WO2013049886A1 - Perfectionnements apportés à l'extraction de métaux à partir de minerais - Google Patents

Perfectionnements apportés à l'extraction de métaux à partir de minerais Download PDF

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Publication number
WO2013049886A1
WO2013049886A1 PCT/AU2012/001201 AU2012001201W WO2013049886A1 WO 2013049886 A1 WO2013049886 A1 WO 2013049886A1 AU 2012001201 W AU2012001201 W AU 2012001201W WO 2013049886 A1 WO2013049886 A1 WO 2013049886A1
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Prior art keywords
solution
oxidising
ore
persulphate
aqueous
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PCT/AU2012/001201
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English (en)
Inventor
William James KYTE
Peter Marino PAVLOVICH
Craig Rothwell HUGHES
Brendan Allan WOODLEY
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Fine Gold Recovery Pty Ltd
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Filing date
Publication date
Priority claimed from AU2011904089A external-priority patent/AU2011904089A0/en
Application filed by Fine Gold Recovery Pty Ltd filed Critical Fine Gold Recovery Pty Ltd
Priority to US14/349,042 priority Critical patent/US20140230604A1/en
Priority to AU2012321049A priority patent/AU2012321049B2/en
Publication of WO2013049886A1 publication Critical patent/WO2013049886A1/fr
Priority to US15/358,647 priority patent/US20170073794A1/en
Priority to AU2017213591A priority patent/AU2017213591B2/en

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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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/02—Apparatus therefor
    • 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
    • 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 invention relates to cyanide- free and mercury- free aqueous chemical processes and solutions for the recovery of metals, including precious or noble metals, copper, zinc and other metals from ores or other sources including rubbish, tailings and mullock.
  • the oxidation potential (with respect to a standard hydrogen electrode) of various materials is described herein as E , given in volts.
  • Ole includes without limitation carbonaceous (carbonate) ores, sulphide ores, porphyry ores, massive metal such as in quartz ores, selected industrial waste such as electronic parts, and tailings and mullock.
  • Van Antwerp et al (1987) in US 4642134 used a combination of a low pH of about 3, in combination with a reduction potential E in the oxidising solution including ozone, having a potential of no more than 2.4 volts. They state that 2.4 V is at about the upper limit of ultraviolet- generated ozone in solution. (Such a potential is insufficient for some forms of gold). After the gold is oxidized, conventional leaching chemicals are used to recover the gold. Van Antwerp et al (1987) in US 4752412 also used activated oxygen / ozone derived from effects of UV light. Note that their preference for acetic acid 1-3% by volume necessarily prevents the pH from being lower than about 3.
  • Lakshmanan et al in US 4537628 used peroxymonosulphuric acid (H 2 S0 5 or Caro's acid) to extract gold from arsenic-containing gold ore, followed by a cyanide process.
  • Scheiner et al (1973) in US 3764650 a combination of a very low pH of no higher than about 1 and a reduction potential E of more than 1.4 volts, sodium chloride, sulphuric acid, and ozone in an 8-hour process.
  • Scheiner et al in US 3574600 said the ozone was to prevent reabsorbtion of gold, and completed the process with cyanide - after neutralisation.
  • Hansen et al in US3545964 (1970) used a low pH in combination with a reduction potential E h of more than 1.4 volts, and potassium thiocyanate in a 10-day process, reliant on organic solvents.
  • Joseph (US732641) (1903) used an acidic oxidising solution including sulphuric acid, potassium permanganate, nitric acid and sodium hyposulphite and also sodium chloride, with an unspecified leaching process.
  • An object of the present application is to provide a solution or composition, and a process for recovering metals including noble metals from an ore, or at least to provide the public with a useful choice.
  • the invention provides a cyanide-free and mercury- free aqueous process for recovery of one or more desired metals, including precious metals and other metals from an ore, more particularly wherein the first aspect relates to an aqueous oxidising solution
  • the aqueous oxidising solution has a pH of less than 0.7 primarily as a result of the presence of at least one strong acid and a reduction potential (E h ) of at least 2.5 V primarily as a result of the presence of persulphate anions and contains anions selected from a group consisting of chloride, bromide, iodide and nitrate ions.
  • the oxidising solution when freshly prepared, has a pH of less than 0.7 and a reduction potential E h of at least 2.5 V and the oxidising solution is maintained in an acidic state with a pH of less than 3 throughout the process.
  • the oxidising solution includes at least one compound selected from the range of: hydrogen peroxide, and freshly made ozone in solution.
  • the invention provides an oxidising solution as previously described in this section wherein the solution includes an effective amount of at least one strong acid or mixture of strong acids capable of lowering the pH of the solution to about 0.6 or less, said acid being selected from a range including hydrochloric acid, sulphuric acid, persulphuric acid and nitric acid, and wherein the solution includes a sufficient amount of an oxidizing agent selected from a range including without limitation one or more of the oxidising salts potassium
  • KHS0 5 (CAS 10361-76-9), sodium persulphate Na 2 S 2 0 8 , (CAS 7775-27- 1) and ammonium persulphate CAS 7727-54-0), together with the oxidising agent hydrogen peroxide, such that the reduction potential is at least 2.5 Eh.
  • the solution includes a halide salt selected from a range including sodium chloride, potassium chloride, sodium bromide or potassium bromide.
  • the aqueous oxidizing solution includes at least the following ingredients:
  • a persulphate selected from the group consisting of sodium persulphate potassium persulphate and ammonium persulphate;
  • the oxidising solution includes 8.4% by volume of concentrated hydrochloric acid, 0.09 % by weight of sodium persulphate or ammonium persulphate, 0.18% by weight of sodium bromide, 0.16% by volume of commercial strength hydrogen peroxide, ozone at about 0.75 mg/litre made by ultraviolet irradiation of oxygen, and water.
  • the oxidizing potential (E h ) of the solution is capable of reaching about 2.8 V.
  • the invention provides a process for using the aqueous oxidising solution as claimed in any one of claims 1 to 5, characterised in that the process includes a first formulation step of formulating the aqueous oxidising solution by addition of ingredients to water, a second metal solubilisation step of oxidising and thereby rendering soluble a desired at least one metal from a ground amount of ore in suspension, a third collecting step of collecting a pregnant liquor from the suspension, a fourth metal extraction step of selectively removing at least a portion of the at least one metal from the liquor while at a pH of less than 3; such that any remaining liquid is a recyclable liquor.
  • process is adapted for recycling of the solution by maintaining the oxidising solution with a pH of less than about 3 at all times.
  • the process includes a first stage of forming the acidic, oxidising solution by addition of ingredients to water in a tank, a second stage of leaching the desired metal or metals from a ground aliquot of ore in suspension in another tank, a third stage of collecting a pregnant liquor from the suspension into yet another tank, a fourth stage of selectively removing the desired metal or metals from the liquor while at a pH of less than 3, thereby creating a recyclable liquor, and a fifth stage of holding the recyclable liquor in a tank ready for re-use.
  • the process divorces a first process of leaching of the ore from a second process of recovery of the desired one or more metals by providing a storage tank for holding pregnant liquor prior to metal extraction, and a second storage tank for holding recyclable liquor after metal extraction, from which it may be recycled into a substantially original state by addition of those ingredients that have been consumed.
  • the method provides a plurality of paths for separate extraction of more than one metal from the same ore in a series of steps; each path including a storage tank for holding pregnant liquor prior to metal extraction, and a second storage tank for holding recyclable liquor after metal extraction, wherein the pH of the oxidising solution is reduced and the reduction potential is increased with each succeeding step.
  • the same charge of ore is re-exposed to one or more further batches of fresh or restored solution until a test discloses that an amount of recovered metal in the suspension is no longer adequate and the ore is discarded.
  • the ozone is also added to the solution during a leaching procedure and recirculates the solution past a source of ultraviolet light at or about 254 nm wavelength during the solubilising process, thereby causing reactions to occur that release oxidising radicals including without limit the oxygen singlet and ozone radical.
  • the source material or ore is finely ground, so that it will remain suspended as fine particles in the aqueous solution while being recirculated and so that the reaction rate is not unduly slowed.
  • a preferred period of time for oxidising a batch of the suspension of at least carbonaceous and porphyry-based ore is between 5 and 120 minutes at ambient temperature; alternatively ores not finely ground or of recalcitrant types may require exposure for up to about 3 weeks.
  • One preferred method for extracting said at least one metal from the pregnant liquor comprises passing the pregnant liquor which has a pH of less than about 3 through a series of selective electrolysis cells or electrowinning cells.
  • Fig 1 Outline of a single-path recirculating processing plant, according to the present invention.
  • Fig 2 Outline of a multi-path recirculating processing plant, according to the present invention.
  • Fig 3 Outline diagram of a processing plant including direct photochemical oxidation of the liquid, according to the present invention.
  • Fig 4 Outline of a multi-step recirculating processing plant, according to the present invention.
  • the present invention provides solutions each having a composition that provides conditions capable of solubilising gold (or other desired metals) in a variety of types of ore.
  • Problems with implementation of this discovery include keeping the ionized metals in solution until it is brought to a reclaiming step in a process and there is reclaimed efficiently.
  • Halide ions - chloride, bromide or iodide - are used to assist this purpose, particularly with gold. The inventors do not assert that this explanations or their theories are correct or complete, and note that the chemistry of strong oxidising solutions especially in combination with ozone and ultraviolet light is not well established.
  • the invention provides an oxidising solution and a process for use in the recovery of one or more metals, such as, but not limited to gold from an ore as defined above.
  • the solution comprises variants of an acidic aqueous solution including hydrogen, chloride and bromide ions and strong oxidants including peroxydisulphate or persulphate ions, ozone, and hydrogen peroxide.
  • the initial oxidising power of this solution is maintained during treatment of a batch of ore by mixing externally, freshly generated ozone supplied from generator 109 either before, or during suspension while it is being agitated inside reaction vessel 101.
  • When recycling the oxidising solution its pH and E are restored by addition of reagents.
  • the inventors have observed that adding a small amount of ozone to the solution before a leaching process, such as 0.75 g of ozone, causes the amount of recoverable gold in the supernatant to rise up to a usefully recoverable amount in a few minutes, whereas if the ozone is not added, the gold concentration may take a week or longer to rise by the same amount. This effect occurs despite the presence of persulphate but is, of course, dependent on the ore and particle sizes in the suspension.
  • hydroxyl radicals are generated by reactions between ozone and hydrogen peroxide. This type of mixture is also known as "peroxone". The presence of hydrogen peroxide shortens the half-life of ozone.
  • the "oxidising strength" of the hydroxyl radical (as OH + e " > OFl ⁇ is +2.8V E , a little less than that of fluorine.
  • the inventors have not yet explored uses and advantages of various types of ozone radicals.
  • the oxidising capacity of the preferred persulphate radical is almost as high, at 2.7 V E h , as the hydroxyl radical.
  • separating means 116 Refer to the plant 100 in Fig 1. Ore enters the process at mill 102 and leaves the process, optionally to be recycled, at exit 114 after separation in a hydrocyclone 113. Liquid is recycled through the four connected tanks. 101 is the stirrable reaction tank, 103 holds recyclable liquid for re-use, 119 is a tank used for mixing fresh batches of the oxidising solution or for rejuvenating recycled solution (recyclable liquid) and 115 is a tank for holding pregnant liquors for separation of recovered metals (if present) within separating means 116.
  • the tanks may be made of steel or stainless steel, preferably coated with a paint or other polymer. Alternatively, plastics materials may be used. Polypropylene is suitable.
  • water 108 In order to commence a new batch, water 108, optionally existing recyclable liquid 103, and reagents 104, 105, 106, 107 (see list below) and ozone from the gas generator 109 are placed in tank 119, and thoroughly stirred as indicated by the curved arrows.
  • This liquid which has a pH of around 0.6 and is strongly oxidising, is transferred to tank 101.
  • An amount of ore which has been ground to a suitably fine size in mill 102; for example such that 95% passes a 0.1 mm diameter sieve is added to tank 101 such that a suspension is formed in the oxidising solution without any caking.
  • the slurry preferably holds at least 5 - 10% by weight of ore (the pulp ratio), although this amount may depend on the particular ore being processed.
  • An internal agitator 121 (motor not shown) maintains the slurry in suspension.
  • leaching tank 101 may in fact comprise a series of such tanks, or an elongated trough, preferably including mixing means.
  • a graded series of solutions may be used, optionally followed by a leaching time. (See also Example 2.)
  • inclusion of ozone greatly speeds the process. An extraction that might have taken a week without ozone may be substantially complete in a few minutes, though this depends on the ore. But if metallic gold is present, the "etching rate" may be slow using any solution.
  • Leaching efficacy may be determined by repeatedly sampling the suspension and testing for solubilised gold ions (or other metals of interest) with a suitable test device such as an atomic absorbtion spectrophotometer (Varian Associates) or an inductively coupled or a microwave- generated plasma discharge device plus spectrograph, or a mass spectrograph, as known to those skilled in the art.
  • a suitable test device such as an atomic absorbtion spectrophotometer (Varian Associates) or an inductively coupled or a microwave- generated plasma discharge device plus spectrograph, or a mass spectrograph, as known to those skilled in the art.
  • pregnant liquor is withdrawn for metal extraction.
  • the plant provides for two methods for removal.
  • the agitator paddle 121 is stopped and after a settling period a side port 120 in leaching tank 101 located at position (A) as shown in Fig 2, placed so as to be a little above the level of the settled charge of ore, is opened so that nearly all of the supernatant will flow through pipe 122 into the tank 115, for receiving pregnant liquor.
  • port 120 is closed and another oxidising solution (which may be a different solution - see Example 2) is admitted from preparation tank 119 and agitation of the same batch of ore recommences.
  • the agitator paddle within reaction tank 101 is kept running while the suspension is entirely removed through valve 110 to hydrocyclone 113; the pregnant liquor is drained into tank 115 and the separated, exhausted solids 114 are then discarded into a tailings dam or the like. Further solution is admitted into tank 101 from tank 119 so that the agitator does not run dry. Preferably all remaining acidity in the tailings emitted at 114 is neutralised with ground limestone, phosphate rock or the like, for the sake of the environment. Recyclable liquor is likewise neutralised if discarded.
  • the astute reader will note that exact duration and replenishments are not prescribed since different metals and different ores may need different times.
  • the pregnant liquor now stored in tank 115 typically now has a pH of up to about 2 to 3. That is, the hydrogen ions of the acid have been partially consumed.
  • the pregnant liquor held in tank 115 is passed through preferably a selected differential metal extraction means 116.
  • the rate of flow through the extraction means is not tied to the rate of flow through the reaction vessel 101, and the metal extraction means may be kept running continuously from pregnant liquor held in tank 115 even while the next batch of suspended ore is being exposed to the solution.
  • One preferred extraction means 116 which is well known to those skilled in the art of extractive metallurgy, involves selective electrolysis or electrowinning.
  • a series of individual electrolytic cells, arranged in a series according to threshold conditions such as the potential applied within and/or the current density per unit area of the cathode is capable of recovering one or more relatively pure metals 118 on separate sets of electrolysis plates (not shown).
  • Equipment for carrying out selective electrowinning metals such as aluminium, cobalt, copper, lead, precious metals and rare earth metals is commercially available from many suppliers such as
  • oxidising solution does not require to be replenished.
  • a fresh solution may be prepared for each extraction. Recycling should be more economical.
  • Another extraction means well known to those skilled in the relevant arts employs adsorbtion of the gold on to activated carbon 116, then stripping the gold from the carbon and processing the gold after several steps into relatively impure metal bars called Dore bars.
  • Further options at 116 for metal recovery include the already well-known chemical and electrochemical techniques in common use in the mining industry.
  • the recyclable liquor returned to tank 103 may still have a low pH typically 2-3.
  • supplementary amounts of reagents 104, 105, 106, 107 are added in order to make up any losses, for instance to overcome a rise in pH.
  • Acidic, highly oxidising solutions are employed in order to maximise the extraction of preferred metals such as gold and maintain it in ionic form stabilised by means of chloride or other halide ions, oxidising conditions and a low pH.
  • oxidising solution may be varied according to ore type for example, a starting point and a suggested range for such solutions is as follows.
  • Example 1 An oxidising solution Typical Range
  • ammonium persulphate NH 4 ) 2 S 2 08 (CAS 7727-54-0), or 1 kg potassium persulphate, Sodium Bromide (or potassium bromide) 1.8 kg 0 to 3 kg
  • Hydrogen Peroxide commercial strength (about 30%) 1.6 litres 0 to 2 litres
  • the ozone is manufactured on site by irradiating air with ultra-violet light at about 184 or 254 nm, using for example low pressure mercury lamps in quartz or other envelopes, or deuterium or xenon lamps, and bubbling the gas into the mixing tank 119.
  • the pH is about 0.6 and the E is preferably up to 2.8 V.
  • the bromide may be optional given that some other halide, namely chloride ions are provided by the hydrochloric acid, although it is known that gold bromide and gold iodide are stable. Further experimentation and trials with different ores may uncover more precise formulations.
  • This layout 200 extends the principles shown in Fig 1 and includes a parallel set of processes.
  • three sets of metal extraction lines such as for copper (A), silver (B) and gold (C) and their associated tanks are supplied with an oxidising solution from a single set of a mixing tank 119 and a reaction tank 101 (which is shown with the slurry settled and a supernatant ready to be drawn by selective operation of valves into an appropriate metal extraction line).
  • the preferred way to use a plant constructed according to this layout is to treat a mixed ore, which might for example contain copper, zinc, and gold, in a sequence, with each subsequent stage applying a higher reduction potential E and a lower pH within the oxidising solution so that the most easily oxidised or solubilised metal is removed first from the ore and is then diverted into a particular stream (A, B or C) appropriate for extraction of that metal.
  • a mixed ore which might for example contain copper, zinc, and gold
  • Each of the "A" stream, "B” stream and “C” streams that include corresponding pregnant liquor tanks 115A or 115B or 115C, appropriate metal extraction devices 116A or 116B or 116C, and recyclable liquid tanks 103 A, 103B and 103C operate with a different chemical solution, as made up in the single mixing tank 119 from supply tanks 104, 105, 106, 107 and 108.
  • Each stream stays relatively separate so long as the relevant valves are correctly controlled, and is not mixed with other streams.
  • a single mix can be used several times over in a sequence C then B then A as its acidity and reduction potential decline with use.
  • Solution 1 (which itself is not a definitive prescription) may be modified as follows in relation to each particular type of ore and metals to be extracted, for instance
  • each metal extraction device 116A or B or C may be optimised for a particular metal, such as by employing different electro winning sets or, for any one metal, a series of chemical stages optionally including precipitation, centrifugation, filtering, foam separation or the like (as at 116A).
  • the raw metals 118A, 118B and 118C are separate outputs from this separation plant.
  • tank sizes are shown as the same size in Fig 2. In practice tank sizes, and number and type of metal extraction devices would depend on the particular ore being processed.
  • Solubilisation of massive metals may be the slowest phase.
  • Metal extraction can proceed at an independently controlled pace determined by technical limits and amount of metal ions present, for example, drawing pregnant liquor from tank 115A or B or C and returning it to tank 103 A or B or C while slurry extraction proceeds at an independent rate.
  • valves crossed circles, not labelled for simplicity
  • pumps not shown
  • Liquids in each stream are mixed to a small extent only such as within pipes and by being entrapped within the ore particles, and remain reasonably optimised.
  • the repeatedly applied test and replenishment process used at tank 119 will maintain the required characteristics of each set of liquids.
  • the inventors have noted a reasonably good recovery of silver in their chloride/bromide process at low pH and relatively high reduction potential, although silver ions may tend to be adsorbed on to the ore slurry and lost. A decision to use a nitric acid process might be based on economics. If halide contamination is a significant adverse effect on recovery, the silver extraction could comprise a pre-treatment of the ground ore.
  • the pH and reduction potential of the oxidising solution may be substantially reduced (E 0.4V to IV, pH less than about 5) and the same plant may be used without the ozone.
  • the overall inputs into this Recirculating Batch Plant are ore, reagents including water (104-108) and energy for grinding, pumps, agitators and metal extraction. No heat is required. All operations occur at ambient temperature. Acid is consumed and needs replenishment at each pass, depending on the ore type.
  • the outputs are neutralised, spent ore (at 114), and extracted metals (118 A, B and C). From time to time it may be necessary to reject recycled recyclable liquid, which will be salty and acidic and which may have accumulated toxic materials such as arsenic. Such contaminants must be dealt with in order to avoid environmental pollution and breach of relevant laws. More or less than the 3 streams (A, B and C) shown may be used.
  • Example 2 differs from Example 1 mainly in that instead of stirring a slurry mixed with a single charge of ozonised solution, the slurry during leaching is repeatedly pumped from tank 301 by diaphragm pump 311 through a mixing tube 319, past an ozone entry port 309, and then past a battery of ultraviolet lamps 310 so that the ozone is repeatedly refreshed and maintained at a high level, until experience, or on-line tests indicate that solubilisation of the desired metals is substantially complete.
  • Shearing or mixing tube 319 subjects the particles of the suspension to shear forces, helping to ensure that the suspended particles (at a low pulp ratio) remain free of any accretion at a microscopic level.
  • Example shearing or mixing tubes containing a series of deflection vanes which force the suspension to change direction repeatedly. Such tubes are well known in the relevant arts.
  • the stirred output passes an optional entry port for injecting freshly prepared ozone gas from the ozone generator 109.
  • an ozone generator capable of producing 6 grams of ozone per hour was used.
  • the ozone may be generated by exposure of air or oxygen to an ultraviolet lamp, including low pressure mercury, deuterium or xenon lamps equipped with quartz envelopes, or by exposure to a spark or a radio frequency arc.
  • an ultraviolet exposure means or "reactor” 310 comprising a circular array of typically 6 low-pressure mercury vapour lamps having the same configuration as 1200 mm or 1500 mm long 40 watt fluorescent lamps, but with quartz envelopes, so that the suspension is directly irradiated with ultraviolet light.
  • the electrical connections to the lamps are of course sealed from contamination with liquid.
  • This treatment has the effect of further raising the oxidation potential of the active components of the aqueous mixture by direct interaction of ultraviolet photons with the active components. Hydroxyl radicals are made. The problem of a short half-life of the most active oxidising species is overcome.
  • the combination of the recycling pump 311 and a relatively low "pulp ratio" of suspended ore helps ensure that the suspension remains evenly distributed within the tank 401 during processing, although an internal agitator may also be included.
  • the batch is drawn out of the processing tank 301 by activating the pump or valve 312 and shifting the suspension across to a solids separation means 113, such as a dewatering hydrocyclone.
  • the pregnant liquor which now preferably includes an amount of gold in ionic form stabilised by means of chloride anions, oxidising conditions and a low pH is transferred to tank 115 while the solid waste or tailings 114 is disposed of as described in Example 1.
  • the liquid in tank 415 is passed through a gold extraction means.
  • a gold extraction means that are well known to those skilled in the relevant arts employs adsorbtion of the gold on to activated carbon 316, then stripping the gold from the carbon and processing the gold after several steps into relatively impure metal bars called Dore bars, a standard industry term allowing for the likely co-presence of other metals such as silver.
  • the remaining acidic and re-usable liquid now termed a "recyclable solution” is pumped into tank 303 through pipe 117 to await optional supplementation and then re-use.
  • a recyclable solution is pumped into tank 303 through pipe 117 to await optional supplementation and then re-use.
  • the recyclable solution is tested for pH, halide ion concentration, and redox potential in order to determine what supplementation is required for restoration of the original solution, as follows.
  • ozone is continuously added to the solution from an ozone generator operated beside the apparatus at a rate of about 12 grams per 1000 litres per hour.
  • This Example differs from Example 2 by applying the highly acidic, high oxidising capacity oxidising solution to the ore in the first instance, and then passing the same pregnant liquor through a series of appropriate metal-specific procedures 116A, 116B and 116C selected, as would be known to a skilled addressee, from a range including electrowinning, chemical precipitation, ion exchange, and active carbon adsorbtion in order to extract (for example) copper, silver, gold, lead, zinc and the like.
  • Each metal-specific procedure is connected in series by conduits 401 and 402.
  • Each metal-specific procedure may optionally be separated from adjacent procedures by a storage tank 115A preceding procedure 116A and another storage tank 103 A following procedure 116A in order to allow different rates of processing to be applied.
  • the process is able to recover economically useful amounts of gold including from tailings which have previously been processed and discarded as uneconomic;
  • the process separates a leaching flow rate of the oxidising solution applied to the ore from a metal extraction rate or rates;
  • the process is compatible with most types of ore, including carbonaceous ores and porphyry ores, as well as with quartz, and with industrial rubbish such as used printed-circuit boards, electrical connectors and other items carrying gold;
  • the process is substantially immune to the presence of sulphides, unlike existing methods such as cyanide recovery that are difficult to use in the presence of sulphides;

Abstract

L'invention concerne un procédé d'oxydation de minerai broyé en vue de l'extraction de métaux nobles, y compris l'or, l'argent et la famille des platines, et d'autres métaux incluant le cuivre. Une solution d'oxydation aqueuse acide (pH inférieur à 0,7) comprend des ions chlorure et bromure et des oxydants forts, y compris des ions persulfate. Le potentiel de réduction de cette solution peut atteindre environ 2,6 V. De préférence, on ajoute de l'ozone obtenu par des moyens photochimiques. La solution de suspension du minerai pulvérisé est éventuellement irradiée à l'aide d'un rayonnement ultraviolet. Un ou plusieurs métaux sont extraits de la liqueur d'attaque acide par des procédés connus, y compris l'extraction électrolytique et l'échange d'ions. Un procédé de recyclage de solution est décrit.
PCT/AU2012/001201 2011-10-04 2012-10-04 Perfectionnements apportés à l'extraction de métaux à partir de minerais WO2013049886A1 (fr)

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Application Number Priority Date Filing Date Title
US14/349,042 US20140230604A1 (en) 2011-10-04 2012-10-04 Recovery of metals from ores
AU2012321049A AU2012321049B2 (en) 2011-10-04 2012-10-04 Improvements in recovery of metals from ores
US15/358,647 US20170073794A1 (en) 2011-10-04 2016-11-22 Recovery of Metals from Ores
AU2017213591A AU2017213591B2 (en) 2011-10-04 2017-08-14 Improvements in recovery of metals from ores

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AU2011904089A AU2011904089A0 (en) 2011-10-04 Improvements in recovery of metals from ores
AU2011904088A AU2011904088A0 (en) 2011-10-04 Improvements in the recovery of precious metals
AU2011904088 2011-10-04
AU2011904089 2011-10-04

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US15/358,647 Continuation US20170073794A1 (en) 2011-10-04 2016-11-22 Recovery of Metals from Ores

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* Cited by examiner, † Cited by third party
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Publication number Priority date Publication date Assignee Title
US10400306B2 (en) 2014-05-12 2019-09-03 Summit Mining International Inc. Brine leaching process for recovering valuable metals from oxide materials
CN105886780A (zh) * 2016-06-27 2016-08-24 董博文 一种非氰高效溶浸含金物料中金的药剂
RU2788138C1 (ru) * 2021-10-05 2023-01-17 Федеральное государственное бюджетное учреждение науки "Федеральный исследовательский центр "Пущинский научный центр биологических исследований Российской академии наук" (ФИЦ ПНЦБИ РАН) Способ извлечения металлов

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AU2012321049A2 (en) 2014-09-11
CL2014000772A1 (es) 2014-11-28

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