WO2004042094A1 - Reducing cyanide consumption in gold recovery from finely ground sulphide ores and concentrates - Google Patents
Reducing cyanide consumption in gold recovery from finely ground sulphide ores and concentrates Download PDFInfo
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- WO2004042094A1 WO2004042094A1 PCT/AU2003/001400 AU0301400W WO2004042094A1 WO 2004042094 A1 WO2004042094 A1 WO 2004042094A1 AU 0301400 W AU0301400 W AU 0301400W WO 2004042094 A1 WO2004042094 A1 WO 2004042094A1
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- WIPO (PCT)
- Prior art keywords
- cyanide
- leach
- gold
- ore
- lime
- Prior art date
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- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 229910052737 gold Inorganic materials 0.000 title claims abstract description 56
- 239000010931 gold Substances 0.000 title claims abstract description 56
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 title claims abstract description 55
- 239000012141 concentrate Substances 0.000 title claims description 45
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 title claims description 43
- 238000011084 recovery Methods 0.000 title description 17
- 238000002386 leaching Methods 0.000 claims abstract description 49
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 43
- 235000011941 Tilia x europaea Nutrition 0.000 claims abstract description 43
- 239000004571 lime Substances 0.000 claims abstract description 43
- 235000019738 Limestone Nutrition 0.000 claims abstract description 20
- 239000006028 limestone Substances 0.000 claims abstract description 20
- 238000000227 grinding Methods 0.000 claims abstract description 17
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 14
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 14
- 239000001301 oxygen Substances 0.000 claims abstract description 14
- 230000003647 oxidation Effects 0.000 claims description 39
- 238000007254 oxidation reaction Methods 0.000 claims description 39
- 238000000034 method Methods 0.000 claims description 32
- 230000008569 process Effects 0.000 claims description 28
- 239000000463 material Substances 0.000 claims description 18
- 238000000605 extraction Methods 0.000 claims description 15
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 claims description 13
- 229910052683 pyrite Inorganic materials 0.000 claims description 13
- 239000011028 pyrite Substances 0.000 claims description 12
- 239000011819 refractory material Substances 0.000 claims description 6
- 229910052709 silver Inorganic materials 0.000 claims description 6
- 239000004332 silver Substances 0.000 claims description 6
- 239000007800 oxidant agent Substances 0.000 claims description 5
- MJLGNAGLHAQFHV-UHFFFAOYSA-N arsenopyrite Chemical compound [S-2].[Fe+3].[As-] MJLGNAGLHAQFHV-UHFFFAOYSA-N 0.000 claims description 3
- 229910052964 arsenopyrite Inorganic materials 0.000 claims description 3
- 229910052959 stibnite Inorganic materials 0.000 claims description 3
- IHBMMJGTJFPEQY-UHFFFAOYSA-N sulfanylidene(sulfanylidenestibanylsulfanyl)stibane Chemical compound S=[Sb]S[Sb]=S IHBMMJGTJFPEQY-UHFFFAOYSA-N 0.000 claims description 3
- 239000002184 metal Substances 0.000 claims 4
- 229910052751 metal Inorganic materials 0.000 claims 4
- 239000010970 precious metal Substances 0.000 abstract description 4
- 239000003513 alkali Substances 0.000 description 26
- 239000000203 mixture Substances 0.000 description 24
- 229910052500 inorganic mineral Inorganic materials 0.000 description 17
- 239000011707 mineral Substances 0.000 description 17
- 235000010755 mineral Nutrition 0.000 description 17
- 238000012360 testing method Methods 0.000 description 17
- 230000000694 effects Effects 0.000 description 13
- 230000001590 oxidative effect Effects 0.000 description 13
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 12
- KXZJHVJKXJLBKO-UHFFFAOYSA-N chembl1408157 Chemical compound N=1C2=CC=CC=C2C(C(=O)O)=CC=1C1=CC=C(O)C=C1 KXZJHVJKXJLBKO-UHFFFAOYSA-N 0.000 description 12
- 239000002245 particle Substances 0.000 description 9
- 239000002002 slurry Substances 0.000 description 8
- 238000004458 analytical method Methods 0.000 description 7
- 239000002244 precipitate Substances 0.000 description 7
- 229910052742 iron Inorganic materials 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000003153 chemical reaction reagent Substances 0.000 description 5
- 239000002562 thickening agent Substances 0.000 description 5
- 230000009467 reduction Effects 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 150000004763 sulfides Chemical class 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 229910052598 goethite Inorganic materials 0.000 description 3
- AEIXRCIKZIZYPM-UHFFFAOYSA-M hydroxy(oxo)iron Chemical compound [O][Fe]O AEIXRCIKZIZYPM-UHFFFAOYSA-M 0.000 description 3
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 238000002441 X-ray diffraction Methods 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 239000011324 bead Substances 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 229910001919 chlorite Inorganic materials 0.000 description 2
- 229910052619 chlorite group Inorganic materials 0.000 description 2
- QBWCMBCROVPCKQ-UHFFFAOYSA-N chlorous acid Chemical compound OCl=O QBWCMBCROVPCKQ-UHFFFAOYSA-N 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 229910001254 electrum Inorganic materials 0.000 description 2
- XXOYNJXVWVNOOJ-UHFFFAOYSA-N fenuron Chemical compound CN(C)C(=O)NC1=CC=CC=C1 XXOYNJXVWVNOOJ-UHFFFAOYSA-N 0.000 description 2
- 150000002344 gold compounds Chemical class 0.000 description 2
- -1 gold tellurides Chemical class 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 150000002505 iron Chemical class 0.000 description 2
- 239000010909 process residue Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 125000000446 sulfanediyl group Chemical group *S* 0.000 description 2
- 229910021653 sulphate ion Inorganic materials 0.000 description 2
- 150000004772 tellurides Chemical class 0.000 description 2
- 229910052714 tellurium Inorganic materials 0.000 description 2
- PORWMNRCUJJQNO-UHFFFAOYSA-N tellurium atom Chemical compound [Te] PORWMNRCUJJQNO-UHFFFAOYSA-N 0.000 description 2
- 150000003567 thiocyanates Chemical class 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 229910021532 Calcite Inorganic materials 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- BUGBHKTXTAQXES-UHFFFAOYSA-N Selenium Chemical compound [Se] BUGBHKTXTAQXES-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- MOAOBEKGMNGXJG-UHFFFAOYSA-N [Te].[Te].[Te].[Au].[Au] Chemical compound [Te].[Te].[Te].[Au].[Au] MOAOBEKGMNGXJG-UHFFFAOYSA-N 0.000 description 1
- 229910000512 ankerite Inorganic materials 0.000 description 1
- 230000003466 anti-cipated effect Effects 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- PASHVRUKOFIRIK-UHFFFAOYSA-L calcium sulfate dihydrate Chemical compound O.O.[Ca+2].[O-]S([O-])(=O)=O PASHVRUKOFIRIK-UHFFFAOYSA-L 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- YGANSGVIUGARFR-UHFFFAOYSA-N dipotassium dioxosilane oxo(oxoalumanyloxy)alumane oxygen(2-) Chemical compound [O--].[K+].[K+].O=[Si]=O.O=[Al]O[Al]=O YGANSGVIUGARFR-UHFFFAOYSA-N 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 229920001903 high density polyethylene Polymers 0.000 description 1
- 239000004700 high-density polyethylene Substances 0.000 description 1
- 229910052935 jarosite Inorganic materials 0.000 description 1
- 239000012633 leachable Substances 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 229910052960 marcasite Inorganic materials 0.000 description 1
- 238000003801 milling Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052627 muscovite Inorganic materials 0.000 description 1
- 230000003287 optical effect Effects 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 229910052711 selenium Inorganic materials 0.000 description 1
- 239000011669 selenium Substances 0.000 description 1
- 150000003346 selenoethers Chemical class 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 238000004513 sizing Methods 0.000 description 1
- MNWBNISUBARLIT-UHFFFAOYSA-N sodium cyanide Chemical compound [Na+].N#[C-] MNWBNISUBARLIT-UHFFFAOYSA-N 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 230000008719 thickening Effects 0.000 description 1
- 238000003260 vortexing Methods 0.000 description 1
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
- C22B11/08—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
- 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
- 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
- C22B3/12—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic alkaline 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
- This invention is directed to a process by which gold, silver and other precious minerals can be recovered from a refractory material such as an ore/concentrate/residue in such a manner that the amount of cyanide consumption is reduced.
- Gold in sulphide mineralisation can occur in several forms: free gold and electrum and fine inclusions of these particles in sulphide minerals gold compounds (tellurides and selenides) • gold locked in the lattice of pyrite, arsenopyrite, stibnite etc (invisible gold)
- particulate free gold and electrum can be recovered by conventional gravity and cyanidation methods.
- fine grinding is used to liberate the particles prior to cyanide leaching.
- Fine gold particles locked in other minerals can be liberated by fine grinding from p80 « 70 ⁇ to p80 « 12 ⁇ .
- This liberation of fine gold particles from sulphides and quartz gange particles by fine grinding and cyanide leaching is well known. It has been found that fine grinding to circa 10 microns and leaching with sodium cyanide can recover the majority of the free gold and the gold present as gold compounds.
- High pH (-11 - 12) high cyanide concentration (2 - 5000 ppm NaCN vs 200 - 300 ppm used conventionally) and long leach times are required, (48 - 72 hours vs 18 - 24 hours required conventionally).
- recoveries of 80 - 90% for gold can be achieved with consumptions of lime of 5 -15 kg/t and 12 - 20 kg/t of sodium cyanide. Normal commercial operation results in consumption of 1.5 - 5 kg/t of lime and 1.5 - 2.5 kg/t of sodium cyanide.
- the sulphide minerals are also finely ground and a large surface area of fresh unoxidised sulphide mineralisation is exposed. It is this sulphide surface which reacts with cyanide during cyanide leaching for gold extraction to form thiocyanates and other thio species. This results in the high cyanide consumption observed during cyanide leaching of finely ground sulphidic gold ores.
- a typical refractory ore comprises a sulphide ore and a carbonaceous ore.
- Alkaline leaching is known but alkaline leaching is not very efficient with refractory materials.
- a disadvantage with the above alkaline leaching process is that the amount of cyanide consumed during the extraction process is rather high which adds to the cost of the overall process. Also, the reaction time is quite long.
- the sulphide minerals are finely ground and a large surface area of fresh unoxidised sulphide mineralisation is exposed. It is this sulphide surface which reacts with cyanide during cyanide leaching for gold extraction to form thiocyanates and other thio species. This results in the high cyanide consumption observed during cyanide leaching of finely ground sulphidic gold ores. In our previous process described in the above International patent application, the sulphide was almost totally oxidised but even so, there was still a large consumption of cyanide.
- the present invention is directed to the discovery that the amount of cyanide consumed during an alkaline extraction process can be remarkably reduced (for instance by up to 66%) by only partially oxidising the ore/concentrate in a pretreatment step prior to extraction with cyanide.
- the invention resides in a process for extracting gold and other precious metals from a refractory material (such as an ore/concentrate - such as a sulphide ore), the method comprising fine grinding the ore, subjecting the ground ore to an leaching step in the presence of an alkaline material (which may be lime and limestone) and oxygen as the oxidising agent, adjusting the leaching step such that the amount of oxidation is between 9%-20% , and subjecting the partially oxidated ore/concentrates to a cyanide extraction step.
- a refractory material such as an ore/concentrate - such as a sulphide ore
- the refractory ore/concentrate may comprise a sulphide ore a carbonaceous ore, pyrites, arsenopyrite, stibnite and may contain other compounds such as selenium and tellurium.
- the ore/concentrate is typically finely ground to a p80 of ⁇ 20 microns.
- Various devices are commercially available to grind a solid to this particle size.
- the alkaline leaching step is preferably conducted at a temperature of between 60-95° as this can provide a further reduction in the consumption of cyanide during the extraction process. For instance, the amount of cyanide consumed at 70-85° is approximately half of that consumed at between room temperature-50° by solids partially oxidised.
- the leaching step can be conducted to provide a sulphide oxidation of between 8-15% by solids partially oxidized.
- the oxidation is typically carried out using oxygen introduced into a leach reactor. When the desired level of sulphide oxidation had occurred, oxygen is no longer added to the reactor.
- the alkaline conditions (more correctly conditions which are less acidic than the very well-known acid leaching in sulphuric acid) can be maintained using limestone and lime.
- the amount of lime can be between 8%-20%.
- the pH of the leach is typically maintained between 5-7.
- the leached solution is then typically subjected to a cyanide extraction step to extract the gold and other precious minerals from the ore/concentrate.
- Trials were carried out to test the cyanide consumption of materials oxidised in a flow system.
- the principle variables trialled were the level of sulphide oxidation, vessel temperature, which was varied in the range 60 - 70 degrees, and the blend of limestone and lime components in the alkali added to the leach.
- the concentrate sample consisted predominantly of pyrite, with silica, sericite, muscovite and chlorite making up the major gangue components.
- the sample contained 213 ppm tellurium; however no tellurides were visible under optical microscope.
- the sample contained a minor amount of calcite, and had an 80% passing size of 91.5 microns.
- the continuous leach run was carried out as follows: 100 kg of concentrate was finely ground as feed to a continuous reactor and split into representative 20 kg sub samples. The slurry was ground to 80% passing 12 microns, and sent for head analysis.
- a three stage continuous oxidative leach reactor was set up and commissioned.
- the reactor was designed to operate for 24 hours per day with continuous feed of both concentrate and alkali slurry at measured rates.
- Discharge from the leach was to be gravitated to a thickener for thickening, with the thickener overflow stream used as makeup water to the feed and alkali circuits.
- the continuous leach reactor consisted of three stainless steel vessels connected in series using overflow ports. Each reactor had a live volume of 5 litres and an aspect ratio of 1. Each reactor was baffled to prevent solution vortexing, and agitated by a 100 mm diameter radial impeller. Oxygen was introduced into each reactor by air spear, which terminated directly below the impeller. Oxygen flow was controlled off a pressure cylinder using rotameters. Each vessel was jacketed, with hot water continuously circulated through the jacket to maintain the temperatures within the leach at the desired level. The outside of the jacket was insulated to minimise heat loss.
- the overflow port was located at the top of each reactor, with the inlet port located below the impeller line. This facilitated slurry transport between the vessels.
- the partially oxidised leach residues collected during the leaching program were tested for gold and silver recovery by cyanidation in a bottle roll apparatus. Approximately 1000 grams of residue at 35 % w/w solids was be added to a 5 HDPE bottle, and the bottle rotated at 30 rpm on a set of rollers. Cyanide and hydrated lime were added to the bottle prior to starting the test.
- the main operating parameter that required optimising in the continuous leach run was the level of sulphide oxidation required.
- the batch testwork had narrowed the target range to 8 - 14 % w/w, however the aim of the continuous test was to reduce the target range to within 1 %. This was examined in the first oxidative leach run, with the level of sulphide oxidation varied in the first 250 hours of operation.
- the sodium cyanide consumption observed for the residue oxidised to a sulphide oxidation of 12.5% was 2.4 kg/tonne of oxidised residue (2.6 kg/tonne of feed), at a lime consumption of 1.65 kg/tonne of oxidised residue (1.8 kg/tonne of feed).
- the level of sulphide oxidation in the range given in table 5 did not appear to have much impact on the cyanide consumption, with a cyanide consumption in the range 2.2 - 2.5 kg/tonne of residue noted at sulphide oxidation levels in the range 8 - 14%.
- All of the cyanide leach tests were carried out at a free cyanide level of 500 ppm, and at pH 10.5. Lime was added to the tests to hold the pH at this level, rather than as a single addition and the pH was stable throughout the cyanide leach tests, with low lime consumption observed.
- the cyanide level was stable throughout the cyanide leach tests, and was easy to control at the target level of 500 ppm.
- Leach Run No 1 was carried out at a temperature of 70 degrees, whereas for leach Run No 2 the temperature was lowered to 60 degrees.
- the average gold recovery from oxidised residues produced in Leach run No 1 was 87%, with the gold recovery ranging from 85 - 90%.
- the average sodium cyanide consumption was 2.8 kg/tonne, at an average lime consumption of 1 - 1.5 kg/tonne.
- the average sulphide oxidation achieved at 70 degrees was 11.5% w/w, with approximately 90 - 95% of the limestone/lime blend added to the leach consumed in the oxidation.
- the average gold recovery from the oxidised residue was 88%, at an average sodium cyanide consumption of 2.5 kg/tonne, and a lime consumption of 1.4 kg/tonne.
- the level of sulphide oxidation achieved at 60 degrees was 10.8% w/w on average.
- the amount of limestone/lime blend consumed in the oxidation was again over 90%.
- the final variable tested in Leach run No 3 was the amount of lime in the blend, which was decreased from 20% down to 8%.
- Leach Run No 1 was carried out at a temperature of 70 degrees, with 20% lime present in the alkali blend.
- Leach Run No 3 was carried out at a temperature of 70 degrees, with the amount of lime in the alkali blend reduced to 8%.
- the sulphide oxidation ranged from 7.5 - 15%.
- the average gold recovery from the oxidised residue was 88%, at an average sodium cyanide consumption of 2.6 kg/tonne, and a lime consumption of 1.9 kg/tonne.
- the lime consumption in the cyanide leach stage was slightly elevated with 8% lime in the alkali blend, compared to residues produced with 20% lime in the alkali blend.
- Leach Run No 3 was carried out at 70°C, with a lime level of 8% w/w in the alkali blend.
- the discharge pH from the leach was above 5 throughout the run, and so there was little driving force for the formation of sulphated iron precipitates.
- the data was collected by chemical analysis and XRD analysis of samples taken from each tank when the leach was operating at steady state.
- FeS 2 + 2CaO + 15/40 2 + 5/2H 2 O FeO.OH + CaSO 4 .2H 2 O
- the mass increase across the oxidative leach was approximately 14%, with the bulk of the increased mass present as goethite and gypsum. Approximately 10% of the final leach residue was made up of gypsum.
- gangue minerals present in the concentrate sample in particular chlorite and ankerite, were consumed in the oxidative leach.
- the most likely by products from reaction of these gangue minerals would magnesium and aluminium oxides, which would not be resolved clearly in the XRD analysis, as they tend to be amorphous.
- the only iron reaction product identified in the XRD was goethite, FeO.OH. No sulphated iron precipitates were identified by XRD.
- the leach residues were relatively simple, with few reaction products, which confirmed that the majority of the reacted pyrite leached according to the leach reaction specified above. This simple reaction system greatly simplifies the heat and material balance for the process.
- the leach discharge pH varied, as the amount of alkali added to the leach was varied.
- the exit pH increased gradually across the first 200 hours of operation, varying from 2 - 5, before settling down in the range 5 - 6 once the alkali blend addition was optimised.
- Discharge pH had a significant effect on reagent consumption levels in the cyanide leach.
- the recommended discharge pH for the leach would be in the range 5 - 6, to achieve a cyanide consumption of 3 kg/tonne or less.
- the alkali stream will need to be added to the leach at a slight excess over stoichiometric, and a 10% excess is recommended.
- Table 8 outlines the relative cyanide leach kinetics for a preferred process residue, oxidised to 12 % w/w sulphide oxidation, relative to a sample of finely ground concentrate leached under similar conditions.
- the process oxidative pretreatment of the pyrite concentrate results in a significant increase in the cyanide leach kinetics. Leaching of the process residue is essentially complete within 8 - 24 hours of leaching, compared to 54 - 72 hours for the un-oxidised finely ground concentrate.
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2003273610A AU2003273610B2 (en) | 2002-11-06 | 2003-10-22 | Reducing cyanide consumption in gold recovery from finely ground sulphide ores and concentrates |
CA2504934A CA2504934C (en) | 2002-11-06 | 2003-10-22 | Reducing cyanide consumption in gold recovery from finely ground sulphide ores and concentrates |
US10/533,317 US7488370B2 (en) | 2002-11-06 | 2003-10-22 | Reducing cyanide consumption in gold recovery from finely ground sulphide ores and concentrates |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2002952490A AU2002952490A0 (en) | 2002-11-06 | 2002-11-06 | Reducing cyanide consumption in gold recovery from finely ground sulphide ores and concentrates |
AU2002952490 | 2002-11-06 |
Publications (1)
Publication Number | Publication Date |
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WO2004042094A1 true WO2004042094A1 (en) | 2004-05-21 |
Family
ID=28795880
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/AU2003/001400 WO2004042094A1 (en) | 2002-11-06 | 2003-10-22 | Reducing cyanide consumption in gold recovery from finely ground sulphide ores and concentrates |
Country Status (10)
Country | Link |
---|---|
US (1) | US7488370B2 (en) |
AR (1) | AR042187A1 (en) |
AU (1) | AU2002952490A0 (en) |
BG (1) | BG66351B1 (en) |
CA (1) | CA2504934C (en) |
DO (1) | DOP2003000746A (en) |
MY (1) | MY134378A (en) |
PE (1) | PE20040480A1 (en) |
WO (1) | WO2004042094A1 (en) |
ZA (1) | ZA200501271B (en) |
Cited By (14)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2007019707A1 (en) | 2005-08-18 | 2007-02-22 | Gilles Fiset | Method and apparatus for the recovery of refractory mineral ores |
CN1304606C (en) * | 2005-09-22 | 2007-03-14 | 华南理工大学 | Method for extracting gold |
WO2007109841A1 (en) * | 2006-03-28 | 2007-10-04 | Dundee Precious (Barbados) Inc | Improved processing of metal values from concentrates |
CN100351407C (en) * | 2006-03-24 | 2007-11-28 | 李宇文 | Method for extracting gold from gold tailings |
AU2009101298B4 (en) * | 2009-12-16 | 2010-02-11 | Rohan Bose | Process for recovering gold otherwise lost to the antimony bearing PLS from alkaline leaching of aurostibnite ores |
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CN104694764A (en) * | 2015-03-09 | 2015-06-10 | 中南大学 | Reinforced leaching method of fine-grained encapsulated gold |
RU2622534C2 (en) * | 2015-09-23 | 2017-06-16 | Общество с ограниченной ответственностью "НВП Центр-ЭСТАгео" (ООО НВП Центр-ЭСТАгео") | Method of precious metals recovery from heap leaching robbed-out bings |
CN108018418A (en) * | 2017-11-29 | 2018-05-11 | 长春黄金研究院 | A kind of wet type preprocess method of sulfide coated difficult-treating gold mine |
RU2705585C1 (en) * | 2018-11-12 | 2019-11-12 | Акционерное общество "Иркутский научно-исследовательский институт благородных и редких металлов и алмазов" АО "Иргиредмет" | Method of extracting gold from mineral material by cyanidation while stirring |
Also Published As
Publication number | Publication date |
---|---|
AU2002952490A0 (en) | 2002-11-21 |
BG108310A (en) | 2004-10-29 |
US7488370B2 (en) | 2009-02-10 |
PE20040480A1 (en) | 2004-09-08 |
AR042187A1 (en) | 2005-06-15 |
BG66351B1 (en) | 2013-08-30 |
DOP2003000746A (en) | 2004-06-15 |
MY134378A (en) | 2007-12-31 |
ZA200501271B (en) | 2006-08-30 |
CA2504934C (en) | 2011-01-04 |
CA2504934A1 (en) | 2004-05-21 |
US20060185475A1 (en) | 2006-08-24 |
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