属的方法 |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3994789A (en) * | 1974-10-02 | 1976-11-30 | Progressive Scientific Associates, Inc. | Galvanic cementation process |
| US5100528A (en) * | 1989-03-28 | 1992-03-31 | Noranda, Inc. | Continuous silver refining cell |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85103707B (zh) * | 1985-05-13 | 1987-05-06 | 华东化工学院 | 从金矿中综合提取金、银 、铜的工艺过程 |
| US5607619A (en) * | 1988-03-07 | 1997-03-04 | Great Lakes Chemical Corporation | Inorganic perbromide compositions and methods of use thereof |
-
2010
- 2010-12-09 MX MX2010013510A patent/MX2010013510A/es active IP Right Grant
-
2011
- 2011-12-09 PE PE2013001393A patent/PE20140643A1/es not_active Application Discontinuation
- 2011-12-09 CN CN201180067296.3A patent/CN103842557A/zh active Pending
- 2011-12-09 BR BR112013014261A patent/BR112013014261A2/pt not_active IP Right Cessation
- 2011-12-09 AU AU2011339119A patent/AU2011339119A1/en not_active Abandoned
- 2011-12-09 EP EP20110813914 patent/EP2650403A2/en not_active Withdrawn
- 2011-12-09 CA CA2821042A patent/CA2821042A1/en not_active Abandoned
- 2011-12-09 JP JP2013543122A patent/JP2014501850A/ja active Pending
- 2011-12-09 US US13/992,713 patent/US20140311896A1/en not_active Abandoned
- 2011-12-09 RU RU2013131237/02A patent/RU2013131237A/ru not_active Application Discontinuation
- 2011-12-09 WO PCT/MX2011/000150 patent/WO2012078019A2/es active Application Filing
-
2013
- 2013-07-08 CO CO13161590A patent/CO6801690A2/es not_active Application Discontinuation
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3994789A (en) * | 1974-10-02 | 1976-11-30 | Progressive Scientific Associates, Inc. | Galvanic cementation process |
| US5100528A (en) * | 1989-03-28 | 1992-03-31 | Noranda, Inc. | Continuous silver refining cell |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9777346B2 (en) | 2015-09-03 | 2017-10-03 | Battelle Energy Alliance, Llc | Methods for recovering metals from electronic waste, and related systems |
| US10378081B2 (en) | 2015-09-03 | 2019-08-13 | Battelle Energy Alliance, Llc | Methods for recovering metals from electronic waste, and related systems |
| US11035023B2 (en) | 2015-09-03 | 2021-06-15 | Battelle Energy Alliance, Llc | Reactor systems for recovering metals, and related methods |
| US10807085B2 (en) * | 2017-11-17 | 2020-10-20 | University Of Massachusetts | Silver recovery as Ag0nanoparticles from ion-exchange regenerant solution |
| CN114774686A (zh) * | 2022-05-06 | 2022-07-22 | 河南理工大学 | 一种在硫代硫酸盐浸金体系中置换回收金的装置及方法 |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2012078019A3 (es) | 2012-12-06 |
| CN103842557A (zh) | 2014-06-04 |
| MX2010013510A (es) | 2012-06-08 |
| RU2013131237A (ru) | 2015-01-20 |
| WO2012078019A2 (es) | 2012-06-14 |
| WO2012078019A4 (es) | 2013-01-24 |
| CA2821042A1 (en) | 2012-06-14 |
| BR112013014261A2 (pt) | 2017-08-01 |
| JP2014501850A (ja) | 2014-01-23 |
| CO6801690A2 (es) | 2013-11-29 |
| AU2011339119A1 (en) | 2013-08-01 |
| PE20140643A1 (es) | 2014-06-02 |
| EP2650403A2 (en) | 2013-10-16 |
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