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US20080069723A1 - Method for oxidizing carbonaceous ores to facilitate precious metal recovery - Google Patents

Method for oxidizing carbonaceous ores to facilitate precious metal recovery Download PDF

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Publication number
US20080069723A1
US20080069723A1 US11/858,480 US85848007A US2008069723A1 US 20080069723 A1 US20080069723 A1 US 20080069723A1 US 85848007 A US85848007 A US 85848007A US 2008069723 A1 US2008069723 A1 US 2008069723A1
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precious metal
containing material
carbon
oxidized
microwave energy
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US11/858,480
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James Tranquilla
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HW ADVANCED Tech Inc
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HW ADVANCED Tech Inc
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Publication of US20080069723A1 publication Critical patent/US20080069723A1/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
    • C22B4/00—Electrothermal treatment of ores or metallurgical products for obtaining metals or alloys
    • 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
    • C22B1/00—Preliminary treatment of ores or scrap
    • 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
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/02—Roasting processes
    • 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
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/02—Roasting processes
    • C22B1/10—Roasting processes in fluidised form
    • 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
    • C22B11/02—Obtaining noble metals by dry processes
    • 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
    • C22B11/08—Obtaining noble metals by cyaniding
    • 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
    • C22B9/00—General processes of refining or remelting of metals; Apparatus for electroslag or arc remelting of metals
    • C22B9/16—Remelting metals
    • C22B9/22—Remelting metals with heating by wave energy or particle radiation
    • C22B9/221—Remelting metals with heating by wave energy or particle radiation by electromagnetic waves, e.g. by gas discharge lamps
    • C22B9/225—Remelting metals with heating by wave energy or particle radiation by electromagnetic waves, e.g. by gas discharge lamps by microwaves

Definitions

  • the invention relates generally to precious metal recovery and particularly to recovery of precious metals from refractory carbonaceous materials using thermal oxidation techniques.
  • Carbon is an extremely abundant natural element whose unique characteristics include the ability to physically entrap or adsorb gold particles. Where the evolution of certain gold deposits coincides with the natural presence of carbon, the carbon acts as a filter to entrap the gold, producing a class of gold mineralogy known as carbonaceous ore.
  • the gold-attracting quality of carbon is widely exploited in commercial gold recovery techniques where gold is produced in a solution medium to which activated carbon is intentionally introduced.
  • the carbon becomes “loaded” with gold through adsorption, is removed from the solution environment, chemically stripped of its gold and then returned to the processing circuit to be reused in the recovery process.
  • preg robbing When the carbon occurs naturally in the gold ore, the ore cannot be directly leached through the normal cyanide treatment (cyanidation) owing to the dominant influence of the carbon; this situation is known as “preg robbing”.
  • Adsorption of the gold lixiviant complex by refractory carbonaceous material is very complicated, due to three major factors. First, the precise chemical and physical nature of the carbonaceous matter is difficult to define, and varies from one ore body to the next. Second, the mechanism by which the carbonaceous material adsorbs gold is still being investigated. Third, although it has been known for some time that preg-robbing carbonaceous material can be passivated, or treated so as not to adsorb gold, the mechanism by which this occurs is not fully understood.
  • Preg robbing is counteracted by removing or otherwise treating the organic carbon prior to cyanidation.
  • U.S. Pat. No. 3,639,925 (Scheiner) teaches the pretreatment of the carbonaceous ore by an alkaline hypochlorite.
  • U.S. Pat. No. 4,289,532 (Matson) combines a two stage oxygenation and chlorination pretreatment process.
  • U.S. Pat. No. 4,188,208 (Guay) teaches the introduction of surplus organic carbon to act as a collector for gold, thus diluting the concentration of gold remaining in the carbonaceous ore.
  • the present invention is directed generally to recovery of precious metals from refractory carbonaceous materials.
  • Carbonaceous means carbon-containing and includes any carbon-containing constituent, whether or not preg robbing.
  • a method of recovering precious metals from a carbonaceous precious metal-containing material includes:
  • step (b) during step (a), passing a molecular oxygen-containing gas through reaction chamber to oxidize carbon in the precious metal-containing material and form an oxidized precious metal-containing material;
  • the carbon-containing components of the material are heated to a temperature sufficiently high to combust the component and convert the carbon into a gaseous carbon oxide (whether carbon monoxide or dioxide).
  • the temperature ranges from about 450° C. to about 1,000° C.
  • the reactor can be of any suitable design, with a fluidized bed reactor, a rotary kiln, and a plug flow reactor being more preferred.
  • the microwave energy source comprising one or more individual generating units has a preferred power level in the range of about 1 kw to about 150 kw per generating unit and operates at a preferred frequency ranging from about 300 MHz to about 20 GHz.
  • the reaction chamber preferably has an unloaded Q value ranging from about 1,000 to about 25,000, and the microwave energy delivered to the material preferably ranges from about 250 to about 300,000 Joules/gm.
  • the completion of carbon removal can be determined in many ways.
  • One way is to maintain the material in the reactor for a minimum residence time.
  • Another way is to determine when a temperature of the oxidized precious metal-containing material decreases, typically by at least about 100° C., notwithstanding the continued application of microwave energy to the oxidized precious metal-containing material. When this occurs, most, if not all, of the carbon in the precious metal-containing material has been converted into gaseous carbon oxides. The temperature decrease is a result of removal of the carbon, which is more microwave absorptive than other constituents of the material.
  • microwave energy to effect carbon removal can have substantial benefits over traditional roasters.
  • Traditional roasters require additional fuel to be added to the carbonaceous material since the carbon content, usually of the order of a few percent of the ore mass, would not otherwise be sufficient to sustain autogenous operation (which is the basis of the roaster function).
  • the present invention can offer an alternative to the conventional roaster and differs fundamentally from conventional roasters in that microwave energy is used to supply the combustion energy, thus removing the need for additional fuel.
  • the material After carbon removal, the material is no longer refractory due to preg robbing carbon.
  • the precious metal can therefore be recovered inexpensively by conventional cyanide leaching techniques.
  • each of the expressions “at least one of A, B and C”, “at least one of A, B, or C”, “one or more of A, B, and C”, “one or more of A, B, or C” and “A, B, and/or C” means A alone, B alone, C alone, A and B together, A and C together, B and C together, or A, B and C together.
  • carbonaceous refers to materials containing carbon.
  • Carbonaceous materials include a variety of compounds or minerals, including graphite, carbonates (e.g., calcite, dolomite, siderite, magnesite, aragonite, azurite, and malachite), activated carbon-type material, long-chain hydrocarbons and organic acids, such as humic acid, to name but a few.
  • FIG. 1 is a cross-sectional view of a fluidized fed reactor used in a first embodiment of the present invention
  • FIG. 2 is a cross-sectional view of a rotary kiln reactor used in a second embodiment of the present invention.
  • FIG. 3 is a plug flow microwave reactor used in a third embodiment of the present invention.
  • a fluidized bed reactor includes a tubular reactor chamber or cavity 10 , a bed fluidizer screen 12 , and a pressure chamber 14 .
  • the reactor chamber 10 is connected to a microwave energy source (not shown) via waveguide fittings 16 and 18 , which may include a coupling iris (not shown) or equivalent tuning device (not shown), and a pressurized gas seal 20 .
  • the reactor chamber 10 has a material inlet valve 22 , a material exit valve 24 , gas inlet valve 26 , and a gas exhaust port 28 .
  • Exhaust port 28 is connected to pipe 30 , which is, in turn, connected to a particulate separator 32 (which may be a cyclonic separator). Material collected in the particulate separator may flow through pipe 34 (as shown) to join the material exit valve 24 , depending upon whether the particulate material has been suitably oxidized or otherwise essentially depleted of its carbon.
  • the microwave containment walls of the reactor 10 are preferably constructed of a microwave reflective material.
  • the reaction vessel may optionally include an inner vessel which is constructed of essentially microwave-transparent material.
  • suitable materials include alumina, aluminum silicate, quartz, and low-metal ceramics (which are substantially transparent to microwave energy) and stainless steel, mild steel, nickel alloys, and aluminum alloys (which are reflective of microwave energy).
  • a typical refractory carbonaceous precious metal-containing material includes a variety of materials.
  • Common refractory carbonaceous materials include from about 0.1% to about 5 wt. % carbon-containing materials, from about 0.1% to about 2 wt. % sulfide sulfur, from about 0.1 to about 1 oz/ton gold, and from about 0 to about 2 oz/ton silver.
  • the carbon can be in a variety of forms including graphite, carbonates, activated carbon-type material, long-chain hydrocarbons and organic acids, such as humic acid, to name a few.
  • the material may be in the form of an ore, concentrate, tailings, or combinations thereof.
  • the material be dried before processing the reactor chamber 10 . This is preferably done by heating the material at low temperature and/or exposing the material to sunlight for a prolonged period.
  • the water content of the material is no more than about 10 wt. % and even more preferably no more than about 1 wt. %. Excess water in the material can increase microwave energy requirements.
  • Carbonaceous material to be processed in the reactor chamber 10 is comminuted to a P 80 size of preferably from about 10 mesh to about 50 mesh and introduced through the inlet valve 34 at a material flow rate coinciding with an average residence time in the reactor vessel of from about 30 seconds to about 5 minutes and fluidized by gas 36 , which is supplied from an external source pipe 38 to control valve 40 and the gas inlet valve 26 .
  • the introduction of the gas will cause the material which has been introduced through the inlet valve to form a fluid bed 42 , which is suspended through the adjustment of the gas pressure in the pressure chamber 14 and the bed fluidizer screen 12 .
  • the fluidized bed is then ready for treatment with microwave energy, which is introduced into the reaction chamber via the waveguide fittings.
  • the solid material When the bed is in a fluidized state, the solid material is heated by the dielectric and resistive effects caused by interaction between the electromagnetic field and the solid material constituents.
  • the basic mechanism for microwave heating is a combination of dielectric and ohmic heating, whereby both electrical displacement and conduction currents are used to convert the electromagnetic energy directly into heat within the material. The efficiency of this energy conversion is dependent upon the dielectric properties of the material to be treated.
  • Microwave receptor elements principally carbon, are rapidly heated in a controlled manner. For most refractory carbonaceous materials, carbon has the greatest microwave-absorptive properties compared to that of the other material constituents. Thus, the carbon-containing compounds are preferentially heated.
  • the fluidizing gas is continuously passed through valve 26 and exhausted through port 28 during the treatment process.
  • the exhaust stream is passed through a particulate separator 32 to clean the gas of particulate matter (principally fines blown free from the fluidized bed).
  • the stream is passed through a heat exchanger 44 to preheat the inlet gas and conserve energy.
  • the exhaust stream is then directed to an external bag house and ultimately discharged into the atmosphere.
  • the molecular oxygen is present in an amount that is at least stoichiometric relative to the carbon content of the carbonaceous material and even more preferably in an amount that is at least about 110 to about 200% of the stoichiometric amount, and the molecular oxygen content of the fluidizing gas when introduced into the bottom of the reactor vessel is at least about 20 mole % and even more preferably ranges from about 20 to about 30 mole %.
  • the fluidizing velocity of the gas is preferably sufficient to suspend the material in the chamber.
  • the velocity of the fluidizing gas is maintained to be not less than the minimum fluidization velocity of the largest mineral particle size and not greater than the terminal velocity of the smallest mineral particle size.
  • the region 46 above the suspended fluidized bed 42 is generally essentially free of solid material and consists primarily of fluidizing gas and gaseous reaction products.
  • the gas seal 20 permits the transmission of microwave energy into the reactor chamber 10 while isolating the atmosphere and contents of the chamber from the connecting waveguide via fittings 16 and 18 .
  • the microwave energy heats the carbon-containing materials to a temperature sufficiently high to oxidize the carbon in the carbon-containing materials according to the following reaction: C+O 2 ⁇ CO 2 .
  • the operating temperature of the bed is preferably at least about 450° C., more preferably ranges from about 450° C. to about 1,000° C., even more preferably ranges from about 650° C. to about 850° C., and even more preferably ranges from about 700° C. to about 750° C.
  • the inflow rate of oxygen into the reaction chamber is controlled to provide sufficient molecular oxygen to maintain the reaction and preferably convert at least most, more preferably at least about 90% and even more preferably at least about 99% of the carbon in the material into carbon dioxide.
  • the material outputted via output 24 from the reactor chamber has a preferred maximum carbon content of about 0.2 wt. % and even more preferably of about 0.05 wt. %.
  • Temperature, heating rate, and/or microwave coupling can be controlled in a number of ways. As will be appreciated, dielectric loss factors of the material constituents can be temperature dependent. Accordingly, it is desirable to optimize dynamically the coupling between the magnetron or other microwave generating source and the chamber 10 and the resonant tuning of the chamber 10 . The degree of coupling or matching of the cavity with the magnetron determines the efficiency with which energy is delivered to the chamber 10 . Preferred coupling is as close to unity as possible. In one approach, the power of the microwaves and the time of application of the microwaves are controlled. In another approach, the power of the microwaves is adjusted according to the heating temperature.
  • an aperture size of a variable iris and/or tuner positioned in the waveguide is adjusted in response to the temperature of the bed and/or the power of the reflected microwaves (relative to the microwaves entering the reactor). Coupling is optimized as reflected energy is minimized.
  • the microwave source comprising one or more individual generating units generates power levels in the range of about 1 kw to about 150 kw per generating unit.
  • a preferred power level is from about 80 to about 125 kw.
  • the specific energy delivered to the bed in the chamber 10 ranges from about 250 to about 300,000 Joules/gm or from about 2 to about 20 kW-h/t.
  • the unloaded Q factor in the chamber 10 preferably ranges from about 1,000 to about 25,000, but most preferably is at least about 200,000.
  • the frequency of the microwave source preferably ranges from about 300 MHz to about 30 GHz, with preferred microwave frequencies being within the Industrial, Scientific, and Medical (ISM) bands of about 915 MHz and about 2,450 MHz.
  • ISM Industrial, Scientific, and Medical
  • Process control is normally effected using a variety of instrumentation positioned in the chamber 10 .
  • temperature probes are installed at various positions within the fluidized bed and all feed and discharge lines, including the gas inlet and outlet lines.
  • Gas pressure and product monitors are installed in all gas lines. Material flow through the reactor chamber is measured either through flow meters or by mass measurements.
  • a microwave reflection detector is positioned in the waveguide.
  • Completion of carbon oxidation is normally indicated by a substantial drop in bed temperature even though microwave energy is still being passed through the bed. This is so because the microwave absorptivities of the non-carbonaceous components of the material are substantially less than that of carbon.
  • the oxidized material is removed from the chamber when the bed temperature decreases, even more typically when the bed temperature decreases by at least about 50° C., even more typically by at least about 100° C., and even more typically by at least about 200° C.
  • the residence time of the carbon-containing material in the reactor chamber 10 preferably is no more than about 15 minutes and even more preferably ranges from about 2 to about 4 minutes, though the precise residence time depends on the power of the microwave source and the nature of the other constituents of the material.
  • the oxidized material is removed from the reactor and subjected to further processing to recover gold.
  • the oxidized material is further comminuted, slurried, and subjected to cyanide leaching in a suitable vessel by known techniques.
  • the oxidized material is agglomerated onto itself or coated onto an inert substrate and subjected to cyanide heap leaching by known techniques.
  • a rotary kiln in a second embodiment, is used.
  • the kiln includes a reactor vessel having an interior reaction chamber.
  • the chamber is a rotating, inclined metallic cylinder 50 into which microwave energy is introduced via a waveguide conduit 52 and carbonaceous material in hopper 54 is introduced via a chute 56 .
  • Both the microwave energy and carbonaceous material enter the reactor vessel through an appropriate rotary joint 58 .
  • This joint is also fitted to allow the introduction of a molecular oxygen-containing gas stream, usually in the form of atmospheric air, into the reaction chamber of the vessel.
  • the material once in the vessel, is elevated up the incline by means of lifting vanes 60 fixed to the interior vessel wall and acting as a screw elevator.
  • the material is mixed with molecular oxygen (air) and simultaneously and continuously exposed to microwave energy.
  • the material is ultimately ejected through the exhaust port 62 , which is also fitted with an appropriate gas exhaust system 64 which collects the exhaust gas products and directs them for cleaning and discharge.
  • the discharged ore 66 is collected for cyanidation leaching or other appropriate metal recovery processes.
  • a motor or suitable driving device 68 provides the rotary motion to the reactor vessel.
  • a plug flow vessel may be used as shown in FIG. 3 in which a dielectric tube 80 forms the reaction vessel into which carbonaceous material is introduced through a chute.
  • An oxidizing gas is passed through the reactor vessel either in the same direction as the ore material being processed or in a countercurrent direction.
  • the direction of flow of the oxidizing gas is opposed to the primary direction of flow of the microwave power.
  • the material either partially or completely fills the vessel, travels through the tube either under the force of gravity or by means of an appropriate screw feed mechanism, and is discharged into a discharge hopper 92 .
  • the discharged oxidized material is subjected to subsequent treatment for metal recovery by means of cyanidation or other processes.
  • the rate at which the material passes through the tube is controlled by a damper plate 84 , which acts as a valve to regulate the flow.
  • a gas containing molecular oxygen usually in the form of atmospheric air, is introduced by means of an appropriate fixture 86 and perforations 88 in the vessel and exhausts via another fixture 90 . The exhausted gas is directed to appropriate cleaning equipment and discharged to the atmosphere.
  • Interaction between the material and microwave energy is accomplished by mounting the reactor vessel 80 within a waveguide conduit apparatus 94 .
  • Microwave energy is transmitted through the waveguide and passes through the dielectric vessel material, such that substantially all of the microwave energy is absorbed within the material passing through the vessel.
  • the carbon is preferentially heated by the microwave energy.
  • the carbonaceous material is first loaded into a reaction chamber where the ore is mixed with molecular oxygen, which is generally atmospheric air. Next, microwave energy is applied. The microwave energy raises the air-material mixture to the preferred operating temperature in the range of about 700-750° C., at which temperature the reaction takes place as C+O 2 ⁇ CO 2 .
  • This chemical reaction is exothermic and, depending upon the quantity of carbon present, contributes heat energy to the process.
  • the microwave energy is thus required to make up the balance of energy required for the reaction to proceed.
  • the use of microwave energy is advantageous since the carbon acts to preferentially convert the microwave energy into heat within the mineral.
  • the treatment process is operated in a continuous manner and the material flowrate through the reactor vessel is controlled such that the ore being discharged from the reactor is depleted of carbon to any desired extent, the material so discharged being continuously monitored for carbon content.
  • Dominant mineralization quartz, dolomite, calcite Dominant mineralization quartz, dolomite, calcite.
  • the material was sized to >10 mesh (Tyler) to minimize blow through of fine material in the reactor.
  • the test material was separated into two lots and both lots were processed identically.
  • the material was batch heated in the reactor to an indicated temperature of from about 660°-700° C.
  • the completion of the reaction was indicated by a temperature reduction to about 350-400° C., corresponding to the depletion of carbon and the resultant lower microwave absorptive properties of the remaining calcine material.
  • the calcine material was ground to 100% minus 200 mesh and leached in sodium cyanide for up to 48 hours and the gold in solution was measured.
  • the carbon content was measured to be 0.09% by weight.
  • the material was sized to between about 10 and 50 mesh (Tyler).
  • the test material was separated into two lots and both lots were processed identically.
  • the material was batch heated in the reactor to an indicated temperature of approximately 700° C.
  • the completion of the reaction was indicated by a temperature reduction to about 500° C., corresponding to the depletion of carbon and the resultant lower microwave absorptive properties of the remaining calcine material.
  • the calcine was ground to 100% minus 200 mesh and leached in sodium cyanide for up to 48 hours and the gold and silver in solution were measured.
  • the carbon content was measured to be 0.14% by weight.
  • test material was finely ground as conventional roaster feedstock. Each test was operated as a continuous operation in which the reactor charge of approximately 55 lbs of test material was initially heated to reaction temperature. Upon reaching operating temperature, fresh feed was introduced while calcined product was recovered from the calcine discharge and cyclone underflow. All of the samples used for gold recovery were obtained while the reactor was operating in continuous steady state condition. Operating temperatures throughout the test series ranged from 470-660° C.
  • Cyanide soluble gold recoveries from processed materials over all tests ranged from 85.8-96.0%. For the best test, conducted at an operating temperature of between 480-550° C., the average cyanide soluble gold recovery was 92.9% for the calcine discharge material and 88.3% for the cyclone underflow material.
  • microwave process is effective at indicated temperatures, which are substantially lower than the known reaction temperature of the oxidation of carbon, being above approximately 600° C. This is indicative of the selective absorption and heating properties of carbon whereby the total bulk (ore) temperature is not required to reach reaction temperatures in order for the localized carbon temperatures to reach the necessary levels. This feature leads to potential economic savings through more efficient energy utilization.
  • microwave process is effective without the addition of combustible fuels to sustain operating temperatures and that, in fact, the microwave process continues to be effective at all values of carbon content until the organic carbon is totally depleted.
  • the process is used to recover other metals the recovery of which is complicated by the presence of carbon in the metal-containing material.
  • the present invention in various embodiments, includes components, methods, processes, systems and/or apparatus substantially as depicted and described herein, including various embodiments, subcombinations, and subsets thereof. Those of skill in the art will understand how to make and use the present invention after understanding the present disclosure.
  • the present invention in various embodiments, includes providing devices and processes in the absence of items not depicted and/or described herein or in various embodiments hereof, including in the absence of such items as may have been used in previous devices or processes, e.g., for improving performance, achieving ease and ⁇ or reducing cost of implementation.

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US20080069746A1 (en) * 2006-09-20 2008-03-20 Hw Advanced Technologies, Inc. Method and apparatus for microwave induced pyrolysis of arsenical ores and ore concentrates
US20080118421A1 (en) * 2006-09-20 2008-05-22 Hw Advanced Technologies, Inc. Method and means for using microwave energy to oxidize sulfidic copper ore into a prescribed oxide-sulfate product
WO2012135826A1 (fr) * 2011-04-01 2012-10-04 Flsmidth A/S Système et procédé de récupération continue de métaux
CN102758079A (zh) * 2012-07-25 2012-10-31 福建省双旗山矿业有限责任公司 一种对含硫金矿物进行微波焙烧和非氰浸金的节能优化工艺
WO2014105944A1 (fr) * 2012-12-28 2014-07-03 Flsmidth A/S Utilisation d'enzymes pour la récupération d'un métal à partir d'un minerai contenant un métal
CN103937964A (zh) * 2014-04-28 2014-07-23 南华大学 一种新的含金硫砷精矿微波焙烧提金方法
WO2023034590A1 (fr) * 2021-09-02 2023-03-09 Nevada Gold Mines LLC Procédé d'oxydation sous pression à haute température à étapes multiples pour des matières contenant un métal précieux réfractaire double

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PL440757A1 (pl) * 2022-03-25 2023-10-02 Akademia Górniczo-Hutnicza im. Stanisława Staszica w Krakowie Sposób odzysku Pt, Pd, Rh, Au z silnie rozcieńczonych roztworów wodnych i układ do odzysku Pt, Pd, Rh, Au z silnie rozcieńczonych roztworów wodnych

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US20080069746A1 (en) * 2006-09-20 2008-03-20 Hw Advanced Technologies, Inc. Method and apparatus for microwave induced pyrolysis of arsenical ores and ore concentrates
US20080118421A1 (en) * 2006-09-20 2008-05-22 Hw Advanced Technologies, Inc. Method and means for using microwave energy to oxidize sulfidic copper ore into a prescribed oxide-sulfate product
WO2012135826A1 (fr) * 2011-04-01 2012-10-04 Flsmidth A/S Système et procédé de récupération continue de métaux
CN102758079A (zh) * 2012-07-25 2012-10-31 福建省双旗山矿业有限责任公司 一种对含硫金矿物进行微波焙烧和非氰浸金的节能优化工艺
WO2014105944A1 (fr) * 2012-12-28 2014-07-03 Flsmidth A/S Utilisation d'enzymes pour la récupération d'un métal à partir d'un minerai contenant un métal
CN103937964A (zh) * 2014-04-28 2014-07-23 南华大学 一种新的含金硫砷精矿微波焙烧提金方法
WO2023034590A1 (fr) * 2021-09-02 2023-03-09 Nevada Gold Mines LLC Procédé d'oxydation sous pression à haute température à étapes multiples pour des matières contenant un métal précieux réfractaire double
US12378631B2 (en) 2021-09-02 2025-08-05 Nevada Gold Mines LLC Multi-staged high temperature pressure oxidation process for double refractory precious metal-containing materials

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