EP1185717A1 - Gewinnung von edelmetallen mittels oxidierender halid-laugung unter druck - Google Patents

Gewinnung von edelmetallen mittels oxidierender halid-laugung unter druck

Info

Publication number
EP1185717A1
EP1185717A1 EP20000926596 EP00926596A EP1185717A1 EP 1185717 A1 EP1185717 A1 EP 1185717A1 EP 20000926596 EP20000926596 EP 20000926596 EP 00926596 A EP00926596 A EP 00926596A EP 1185717 A1 EP1185717 A1 EP 1185717A1
Authority
EP
European Patent Office
Prior art keywords
precious metal
degrees celsius
chloride
host material
leach solution
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.)
Withdrawn
Application number
EP20000926596
Other languages
English (en)
French (fr)
Inventor
Christopher A. Fleming
David Dreisinger
P. Terry O'kane
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.)
International PGM Technologies Ltd
Original Assignee
International PGM Technologies 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 US09/300,878 external-priority patent/US6315812B1/en
Application filed by International PGM Technologies Ltd filed Critical International PGM Technologies Ltd
Publication of EP1185717A1 publication Critical patent/EP1185717A1/de
Withdrawn legal-status Critical Current

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
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • C22B3/10—Hydrochloric acid, other halogenated acids or salts thereof
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • 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
    • C22B11/00—Obtaining noble metals
    • C22B11/04—Obtaining noble metals by wet processes
    • C22B11/042—Recovery of noble metals from waste materials
    • C22B11/044—Recovery of noble metals from waste materials from pyrometallurgical residues, e.g. from ashes, dross, flue dust, mud, skim, slag, sludge
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • 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
    • C22B7/04—Working-up slag
    • 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 present invention relates to methods for the recovery of precious metals from host materials, using pressure oxidation.
  • platinum group metals which include platinum and palladium, rhodium, ruthenium, osmium and iridium.
  • platinum group metals which include platinum and palladium, rhodium, ruthenium, osmium and iridium.
  • the term 'precious metals' as used herein will refer to both gold and the platinum group metals that are present in the host material either as single elements or in any combination thereof .
  • these precious metals are present in host materials along with other metals such as the base metals copper and nickel, in varying concentrations. These host materials are normally treated by grinding and flotation to produce a concentrate, which is then smelted.
  • the constituent precious and base metals typically report to a matte phase during smelting.
  • the matte phase is then processed by a variety of well established techniques to separate and recover the individual constituents in substantially pure form.
  • the matte typically undergoes oxidative pressure leaching at temperatures of 130 to 150 degrees Celsius which leaches the base metal component of the matte leaving the platinum group metals in the residue. After separating the solution from the residue, the residue is then typically leached, in atmospheric conditions, with concentrated hydrochloric acid and chlorine gas as the oxidant to dissolve the platinum group metals.
  • the solid phase leaving the pressure leach step retains the precious metals while the copper and nickel transfer to the leach solution, for further processing by various hydrometallurgical procedures well known to the art.
  • the precious metal constituent is recovered from the solid phase by relatively complex and expensive procedures, including leaching by chlorination or pressure cyanidation, followed by precious metal recovery by precipitation, solvent extractions or ion exchange techniques well known to the art. Though these processing routes may prove satisfactory in some cases, there are many host materials in which either the leach efficiency or the concentration of precious metals is insufficient for this relatively complex metallurgical flowsheet to be economically viable.
  • the invention provides a method for recovering a precious metal portion and a base metal portion from a host material, comprising the steps of:
  • the invention provides a method for leaching a precious metal from a host material, comprising the steps of:
  • the leach solution is at a pH of between 0 and 1 , more preferably between 0 and 0.5.
  • the temperature ranges from about 170 to about 275 degrees Celsius, more preferably 195 to 275 degrees Celsius.
  • the temperature may be at least 180 degrees Celsius, more preferably 180 to 275 degrees Celsius.
  • the invention provides a method for leaching a precious metal and a base metal from a host material in a single step by subjecting the host material to an oxidative pressure leach process, in the presence of a chloride ion constituent and at a temperature of at least 170 degrees Celsius in order to form a leach solution containing at least one precious metal- bearing chloride complex and the base metal.
  • the invention provides a method for economically leaching a precious metal from a host material, comprising the step of leaching said host material with salt water at a temperature of at least 170 degrees Celsius, in the presence of an oxidant and at sufficient pressure to form, in the leach solution, a chloride complex containing the precious metal.
  • the salt water can be ground water, sea water or otherwise naturally formed or may simply be a prepared.
  • the base metal is contained in a base metal sulfate complex and the precious metal bearing chloride complex is a platinum-, palladium- or a gold-bearing complex.
  • the invention provides a method for recovering a precious metal from a host material, comprising the steps of:
  • the halide ion is selected from the group chloride, iodide or bromide.
  • fluoride is not included because it is not sufficiently reactive with (or does not effectively complex with) gold and other precious metals.
  • Chloride is particularly preferable because of its convenience and ease of handling as a salt, although chloride is generally inefficient, at lower concentrations (such as 20 g/L at 200 degrees Celsius) to recover silver.
  • the term 'precious metal' as used herein refers to both gold and the platinum group metals that are present in the host material either as single elements or in any combination thereof. Thus, for host materials which have an economical quantify of silver, it may be appropriate to increase the chloride levels to above 50 g/L.
  • the halide ion originates from a halide salt which is added to the leach solution.
  • the halide ion is a chloride ion provided to the leach solution by a chloride salt.
  • the chloride salt may include sodium chloride, calcium chloride or potassium chloride, as well as ferrous or ferric chloride, hydrochloric acid, cupric or cuprous chloride, lithium chloride, magnesium chloride and ammonium chloride, among still others.
  • sufficient chloride salt constituent is present in solution to provide a chloride ion concentration ranging from about 0.5 g/L to about 100 g/L, more preferably from 1 to 20 g/L, still more preferably from 1.5 to 10 g/L. Still more preferably, the chloride ion constituent is present at a concentration ranging from about 3 to about 6 g/L. In one embodiment, the chloride salt is sodium chloride which itself is provided at a concentration of about 10 g/L.
  • a method for recovering a precious metal from a host material comprising the steps of:
  • barren solid is separated from the leach solution, although it may be desirable in some cases to recover the precious metal from the leach solution before separating the barren solid, for example to minimize the loss of precious metals contained in the residual leach solution which can be lost with the separated barren solids.
  • the oxidative pressure leach process takes place in the presence of a gaseous oxidant.
  • the gaseous oxidant is oxygen gas.
  • the oxygen gas is preferably injected into the vessel at an oxygen partial pressure of between 1 and 500 psig, still more preferably between 10 and 200 psig and still more preferably between 50 and 100 psig.
  • Other oxidants may also be effective including chlorine, the ferric ion. hydrogen peroxide and Caro's acid, though these may not in some cases be as economical as oxygen gas.
  • the temperature ranges from about 170 degrees Celsius to about 300 degrees Celsius, more preferably from about 180 degrees Celsius to about 295 degrees Celsius, more preferably from about 195 degrees Celsius to about 275 degrees Celsius, more preferably from 200 degrees Celsius to 250 degrees Celsius, still more preferably from 210 degrees Celsius to about 230 degrees Celsius.
  • the upper limit of 300 degrees Celsius is limited to the physical constraints of the pressure leaching systems currently available.
  • the leach solution is acidic.
  • the acid constituent is sulphuric acid at a concentration ranging from 1 to 500 g/L. More preferably, the sulphuric acid is at a concentration ranging from about 5 to about 250 g/L, more preferably at a concentration ranging from about 10 to about 100 g/L.
  • oxidation potential in solution during the leach for example at levels greater than 500 mV versus Ag/AgCl
  • a tramp ion constituent which is added as a consequence of grinding or re-grinding the feed to the process, may also contribute to a reduction in the precious metal recovery. This is especially true in the case of gold.
  • the host material may be in any one of a number of forms, including a primary sulphide or oxide ore body which has been processed by grinding and the like, an ore concentrate, or a secondary material containing precious metals, such as for example a spent oxidation catalyst.
  • a primary oxide ore body would be a laterite, which contains nickel and cobalt as well as PGMs in some cases, and which is normally treated by pressure acid leaching to recover the nickel and cobalt.
  • the host may also be a matte material from a smelting operation which, in contrast to the ore concentrates, can have precious metal concentrations of up to 10 percent, with the balance being base metals and sulphide.
  • the host may also, in some cases, be a mixture of matte material and flotation concentrate. In these cases, it may be desirable either to recover the precious metals and base metals together into the leach solution or, alternatively, use a multiple step process to recover the base metals first and then the precious metals second.
  • the base metals can be recovered to a first leach solution as in the prior art using concentrations of oxygen and suitable temperatures to obtain a first leach solution of base metals with residual amounts of sulphuric acid.
  • the precious metals will be retained in the residue and may then be removed in a second phase at the conditions disclosed herein to recover the precious metals to a second leach solution.
  • the first phase may be carried out using just air or oxygen in the absence of a halide ion constituent to recover the base metal constituents as in the form of one or more sulphate complexes, such as copper(II)sulphate, nickel(II)sulphate and cobalt(II)sulphate.
  • a halide ion constituent such as copper(II)sulphate, nickel(II)sulphate and cobalt(II)sulphate.
  • the oxidative leach autoclave of the first phase will likely be operating at relatively lower temperatures, than the oxidative leach process of the second phase which will have relatively higher temperature and be exposed to the halide ion constituent.
  • the first phase may be carried out in the presence of a halide ion constituent at conditions as disclosed herein to recover the base and precious metal constituents simultaneously.
  • the present invention provides a method for recovering a precious metal from a smelt matte material, wherein said matte material includes a precious metal constituent and a base metal constituent, comprising the steps of:
  • the first oxidative pressure leach process occurs at a temperature ranging from 100 to 190 degrees Celsius, more preferably from 120 to 170 degrees Celsius, still more preferably from 130 to 150 degrees Celsius.
  • the second oxidative pressure leach process occurs at temperature ranging from about 170 degrees Celsius to about 300 degrees Celsius, more preferably from about 180 degrees Celsius to about 260 degrees Celsius, more preferably from about 195 degrees Celsius to about 275 degrees Celsius, more preferably from 200 degrees Celsius to 250 degrees Celsius, still more preferably from 210 degrees Celsius to about 230 degrees Celsius.
  • the present invention provides a method for recovering a precious metal from a smelt matte material, wherein said matte material includes a precious metal constituent and a base metal constituent, comprising the steps of:
  • the halide is chloride, though the other halides as disclosed herein are also contemplated.
  • the invention provides a method for recovering a platinum group metal or gold from a host material, comprising the steps of:
  • Figure 1 is a schematic view of a method for recovering precious metals
  • FIGS. 2a, 2b and 2c are Eh - pH diagrams for several process examples
  • Figure 3 is a plot of percent extraction versus temperature for several process examples
  • Figure 4 is a plot of percent extraction versus chloride concentration for several process examples
  • Figure 5 is a Cu extraction isotherm for one process example
  • Figure 6 is a flowsheet for gold, PGM and base metal recovery for one process example.
  • Figure 7 is a flowchart for another process example.
  • the present method is based, in part, on the discoveries that:
  • one or a number of the precious metals and base metals may be leached from a host material in a single oxidative pressure leach process, whose leach solution may be treated to recover the individual precious and base metals, as desired;
  • this reaction can occur successfully with a relatively low concentration of halide ion in the leach solution , provided the selected halide ion is sufficiently reactive with the precious metals being recovered.
  • the present method involves the following steps:
  • the host material is a sulphide ore body or ore concentrate.
  • the sulphide component of the host material is oxidized to sulphuric acid.
  • the process takes place in an acidic environment ranging from 20 to 100 g/L sulphuric acid.
  • the acid is produced during the reaction to solubilize the copper and nickel.
  • the successful leach of precious metals and base metals from a host material occurs in the presence of an acid, in this case, sulphuric acid and at a temperature of at least 200 degrees Celsius. It is believed that the process may also function at temperatures below 200 degrees Celsius and to temperatures as high as economically achievable. It is also believed that the presence of acid in the leach solution has a desirable effect of increasing the overall recovery of precious metals from the host material.
  • the temperature selected for the pressure leach reaction of the present process will depend on the mineralogical characteristics and particle size of the feed material, the concentration of precious metals in the feed material, the acid strength, the oxygen partial pressure and the residence time in the pressure leaching vessel.
  • the chloride salt may be preferably selected from sodium chloride, calcium chloride or potassium chloride. More preferably, the salt is sodium chloride and is provided at a concentration ranging from about 1 g/L to about 100 g/L, still more preferably from 2 to 20 g/L, still more preferably from 5 to 15 g/L, still more preferably from 8 to 12 g/L.
  • the chloride salt is sodium chloride at a concentration of about 10 g/L in solution.
  • concentration of the chloride ion will likely tend to be higher with increasing concentration of the precious metal being recovered.
  • the oxidative pressure leach process takes place in the presence of a gaseous oxidant.
  • the gaseous oxidant is oxygen gas.
  • the oxygen gas is preferably injected into the vessel at an oxygen partial pressure of between 1 and 500 psig, still more preferably between 10 and 200 psig and still more preferably between 50 and 100 psig.
  • the precious metals leaching costs should be absorbed in the base metal leaching costs.
  • the present process does not require catalysts such as ammonia to promote the reaction to form a precious metal-bearing complex.
  • the high temperature autoclave oxidation process converts metal sulfide minerals into metal sulfates and iron hydrolysis products (primarily hematite).
  • the oxidation of gold, palladium, platinum and other precious metals is favoured by the presence of relatively small amounts of chloride in solution.
  • the chloride stabilizes the various platinum group elements as dissolved chloro complexes.
  • the chemical reactions believed to occur during the present process are shown below.
  • the mineralogy of the precious metals may be very complex, but for simplicity only the metallic species are considered.
  • Gold Oxidation/Chlorocomplex Formation Au + l/40 2 + 1/2H 2 S0 4 + 4NaCl ⁇ Na,AuCl 4 + l/2Na 2 S0 4 + 1/2H 2 0 (5)
  • a number of approaches can be selected to recover the precious metal constituent first, such as by the use of activated carbon adsorption or ion exchange resin adsorption, or reduction with of sulphur dioxide and a precipitation with sodium hydrosulfide and other suitable sulfide containing compounds such as Na 2 S and H 2 S, as well as copper cementation.
  • the precious metals constituent can be recovered directly, if desired, from the acidic pulp phase prior to solid liquid separation, which may be advantageous in some circumstances.
  • Tests were conducted with 5 and 10 g/L NaCl added to the pressure leach solution for a precious metal-bearing ore flotation concentrate, including gold, platinum and palladium.
  • the pressure leach was carried out in an autoclave.
  • the efficacy of the process may be improved with an increase in surface area of the host material to the pressure leach solution and, desirably, the ore may be ground to 75% passing 75 microns or a concentrate may be re-ground to 75 percent passing 20 microns.
  • thermodynamic stability at 25°C of the chloro-complexes of gold, platinum and palladium, at concentrations similar to those encountered during these examples, is graphically presented as Eh-pH in Figures 2. These equilibrium diagrams indicate that the oxidizing potential required to form the chloro-complex of Pd in the acidic domain is lower than those of platinum and gold.
  • NaHS sodium hydrogen sulphide
  • the precious metal precipitate could either be sold directly to a copper smelter or, preferably, pretreated in a small pressure leach reactor to dissolve the copper and produce a very high grade precious metal residue (>10% precious metal's) for sale to a precious metal refinery.
  • the present process has a wide range of application. It can be applied to feeds other than Cu Ni concentrates, for example mattes and copper-gold concentrates.
  • Table 8 presents head assays of samples of matte and copper concentrate submitted to the present process to the test conditions of table 7.
  • the matte was produced in a SIROSMELT ( a trademark) furnace, while the copper concentrate was a typical chalcopyrite concentrate.
  • the two samples were submitted the test conditions at table 7. The results are presented in Table 9.
EP20000926596 1999-04-28 2000-04-27 Gewinnung von edelmetallen mittels oxidierender halid-laugung unter druck Withdrawn EP1185717A1 (de)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
US09/300,878 US6315812B1 (en) 1999-04-28 1999-04-28 Oxidative pressure leach recovery using halide ions
US300878 1999-04-28
CA2303661 2000-04-03
CA2303661 2000-04-03
PCT/CA2000/000438 WO2000065111A1 (en) 1999-04-28 2000-04-27 Oxidative pressure leach recovery of precious metals using halide ions

Publications (1)

Publication Number Publication Date
EP1185717A1 true EP1185717A1 (de) 2002-03-13

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP20000926596 Withdrawn EP1185717A1 (de) 1999-04-28 2000-04-27 Gewinnung von edelmetallen mittels oxidierender halid-laugung unter druck

Country Status (3)

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EP (1) EP1185717A1 (de)
AU (1) AU763167B2 (de)
WO (1) WO2000065111A1 (de)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FI20135984A (fi) 2013-10-02 2015-04-03 Outotec Finland Oy Menetelmä ja laite arvometallien erottamiseksi mineraaleista
DE102019113198B3 (de) * 2018-06-22 2019-10-24 Bernd Kunze Auslaugungsverfahren für Edelmetalle aus verbrauchten Katalysatoren
CN115216640B (zh) * 2022-06-14 2023-08-22 江西思远再生资源有限公司 一种萃取分离铂的绿色环保工艺

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Also Published As

Publication number Publication date
WO2000065111B1 (en) 2001-01-25
AU763167B2 (en) 2003-07-17
WO2000065111A1 (en) 2000-11-02
AU4529500A (en) 2000-11-10

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