[go: up one dir, main page]

WO2025102113A1 - Procédé de production d'un concentré - Google Patents

Procédé de production d'un concentré Download PDF

Info

Publication number
WO2025102113A1
WO2025102113A1 PCT/AU2024/051206 AU2024051206W WO2025102113A1 WO 2025102113 A1 WO2025102113 A1 WO 2025102113A1 AU 2024051206 W AU2024051206 W AU 2024051206W WO 2025102113 A1 WO2025102113 A1 WO 2025102113A1
Authority
WO
WIPO (PCT)
Prior art keywords
metal
concentrate
leach
flotation
feed material
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/AU2024/051206
Other languages
English (en)
Inventor
Glen Peter O’MALLEY
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mining and Process Solutions Pty Ltd
Original Assignee
Mining and Process Solutions Pty Ltd
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
Priority claimed from AU2023903681A external-priority patent/AU2023903681A0/en
Application filed by Mining and Process Solutions Pty Ltd filed Critical Mining and Process Solutions Pty Ltd
Publication of WO2025102113A1 publication Critical patent/WO2025102113A1/fr
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

Links

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
    • C22B11/04—Obtaining noble metals by wet processes
    • C22B11/042—Recovery of noble metals from waste materials
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/02—Froth-flotation processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/08—Subsequent treatment of concentrated product
    • B03D1/082—Subsequent treatment of concentrated product of the froth product, e.g. washing
    • 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
    • C22B1/005—Preliminary treatment of 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
    • C22B11/00—Obtaining noble metals
    • C22B11/04—Obtaining noble metals by wet 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
    • C22B15/00—Obtaining copper
    • C22B15/0063—Hydrometallurgy
    • C22B15/0065—Leaching or slurrying
    • C22B15/0067—Leaching or slurrying with acids or salts thereof
    • C22B15/0073—Leaching or slurrying with acids or salts thereof containing nitrogen
    • 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
    • C22B3/16—Extraction of metal compounds from ores or concentrates by wet processes by leaching in organic solutions
    • C22B3/1608—Leaching with acyclic or carbocyclic agents
    • C22B3/1616—Leaching with acyclic or carbocyclic agents of a single type
    • C22B3/165—Leaching with acyclic or carbocyclic agents of a single type with organic acids
    • 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
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/005—Separation by a physical processing technique only, e.g. by mechanical breaking
    • 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
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/006—Wet 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
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/006—Wet processes
    • C22B7/008—Wet processes by an alkaline or ammoniacal leaching
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D2203/00—Specified materials treated by the flotation agents; Specified applications
    • B03D2203/02—Ores
    • B03D2203/025—Precious metal ores
    • 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
    • C22B13/00—Obtaining lead
    • C22B13/04—Obtaining lead by wet 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
    • C22B17/00—Obtaining cadmium
    • C22B17/04—Obtaining cadmium by wet 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
    • C22B19/00—Obtaining zinc or zinc oxide
    • C22B19/20—Obtaining zinc otherwise than by distilling
    • 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
    • C22B19/00—Obtaining zinc or zinc oxide
    • C22B19/20—Obtaining zinc otherwise than by distilling
    • C22B19/22—Obtaining zinc otherwise than by distilling with leaching with acids
    • 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
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0407—Leaching processes
    • C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts 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

  • a process for the production of a concentrate.
  • the process may be used in the production of a metal concentrate from ores, ore concentrates or tailings, or from other metal containing materials including jewellery, electronic scrap, and other scrap materials.
  • a metal extraction method that includes the process for the production of a metal concentrate.
  • the metal extraction method is particularly applicable to the recovery of precious metals and/or base metals from an ore material (including an ore concentrate) and discussion will therefore focus on such metals. However, it is to be understood that the process is not limited to such recovery.
  • the recovery of metal values from ore minerals generally includes a number of common unit operations including comminution (crushing and grinding), separation of ore from gangue (e,g by gravity and flotation), metal extraction (e,g leaching) and metal recovery (e,g SX, IX, precipitation, activated carbon, EW).
  • Leaching is a method where the feed material (such as ore, concentrate or tailings) is contacted with an aqueous solution containing a lixiviant to solubilise a target metal into the solution phase.
  • Flotation is a method of separating the target metal rich component (such as ore minerals) from the target metal poor component (such as gangue) of a ground ore or ore concentrate by exploiting respective differences in hydrophobicity of the two components.
  • the difference in hydrophobicity is enhanced by using a collector.
  • the collector In the case of flotation of sulphide ores, the collector is typically a xanthate.
  • An aqueous slurry of the particles treated with the collector is aerated in flotation cells to produce bubbles. The hydrophobic particles attach to the air bubbles and are then skimmed off the top or overflow into a launder to produce a concentrate of the metal values.
  • a concentrate fraction that comprises metal sulphide minerals (e.g., pyrite, chalcocite, covellite, chalcopyrite, bornite, millerite, pentlandite, sphalerite, cattierite, linnaeite, galena or sphalerite) and a tailings fraction.
  • metal sulphide minerals e.g., pyrite, chalcocite, covellite, chalcopyrite, bornite, millerite, pentlandite, sphalerite, cattierite, linnaeite, galena or sphalerite
  • the precious metals mostly (around 50 to 90%, depending on mineralogy) report to the concentrate fraction, with the remainder reporting to the tailings fraction.
  • the tailings fraction may be subjected to a cyanide leach to recover the remaining precious metals.
  • a process for producing a concentrate from a feed material containing a first metal-containing phase and a second metal-containing phase said process including:
  • a metal phase which may be desirable, such as a precious metal or undesirable, such as an impurity phase
  • a metal phase which may be desirable, such as a precious metal or undesirable, such as an impurity phase
  • Reversal of the leaching and flotation steps is facilitated by using a leaching solution that includes an amino acid lixiviant, which may be in the presence of a leach enhancer, to treat the feed material.
  • an amino acid lixiviant allows enhanced extraction of precious metals without the prior problems associated with using cyanide as the primary lixiviant discussed above.
  • amino acids lixiviants are generally more environmentally and/or cost-wise advantageous as compared with other lixiviants such as thiosulfate, thiourea, halides and mercury.
  • the sulfide source may comprise a hydrosulfide (e,g NaHS).
  • an amino acid lixiviant has the additional surprising advantage that the effectiveness of a subsequent flotation step is enhanced.
  • amino acid retained in the leach residue ("ripios") produced in step (i) enhances the adsorption of a collector on ore particles and improves the floatability of ore minerals in step (ii).
  • the first metal containing fraction is more efficiently separated from gangue during the flotation step. This further improves the purity of the final first metal containing concentrate.
  • the feed material may comprise an ore, an ore concentrate, a process by-product or a waste product such as a flotation tailings fraction.
  • the feed material may also or instead comprise other metal containing materials including jewellery, electronic scrap, and other scrap materials.
  • the feed material may include one or more sulfides of the first metal.
  • the first metal may comprise a chalcophile metal (as defined herein) and discussion herein will accordingly focus on chalcophile metals- although it is to be understood that the process is not limited to such metals.
  • the feed material may include one or more metal sulfides selected from pyrite, chalcocite, covellite, chalcopyrite, bornite, millerite, pentlandite, sphalerite, cattierite, linnaeite, galena or sphalerite.
  • the first metal may instead or additionally be present as a native metal.
  • the term "native metal” means a metal that is present in the feed material in its elemental form either as an alloy or in its pure form.
  • the second metal containing phase may comprise a metal value, such as precious metal (e,g gold silver and/or PGMs).
  • the second metal containing phase may comprise an impurity phase such as a metal oxide.
  • the metal oxide may be an oxide of the first metal, for example, a chalcophile metal oxide.
  • An example of a chalcophile metal oxide is a copper oxide such as malachite.
  • the chalcophile metal oxide may be a secondary mineral phase produced by the oxidation or weathering of the primary sulfide mineral. The presence of such impurity phases in the feed material can be problematic in conventional flotation processes as they do not report to the concentrate fraction during flotation and therefore may end up in tailings, resulting in reduced recovery of the chalcophile metals.
  • lixiviant refers to a specific active chemical of a leaching solution that complexes with and enables the extraction or dissolution of target elements from a feed material (e.g., ore).
  • a “primary lixiviant” is the primary (or main) active chemical in the leaching solution that complexes with and enables the extraction or dissolution of target elements from the feed material. Accordingly, the “primary lixiviant” may mean (i) the sole lixiviant present in a leaching solution, or (ii) in the case of a leaching solution containing more than one lixiviant, the lixiviant that is present in solution in the highest concentration.
  • the primary lixiviant comprises an amino acid, or derivative thereof, such as an amino acid salt.
  • amino acid means an organic compound containing both a carboxyl (- COOH) and an amino (-NH 2 ) functional group.
  • the amino acid contains a -CHR or CH 2 group.
  • the amino (-N H 2 ) group and the carboxyl (-COOH) group connects to the same - CHR or -CH 2 connecting group and are referred to as primary alpha-amino-acids.
  • the "R” group in the -CHR connecting group can take on any organic structure, such as aliphatic hydrocarbon groups to complex organic structures including aromatic groups, heterocyclic groups, and poly-nuclear groups or various other organic groups.
  • the R-group is only hydrogen, in which case the molecule reverts to the simplest primary alpha-amino-acid, called glycine.
  • amino acid salt includes an alkali metal salt, for example, a sodium or potassium glycinate.
  • the amino acid salt may be an alkaline earth salt (for example its calcium salt).
  • the alkaline solution may additionally include a leach enhancer which may enhance the leaching function of the amino acid or its derivative and/or may reduce the temperature requirements for the leaching process.
  • a leach enhancer refers to an aqueous species that facilitates the function of the lixiviant to enhance the leaching process.
  • the leach enhancer may have a catalyst function on the extraction.
  • the primary lixiviant is still the amino acid or its derivative or salt.
  • the leach enhancer may comprise one or more of the following species: iodine and/or iodide mixtures, bromine and/or bromide mixtures, ammonia, thiourea, copper salts, and cyanide in its various salts, or mixtures of these species.
  • the leach enhancer comprises a cyanide salt (such as sodium cyanide).
  • the leach enhancer is the sparsely soluble copper glycinate (Cu(Gly) 2 ) which catalyses the leaching of the feed material.
  • the leach enhancer may particularly increase the rate of leaching of precious metals, as well as chalcophile base metals from the feed material.
  • the leach enhancer may be present in solution at a concentration of 2 molar or less. In an embodiment, the leach enhancer has a concentration of 1.5 molar or less. In another embodiment, the leach enhancer has a concentration of 1 molar or less. In an embodiment, the leach enhancer has a concentration of 0.5 molar or less.
  • the leach enhancer has a minimum concentration of 1.5 molar or less. In another embodiment, the leach enhancer has a minimum concentration of 0.1 molar. In another embodiment, the leach enhancer has a minimum concentration of 0.2 molar. In another embodiment, the leach enhancer has a minimum concentration of 0.3 molar.
  • the step of contacting the material with an alkaline solution containing a lixiviant comprising an amino acid may comprise the selective leaching process disclosed in WO 2016/141438 Al, the entire disclosure of which is incorporated herein by reference.
  • a material containing at least one Chalcophile Group Element (“CPM”) as herein defined and one or more non Chalcophile Group Elements (“NCE”) as herein defined is contacted with an alkaline solution containing a lixiviant comprising an amino acid or derivative thereof in order to selectively leach the CPM from the material to produce a CPM containing leachate and a NCE containing residue.
  • CPM is then recovered from the leachate such as by using conventional methods familiar with those skilled in the art.
  • the CPMs comprise: Co, Ni, Cu, Zn, Ga, Ge, Rh, Pd, Ag, Cd, In, Sn, Ir, Pt, Au, Hg, Tl, Pb and Bi.
  • the CPMs may comprise: Co, Ni, Zn, Ga, Ge, Rh, Pd, Ag, Cd, In, Sn, Ir, Pt, Hg, Tl, Pb and Bi.
  • the CPMs may comprise: Co, Ni, Zn, Ga, Ge, Rh, Pd, Cd, In, Sn, Ir, Pt, Hg, Tl, Pb and Bi.
  • the CPMs may comprise Co, Ni, Zn, Ga, Ge, Cd, In, Sn, Hg, Tl, Pb, Bi.
  • the CPMs may exclude Pb.
  • the NCEs comprise all elements that are not members of the CPMs.
  • the weight ratio of amino acid to the leach enhancer in solution during contact with the feed material is greater than 2:1 (conversely, the leach enhancer preferably does not make up more than 33 weight% of the combined mass of amino acid and leach enhancer).
  • the weight ratio of amino acid to the leach enhancer may be greater than 3:1. However, typically the ratio of amino acid (e.g. glycine) to the leach enhancer is higher, such as a minimum of 10:1. In an embodiment, the minimum weight ratio of amino acid to leach enhancer is 100:1.
  • the weight ratio may be as high as 1000:1, particularly where high ratios of CPM base metals (e.g. Ni, Cu, Co, Zn, Pb) to CPM precious 30 metals (Au, Ag Pt, Pd, Rh, Ir) are present.
  • the amino acid concentration in solution may vary from 0.1 to 240 grams per litre.
  • the amino acid concentration may be a minimum of 3.75 grams per litre and in an embodiment may be a minimum of 16 grams per litre.
  • the maximum amino acid concentration may be 60 grams per litre and in another embodiment, the amino acid concentration is a maximum of 37.8 grams per litre.
  • the leaching step (i) is conducted under alkaline conditions.
  • the leaching step is conducted using a moderately alkaline solution having a pH above 7.
  • the pH is at least 8.
  • the pH is at least 8.5.
  • the pH is at least 9.
  • the pH is at least 9.5.
  • the pH is at least 9.5.
  • the pH is at least 10.
  • the pH is a maximum of 13.
  • the pH range is a maximum of 11.5.
  • the pH is a maximum of 10.
  • the chalcophile metal containing leach residue is subjected to flotation to produce a chalcophile metal concentrate and a tailings fraction.
  • the leach residue contains one component that is rich in a target metal and another component that is poor in the target metal.
  • the component that is rich in a target metal may largely comprise metal sulfides and the component that is poor in the target metal may largely comprise gangue minerals.
  • the flotation step may comprise forming an aqueous slurry of particles of the leach residue which is treated with a collector (such as a xanthate) and aerated in flotation cells to produce bubbles.
  • a collector such as a xanthate
  • the flotation step may include treatment of the leach residue in a rougher- scavenger cell and/or a cleaner cell and/or a cleaner- scavenger cell.
  • the process flowsheet for producing the concentrate may include multiple steps that include at least one step of leaching a feed material followed by a step of flotation of the leach residue. These steps may occur at any suitable point in the flowsheet.
  • the feed material for step (i) comprises comminuted run of mine ore.
  • the feed material for step (i) comprises an ore concentrate produced from a separation step, such as by gravity separation or flotation.
  • the feed material for step (i) comprises a rougher- scavenger concentrate.
  • the rougher-scavenger concentrate may be the product of flotation of ground run of mine ore.
  • the leach residue from step (ii) is subjected to flotation in a cleaner cell and/or a cleaner- scavenger cell.
  • the leach reside may undergo grinding prior to flotation in step (ii).
  • the process of the present disclosure may include one or more of the following additional steps: 1) subjecting the chalcophile metal concentrate produced in step (ii) to a further leaching step to produce a further leachate containing the second metal (and optionally the chalcophile metal) and a further leach residue containing the chalcophile metal.
  • the further leach residue may be subjected to a further flotation step to produce a further chalcophile metal concentrate and a further tailings fraction.
  • a process for producing a concentrate of a target metal from a feed material containing one component that is relatively rich in the target metal and another component that is relatively poor in the target metal, the feed material having been leached with an alkaline solution containing a lixiviant comprising an amino acid wherein the process includes:
  • Step (i) may comprise processing the leached feed material in a flotation circuit.
  • Step (i) may comprise subjecting an aqueous slurry of the feed material to flotation whilst being aerated in order to produce the metal concentrate fraction and the tailings fraction
  • a process for recovering a first metal from a feed material containing said first metal containing phase and a second metal containing phase including:
  • the metal/s may be recovered by one or more methods including solvent extraction (SX), ion exchange (IX), precipitation, adsorption, electrowinning, etc.
  • SX solvent extraction
  • IX ion exchange
  • precipitation precipitation
  • adsorption adsorption
  • electrowinning electrowinning
  • the adsorbent may advantageously be activated carbon which is inexpensive and often readily available.
  • the adsorbent may be an ion-exchange resin.
  • the ion-exchange resin may comprise an insoluble polymer matrix containing a backbone of cross-linked styrene or methacrylic acid polymers that are cross-linked with divinylbenzene containing side chains of ion-active functional groups to exchange anions or cations from solution. These "functional groups" contain either positively- charged ions (to absorb cations) or negatively-charged ions (to absorb anions).
  • the two most common commercial resins are made of polystyrene sulfonate, followed by polyacrylate.
  • Figure 1 is a flowsheet of a conventional (prior art) process for production of a copper concentrate and precious metals from a copper-precious metal ore.
  • Figure 2 is a flowsheet of a first embodiment of a process for production of a copper concentrate.
  • Figure 3 is a flowsheet of a second embodiment of a process for production of a copper concentrate.
  • Figure 4 is a flowsheet of a conventional (prior art) process for recovery of precious metals from an ore material containing iron sulfides, precious metal, and a relatively low concentration of copper sulfides (typically less than 0.1% copper).
  • Figure 5 is a flowsheet of a conventional (prior art) process for recovering precious metal from an ore material containing iron sulfides, precious metal, and a relatively high concentration of copper sulfides (typically contain greater than 0.1% copper).
  • Figure 6 is a third embodiment of the present process and is a modification of the flowsheet shown in Figure 4.
  • Figure 7 is a fourth embodiment of the present process and is a modification of the flowsheet shown in Figure 5.
  • Figures 1, 4 and 5 are flowsheets of conventional (prior art) processes whereas Figures 2, 3, 6 and 7 are flowsheets showing embodiments of the present disclosed process.
  • Each of Figures 2, 3, 5 and 7 includes multiple steps in the flowsheets and these multiple steps include at least one leach step that produces a leach residue followed by a flotation step on the leach residue. Accordingly, the leach step followed by the flotation step on the leach residue can be conducted at any suitable point in the flowsheet.
  • Figure 1 shows a flowsheet (10) of a conventional (prior art) process for production of a copper concentrate and precious metals from a copper-precious metal ore.
  • the ore (12) is comminuted in crushing (14) and grinding (16) stages, then undergoes gravity separation (18).
  • the concentrate (20) from the gravity separation is processed in an elution and electrowinning step (22) and then in pyrometallurgy step to produce dore (a semi-pure alloy of gold and silver) (24).
  • the gravity tails (26) undergo flotation in rougher- scavenger cells (28) and the flotation concentrate (30) is subjected to further grinding and gravity separation (32).
  • Tails (34) from the further gravity separation step undergo flotation in cleaner (36) and cleaner-scavenger (38) cells to produce the final copper concentrate (40).
  • Flotation tails (42) from the cleaner-scavenger flotation are then treated with a cyanide carbon in leach (CIL) leach (44) to extract gold which is recovered onto activated carbon and then recovered in the elution and electrowinning step (22).
  • CIL cyanide carbon in leach
  • FIG. 2 shows a flowsheet of a first embodiment of a process (110) for production of a copper concentrate (140) and dore (124) from a copper-precious metal ore (112).
  • the flotation concentrate (130) from the rougher- scavenger cells (128) comprises feed material to a leaching stage (146).
  • the flotation concentrate (130) is leached with an alkaline aqueous solution containing a lixiviant comprising an amino acid (glycine) and a leach enhancer comprising cyanide.
  • the leach (146) is conducted as a carbon-in-leach (CIL) process in which precious metal extracted from the concentrate (130) is adsorbed onto activated carbon particles within the leach solution. The extracted precious metal is then recovered in the elution and electrowinning step (122) to produce dore (124).
  • the leach residue (148) is subjected to further grinding and gravity separation (132). Tails (134) from the further gravity separation step undergo flotation in cleaner (136) and cleanerscavenger (138) cells to produce the final copper concentrate (140).
  • Flotation tails (142) from the cleaner-scavenger flotation (138) are then subjected to a second leaching stage (150) in which the flotation tails (142) are leached with an alkaline aqueous solution containing a lixiviant comprising an amino acid (e,g glycine) and a leach enhancer comprising cyanide.
  • the leach (150) is also conducted as a carbon in leach (CIL) process in which precious metal extracted from the concentrate (130) is adsorbed onto carbon particles and the extracted precious metal is then recovered in the elution step (122) to produce dore (124).
  • CIL carbon in leach
  • Figure 3 shows a flowsheet of a second embodiment of a process (210) for production of a copper concentrate (240) and dore (224) from a copper-precious metal ore (212).
  • the concentrate (220) from the gravity separation (218) is processed in an elution step (222) to produce dore (224).
  • the gravity tails (226) comprise feed material to a leaching stage (246).
  • the gravity tails (226) are leached with an alkaline aqueous solution containing a lixiviant comprising an amino acid (glycine) and a leach enhancer comprising cyanide.
  • the leach (246) is also conducted as a carbon-in-leach (CIL) process in which precious metal extracted from the gravity tails (226) is adsorbed onto carbon particles within the leach solution. The extracted precious metal is then recovered in the elution step (222) to produce dore (224).
  • the leach residue (248) is subjected to flotation in rougher- scavenger cells (228).
  • the flotation concentrate (230) is subjected to further grinding and gravity separation (232). Tails (234) from the further gravity separation step undergo flotation in cleaner (236) and cleaner-scavenger (238) cells.
  • Flotation tails (242) from the cleaner-scavenger flotation (238) are then subjected to a second leaching stage (250) in which the flotation tails (242) are leached with an alkaline aqueous solution containing a lixiviant comprising an amino acid (glycine) and a leach enhancer comprising cyanide.
  • a second leaching stage 250 in which the flotation tails (242) are leached with an alkaline aqueous solution containing a lixiviant comprising an amino acid (glycine) and a leach enhancer comprising cyanide.
  • the leach (250) is also conducted as a CIL process in which precious metal extracted from the flotation tails (242) is adsorbed onto carbon particles and the extracted precious metal is then recovered in the elution step (222) to produce dore (224).
  • Figure 4 is a flowsheet of a conventional process for recovering precious metal from an ore material containing iron sulfides (e,g pyrite and possibly pyrrhotite), precious metal and a relatively low concentration of copper sulfides (e,g chalcopyrite and possibly chalcocite, bornite, etc).
  • the ore material (312) would typically contain less than 0.1% copper. Again, similar reference numerals refer to similar features.
  • the ore (312) is comminuted in crushing (314) and grinding (316) stages, then undergoes gravity separation (318).
  • the concentrate (320) from the gravity separation is processed in an elution and electrowinning step (322) to produce dore (a semi-pure alloy of gold and silver) (324).
  • the gravity tails (326) undergo flotation in rougher- scavenger cells (328) and the flotation concentrate (330) is subjected to ultrafine grinding (332).
  • the ground concentrate is then subjected to an intensive cyanide leach (336).
  • Tails from both the intensive cyanide leach (336) and from the flotation stage (328) undergo further cyanide leaching (344).
  • the leachate is processed in the elution and electrowinning step (322).
  • Figure 5 is a flowsheet of a conventional process for recovering precious metal from an ore material containing iron sulfides (e,g pyrite and possibly pyrrhotite), precious metal and a relatively high concentration of copper sulfides (e,g chalcopyrite and possibly chalcocite, bornite, etc).
  • the ore material (412) would typically contain greater than 0.1% copper. Again, similar reference numerals refer to similar features.
  • the ore (412) is comminuted in crushing (414) and grinding (416) stages, then undergoes gravity separation (418).
  • the concentrate (420) from the gravity separation is processed in an elution and electrowinning step (422) to produce dore (a semi-pure alloy of gold and silver) (424).
  • the ground concentrate is then subjected to an intensive cyanide leach (436) followed by counter current decantation (440).
  • the CCD leachate is then subjected to a Merrill Crowe process stage (430) to precipitate precious metal from solution by zinc cementation which is then recovered in the elution stage (422).
  • the copper is recovered as copper product (450) and recovered cyanide (434) is recycled to the intensive cyanide leaching step (436).
  • FIG. 6 is a third embodiment of the present process and is a modification of the flowsheet shown in Figure 4. Similar reference numerals relate to similar features and discussion of the third embodiment will therefore focus on the differences between it and Figure 4.
  • the flotation concentrate (530) is subjected to ultrafine grinding (532).
  • the ground concentrate is then leached (536) with an alkaline aqueous solution containing a lixiviant comprising an amino acid (glycine) and a leach enhancer comprising cyanide (referred to herein as "GlyCatTM").
  • GlyCatTM an alkaline aqueous solution containing a lixiviant comprising an amino acid (glycine) and a leach enhancer comprising cyanide
  • the leachate from the leach step (544) is processed in the elution and electrowinning step (522), while the leach residue is subjected to flotation in cleaner cells (554).
  • a sulfide source (552), such as NaHS, is added to the flotation slurry to precipitate out any copper metals co-leached with the precious metals and the precipitated copper sulfides report to the flotation concentrate which is recovered as copper concentrate (550).
  • Figure 7 is a fourth embodiment of the present process and is a modification of the flowsheet shown in Figure 5. Similar reference numerals relate to similar features and discussion of the fourth embodiment will therefore focus on the differences between it and Figure 5.
  • the ground concentrate from the ultrafine grinding (632) step is then subjected to a GlyCatTM leach (636) followed by counter current decantation (640).
  • the CCD leachate is then subjected to a Merrill Crowe process stage (630) to precipitate precious metal from solution by zinc cementation which is then recovered in the elution stage (622). Because there is no intensive cyanide leach step (as in Figure 5), there is no requirement for a subsequent SART step to manage and recycle cyanide, leading to considerable cost savings.
  • the CCD tails are treated in a second GlyCatTM leach step (644) and the leachate therefrom is treated in the elution and electrowinning step (622) to produce dore.
  • the leach tails are subjected to flotation in cleaner cells (654).
  • a sulfide source (652), such as NaHS, is added to the flotation slurry to precipitate out copper metals co-leached with the precious metals and the precipitated copper sulfides report to the flotation concentrate which is recovered as copper concentrate (650).

Landscapes

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

Abstract

L'invention concerne un procédé de production d'un concentré à partir d'un matériau d'alimentation contenant une première phase contenant du métal et une seconde phase contenant du métal. Le procédé consiste à mettre en contact le matériau d'alimentation avec une solution alcaline contenant un lixiviant qui comporte un acide aminé, ou un dérivé de celui-ci, et à former un lixiviat contenant le second métal (et éventuellement le premier métal) et un résidu de lixiviation contenant le premier métal. Le procédé consiste également à soumettre le résidu de lixiviation à une flottation et à produire un premier concentré métallique et une fraction de rejets.
PCT/AU2024/051206 2023-11-15 2024-11-14 Procédé de production d'un concentré Pending WO2025102113A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2023903681 2023-11-15
AU2023903681A AU2023903681A0 (en) 2023-11-15 Process for producing a concentrate

Publications (1)

Publication Number Publication Date
WO2025102113A1 true WO2025102113A1 (fr) 2025-05-22

Family

ID=95741767

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/AU2024/051206 Pending WO2025102113A1 (fr) 2023-11-15 2024-11-14 Procédé de production d'un concentré

Country Status (1)

Country Link
WO (1) WO2025102113A1 (fr)

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016141438A1 (fr) * 2015-03-11 2016-09-15 Curtin University Of Technology Procédé pour la récupération sélective d'éléments du groupe des chalcophiles
WO2018234880A1 (fr) * 2017-06-23 2018-12-27 Anglo American Services (Uk) Ltd Enrichissement de métaux de valeur à partir de minerais à l'aide d'un procédé de lixiviation en tas
WO2019243635A1 (fr) * 2018-06-22 2019-12-26 Bernd Kunze Procédé de récupération de métaux nobles à partir de catalyseurs usagés
CN116926336A (zh) * 2023-07-25 2023-10-24 广西森合高新科技股份有限公司 用于黄金选矿废渣回收利用的复合处理剂及其处理方法

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016141438A1 (fr) * 2015-03-11 2016-09-15 Curtin University Of Technology Procédé pour la récupération sélective d'éléments du groupe des chalcophiles
WO2018234880A1 (fr) * 2017-06-23 2018-12-27 Anglo American Services (Uk) Ltd Enrichissement de métaux de valeur à partir de minerais à l'aide d'un procédé de lixiviation en tas
WO2019243635A1 (fr) * 2018-06-22 2019-12-26 Bernd Kunze Procédé de récupération de métaux nobles à partir de catalyseurs usagés
CN116926336A (zh) * 2023-07-25 2023-10-24 广西森合高新科技股份有限公司 用于黄金选矿废渣回收利用的复合处理剂及其处理方法

Similar Documents

Publication Publication Date Title
Oraby et al. The selective leaching of copper from a gold–copper concentrate in glycine solutions
AU2021202669B2 (en) Process for selective recovery of chalcophile group elements
CA2215963C (fr) Procede de lessivage de minerais sous une pression atmospherique
US4571263A (en) Recovery of gold from refractory auriferous iron-containing sulphidic concentrates
CA2706414C (fr) Procede de traitement d'un concentre pyritique contenant de l'or, du cuivre et de l'arsenic
AU664835B2 (en) Process for recovery of metal
AU2007231537A1 (en) Improved processing of metal values from concentrates
CA2974905A1 (fr) Procede d'extraction du cuivre de concentre de sulfure de cuivre arsenical
US11155894B2 (en) Method for reducing arsenic content in arsenic-bearing gold material
WO2025102113A1 (fr) Procédé de production d'un concentré
US12480178B2 (en) Sulphide oxidation in leaching of minerals
FI130407B (en) Hydrometallurgical process for the recovery of metals from sulphide minerals and the use of sulphide minerals as reducing agents for iron
AU2016404384B2 (en) Hydrometallurgical method for silver recovery
US20250305088A1 (en) Methods and systems for leaching a metal-bearing material
EP2742159B1 (fr) Traitement de matières sulfurées
CN1823171A (zh) 加工含有贵金属的硫化物矿石的方法
EA047380B1 (ru) Способ извлечения неблагородных и благородных металлов путем предварительной обработки для солюбилизации их тугоплавких матриц
AU8077698A (en) Leaching of a nickel sulphide concentrate

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 24889821

Country of ref document: EP

Kind code of ref document: A1