WO2009108993A1 - Process for metal seperation using resin-in-pulp or resin-in-solution processes - Google Patents
Process for metal seperation using resin-in-pulp or resin-in-solution processes Download PDFInfo
- Publication number
- WO2009108993A1 WO2009108993A1 PCT/AU2009/000221 AU2009000221W WO2009108993A1 WO 2009108993 A1 WO2009108993 A1 WO 2009108993A1 AU 2009000221 W AU2009000221 W AU 2009000221W WO 2009108993 A1 WO2009108993 A1 WO 2009108993A1
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- WO
- WIPO (PCT)
- Prior art keywords
- resin
- solution
- slurry
- vessel
- metal
- Prior art date
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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
- C22B3/02—Apparatus therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J39/00—Cation exchange; Use of material as cation exchangers; Treatment of material for improving the cation exchange properties
- B01J39/04—Processes using organic exchangers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J41/00—Anion exchange; Use of material as anion exchangers; Treatment of material for improving the anion exchange properties
- B01J41/04—Processes using organic exchangers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J47/00—Ion-exchange processes in general; Apparatus therefor
- B01J47/14—Controlling or regulating
- B01J47/15—Controlling or regulating for obtaining a solution having a fixed pH
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
- B01J49/05—Regeneration or reactivation of ion-exchangers; Apparatus therefor of fixed beds
-
- 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
- C22B15/0084—Treating solutions
- C22B15/0089—Treating solutions 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
- C22B23/04—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
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/42—Treatment or purification of solutions, e.g. obtained by leaching by ion-exchange extraction
-
- 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
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
-
- 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 a process for metal separation using resin-in-pulp (RIP) or resin-in-solution (RIS) processes.
- a number of mining and downstream processing technologies applied to run of mine ores result in the formation of soluble metal containing solutions and pulps (slurries). Some of these solutions or pulps arise from intentional processes (such as leaching and other mineral processing and hydrometallurgical processing technologies) while others may arise from water run-off from tailings dams, waste rock dumps and the like, and may accumulate in abandoned mining pits or be discharged into the surrounding environment.
- Solutions and slurries produced by leaching or other hydrometallurgical processes typically contain one or more soluble valuable metals (in the form of dissolved metal ions), together with one or more soluble impurity components.
- a number of processes are available to separate and recover the valuable metals. These include precipitation, solvent extraction, adsorption and use of ion exchange resins. In the case of ion exchange resins, it is possible to use clarified solutions (known as resin-in-solution) or to directly treat the pulp or slurry (known as resin-in-pulp).
- ion exchange processes such as resin-in-pulp and resin-in-solution processes
- resin-in-pulp and resin-in-solution processes are best applied to solutions and slurries that have relatively low soluble metal concentrations and/or contain soluble metals that have a high intrinsic value.
- metals having a high intrinsic value include gold, uranium and platinum group metals.
- resin-in-pulp and resin-in-solution processes are frequently used in the processing of gold ores and uranium ores.
- Resin-in-pulp and resin-in-solution processes are not normally used for the treatment or recovery of base metals.
- concentration of the dissolved metal is normally much higher than would be experienced in the recovery of gold or uranium.
- the ion exchange resin Due to the high concentration of dissolved valuable metal, the ion exchange resin has to undergo much more frequent cycling through loading with the desired metal ions and regeneration by removing or stripping the metal ions from the resin. More frequent cycling of the resin normally results in more rapid attrition or breakdown of the resin. This, in turn, leads to increased costs for fresh or replacement resin.
- the solid resin needs to be physically transferred in a manner that optimises its efficiency and selectivity for metal removal/recovery and in a manner that minimises the physical and chemical degradation of the solid ion exchange resin through various means such as attrition and/or osmotic shock.
- the present invention provides a process for the treatment of solutions or slurries containing dissolved metals comprising the steps of:
- step (d) transferring regenerated resin from step (d) back to step (a).
- the process further comprises washing the loaded resin to remove entrained solids, solution or slurry prior to step (c) ;
- step (a) results in the resin being introduced into the vessel or column below the surface of the solution or slurry in the vessel or column. This is advantageous in that it assists in mixing and contacting the resin with the solution or slurry. Further, the amount of agitation required to mix the resin with the solution or slurry is minimised which, in turn, minimises attrition of the resin caused by such mixing.
- the slurry or solution may be subjected to a pre-treatment that removes oversize particles and other contaminants therefrom prior to contacting or mixing the slurry or solution with the resin.
- the pre- treatment step may comprise any known treatment step that can remove oversized particles from slurries or solutions. Examples include screening, settling, sedimentation, clarification, hydrocyclones, centrifuging and the like. It is envisaged that pre-screening is the likely treatment to be used in commercial applications of such embodiments of the present invention, but other pre-treatment steps also fall within the scope of the present invention.
- the pre-treatment step to remove any oversized particles and other contaminants stops oversize particles and other contaminants from accumulating in the process circuit. Furthermore, oversize particles and other contaminants tend to increase the attrition of resin particles as the oversize particles may act like grinding media. Therefore, removal of oversize particles and other contaminants will act to minimise attrition of the resin particles.
- the mixing of resins with pulps has historically been achieved by means of air mixers, such as air mixed pachucas. Whilst physical attrition of the resin beads may generally be at an acceptably low level, the operating costs associated with provision of the air supply are often unsustainable in economic terms. The present inventors have found that mechanically agitated mixers may be used in embodiments of the present invention.
- the maximum tip speed of the mixing blades be sufficiently low that physical attrition of the resin beads is minimised. Accordingly, in embodiments of the present invention, it is preferred that low speed and/or low shear mechanical mixers be used to mix the resin with the solution or slurry.
- the desired tip speed of the agitators will depend somewhat on the strength and attrition resistance of the resin being used.
- the agitator design and tip speed are desirably controlled such that a balance between avoidance of "sanding out” (which results in the heavier particles in the pulp settling out) and excessive agitation of the resin is achieved. In some embodiments, with the tip speed of the agitator may be less than 4.0 m/sec, more preferably less than 3.8m/sec.
- pulps and solutions to be treated may require the addition of specific reagents to adjust the pH of the solution/pulp to ensure that the target metal(s) remain in solution while at the same time ensuring that the ion exchange resin is operating within its optimal pH range for metal uptake.
- it may be appropriate to adjust the operating pH to remove potentially interfering non- target soluble metal ions by in-situ precipitation.
- a typical example is the removal of soluble ferric ions by increasing the pH of the solution/pulp to a value typically in the range of about 2.8 to 3.8.
- addition of the neutralising agent generally causes solids to form in the solution and/or increase the percentage of solids when using the RIP mode of operation.
- limestone or other solid neutralising agent is used as the acid neutralising agent, it is preferable to screen out any oversize particles before the pH adjusted solution or pulp is forwarded to the ion exchange circuit. If this oversize material is not removed by this pre-screening step then there may be problems encountered with the resin screening process itself.
- embodiments of the present invention that include the addition of solid reagents or solid reactants to the process may further include a step of treating, such as screening, the solid reagent or solid reactants to remove oversized material therefrom prior to mixing the reagents or reactants with the solution or slurry.
- the present invention encompasses the use of a wide variety of resins.
- selection of resins takes into account both the chemical and physical performance of the resin.
- the resin will typically show selectivity for removing the desired metal ion from solution.
- the resin will also desirably have mechanical properties that limit or minimise attrition of the resin. In some instances, the mechanical strength of the resin may be increased during manufacture of the resin. In some instances, this may adversely impact on the chemical performance or selectivity of the resin.
- the selectivity, loading capacity and elution characteristics of the resin may be tailored to the type and concentration of both the soluble value and the soluble non-value constituents of the solution and/or slurry being processed.
- the selectivity of the resin is simply controlled by the operating pH so that it is possible to separate out the desired metal(s) by a relatively simple pH control procedure.
- the particle size of the resin may suitably have a narrow size range. This is desirable as it allows for efficient separation of the resin from the solution or pulp or slurry.
- soluble iron removal is required and achieved by pH adjustment it may be necessary to oxidise any ferrous iron to the ferric state in order to induce precipitation of the soluble iron.
- mechanically agitated mixers may be supplemented with a suitable air/slurry contactor system to facilitate the oxidation of ferrous iron to the ferric state.
- the loaded resin is separated from the treated solution and/or pulp by use of one or more screens.
- the selection of the optimum resin sizing and resin particle size distribution may be such as to maximise recovery of the loaded resin while at the same time minimising the energy and water washing requirements. If the resin screen size is too large, excessive amounts of loaded resin are lost out of the circuit. If the resin screen size is too small, excessive amount of solids will be recovered along with the loaded resin, leading to a much high level of water washing being required.
- transfer of the resin may be achieved using dense phase hydraulic conveying.
- dense phase hydraulic conveying One example of a suitable dense phase hydraulic conveying process is described in European patent number 0129999, the entire contents of which are here incorporated by cross reference.
- transfer of the resin may be achieved using water eduction, low shear recessed impellers, or peristaltic pumps.
- the selection of the transfer method may depend upon the volume of resin required to be transferred. It may be desirable to keep the percentage of resin solids in the solution or pulp below 50%, or even below 40%, in order to minimise attrition during transfer. However, many resin in pulp systems face water balance issues and consequently resin transfer using large volumes of water is undesirable. However, transferring the resins using large volumes of water and recovering or recycling the water in a closed or partially closed loop enables the resin to be transferred as a relatively low percentage solids slurry without impacting on the water balance of the main processing plant.
- various steps in the process may be conducted such that there is an upflow of water or solution which causes fluidisation or entrainment of the resin in the upflowing liquid.
- Figure 1 shows a process flow sheet of an embodiment of the present invention
- Figure 2 shows a flow sheet of a single resin type, split elution circuit in accordance with an embodiment of the present invention
- Figure 3 shows a flow sheet of a two resins, split elution circuit in accordance with an embodiment of the present invention.
- Figure 1 The following description of a presently preferred but non-limiting embodiment of the invention refers to the overall process outlined in Figure 1.
- this Figure is of a generic nature and all those skilled in the art will understand and acknowledge that there are a number of variations possible that comply with the overall concept of the invention.
- Figure 1 is limited to the treatment and recovery of a single target metal by means of a single resin and a single elution stage with a single eluant.
- the metal-bearing solution or slurry [1] is pumped by conventional means [2] to a pre- screening stage [3] where any oversize material is removed as waste [4].
- a suitable neutralising/pH control reagent [5] which may or may not be supplemented by air sparging to induce oxidation of ferrous iron to the ferric state, may be added directly to the metal-bearing solution or slurry [1] and/or as the metal-bearing solution or slurry is pumped to the pre-screening stage [2] and/or at the pre-screening stage [3] and/or as the pre-screened metal bearing solution or slurry is conveyed to the RIS/RIP circuit [10] and/or at the RIS/RIP circuit [7].
- Recycled resin [6] is added to the RIS/RIP circuit [7] by means of a wet dense phase conveying system [8] together with any resin make-up requirement [9], the pre- screened and optionally pH adjusted feed solution or slurry [10], and any neutralising/pH control reagent [5] required to maximise loading of the target metal onto the selected resin.
- Mixing of the resin with the incoming solution or slurry and any neutralising/pH control reagent is achieved via mechanical methods supplemented by air sparging for oxidation of ferrous iron to the ferrous state if required.
- the RIS/RIP circuit [7] may be designed and operated in conventional sequential column, fluidised bed or carousel modes, the choice depending to a large extent on volume flows, loading and eluting kinetics, and solids densities.
- the metal-loaded resin and the depleted solution or pulp [11] are transferred to the loaded resin screening stage [12].
- the screened loaded resin [13] is transferred by means of the wet dense phase conveying system [8] to the resin washing stage [14] and then to the resin elution stage [13] where the loaded, washed resin is contacted with the appropriate eluent [15].
- the metal-rich eluate [16] is forwarded to the metal recovery circuit [17].
- the eluted, metal-free resin [18] is transferred by means of wet dense phase conveyance system [8] to the resin transfer system [6] for ultimate transfer to the RIS/RIP circuit [7].
- the metal-depleted solution or pulp [19] exiting the loaded resin screening stage [12] is treated by a combination of steps [20] for the safe disposal of all solids and solutions and comprises of appropriate neutralisation and solid/liquid separation stages.
- FIG. 2 shows a flow sheet of a single resin type, split elution circuit in accordance with an embodiment of the present invention.
- a leach liquor containing dissolved metals for example, containing dissolved copper, nickel and cobalt
- a resin for example, containing dissolved copper, nickel and cobalt
- These contacting vessels are denoted by reference numerals 102, 104, 106, 108, 110 and 1 12.
- the resin and liquor are contacted with each other in counter current flow.
- the contacting circuit is effectively divided into two stages.
- the first stage includes vessels 102, 104 and 106.
- Regenerated resin from first elution column 114 is fed to contacting vessel 106 via line 116.
- the resin is transferred from the vessel 106 to vessel 104 via dense phase hydraulic conveying apparatus 118.
- the resin is transferred from vessel 104 to vessel 102 by dense phase hydraulic conveying apparatus 120.
- the resin from vessel 102 is transferred to the elution column 114 via dense phase hydraulic conveying apparatus 122.
- dense phase hydraulic conveying apparatus to transfer the resin assists in minimising attrition of the resin.
- the leach liquor 100 is initially fed to vessel 102. Liquor overflow from vessel 102 is transferred to vessel 104. Similarly, liquor overflow from vessel 104 is transferred to vessel 106.
- a neutralising agent such as a limestone slurry
- a neutralising agent is fed to respective vessels 102, 104, 106 by respective lines 124, 126, 128.
- Each vessel 102, 104, 106 is also provided with a low speed and/or low shear agitator 130, 132, 134, respectively.
- the agitators ensure good mixing and contact between the liquor and the resin whilst also maintaining the pulp in suspension. At the same time, due to the design and speed of the agitators, attrition of the resin is minimised.
- the loaded resin leaving vessel 102 is transferred via line 103 to the first elution column 114.
- acid 136 is mixed with the resin to selectively elute the metal loaded onto the resin.
- copper is loaded onto the resin in vessels 102, 104, 106 by controlling the pH to between 2.5 and 3.5 and utilising a resin that selectively takes up copper from solution in that pH range.
- the liquor 138 leaving vessel 106 is depleted in copper but still contains nickel and cobalt.
- Liquor 138 is fed to vessel 108 and thereafter to vessels 110 and 112.
- Resin (either regenerated or fresh resin) is fed via line 140 to vessel 112 and thereafter by respective dense phase hydraulic conveying apparatus 144, 146 (respectively) to vessel 110 and then to vessel 108.
- Loaded resin is transferred via dense phase conveying apparatus 148 to second elution column 150.
- a neutralising agent such as a limestone slurry, is fed via respective lines 152, 154, 156 to each of the vessels 108, 110, 112, respectively.
- the pH conditions in vessels 108, 1 10, 112 are such that nickel and cobalt are selectively taken up by the resin.
- the pH may be controlled to fall within the range of 3.5 to 4.5.
- the loaded resin that is fed via line 158 to second elution column 150 is loaded with copper and nickel.
- the elution conditions in elution column 150 are such that nickel and cobalt are edited from the resin.
- FIG. 3 shows a flow sheet of a two resins - split elution circuit.
- an acidic leach liquor 200 containing dissolved copper, nickel and cobalt is fed to the first stage of a metals recovery circuit.
- the first stage comprises contacting vessels 202, 204, 206 and 208.
- a first resin is contacted in counter current fashion using similar dense phase hydraulic conveying apparatus as described with reference to figure 2.
- the liquor overflows each upstream vessel into a downstream vessel in a manner similar to that described with reference to figure 2. Again, for brevity of description, this need not be described further.
- Low speed agitators are provided in each vessel to maintain the slurry in suspension and to minimise attrition.
- a neutralising agent is fed to each vessel via respective lines 210, 212, 214, 216.
- a resin that selectively removes one of the metals in solution is used.
- iminodiacetic resin which shows a good uptake of copper
- nickel and a poor uptake of cobalt may be used, with the pH conditions in the first stage being such that copper is selectively taken up by the resin.
- the loaded resin provided via line 218 to elution column 220 is loaded with copper.
- Acid supplied via line 222 is used to elute the copper from the resin and to regenerate the resin.
- the liquor 224 that is depleted in copper, is fed to the second part of the process, which comprises contacting vessels 230, 232.
- a resin that shows a good uptake of nickel and copper is used to remove the nickel and copper from the liquor.
- dense phase hydraulic conveying is used to transfer the resin.
- low speed agitators that minimise attrition of the resin are used.
- a neutralising agent is fed to the respective vessels in the second part via lines 226, 228.
- the resin that is used in the second stage of the process may comprise bospicolyamine resin.
- This resin exhibits a very strong uptake of copper (indeed, so strong that copper is difficult to remove from this resin).
- copper has been removed in the first stage of the process.
- This resin also shows a good uptake of nickel and cobalt, thus making it suitable for use in removing those metals from solution in the second stage.
- This resin is an expensive resin. Therefore, it is used for residual nickel and cobalt recovery after copper has been selectively removed from the liquor in the first stage of the process.
- the loaded resin from vessel 230 is fed via line 234 to elution column 236.
- the loaded resin is contacted with acid 238 to cause elution of the nickel and cobalt from the resin and to form a regenerated resin.
- the regenerated resin is transferred via line 240 back to vessel 232.
- makeup resin may be provided in order to maintain resin balance in light of losses of resin.
- the eluted metal streams may be treated to recover metal therefrom using any process is known to be suitable for that use.
- Ferrous hydroxide does not form a dense, easy to settle/dewater solid precipitate and therefore acidic tail solutions being neutralised are frequently aerated using air or oxygen sparging to convert ferrous to ferric and preferentially precipitate ferric hydroxides. pH control is also used to assist in achieving precipitation of ferric hydroxides.
- Air mixing resin in circuits causes less attrition compared with mechanical agitation but air mixing is an expensive operating cost and most plants now use mechanical mixing rather than air mixing.
- the present invention envisages that the air sparging and design of the contactor can be modified to achieve both duties, i.e. ferrous to ferric conversion and air mixing of the resin with the pulp.
- the two or more types of resin may be contained within separate columns.
- the two or more types of resin may be mixed together and contained within the same column or columns - enhanced efficiency of the RIP and RIS processes by means of appropriate temperature control of the incoming feed pulps or solutions and/or of the resin columns in their loading and/or washing and/or eluting duties.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Mechanical Engineering (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Geology (AREA)
- Geochemistry & Mineralogy (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
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Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2009221628A AU2009221628A1 (en) | 2008-03-03 | 2009-02-26 | Process for metal seperation using resin-in-pulp or resin-in-solution processes |
US12/921,020 US20110030508A1 (en) | 2008-03-03 | 2009-02-26 | Process for Metal Seperation Using Resin-in-Pulp or Resin-in-Solution Processes |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2008901030 | 2008-03-03 | ||
AU2008901030A AU2008901030A0 (en) | 2008-03-03 | An Improved Method of Optimisation of Metal Separation by Means of Resin-in-Pulp and Resin-in-Solution Processes |
Publications (1)
Publication Number | Publication Date |
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WO2009108993A1 true WO2009108993A1 (en) | 2009-09-11 |
Family
ID=41055472
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/AU2009/000221 WO2009108993A1 (en) | 2008-03-03 | 2009-02-26 | Process for metal seperation using resin-in-pulp or resin-in-solution processes |
Country Status (3)
Country | Link |
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US (1) | US20110030508A1 (en) |
AU (1) | AU2009221628A1 (en) |
WO (1) | WO2009108993A1 (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102345020A (en) * | 2011-10-19 | 2012-02-08 | 攀钢集团攀枝花钢铁研究院有限公司 | Method for separating and recycling vanadium and chromium in solution |
CN105779782A (en) * | 2016-04-05 | 2016-07-20 | 昆明理工大学 | Pulp gold extracting process with steps divided in thin pulp screening mode |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
BR112013014005B1 (en) | 2010-12-07 | 2020-01-28 | Barrick Gold Corp | gold and / or silver leaching method |
CA2870199A1 (en) | 2012-05-01 | 2013-11-07 | Dow Global Technologies Llc | Nickel and cobalt recovery using continuous ion exchange |
US10161016B2 (en) | 2013-05-29 | 2018-12-25 | Barrick Gold Corporation | Method for pre-treatment of gold-bearing oxide ores |
US9952944B1 (en) | 2016-10-25 | 2018-04-24 | Sandisk Technologies Llc | First read solution for memory |
PE20211512A1 (en) | 2019-01-21 | 2021-08-11 | Barrick Gold Corp | METHOD FOR CARBON-CATALYZED THOSULFATE LEACHING OF MATERIALS CONTAINING GOLD |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB775415A (en) * | 1954-10-05 | 1957-05-22 | Commw Scient Ind Res Org | Improved method and means for extracting an adsorbable solute from a suspension of finely divided solids in a solution |
US4279755A (en) * | 1980-02-26 | 1981-07-21 | Alexander Himsley | Continuous countercurrent ion exchange process |
US6716344B1 (en) * | 2000-10-02 | 2004-04-06 | The University Of Western Ontario | Liquid-solids circulating fluidized bed |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0129999A3 (en) * | 1983-06-17 | 1986-04-30 | Exxon Research And Engineering Company | A dense phase hydraulic lift process |
-
2009
- 2009-02-26 US US12/921,020 patent/US20110030508A1/en not_active Abandoned
- 2009-02-26 AU AU2009221628A patent/AU2009221628A1/en not_active Abandoned
- 2009-02-26 WO PCT/AU2009/000221 patent/WO2009108993A1/en active Application Filing
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB775415A (en) * | 1954-10-05 | 1957-05-22 | Commw Scient Ind Res Org | Improved method and means for extracting an adsorbable solute from a suspension of finely divided solids in a solution |
US4279755A (en) * | 1980-02-26 | 1981-07-21 | Alexander Himsley | Continuous countercurrent ion exchange process |
US6716344B1 (en) * | 2000-10-02 | 2004-04-06 | The University Of Western Ontario | Liquid-solids circulating fluidized bed |
Non-Patent Citations (1)
Title |
---|
ZAINOL, ZAIMAWATI: "PhD Thesis", 2005, MURDOCH UNIVERSITY, WESTERN AUSTRALIA, article "The development of a Resin-in-pulp process for the recovery of nickel and cobalt from laterite leach slurries" * |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102345020A (en) * | 2011-10-19 | 2012-02-08 | 攀钢集团攀枝花钢铁研究院有限公司 | Method for separating and recycling vanadium and chromium in solution |
CN105779782A (en) * | 2016-04-05 | 2016-07-20 | 昆明理工大学 | Pulp gold extracting process with steps divided in thin pulp screening mode |
Also Published As
Publication number | Publication date |
---|---|
US20110030508A1 (en) | 2011-02-10 |
AU2009221628A1 (en) | 2009-09-11 |
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