EP0089184A1 - Process for the recovery of silver from metallurgical intermediates - Google Patents

Process for the recovery of silver from metallurgical intermediates Download PDF

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Publication number
EP0089184A1
EP0089184A1 EP83301318A EP83301318A EP0089184A1 EP 0089184 A1 EP0089184 A1 EP 0089184A1 EP 83301318 A EP83301318 A EP 83301318A EP 83301318 A EP83301318 A EP 83301318A EP 0089184 A1 EP0089184 A1 EP 0089184A1
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Prior art keywords
silver
solution
thiosulphate
leach
residue
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EP83301318A
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German (de)
French (fr)
Inventor
Eberhard Krause
Victor Alexander Ettel
Bernardus Jacobus Brandt
Gerald Vernon Glaum
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Vale Canada Ltd
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Vale Canada Ltd
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    • 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

Definitions

  • This invention relates to the recovery of silver from metallurgical intermediate materials which also contain one or more other precious metals.
  • base metal ores such as those of copper, nickel, zinc, and lead also contain metals of the platinum group together with silver, gold, selenium, tellurium and other constituents. Such ores form important sources of the valuable metals which are known colloquially as "precious metals", that is to say the six platinum group metals, gold and silver.
  • metals occur in the various metal ores in small amounts and become concentrated during the working up of the base metals in the form of various metallurgical intermediates, including anode sludges, leach residues and cements.
  • the compositionsof these precious metal-containing materials thus vary widely depending upon the nature of the ore. Despite the differences in composition these materials tend to lend themselves to a more or less common scheme of treatment and tend to contain largely the same ingredients, although the proportions of valuable metals therein can vary.
  • metals which may be present in the precious metals intermediate products include all six members of the platinum group, gold, silver, selenium, tellurium, lead, arsenic, antimony, tin, bismuth, copper, nickel, zinc, iron and sulphur.
  • One known method can involve decopperizing of the precious metal intermediate by leaching with sulphuric acid and then smelting in a Dor6 furnace in which silver may be recovered in the form of DorG metal. Such a procedure is expensive and can produce harmful emissions of selenium, arsenic, lead and other heavy metals.
  • the present method provides a hydrometallurgical method for working up precious-metal-containing intermediate materials to give selective and efficient separation of silver therefrom.
  • silver present in a metallurgical intermediate material that also contains one or more other precious metals is concentrated and recovered by slurrying the material with water, chlorinating the aqueous slurry to dissolve platinum group metals and gold present and to produce a residue enriched in silver, dissolving silver from the residue with an aqueous thiosulphate solution and recovering silver from the resulting solution.
  • the silver-containing precious metal intermediates to be treated should be slurried with water in the proportion of from 5 to 50% by weight solids.
  • the resulting slurry is then chlorinated for a time sufficient to convert the silver content to silver chloride and to chlorinate most of the remaining metal values as chlorides.
  • hydrochloric acid can be formed by reactions between chlorine and elements such as sulphur, selenium, tellurium, and arsenic or compounds thereof.
  • a convenient temperature range for chlorination is from 60 to 80°C. Since chlorination is usually exothermic, cooling of the solution may sometimes be required, and the rate of addition of chlorine should be controlled to avoid possible overheating and/or excessive chlorine consumption.
  • the silver-containing residue can then be leached, preferably at ambient temperature, with an aqueous thiosulphate solution, e.g. sodium thiosulphate, to dissolve silver selectively with regard to impurities such as silica and ferrites which may also be present in the silver-containing residue.
  • an aqueous thiosulphate solution e.g. sodium thiosulphate
  • the thiosulphate leach may be conducted at a temperature of from 10 to 80°C.
  • Thiosulphate should be used in approximately the proportions of two to four mols of thiosulphate for each mol of silver to be leached.
  • The'pH of the thiosulphate solution should be at least 2,and when lead is present in the chlorine leach residue to an extent requiring selective removal of the silver, the pH of the thiosulphate leach solution should be at least 7 and more preferably ⁇ pH 9 or pH 10.
  • the thiosulphate leach is highly selective for silver as compared with lead in the precipitate being dissolved.
  • a further advantage of maintaining the thiosulphate solution basic is that the stability of the solution is thereby increased. Small amounts of sulphite, e.g. sodium sulphite, added to the thiosulphate leach solution will also improve its stability.
  • the thiosulphate leach solution containing silver from the residue may be treated in a variety of ways to recover the silver.
  • cementation with metals such as iron, zinc or magnesium at ambient temperature produces cements analyzing about 90% silver.
  • Organic reducing agents e.g. fructose, dextrose and lactose, can be used to produce silver precipitates of high purity, e.g. containing at least 90% of silver.
  • Electrolytic recovery means may also be used.
  • the composition of the silver-containing precious metal intermediates to be treated in accordance with the invention can vary widely depending upon the ore from which they are obtained, and it may be convenient to subject them to preliminary treatment.
  • the sludge may be given a decopperizing leach in sulphuric acid prior to treatment in accordance to the invention.
  • a lead removal step may be employed prior to treatment of the intermediate in accordance with the invention.
  • the chlorine leach residue was then leached with thiosulphate as follows: 33.8 litres of water was added to 15.5 kg of the above chlorine leach residue, which already contained 39% moisture. NaOH was added to the agitated slurry to bring the pH to 10.0 at 22°C. Then 3.75 kg of Na 2 S 2 0 3 was added (3.9 kg Na 2 S 2 0 3 /kg Ag) and the slurry was agitated for 30 minutes at a pH of 10 (22°C). The residue was filtered off and washed with one cake displacement of water.
  • the leach residue contained a large quantity of filter-aid, which tends to trap large amounts of leach liquor
  • the wet residue was subjected to a repulp leach using 11 litres of water and 0.4 kg of Na 2 S 2 0 3 .
  • Leaching was again conducted for 30 minutes at 22°C (pH 10).
  • the leach residue was separated from the solution by filtration.
  • the leach , residue analyzed 0.11% Ag and 5.2% Pb. 99.1% of the silver was extracted with only 0.8% of the lead.
  • This example shows the effect of varying the chlorine leaching conditions.
  • This example shows the effect of acidity on the extraction of silver by a thiosulphate solution.
  • the leach conditions were similar to Example 1 and are listed in Table 2, together with the results of duplicate tests.
  • the extraction of silver was lowest ( ⁇ 97%) at a pH of 2.0, and was generally 99% or higher between pH 4 and 12.
  • the dissolution of lead was strongly influenced by the pH. At pH 6 and below, more than 75% of the Pb was dissolved, whereas at pH 8 less than 20% Pb was extracted and at a pH of 10 the dissolution of Pb was only ⁇ 1%.
  • compositions of five other precious metal-containing materials susceptible to treatment in accordance with the invention are shown in Table 3. Each of these materials was chlorine leached under the conditions and for the times shown in Table 4. It will be seen from Table 4 that excellent extractions of platinum-group metals and gold were achieved with all the materials treated although the compositions thereof varied widely. On the other hand, extractions of silver were low.
  • the compositions, in weight per cent, of the chlorine leach residues are shown in Table 5. All of the chlorine leach residues were susceptible to thiosulphate leaching, in accordance with the invention, to dissolve silver.

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  • 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)

Abstract

An aqueous slurry of the silver-containing intermediate is chlorinated to dissolve platinum group metals and gold leaving the silver in the residue, from which it is dissolved with an aqueous thiosulphate solution. When the intermediate contains lead, the thiosulphate leach solution should have a pH of at least 7. Silver is recovered from the final solution by cementation or reduction.

Description

  • . This invention relates to the recovery of silver from metallurgical intermediate materials which also contain one or more other precious metals.
  • Many base metal ores, such as those of copper, nickel, zinc, and lead also contain metals of the platinum group together with silver, gold, selenium, tellurium and other constituents. Such ores form important sources of the valuable metals which are known colloquially as "precious metals", that is to say the six platinum group metals, gold and silver.
  • These metals occur in the various metal ores in small amounts and become concentrated during the working up of the base metals in the form of various metallurgical intermediates, including anode sludges, leach residues and cements. The compositionsof these precious metal-containing materials thus vary widely depending upon the nature of the ore. Despite the differences in composition these materials tend to lend themselves to a more or less common scheme of treatment and tend to contain largely the same ingredients, although the proportions of valuable metals therein can vary. -Thus, metals which may be present in the precious metals intermediate products include all six members of the platinum group, gold, silver, selenium, tellurium, lead, arsenic, antimony, tin, bismuth, copper, nickel, zinc, iron and sulphur. Once the materials are concentrated,e.g. in the form of anode sludges or leach residues, it then becomes important to recover the metal values as completely as possible and to produce metal concentrates of respectable purity. One known method, for example, can involve decopperizing of the precious metal intermediate by leaching with sulphuric acid and then smelting in a Dor6 furnace in which silver may be recovered in the form of DorG metal. Such a procedure is expensive and can produce harmful emissions of selenium, arsenic, lead and other heavy metals.
  • It is known also to recover precious metal from intermediate products by dissolution in hydrochloric acid with chlorination followed by ammonia extraction of silver from the resulting residues and recovery of platinum group metals, selenium, and tellurium from the leach liquor. It is also known from the photographic art that thiosulphate solutions can be employed to dissolve silver from light-unaffected portions of film which is employed for photographic purposes. Ammonium thiosulphate leaching of gold and silver from ammoniacal leach residues in the presence of cupric ion and free ammonia is also known.
  • Publications relevant to this subject matter include Tsvetnye Metallv, 1963, Vol.36, No.11, pages 85-86; the U.S. Patents Nos. 3,658,510; 4,070,182; 4,269,622 and 4,229,270.
  • The present method provides a hydrometallurgical method for working up precious-metal-containing intermediate materials to give selective and efficient separation of silver therefrom.
  • According to the invention, silver present in a metallurgical intermediate material that also contains one or more other precious metals is concentrated and recovered by slurrying the material with water, chlorinating the aqueous slurry to dissolve platinum group metals and gold present and to produce a residue enriched in silver, dissolving silver from the residue with an aqueous thiosulphate solution and recovering silver from the resulting solution.
  • In carrying out the process, the silver-containing precious metal intermediates to be treated should be slurried with water in the proportion of from 5 to 50% by weight solids. The resulting slurry is then chlorinated for a time sufficient to convert the silver content to silver chloride and to chlorinate most of the remaining metal values as chlorides. In the course of the chlorination a substantial quantity of hydrochloric acid can be formed by reactions between chlorine and elements such as sulphur, selenium, tellurium, and arsenic or compounds thereof. A convenient temperature range for chlorination is from 60 to 80°C. Since chlorination is usually exothermic, cooling of the solution may sometimes be required, and the rate of addition of chlorine should be controlled to avoid possible overheating and/or excessive chlorine consumption.
  • After completion of the chlorine leach, the silver-containing residue is separated from the supernatant solution, which now contains the other precious metals.
  • The silver-containing residue can then be leached, preferably at ambient temperature, with an aqueous thiosulphate solution, e.g. sodium thiosulphate, to dissolve silver selectively with regard to impurities such as silica and ferrites which may also be present in the silver-containing residue. The thiosulphate leach may be conducted at a temperature of from 10 to 80°C.
  • Thiosulphate should be used in approximately the proportions of two to four mols of thiosulphate for each mol of silver to be leached.
  • The'pH of the thiosulphate solution should be at least 2,and when lead is present in the chlorine leach residue to an extent requiring selective removal of the silver, the pH of the thiosulphate leach solution should be at least 7 and more preferably ≥ pH 9 or pH 10. When the thiosulphate solution is sufficiently basic, the thiosulphate leach is highly selective for silver as compared with lead in the precipitate being dissolved. A further advantage of maintaining the thiosulphate solution basic is that the stability of the solution is thereby increased. Small amounts of sulphite, e.g. sodium sulphite, added to the thiosulphate leach solution will also improve its stability.
  • The thiosulphate leach solution containing silver from the residue may be treated in a variety of ways to recover the silver. For example, cementation with metals such as iron, zinc or magnesium at ambient temperature produces cements analyzing about 90% silver. Organic reducing agents, e.g. fructose, dextrose and lactose, can be used to produce silver precipitates of high purity, e.g. containing at least 90% of silver. Electrolytic recovery means may also be used.
  • As noted hereinbefore, the composition of the silver-containing precious metal intermediates to be treated in accordance with the invention can vary widely depending upon the ore from which they are obtained, and it may be convenient to subject them to preliminary treatment. For example, in working up copper refinery sludges to recover silver the sludge may be given a decopperizing leach in sulphuric acid prior to treatment in accordance to the invention. Similarly, a lead removal step may be employed prior to treatment of the intermediate in accordance with the invention.
  • Some examples will now be given.
    • Example 1
  • 66.2 kg of a precious metals-containing feed, analyzing (in per cent by weight) Pt 1.5, Pd 1.6, Au 0.40, Rh 0.16, Ru 0.09, Ag 7.6, Pb 7.1, Se 5.6, Te 0.67, Cu 0.34 was slurried in water at a solids density of n450 g solids per litre of slurry and heated to 60°C. Gaseous chlorine was sparged into the agitated slurry for a total of 4 h at a flowrate of 100 litres/min. After filtration of the leached slurry about 46.5 kg of leach residue was obtained, which was found to an analyze Pt 0.035, Pd 0.016, Au 0.005, Ag 10.1, Pb 3.2%. The following metal extractions were obtained (%): Pt 98, Pd 99.3, Au 99.1, Ag <1.
  • The chlorine leach residue was then leached with thiosulphate as follows: 33.8 litres of water was added to 15.5 kg of the above chlorine leach residue, which already contained 39% moisture. NaOH was added to the agitated slurry to bring the pH to 10.0 at 22°C. Then 3.75 kg of Na2S203 was added (3.9 kg Na2S203/kg Ag) and the slurry was agitated for 30 minutes at a pH of 10 (22°C). The residue was filtered off and washed with one cake displacement of water. Since the leach residue contained a large quantity of filter-aid, which tends to trap large amounts of leach liquor, the wet residue was subjected to a repulp leach using 11 litres of water and 0.4 kg of Na2S203. Leaching was again conducted for 30 minutes at 22°C (pH 10). Finally, the leach residue was separated from the solution by filtration. The leach , residue analyzed 0.11% Ag and 5.2% Pb. 99.1% of the silver was extracted with only 0.8% of the lead.
  • The thiosulphate leach liquor and the repulp leach liquorwere combined, resulting in a solution analyzing (g/1) Ag 18.0 and Pb 0.07. Sulphuric acid was added to the solution to reach a pH of 4.0 at 22°C. Thcniron powder was added to cement the contained silver values. The pH was held at 4 by simultaneous addition of sulphuric acid. When a redox potential of -400 mV(SCE) was reached, the slurry was filtered. The silver cement analyzed (%) Ag 87.1, Fe 9.3, Pb 0.38, S 1.4. More than 99.9% of the silver had been cemented and the barren solution analyzed 10 mg/l Ag.
    • Example 2
  • This example shows the effect of varying the chlorine leaching conditions.
  • 170 g of a moist (39.4% H20) precious metals containing feed analyzing (%) Pt 1.73, Pd 1.65, Au 0.33, Ag 2.00, Pb 3.43 and Si02 52.0 was slurried with water alone and with various amounts of hydrochloric acid, as shown in Table 1. The resulting slurries (30-35% solids) were agitated and heated to 80°C. Gaseous chlorine was bubbled into the slurry at a flowrate of ~1 g/1 slurry/min. for a total of 4 h. The slurry was then filtered and the leach residue and the leach liquor were analyzed.
  • As shown in Table 1, it was found that the extraction of the precious metals Pt, Pd and Au was essentially unaffected by the initial acidity. However, much less silver was extracted (only 0.2%) in the test where the feed was slurried with water. Thus, a better separation of silver from Pt, Pd and Au was achieved.
    • Example 3
  • This example shows the effect of acidity on the extraction of silver by a thiosulphate solution.
  • A chlorine leach residue analyzing, in weight per cent, Ag 17.3 and Pb 9.9, was subjected to thiosulphate leach tests at various pH values between 2 and 12.
    Figure imgb0001
    The leach conditions were similar to Example 1 and are listed in Table 2, together with the results of duplicate tests. The extraction of silver was lowest (~97%) at a pH of 2.0, and was generally 99% or higher between pH 4 and 12. The dissolution of lead was strongly influenced by the pH. At pH 6 and below, more than 75% of the Pb was dissolved, whereas at pH 8 less than 20% Pb was extracted and at a pH of 10 the dissolution of Pb was only ~1%.
    Figure imgb0002
  • The next four Examples (Nos. 4-7) illustrate the recovery of silver from thiosulphate leach solutions obtained in the process of the invention.
    • Example 4
  • A thiosulphate leach liquor (1.0 litres) analyzing (g/1) Ag 18.4 and S203= 68 at pH 10 was acidified to pH 4, and 3.8 g of Mg granules (0.177-0.21mm) was added over 2 h with simultaneous addition of 151.5 ml of 50 g/l H2SO4 solution to maintain pH 4. During this period the temperature rose from 22 to 31°C and the redox potential of the solution decreased from +70 mV to -250 mV (Pt vs SCE). After filtration and drying, the solids (20.14.g) analyzed (%): Ag 90.9, Mg 1.6 and S 3.15. The filtrate (1.085 litres) contained 0.042 g/1 Ag. Thus, 99.7% of the silver was recovered in the solids.
    • Example 5
  • A thiosulphate leach liquor (1.0 litres) analyzing (g/1) Ag 18.5, Pb 0.11 and S203 = 69 at pH 10 was heated at 80°C and 14.3 g of D-fructose was added. The solution was maintained at pH 10 by addition of 72.9 ml of a 150 g/1 NaOH solution. After 15 minutes the redox potential of the solution had decreased from 0 mV to -660 mV (Pt vs SCE) and the silver mirror, originally plated on the sides of the beaker, disappeared leaving a flocculant precipitate (18.23 g) which analyzed (%): Ag 97.5, Pb 0.55, and S 0.66. The filtrate (1.044 litres) analyzed <5 mg/l Ag. Thus, 99.97% of the silver was recovered in the solids.
    • Example 6
  • A thiosulphate leach liquor (1.0 litres) analyzing (g/1) Ag 17.9, Pb 0.10, and S2O3= 67 at pH 10 was heated to 80°C and 14.3 g of D-glucose was added. The solution was maintained at pH 10 by addition of 265 ml of a 38 g/1 NaOH solution. After 30 minutes the redox potential of the solution had decreased from +30 mV to -660 mV (Pt vs SCE) and the silver mirror, originally plated on the sides of the beaker, disappeared leaving a flocculant precipitate (17.45 g) which analyzed (%): Ag 97.9, Pb 0.52, and S 0.56. The filtrate (1.26 litres) contained 40 mg/l Ag. Thus, 99.7% of the silver was recovered in the solids.
    • Example 7
  • A thiosulphate leach liquor (1.0 litres) containing 17.9 g/1 Ag and 67 g/1 S2O3= was adjusted to pH 13 at 24°C by adding 16 g NaOH. Then 14.3 g of D=fructose was added. After 2 hours the redox potential had decreased from +60 mV to -225 mV (Pt vs SCE) and 8.85 g of precipitate was filtered off. After standing overnight, an additional 8.30 g of precipitate was recovered. The combined precipitates analyzed 99.6% Ag while the solution contained only 70 mg/l Ag. Thus, 99.6% of the silver was recovered in the solids.
    • Example 8
  • The compositions of five other precious metal-containing materials susceptible to treatment in accordance with the invention are shown in Table 3. Each of these materials was chlorine leached under the conditions and for the times shown in Table 4. It will be seen from Table 4 that excellent extractions of platinum-group metals and gold were achieved with all the materials treated although the compositions thereof varied widely. On the other hand, extractions of silver were low. The compositions, in weight per cent, of the chlorine leach residues are shown in Table 5. All of the chlorine leach residues were susceptible to thiosulphate leaching, in accordance with the invention, to dissolve silver.
    Figure imgb0003
    Figure imgb0004
    Figure imgb0005

Claims (7)

1. A hydrometallurgical method for treating a metallurgical intermediate material that contains silver and also one or more other precious metals to concentrate and recover silver therefrom, characterised by the steps of slurrying the material with water, chlorinating the aqueous slurry to dissolve platinum group metals and gold and produce a residue enriched in silver, dissolving silver from the residue with an aqueous thiosulphate solution, and recovering silver from the resulting solution.
2. A process according to claim 1, characterised in that the thiosulphate solution has a pH of at least-2.
3. A process according to claim 2, characterised in that the silver-enriched residue also contains lead and the thiosulphate solution has a pH of at least 7.
4. A process according to claim 3, characterised in that the thiosulphate solution has a pH of at least 9.
5. A process according to any preceding claim, characterised in that the thiosulphate leach is conducted at ambient temperature.
6. A process according to any preceding claim, characterised in that the silver is recovered from the final solution by cementation.
7. A process according to any preceding claim, characterised in that the silver is recovered from the final solution by reduction with an organic reducing agent.
EP83301318A 1982-03-11 1983-03-10 Process for the recovery of silver from metallurgical intermediates Withdrawn EP0089184A1 (en)

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Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0176100A1 (en) * 1984-09-26 1986-04-02 Austria Metall Aktiengesellschaft Hydrometallurgical process for treating electrolytic copper refinery anode slimes
EP0212453A1 (en) * 1985-08-07 1987-03-04 Noranda Inc. Process for the recovery of gold from a precious metal bearing sludge concentrate
US4666514A (en) * 1985-01-25 1987-05-19 Austria Metall Aktiengesellschaft Hydrometallurgical process for recovering silver from copper-electrolysis anode sludge
WO1990010721A1 (en) * 1989-03-07 1990-09-20 Dean Robert Butler Recovery of gold, silver and platinum group metals with various leachants at low pulp densities
RU2351666C1 (en) * 2007-07-11 2009-04-10 Институт химии Дальневосточного отделения Российской академии наук (статус государственного учреждения) (Институт химии ДВО РАН) Method of gold and silver recovery from concentrates
RU2607285C1 (en) * 2015-08-17 2017-01-10 Лидия Алексеевна Воропанова Extraction of silver ions from hydrochloric acid solutions with tributyl phosphate
US10400306B2 (en) 2014-05-12 2019-09-03 Summit Mining International Inc. Brine leaching process for recovering valuable metals from oxide materials
RU2699142C1 (en) * 2019-03-27 2019-09-03 Федеральное государственное бюджетное научное учреждение "Федеральный исследовательский центр "Красноярский научный центр Сибирского отделения Российской академии наук" (ФИЦ КНЦ СО РАН, КНЦ СО РАН) Method of extracting silver from hydrochloric acid solutions
CN119662989A (en) * 2025-02-24 2025-03-21 山西建邦集团铸造有限公司 A method for efficient chemical separation of lead and silver

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US1071791A (en) * 1911-11-23 1913-09-02 Frank W Pugsley Process of treating ores.
GB151952A (en) * 1919-10-03 1921-05-26 Amalgamated Zinc De Bavay S Lt Improvements in or relating to the recovery of lead and silver from sulphide ores and metallurgical products
AT140214B (en) * 1933-11-16 1935-01-10 Johann Eder Process for extracting gold from ores that are difficult to digest.
US3658510A (en) * 1970-04-14 1972-04-25 American Metal Climax Inc Recovery of silver from electrolytic copper refinery slimes
US4269622A (en) * 1979-12-28 1981-05-26 Kerley Jr Bernard J Recovery of precious metals from difficult ores
DE3145006A1 (en) * 1980-11-18 1982-06-16 Sumitomo Metal Mining Co. Ltd., Tokyo Process for extracting gold from anode sludges

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US1071791A (en) * 1911-11-23 1913-09-02 Frank W Pugsley Process of treating ores.
GB151952A (en) * 1919-10-03 1921-05-26 Amalgamated Zinc De Bavay S Lt Improvements in or relating to the recovery of lead and silver from sulphide ores and metallurgical products
AT140214B (en) * 1933-11-16 1935-01-10 Johann Eder Process for extracting gold from ores that are difficult to digest.
US3658510A (en) * 1970-04-14 1972-04-25 American Metal Climax Inc Recovery of silver from electrolytic copper refinery slimes
US4269622A (en) * 1979-12-28 1981-05-26 Kerley Jr Bernard J Recovery of precious metals from difficult ores
DE3145006A1 (en) * 1980-11-18 1982-06-16 Sumitomo Metal Mining Co. Ltd., Tokyo Process for extracting gold from anode sludges

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Title
Chemical Abstracts, vol. 75, no. 14, 4 October 1971, Columbus, Ohio, USA V.V. SAFONOV "Chlorination of copper-nickel anode slimes in a mediumn", page 395, column 2, Abstract 93960z & Tr. Mosk. Khim.-Teknnol. Inst. 1969, pages 161-1 *

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0176100A1 (en) * 1984-09-26 1986-04-02 Austria Metall Aktiengesellschaft Hydrometallurgical process for treating electrolytic copper refinery anode slimes
US4666514A (en) * 1985-01-25 1987-05-19 Austria Metall Aktiengesellschaft Hydrometallurgical process for recovering silver from copper-electrolysis anode sludge
EP0212453A1 (en) * 1985-08-07 1987-03-04 Noranda Inc. Process for the recovery of gold from a precious metal bearing sludge concentrate
WO1990010721A1 (en) * 1989-03-07 1990-09-20 Dean Robert Butler Recovery of gold, silver and platinum group metals with various leachants at low pulp densities
GB2248631A (en) * 1989-03-07 1992-04-15 Dean Robert Butler Recovery of gold, silver and platinum group metals with various leachants at low pulp densities
GB2248631B (en) * 1989-03-07 1993-06-09 Dean Robert Butler Recovery of gold, silver and platinum group metals with various leachants at low pulp densities
RU2351666C1 (en) * 2007-07-11 2009-04-10 Институт химии Дальневосточного отделения Российской академии наук (статус государственного учреждения) (Институт химии ДВО РАН) Method of gold and silver recovery from concentrates
US10400306B2 (en) 2014-05-12 2019-09-03 Summit Mining International Inc. Brine leaching process for recovering valuable metals from oxide materials
RU2607285C1 (en) * 2015-08-17 2017-01-10 Лидия Алексеевна Воропанова Extraction of silver ions from hydrochloric acid solutions with tributyl phosphate
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CN119662989A (en) * 2025-02-24 2025-03-21 山西建邦集团铸造有限公司 A method for efficient chemical separation of lead and silver

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