WO1996041025A1 - Process for extraction of nickel and cobalt from laterite ores - Google Patents
Process for extraction of nickel and cobalt from laterite ores Download PDFInfo
- Publication number
- WO1996041025A1 WO1996041025A1 PCT/CA1996/000364 CA9600364W WO9641025A1 WO 1996041025 A1 WO1996041025 A1 WO 1996041025A1 CA 9600364 W CA9600364 W CA 9600364W WO 9641025 A1 WO9641025 A1 WO 9641025A1
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- WO
- WIPO (PCT)
- Prior art keywords
- process according
- slurry
- ore
- gas
- stage
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 48
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 title claims abstract description 47
- 229910052759 nickel Inorganic materials 0.000 title claims abstract description 23
- 229910017052 cobalt Inorganic materials 0.000 title claims abstract description 19
- 239000010941 cobalt Substances 0.000 title claims abstract description 19
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 title claims abstract description 19
- 229910001710 laterite Inorganic materials 0.000 title claims abstract description 14
- 239000011504 laterite Substances 0.000 title claims abstract description 14
- 238000000605 extraction Methods 0.000 title claims abstract description 5
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 51
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 39
- 239000002002 slurry Substances 0.000 claims abstract description 34
- 229910052742 iron Inorganic materials 0.000 claims abstract description 20
- 229910052935 jarosite Inorganic materials 0.000 claims abstract description 17
- 150000003467 sulfuric acid derivatives Chemical class 0.000 claims abstract description 12
- 235000010269 sulphur dioxide Nutrition 0.000 claims abstract description 9
- 239000004291 sulphur dioxide Substances 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims description 19
- 238000010521 absorption reaction Methods 0.000 claims description 18
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 17
- 238000006243 chemical reaction Methods 0.000 claims description 14
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 11
- 229910052751 metal Inorganic materials 0.000 claims description 11
- 239000002184 metal Substances 0.000 claims description 11
- 239000001117 sulphuric acid Substances 0.000 claims description 11
- 235000011149 sulphuric acid Nutrition 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical class OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims description 7
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 6
- 239000011707 mineral Substances 0.000 claims description 6
- 235000010755 mineral Nutrition 0.000 claims description 6
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 5
- 229910052749 magnesium Inorganic materials 0.000 claims description 5
- 239000011777 magnesium Substances 0.000 claims description 5
- 229910021653 sulphate ion Inorganic materials 0.000 claims description 5
- 239000005569 Iron sulphate Substances 0.000 claims description 4
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 239000013535 sea water Substances 0.000 claims description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 claims description 3
- 150000001768 cations Chemical class 0.000 claims description 3
- 229910000514 dolomite Inorganic materials 0.000 claims description 2
- 239000010459 dolomite Substances 0.000 claims description 2
- 230000003647 oxidation Effects 0.000 claims description 2
- 238000007254 oxidation reaction Methods 0.000 claims description 2
- 230000000087 stabilizing effect Effects 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims 5
- 238000010438 heat treatment Methods 0.000 claims 2
- 229910021532 Calcite Inorganic materials 0.000 claims 1
- 229910000512 ankerite Inorganic materials 0.000 claims 1
- KTVIXTQDYHMGHF-UHFFFAOYSA-L cobalt(2+) sulfate Chemical class [Co+2].[O-]S([O-])(=O)=O KTVIXTQDYHMGHF-UHFFFAOYSA-L 0.000 claims 1
- 239000001095 magnesium carbonate Substances 0.000 claims 1
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 claims 1
- 229910000021 magnesium carbonate Inorganic materials 0.000 claims 1
- 235000014380 magnesium carbonate Nutrition 0.000 claims 1
- 239000002562 thickening agent Substances 0.000 description 8
- 239000000243 solution Substances 0.000 description 7
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 6
- 238000001556 precipitation Methods 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- QXZUUHYBWMWJHK-UHFFFAOYSA-N [Co].[Ni] Chemical compound [Co].[Ni] QXZUUHYBWMWJHK-UHFFFAOYSA-N 0.000 description 5
- 238000002386 leaching Methods 0.000 description 5
- 238000000926 separation method Methods 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000013505 freshwater Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000395 magnesium oxide Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 229910044991 metal oxide Inorganic materials 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 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
- 239000003929 acidic solution Substances 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910001429 cobalt ion Inorganic materials 0.000 description 2
- XLJKHNWPARRRJB-UHFFFAOYSA-N cobalt(2+) Chemical compound [Co+2] XLJKHNWPARRRJB-UHFFFAOYSA-N 0.000 description 2
- 239000010410 layer Substances 0.000 description 2
- 239000000391 magnesium silicate Substances 0.000 description 2
- 229910052919 magnesium silicate Inorganic materials 0.000 description 2
- 235000019792 magnesium silicate Nutrition 0.000 description 2
- ZADYMNAVLSWLEQ-UHFFFAOYSA-N magnesium;oxygen(2-);silicon(4+) Chemical compound [O-2].[O-2].[O-2].[Mg+2].[Si+4] ZADYMNAVLSWLEQ-UHFFFAOYSA-N 0.000 description 2
- 230000003472 neutralizing effect Effects 0.000 description 2
- 229910001453 nickel ion Inorganic materials 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 238000010795 Steam Flooding Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- -1 i.e. Chemical compound 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 1
- 235000013980 iron oxide Nutrition 0.000 description 1
- VBMVTYDPPZVILR-UHFFFAOYSA-N iron(2+);oxygen(2-) Chemical class [O-2].[Fe+2] VBMVTYDPPZVILR-UHFFFAOYSA-N 0.000 description 1
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910001813 natrojarosite Inorganic materials 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- FWFGVMYFCODZRD-UHFFFAOYSA-N oxidanium;hydrogen sulfate Chemical compound O.OS(O)(=O)=O FWFGVMYFCODZRD-UHFFFAOYSA-N 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 239000002344 surface layer Substances 0.000 description 1
- 239000011573 trace mineral Substances 0.000 description 1
- 235000013619 trace mineral Nutrition 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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
- C22B23/0461—Treatment or purification of solutions, e.g. obtained by leaching by chemical methods
-
- 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
- C22B23/005—Preliminary treatment of ores, e.g. by roasting or by the Krupp-Renn process
-
- 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
- C22B23/043—Sulfurated acids or salts thereof
-
- 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 relates to a process for extracting nickel and cobalt from laterite ores.
- a high proportion of known world resources of nickel and cobalt are contained in laterite deposits. These deposits are typically derived from weathering of mainly magnesium silicate minerals, such as garnierite, which contain nickel and cobalt, as well as iron, aluminum, chromium and a wide range of trace elements.
- a profile of a fully developed laterite deposit comprises a high iron surface layer (ferricrete) with low nickel and cobalt content; a layer of limonite containing mainly iron oxides, typically more than 40% Fe dry basis, plus nickel-cobalt values; a layer of saprolite, which contains partially weathered magnesium silicate minerals, enriched in nickel and cobalt; fractured but largely weathered garnierite; and basement unweathered garnierite.
- the present invention relates mainly to the limonite portion of lateritic nickel-cobalt deposits.
- the saprolite and weathered garnierite zones of suitable deposits may be used to advantage within the process.
- the principal commercial method involving direct hydrometallurgical treatment of limonitic nickel- cobalt ores is that practised at the Moa Bay mine in Cuba. This process involves high temperature, i.e., greater than 400°F (200°C) , sulphuric acid leaching of laterite. To operate the leach at a temperature greater than 400°F, high pressure reaction vessels are required to maintain the sulphuric acid-water leach solution in the liquid phase.
- the main advantage of the present invention compared to previously disclosed methods arises from essentially complete dissolution of metal oxide components of limonite, i.e., iron, nickel and cobalt, at much lower temperatures, typically 180-212°F (80-100°C) , where steam pressure is minimal.
- metal oxide components of limonite i.e., iron, nickel and cobalt
- a process for the extraction of nickel and cobalt from a laterite ore comprising the steps of reacting the ore, in slurry form, with sulphur dioxide to convert the iron, nickel and cobalt in the ore to soluble sulphates and bisulphites contained in a product slurry.
- the laterite ore may first be treated to extract a limonite portion therefrom, which limonite portion is reacted with said sulphur dioxide.
- the step of reacting the ore with sulphur dioxide may comprise a first stage S0 2 absorption in which a slurry of the ore and water is contacted with a mixture of S0 2 and N 2 such as from combustion of sulphur or sulphide minerals in air, followed by a second stage S0 2 absorption in which the slurry from the first stage is contacted with substantially 100% SO- gas and a pressure leach stage in which the slurry from the second stage S0 2 absorption is subjected to an elevated temperature and pressure.
- Figure 1 is a flow diagram of one embodiment of the process according to the invention.
- FIG. 2 is a flow diagram of another embodiment of the process according to the invention.
- Figures 3 to 5 are flow diagrams illustrating an embodiment of the process in more detail.
- the process comprises a S0 2 absorption step 12 in which a slurry of limonite nickel-cobalt ore and water is contacted with SO, at or below ambient temperature.
- the next step is a pressure leaching step 14 at a temperature of from 180° - 212°F (80 - 100°C) and a S0 2 partial pressure of 80-200 psig (550 - 1400 kPa (gauge) ) to substantially completely dissolve the metallic oxide components of the limonite, such as iron, nickel, cobalt, magnesium and manganese, as the soluble sulphates and bisulphites, according to the following reaction:
- Magnesium, aluminum and other metallic oxides of limonite are similarly dissolved. These components are not oxidized or reduced so that they are also present as sulphates or bisulphites.
- the leach slurry is released to near atmospheric pressure and heated in an atmospheric S0 2 stripping step 16, to decompose the metal bisulphites according to the following reaction:
- step 16 where M represents a metal, such as Fe, Ni, Co, Mg and Mn.
- M represents a metal, such as Fe, Ni, Co, Mg and Mn.
- part of the insoluble metal sulphates formed in step 16 is recycled to the S0 2 absorption step 12 to facilitate the absorption by the following buffering reaction (but this step is optional)
- the slurry is then subjected to oxidation and hydrolysis (oxydrolysis) 20 to precipitate iron as jarosite with concurrent generation of free sulphuric acid and iron (III) sulphate:
- the product of the oxyhydrolysis step 20 is passed to a thickener 22 and part of the acidic solution is recycled to effect the reaction step 18. If desired, the jarosite can be separated in an optional liquid/solid separation step at this stage for disposal or use.
- the balance of the oxydrolysis product is treated in a neutralization step 24 with acid neutralizing material, advantageously saprolite or garnierite containing nickel and cobalt, to precipitate remaining iron as jarosite:
- acid neutralizing material advantageously saprolite or garnierite containing nickel and cobalt
- MgO represents active magnesia from the saprolite or garnierite.
- Other acid neutralizing materials such as limestone or dolomite can also be used. If the neutralization 24 is carried out in seawater or water containing significant amounts of a monovalent cation(s), jarosite precipitation is facilitated by, for example:
- the neutralization step 24 is followed by a liquid/solid separation 26, to separate the jarosite and to produce a pregnant solution containing nickel and cobalt ions in solution, as indicated at 28.
- Nickel and cobalt may be recovered from the solution 28 by one or a combination of known methods, such as sulphide precipitation, liquid ion exchange, i.e. solvent extraction and stripping or hydrous oxide and/or carbonate precipitation, which may optimally be followed by ammonia leaching and separate recovery of nickel- cobalt salts or metals.
- known methods such as sulphide precipitation, liquid ion exchange, i.e. solvent extraction and stripping or hydrous oxide and/or carbonate precipitation, which may optimally be followed by ammonia leaching and separate recovery of nickel- cobalt salts or metals.
- the S0 2 absorption step 12 is carried out in two stages 30 and 32, as shown in Figure 2.
- the first stage 30 is carried out with an S0 2 - N 2 mixture typically generated by the burning of sulphur or roasting of sulphide minerals in air or oxygen enriched air.
- the second stage 32 is carried out with 100% SO- recycled from the steam stripping step 16 and the reaction step 18.
- the gas from the first SO- absorption stage 30 is subjected to a S0 2 scrubbing step 33 to provide a gas which can be vented to atmosphere.
- a S0 2 scrubbing step 33 to provide a gas which can be vented to atmosphere.
- the SO- is converted to H 2 S0 4 which is used in the reaction step 18.
- the process will now be described in more detail, by way of example, with reference to Figures 3 to 5.
- laterite ore is transferred from a stockpile 34 or directly from a mine truck 36 to a dump pocket 38 where it is slurried, as shown at 40, with salt water or sea water, or fresh water to which a source of monovalent jarosite stabilizing cations is added.
- the source of jarosite stabilizer is advantageously added after the thickener 56, which will be referred to below.
- the slurry is passed to a rotary scrubber 41.
- a trommel screen 42 on the scrubber 41 and sieve bends and cyclone the ore is separated into primary fines 44, typically 0.5 mm, which is the limonite fraction of the ore, and oversize 46, which is mainly saprolite, i.e., partially weathered, high magnesium material, which is conveyed to a stockpile 47.
- the primary fines 44 are passed by a secondary screen 48, where further oversize is separated and conveyed to the stockpile 47.
- the secondary fines from the screen 48 go to a pump box 50 from where they are pumped by pump 52 to a cyclone 54 for further separation in fines and oversize.
- the fines from the overflow of the cyclone 54 are passed to the thickener 56.
- the oversize from the cyclone underflow pass by a tertiary screen 62 where oversize is separated which is passed to the jarosite precipitation step 92 for utilization.
- the fines from the screen 62 go to pump box 64 from where they are pumped by pump 66 to the thickener 56.
- the fine slurry of limonite which is passed to the thickener 56 is dilute and it is thickened or concentrated in the thickener 56 for pipeline transfer to an S0 2 absorption stage, as indicated at 58.
- the thickener overflow i.e. seawater diluted by the fresh water content of the raw ore, is discarded, as shown at 60.
- the limonite slurry from the thickener 56 is fed to a counter- current absorption tower 68 where it contacts S0 2 from an S0 2 /N 2 mixture of about 20% S0 2 and about 80% N 2 , which is also fed to the tower 68, as indicated at 70.
- the slurry, ' now in equilibrium with the SO- gas passes to a second ⁇ ountercurrent absorption tower 72 to which is fed essentially 100% S0 2 gas from the S0 2 stripping of reduction autoclave product which is a later stage in the process and which will be described below.
- the slurry now equilibrates with the 100% SO- gas in the tower 72.
- Gas exhausting from the first countercurrent tower 68 has residual S0 2 which must be scrubbed out before the gas can be exhausted.
- the S0 2 is reacted with excess air in an iron sulphate solution a shown as 74, to generate sulphuric acid, leaving an SO- free vent gas.
- the sulphuric acid produced is reacted with the FeS0 3 slurry from the S0 2 stripping step 80, which will be described below, for the optimization of SO- recovery.
- the limonite slurry now saturated with S0 2 at or slightly above atmospheric pressure, passes to a reduction leach autoclave 76, where heat, such as in the form of steam, is supplied to accelerate or facilitate process reaction (1) above.
- the autoclave 76 operates at 180-212°F (80-
- the reduced slurry exiting the autoclave 76 is indicated at 78.
- Figure 5 shows the reduced slurry 78 passing to a series of S0 2 strip tanks 80 operated at slightly above atmospheric pressure in which steam drives off dissolved and reactive S0 2 , e.g.,
- the essentially 100% SO- gas from the strip tanks 80 is cooled in a cooler (not shown) and recycled to the second absorption tower 72, as indicated at 82. .
- the stripped slurry passes to an oxydrolysis autoclave 84 in which reaction with oxygen produces jarosite essentially free of Ni and Co.
- the jarosite is filtered by a drum filter 86 and pumped, by pump 88 to a tailing pond as shown at 90.
- the acidic solution from the filtration is further treated with prepared finely crushed saprolite to eliminate iron in a secondary jarosite precipitation stage, according to reaction aquation (7) above, and as indicated at 92.
- the product of the secondary precipitation stage 92 is passed to a mixing tank 94 and pumped by pump 96 to a drum filter 98 to separate the solids from the secondary separation 92, which solids are disposed of, as indicated at 100.
- the liquid product from the filter 98 is the pregnant solution which is the product of the process containing the nickel and cobalt ions in solution and indicated at 102. While only preferred embodiments of the invention have been described herein in detail, the invention is not limited thereby and modifications can be made within the scope of the attached claims.
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Abstract
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU58888/96A AU5888896A (en) | 1995-06-07 | 1996-06-04 | Process for extraction of nickel and cobalt from laterite or es |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US48170295A | 1995-06-07 | 1995-06-07 | |
US08/481,702 | 1995-06-07 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1996041025A1 true WO1996041025A1 (en) | 1996-12-19 |
Family
ID=23913029
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/CA1996/000364 WO1996041025A1 (en) | 1995-06-07 | 1996-06-04 | Process for extraction of nickel and cobalt from laterite ores |
Country Status (2)
Country | Link |
---|---|
AU (1) | AU5888896A (en) |
WO (1) | WO1996041025A1 (en) |
Cited By (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2798144A1 (en) * | 1999-09-07 | 2001-03-09 | Rech S Geol Et Minieres Brgm B | PROCESS AND DEVICE FOR CONTINUOUS PROCESSING OF COPPER SULFIDE MINERALS |
WO2001029276A1 (en) * | 1999-10-15 | 2001-04-26 | Bhp Minerals International, Inc. | Resin-in-pulp method for recovery of nickel and cobalt from oxidic ore leach slurry |
WO2001032943A2 (en) * | 1999-11-03 | 2001-05-10 | Bhp Minerals International, Inc. | Atmospheric leach process for the recovery of nickel and cobalt from limonite and saprolite ores |
WO2001032944A1 (en) * | 1999-11-03 | 2001-05-10 | Bhp Minerals International, Inc. | Method for leaching nickeliferous oxide ores of high and low magnesium laterites |
WO2002036838A2 (en) * | 2000-10-31 | 2002-05-10 | Curlook Enterprises Inc. | Direct atmospheric leaching of highly-serpentinized saprolitic nickel laterite ores with sulphuric acid |
WO2004031422A1 (en) * | 2002-10-01 | 2004-04-15 | European Nickel Plc | Heap leaching base metals from oxide ores |
EP1752550A1 (en) * | 2004-05-27 | 2007-02-14 | Pacific Metals Co., Ltd. | Method of recovering nickel and cobalt |
EP1777304A1 (en) * | 2004-05-27 | 2007-04-25 | Pacific Metals Co., Ltd. | Method of recovering nickel or cobalt |
WO2007092994A1 (en) * | 2006-02-15 | 2007-08-23 | Andreazza Consulting Pty Ltd | Processing of laterite ore |
WO2011015991A3 (en) * | 2009-08-03 | 2011-05-19 | Anglo Operations Limited | Process for the recovery of metals such as nickel from an iron- containing ore by leaching with acidic sulfate solution |
WO2017185946A1 (en) * | 2016-04-26 | 2017-11-02 | 上海鑫和镍业科技有限公司 | Method for processing low-grade laterite nickel ore and beneficiation method therefor |
JP2019157233A (en) * | 2018-03-15 | 2019-09-19 | 住友金属鉱山株式会社 | Supply blocking system of high pressure steam, and high pressure acid exudation facility with the same |
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Cited By (21)
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WO2001018265A1 (en) * | 1999-09-07 | 2001-03-15 | B.R.G.M. - Bureau De Recherches Geologiques Et Minieres | Method and device for continuous treatment of copper sulphide containing ore by biological leaching |
FR2798144A1 (en) * | 1999-09-07 | 2001-03-09 | Rech S Geol Et Minieres Brgm B | PROCESS AND DEVICE FOR CONTINUOUS PROCESSING OF COPPER SULFIDE MINERALS |
US6350420B1 (en) | 1999-10-15 | 2002-02-26 | Bhp Minerals International, Inc. | Resin-in-pulp method for recovery of nickel and cobalt |
WO2001029276A1 (en) * | 1999-10-15 | 2001-04-26 | Bhp Minerals International, Inc. | Resin-in-pulp method for recovery of nickel and cobalt from oxidic ore leach slurry |
US6680035B2 (en) | 1999-11-03 | 2004-01-20 | Bhp Minerals International Inc. | Atmospheric leach process for the recovery of nickel and cobalt from limonite and saprolite ores |
WO2001032943A3 (en) * | 1999-11-03 | 2001-09-27 | Bhp Minerals Int Inc | Atmospheric leach process for the recovery of nickel and cobalt from limonite and saprolite ores |
WO2001032944A1 (en) * | 1999-11-03 | 2001-05-10 | Bhp Minerals International, Inc. | Method for leaching nickeliferous oxide ores of high and low magnesium laterites |
US6379636B2 (en) | 1999-11-03 | 2002-04-30 | Bhp Minerals International, Inc. | Method for leaching nickeliferous laterite ores |
WO2001032943A2 (en) * | 1999-11-03 | 2001-05-10 | Bhp Minerals International, Inc. | Atmospheric leach process for the recovery of nickel and cobalt from limonite and saprolite ores |
WO2002036838A2 (en) * | 2000-10-31 | 2002-05-10 | Curlook Enterprises Inc. | Direct atmospheric leaching of highly-serpentinized saprolitic nickel laterite ores with sulphuric acid |
WO2002036838A3 (en) * | 2000-10-31 | 2002-09-26 | Walter Curlook | Direct atmospheric leaching of highly-serpentinized saprolitic nickel laterite ores with sulphuric acid |
WO2004031422A1 (en) * | 2002-10-01 | 2004-04-15 | European Nickel Plc | Heap leaching base metals from oxide ores |
EP1777304A1 (en) * | 2004-05-27 | 2007-04-25 | Pacific Metals Co., Ltd. | Method of recovering nickel or cobalt |
EP1752550A1 (en) * | 2004-05-27 | 2007-02-14 | Pacific Metals Co., Ltd. | Method of recovering nickel and cobalt |
EP1777304A4 (en) * | 2004-05-27 | 2008-12-24 | Pacific Metals Co Ltd | Method of recovering nickel or cobalt |
EP1752550A4 (en) * | 2004-05-27 | 2008-12-31 | Pacific Metals Co Ltd | Method of recovering nickel and cobalt |
WO2007092994A1 (en) * | 2006-02-15 | 2007-08-23 | Andreazza Consulting Pty Ltd | Processing of laterite ore |
WO2011015991A3 (en) * | 2009-08-03 | 2011-05-19 | Anglo Operations Limited | Process for the recovery of metals such as nickel from an iron- containing ore by leaching with acidic sulfate solution |
WO2017185946A1 (en) * | 2016-04-26 | 2017-11-02 | 上海鑫和镍业科技有限公司 | Method for processing low-grade laterite nickel ore and beneficiation method therefor |
JP2019157233A (en) * | 2018-03-15 | 2019-09-19 | 住友金属鉱山株式会社 | Supply blocking system of high pressure steam, and high pressure acid exudation facility with the same |
JP7047502B2 (en) | 2018-03-15 | 2022-04-05 | 住友金属鉱山株式会社 | High-pressure steam supply cutoff system and high-pressure acid leaching equipment equipped with this system |
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