WO2001083835A2 - Procede de recuperation d'or - Google Patents

Procede de recuperation d'or Download PDF

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Publication number
WO2001083835A2
WO2001083835A2 PCT/ZA2001/000050 ZA0100050W WO0183835A2 WO 2001083835 A2 WO2001083835 A2 WO 2001083835A2 ZA 0100050 W ZA0100050 W ZA 0100050W WO 0183835 A2 WO0183835 A2 WO 0183835A2
Authority
WO
WIPO (PCT)
Prior art keywords
gold
process according
chlorine
concentrate
tank
Prior art date
Application number
PCT/ZA2001/000050
Other languages
English (en)
Other versions
WO2001083835A3 (fr
Inventor
Roger Leslie Paul
Joao Manuel De Sousa Rodrigues
Susanna Petronella O'connell
Gregory Owen Lewis
Nicole De Jager
Gary Pattrick
Original Assignee
Mintek
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Mintek filed Critical Mintek
Priority to AU2001257646A priority Critical patent/AU2001257646A1/en
Publication of WO2001083835A2 publication Critical patent/WO2001083835A2/fr
Publication of WO2001083835A3 publication Critical patent/WO2001083835A3/fr

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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
    • C22B11/042—Recovery of noble metals from waste materials
    • C22B11/044—Recovery of noble metals from waste materials from pyrometallurgical residues, e.g. from ashes, dross, flue dust, mud, skim, slag, sludge
    • 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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • C22B3/10—Hydrochloric acid, other halogenated acids or salts thereof
    • 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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
    • 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

  • This invention relates to a hydrometallurgical process for the recovery of gold from a gold bearing material which may be in the form of a gold bearing gravity concentrate which has a relatively low gold content, or in the form of a gold feed other than a gravity concentrate which has a relatively high gold content, typically in excess of 10%.
  • Direct smelting is a pyrometallurgical process, which requires a high-grade concentrate containing from 15% to 50% Au. The process produces a low-grade bullion of from 50% to 90% Au and a slag which contains small amounts of Au. This slag usually requires further treatment to recover the Au.
  • cyanidation is a hydrometallurgical process, which by implication requires significantly higher levels of cyanide than that normally used. The process does not yield good recoveries if the gold concentrate is of a refractory nature, eg. a gold sulphide complex.
  • Sulphide roasting involves a pyrometallurgical step to oxidise the sulphides to gaseous sulphur dioxide.
  • the residue referred to as calcine, contains the gold, which is in a form that can be leached in a normal cyanide leach.
  • the roasting process is more suited to higher sulphide content concentrates, while the sulphur dioxide has to be converted into sulphuric acid.
  • Sulphide roasting and associated gas recovery are complex metallurgical operations.
  • Gold feeds other than gravity concentrates typically include electrolytic sludges, zinc- gold precipitates and general gold scrap.
  • a pyrometallurgical smelting process is the conventional method for processing feeds of this type ie. excluding gravity concentrates. Depending on the type of the feed material, pre-treatment steps may be required ahead of the main smelting process step.
  • Smelting is essentially a gold upgrading step, which removes most of the unwanted impurities in a slag to produce a gold bullion containing from 50% to 90 % Au, the remainder being Ag and small levels of base metals.
  • the slag contains finely disseminated gold particles, typically 500 - 2000 g/t, and therefore requires further treatment to recover the gold.
  • Feed derived from electrolytic sludges originates from two electrowinning technologies namely, electrowinning onto mild steel wool cathodes or onto stainless steel wool cathodes. Removal of the gold from mild steel wool cathodes requires calcination prior
  • the gold deposited onto stainless steel wool is removed by washing with water, which after filtration and drying is smelted. Unlike the mild steel wool, the stainless steel wool cathode is reused.
  • Feed derived from older gold operations is typically in the form of a gold-zinc precipitate.
  • the precipitate typically contains a gold content of from 15% to 35%, the balance being predominantly zinc and silica.
  • Such precipitates require two pre- treatment steps ahead of smelting. The first step is optional and involves an acid treatment to dissolve most of the excess zinc. After filtration and drying, the upgraded zinc-gold precipitate is heat treated or calcined to oxidise the remaining zinc and other base metals. This calcine is then fluxed and smelted to produce gold bullion. Feed derived from scrap gold is smelted directly to produce bullion.
  • the gold bullion is produced, it is transported from site to a central refinery where the gold is refined by either a combination of a pyrometallurgical and electrochemical process or a hydrometallurgical process.
  • silver is separated and refined, while two grades of gold are typically produced.
  • the one grade has a purity of 99.5% and is used for casting monetary bars, while the other grade has a purity greater than 99.99% and is used for jewellery, coins and other industrial applications.
  • the entire process from primary gold bullion to monetary gold product can take a few days.
  • the invention provides a process for the recovery of gold from gold-bearing concentrate which include the steps of:
  • step (b) subjecting a slurry produced by step (a) to a solid/liquid separation step to produce a gold bearing solution, and (c) precipitating gold from the solution.
  • Step (b) may be effected by means of filtration. Solids, separated from the slurry, may be repulped and subjected to a silver recovery process.
  • Step (c) may be carried out by treating the solution with a suitable reductant to precipitate the gold as a powder.
  • the reductant may be of any appropriate kind for example gaseous SO 2 , sodium metabisulphite or copper and aluminium powder. Preferably, however, use is made of ferrous sulphate.
  • the chlorine used in step (a) may be derived from bottled gas or may be generated on site.
  • the feed material is a gold bearing gravity concentrate, typically containing in excess of 1 % gold (by weight), then it is preferred for economic reasons to make use of chlorine gas which is generated at site.
  • Figure 1 is a flow chart of a hydrometallurgical gold recovery process applied to a feed material which has a relatively high gold content such as an electrolytic sludge, a zinc- gold precipitate and general gold scrap,
  • Figure 2 is in many respects similar to Figure 1 and illustrates steps in the process of recovering gold from a gold bearing gravity concentrate which has a relatively low gold content
  • FIG 3 illustrates a chlorine generation cell which is used in the process of Figure 2.
  • Figure 1 illustrates the process of the invention used for the recovery of gold from a feed material 10 which has a relatively high gold content such as an electrolytic sludge, a zinc-gold precipitate or general gold scrap.
  • the feed material 10 with a relatively high gold content is fed into a leach tank 12.
  • Concentrated hydrochloric acid 14 and water 16 are added to the leach tank to produce a leaching solution with a hydrochloric acid concentration of 5 to 6 M.
  • Mixing of the leach slurry is induced by re-circulating the leach from the upper section of the leach tank through the bottom of the tank. The mixing improves
  • Chlorine gas 18 from bottles is continuously sparged into the bottom of the tank 12.
  • the pressure in the leach tank is maintained at as close as possible to atmospheric pressure by a pressure regulating system.
  • Excess chlorine 20 is absorbed in a chemical scrubber 22.
  • the gold and base metals are dissolved resulting in a dilute slurry 24 of insoluble silver chloride and small amounts of silica.
  • the silica in the residue originates from feed material consisting of gold-zinc precipitates.
  • the leach is complete when there is no further demand for chlorine. Air 26 is then sparged into the leach tank to remove entrained chlorine gas from the slurry.
  • the leach slurry 24 is discharged from the leach tank, and filtered (step 28). The residue is washed with water 30 and then discharged from the filter for further processing 32 to produce high purity metallic silver 34. Production of high purity silver is not part of this process.
  • the filtrate 36 containing dissolved gold and base metals, is transferred to a gold precipitation tank 38 for further treatment.
  • leaching parameters are as follows: Leaching time 2 - 6 hours
  • the first step during precipitation is the removal of any residual chlorine from the leach filtrate by sparging with air 40.
  • the resulting air/chlorine mixture 42 is vented to
  • a suitable reductant 44 such as gaseous S0 2 , sodium metabisulphite, or copper and aluminium powder, but preferably ferrous sulphate, is added into the precipitation tank 38 to reduce the aqueous gold to metallic powder. Very little silver and none of the base metals are precipitated with the gold. The precipitation reaction is enhanced by gentle mechanical agitation.
  • the gold-barren solution and gold precipitate 46 is filtered (step 48) to separate the precipitate, which after washing with water 50 is dried to form a powder 52.
  • the filtrate 54 is transferred into a neutralisation tank 56 for further treatment.
  • the gold powder 52 which has a purity of approximately 99.9%, can be melted to produce monetary gold bars on site, or may undergo further refining to produce a purity of 99.99%.
  • the melting and additional refining steps do not form part of the process of the invention.
  • precipitation parameters are as follows:
  • All gases (20 and 42) extracted from tanks and filters are scrubbed through the chemical scrubber 22 before venting to atmosphere.
  • the scrubber effluent 58 is pumped into the neutralisation tank 56 where it is mixed with the acidicfiltrate 54.
  • the excess acid is neutralised with lime 60 and the pH is raised to pH 10 - 11 before disposal.
  • the contents of the tank are agitated by sparging with air 62 and water 64 is added, as necessary. Failure to neutralise the effluent 54 adequately may result in the generation of hydrogen cyanide when contact is made with a cyanide-bearing stream.
  • the resulting slurry 66 is fed to an existing gold residue treatment plant.
  • Figure 2 illustrates steps in a process for the recovery of gold from gold concentrates ie. under conditions in which the gold content is low but in excess of 1%.
  • steps are the same as what has been described in connection with Figure 1 and, for this reason, such steps bear the same reference numerals as the corresponding steps in Figure 1.
  • Figure 3 illustrates a chlorine generation cell used for the generation of on-site chlorine, in the implementation of the method of Figure 2.
  • a gold gravity concentrate 10 with a grade >1% is fed into a leach tank 12, with or without a draft tube.
  • Concentrated hydrochloric acid 14 and water 16 are supplied to the leach tank to create a leaching medium with a hydrochloric content of about 5 to 6 M.
  • the solids in the tank are partially fluidised by circulating a dilute slurry mixture from the upper section of the leach tank and recirculating this through the bottom of the tank.
  • Another stream is removed from the upper level of the leach tank and is circulated through a pipe reactor 70 or a similar item of equipment and returned to the leach tank.
  • the chlorine 18 is generated by a chlorine cell 72 which is started at the beginning of the leach and the generated chlorine gas 18 is continuously induced into the pipe reactor 70.
  • the chlorine gas dissolves in the dilute slurry in the pipe reactor 70 to form aqueous chlorine before entering the leach tank 12.
  • Leaching is preferably carried out at ambient temperature and pressure. Excess chlorine 20, vented from the
  • the chlorine cell 72 is shut down to stop the generation of chlorine gas 18.
  • Air 26 is then sparged into the leach tank to remove entrained chlorine gas from the slurry.
  • the slurry 24, which contains insoluble silver chloride and residual silica, is discharged from the leach tank and filtered (step 28).
  • the residue is washed with water 30 as required and is then re-pulped in a repulper tank 74 with water 32 before being transferred to a milling circuit 76 in the main plant, where the silver chloride and any residual gold will be recovered in the cyanidation circuit.
  • the filtrate 36 containing dissolved base and precious metals, is transferred to the gold precipitation tank 38 for further treatment.
  • leaching parameters are as follows: Leaching time 12 - 18 hours Operating temperature 25°C - 50°C Au leaching efficiency > 98% HCl concentration 3 - 10 M
  • FIG. 3 schematically shows the chlorine generating cell 72.
  • the cell is a simple low- pressure chlorine generator and has a body which is fabricated from plastic and consists of a number of anode and cathode compartments 80 fastened by tie rods 82 which extend between end and pressure plates 84 and 86 to form a sealed unit. Recessed seals between each compartment ensure that no leakage occurs from the cell structure.
  • a permeable polypropylene diaphragm or ion exchange membrane separates the anolyte and catholyte solutions. Because of the bi-polar design, i.e there are only two electrical contacts 88 and 90.
  • Each electrode which is fabricated from titanium, acts as an anode and a cathode. The anode side of the electrode is coated with Ru0 2 to prevent passivation, while the cathode side is uncoated.
  • brine solution is electrolysed to form the chlorine gas 18, while at the cathode, water dissociates to form hydroxyl ions and hydrogen gas 94.
  • the sodium ions in the anode compartment pass through a permeable diaphragm and combine with the hydroxyl ions to form sodium hydroxide - caustic soda 96.
  • a concentrated brine solution is pumped (91) from a brine storage tank 98 into the anode compartment, via an inlet 100, where it is electrolysed to form chlorine gas.
  • the anolyte which consists of a mixture of brine and wet chlorine gas, overflows from the top of the anode compartment into a cavity where the gas separates from the brine solution and exits via outlets 102 and 104.
  • the chlorine gas 18 is removed from this cavity by suction.
  • the partially depleted brine solution is pumped (92) back to the brine storage tank 98 where it is re-saturated with salt. Re-saturation is achieved by circulating (106) the depleted brine solution through a saturation tank 108 containing coarse salt 110.
  • a caustic solution 112 is pumped from a caustic storage tank 114 into the cathode compartment, via another inlet in the bottom of the cell (opposite the brine inlet).
  • the catholyte which contains a higher concentration of caustic soda and hydrogen gas, overflows from the top of the cathode compartment into a cavity where the gas separates from the caustic solution and exits via outlets 116 and 118.
  • the hydrogen gas 94 is vented from this cavity and after dilution with air 120, to produce a gas mixture well below the explosive limit for hydrogen in air, is exhausted to atmosphere.
  • the more concentrated caustic solution 96 is pumped back to the caustic tank 114 where the concentration is controlled by dilution with water 122.
  • Excess caustic solution 124 is bled continuously from the caustic tank to a dechlorination tank 138. Some of this bleed 128 is used to replenish caustic in the gas scrubber system (22).
  • the anolyte operates at a slightly higher level than the catholyte to ensure a small flow of brine solution through the permeable diaphragm into the catholyte solution.
  • This flow of brine is necessary to minimise back-diffusion of sodium hydroxide into the brine and consequent formation of undesirable hypochlorite.
  • This flow of brine, designated 130, is shown figuratively in Figure 2.
  • a baffle at the top of the anode compartment, prevents the mixture of hydrogen and chlorine gases. Furthermore, atmospheric vents in the cell prevent the build-up of pressure in the cell. Since the chlorine 18 is removed from the cell by suction, no gas leaks occur to atmosphere. No brine bleed would occur if an ion exchange membrane were used.
  • a first step in the precipitation process is the removal of any remaining chlorine from the leach filtrate by sparging with air 40. This is followed by the addition of a suitable reductant 44, such as gaseous SO 2 , sodium metabisulphite, a copper and aluminium powder, but preferably use is made of ferrous sulphate, which reduces the aqueous gold to metallic powder. Very little silver and none of the base metals are precipitated with the gold. The precipitation reaction is enhanced by gentle mechanical agitation.
  • the gold-barren solution and gold precipitate 46 is filtered (step 48) to separate the precipitate, which after washing (50) is dried to form a powder 52.
  • the filtrate 54 is transferred into the neutralisation tank 56 for further treatment.
  • the gold powder 52 which has a purity of approximately 99.9%, can be melted to produce monetary gold bars on site, or may undergo further refining to produce a purity of 99.99%.
  • the melting and additional refining steps do not form part of the process of the invention.
  • precipitation parameters are as follows: Precipitation time 1 - 2 hours
  • the scrubber effluent 136, brine bleed 130, and caustic bleed 124 contain some sodium hypochlorite, while the leach/precipitation filtrate 54 contains hydrochloric acid and sulphuric acid.
  • the effluent treatment circuit consists of a dechlorination tank 138 and the neutralisation tank 56 in which dechlorination and neutralisation are carried out respectively.
  • the scrubber effluent 128, bleed 130 and caustic bleed 124 are transferred into the dechlorination tank 138, while the acidic gold-barren leach filtrate 54 is transferred directly into the neutralisation tank 56.
  • a solution of sodium thiosulphate 140 is added to the dechlorination tank to destroy hypochlorite.
  • the alkaline solution 142 is transferred to the neutralisation tank 56, where it neutralises some of the acid in the leach/precipitation filtrate.
  • the pH in the neutralisation tank is then adjusted with slaked lime 60 to a value of 10 to 11.
  • Failure to dechlorinate or neutralise the effluent may result in the generation of cyanogen chloride or hydrogen cyanide when contact is made with a cyanide-bearing stream.
  • the generation of chlorine gas in the chlorine cell 72 using brine as a chlorine source and the use of the gas for the recovery of gold, in the manner described, has a number of advantages with include the following: • the process is not labour intensive and therefore poses a lower security risk with respect to gold losses due to less handling;

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • Metallurgy (AREA)
  • Mechanical Engineering (AREA)
  • Materials Engineering (AREA)
  • Geology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Geochemistry & Mineralogy (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

L'invention concerne un procédé de récupération d'or d'un concentré, tel qu'une boue électrolytique, un précipité zinc-or, des déchets globaux d'or et un concentré obtenu par gravité. Ce concentré est lessivé dans une solution HCl à base de chlore gazeux afin de dissoudre l'or. Les métaux de base et l'or sont ensuite précipités à partir d'une solution extraite d'une bouille produite au moyen du procédé de lessivage. Le chlore est produit sur site si le contenu en or de la bouille est > 1 %, alors que le gaz en bouteille est utilisé si le contenu en or est > 10 %.
PCT/ZA2001/000050 2000-04-28 2001-04-26 Procede de recuperation d'or WO2001083835A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU2001257646A AU2001257646A1 (en) 2000-04-28 2001-04-26 Gold recovery process

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ZA200002053 2000-04-28
ZA2000/2053 2000-04-28

Publications (2)

Publication Number Publication Date
WO2001083835A2 true WO2001083835A2 (fr) 2001-11-08
WO2001083835A3 WO2001083835A3 (fr) 2002-03-07

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Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ES2304095A1 (es) * 2003-09-23 2008-09-01 Outokumpu Technology Oyj Metodo para el tratamiento de lodos anodicos.
CN100473732C (zh) * 2007-02-09 2009-04-01 上海大学 一种电化学氧化法浸取难浸金矿的设备
CN100485055C (zh) * 2007-02-09 2009-05-06 上海大学 电化学氧化法浸取难浸金矿的方法
US20120067169A1 (en) * 2009-04-24 2012-03-22 Precious Metals Recovery Pty Ltd Method for processing precious metal source materials
CN102690942A (zh) * 2012-06-18 2012-09-26 中南大学 一种含硫金精矿焙砂还原焙烧强化酸溶的方法
EP2662464A1 (fr) * 2012-05-09 2013-11-13 Inter-Euro Technology Limited Récupération d'or
EP3026130A1 (fr) * 2014-11-26 2016-06-01 Lifezone Limited Procédé de traitement d'extraction d'éléments de terres rares de base et précieux
WO2017193726A1 (fr) * 2016-05-10 2017-11-16 中国恩菲工程技术有限公司 Système et procédé de purification de solution
US10144989B2 (en) 2015-03-18 2018-12-04 Outotec (Finland) Oy Recovery of gold from solution
CN109881023A (zh) * 2019-01-30 2019-06-14 东北大学 一种含氰贫液保护电沉积循环利用的方法
CN109881022A (zh) * 2019-01-30 2019-06-14 东北大学 一种含氰贫液全流程绿色循环利用的方法
US10400306B2 (en) 2014-05-12 2019-09-03 Summit Mining International Inc. Brine leaching process for recovering valuable metals from oxide materials
US10648062B1 (en) 2017-03-23 2020-05-12 George Meyer Strategic metal and mineral element ore processing using mixing and oxidant treatment
CN114555840A (zh) * 2019-11-18 2022-05-27 贺利氏德国有限两合公司 用于回收贵金属的方法
CN114892007A (zh) * 2022-05-18 2022-08-12 云南锡业股份有限公司铜业分公司 一种复杂铜阳极泥蒸硒渣中回收有价金属的方法

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Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ES2304095A1 (es) * 2003-09-23 2008-09-01 Outokumpu Technology Oyj Metodo para el tratamiento de lodos anodicos.
AU2004274670B2 (en) * 2003-09-23 2009-09-03 Metso Outotec Finland Oy Method for processing anode sludge
US7731777B2 (en) * 2003-09-23 2010-06-08 Outotec Oyj Method for processing anode sludge
CN100473732C (zh) * 2007-02-09 2009-04-01 上海大学 一种电化学氧化法浸取难浸金矿的设备
CN100485055C (zh) * 2007-02-09 2009-05-06 上海大学 电化学氧化法浸取难浸金矿的方法
US20120067169A1 (en) * 2009-04-24 2012-03-22 Precious Metals Recovery Pty Ltd Method for processing precious metal source materials
US20120067170A1 (en) * 2009-04-24 2012-03-22 Precious Metals Recovery Pty Ltd Extraction of gold from cathode associated gold concentrates
CN104302793A (zh) * 2012-05-09 2015-01-21 Inter-Euro科技有限公司 金回收
EP2662464A1 (fr) * 2012-05-09 2013-11-13 Inter-Euro Technology Limited Récupération d'or
WO2013167714A1 (fr) 2012-05-09 2013-11-14 Inter-Euro Technology Limited Récupération d'or
US9689054B2 (en) 2012-05-09 2017-06-27 High Value Metals Recovery Ltd Gold recovery
CN102690942A (zh) * 2012-06-18 2012-09-26 中南大学 一种含硫金精矿焙砂还原焙烧强化酸溶的方法
US10400306B2 (en) 2014-05-12 2019-09-03 Summit Mining International Inc. Brine leaching process for recovering valuable metals from oxide materials
US9982320B2 (en) 2014-11-26 2018-05-29 Lifezone Limited Treatment process for extraction of precious, base and rare elements
EP3026130A1 (fr) * 2014-11-26 2016-06-01 Lifezone Limited Procédé de traitement d'extraction d'éléments de terres rares de base et précieux
US10144989B2 (en) 2015-03-18 2018-12-04 Outotec (Finland) Oy Recovery of gold from solution
WO2017193726A1 (fr) * 2016-05-10 2017-11-16 中国恩菲工程技术有限公司 Système et procédé de purification de solution
US10648062B1 (en) 2017-03-23 2020-05-12 George Meyer Strategic metal and mineral element ore processing using mixing and oxidant treatment
CN109881023A (zh) * 2019-01-30 2019-06-14 东北大学 一种含氰贫液保护电沉积循环利用的方法
CN109881022A (zh) * 2019-01-30 2019-06-14 东北大学 一种含氰贫液全流程绿色循环利用的方法
CN114555840A (zh) * 2019-11-18 2022-05-27 贺利氏德国有限两合公司 用于回收贵金属的方法
CN114892007A (zh) * 2022-05-18 2022-08-12 云南锡业股份有限公司铜业分公司 一种复杂铜阳极泥蒸硒渣中回收有价金属的方法

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