AU2004233790A1 - Interlaced series parallel configuration for metal solvent extraction plants - Google Patents
Interlaced series parallel configuration for metal solvent extraction plants Download PDFInfo
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- AU2004233790A1 AU2004233790A1 AU2004233790A AU2004233790A AU2004233790A1 AU 2004233790 A1 AU2004233790 A1 AU 2004233790A1 AU 2004233790 A AU2004233790 A AU 2004233790A AU 2004233790 A AU2004233790 A AU 2004233790A AU 2004233790 A1 AU2004233790 A1 AU 2004233790A1
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- organic phase
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- copper
- solution
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- 229910052751 metal Inorganic materials 0.000 title claims description 84
- 239000002184 metal Substances 0.000 title claims description 84
- 238000000638 solvent extraction Methods 0.000 title description 5
- 239000012074 organic phase Substances 0.000 claims description 75
- 239000010949 copper Substances 0.000 claims description 65
- 238000000605 extraction Methods 0.000 claims description 63
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 60
- 229910052802 copper Inorganic materials 0.000 claims description 60
- 239000000243 solution Substances 0.000 claims description 59
- 238000000034 method Methods 0.000 claims description 52
- 239000003153 chemical reaction reagent Substances 0.000 claims description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 18
- 239000000203 mixture Substances 0.000 claims description 17
- 239000002904 solvent Substances 0.000 claims description 10
- 150000001412 amines Chemical class 0.000 claims description 9
- 239000007864 aqueous solution Substances 0.000 claims description 9
- 238000009472 formulation Methods 0.000 claims description 9
- FZENGILVLUJGJX-NSCUHMNNSA-N (E)-acetaldehyde oxime Chemical compound C\C=N\O FZENGILVLUJGJX-NSCUHMNNSA-N 0.000 claims description 8
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 8
- 239000011260 aqueous acid Substances 0.000 claims description 6
- 239000003607 modifier Substances 0.000 claims description 6
- 239000008346 aqueous phase Substances 0.000 claims description 5
- 229910017052 cobalt Inorganic materials 0.000 claims description 5
- 239000010941 cobalt Substances 0.000 claims description 5
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 5
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 4
- 229910052770 Uranium Inorganic materials 0.000 claims description 4
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims description 4
- 229910052750 molybdenum Inorganic materials 0.000 claims description 4
- 239000011733 molybdenum Substances 0.000 claims description 4
- 229910052759 nickel Inorganic materials 0.000 claims description 4
- -1 organo phosphonic acid Chemical compound 0.000 claims description 4
- JFALSRSLKYAFGM-UHFFFAOYSA-N uranium(0) Chemical compound [U] JFALSRSLKYAFGM-UHFFFAOYSA-N 0.000 claims description 4
- 229910052725 zinc Inorganic materials 0.000 claims description 4
- 239000011701 zinc Substances 0.000 claims description 4
- 150000001732 carboxylic acid derivatives Chemical class 0.000 claims description 3
- 238000005363 electrowinning Methods 0.000 claims description 3
- ACVYVLVWPXVTIT-UHFFFAOYSA-N phosphinic acid Chemical compound O[PH2]=O ACVYVLVWPXVTIT-UHFFFAOYSA-N 0.000 claims description 3
- 239000012071 phase Substances 0.000 claims description 2
- 239000002253 acid Substances 0.000 claims 2
- 238000011084 recovery Methods 0.000 description 11
- 238000010586 diagram Methods 0.000 description 8
- 238000002386 leaching Methods 0.000 description 8
- 239000000284 extract Substances 0.000 description 6
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000003792 electrolyte Substances 0.000 description 4
- 150000002739 metals Chemical class 0.000 description 4
- BWZOPYPOZJBVLQ-UHFFFAOYSA-K aluminium glycinate Chemical compound O[Al+]O.NCC([O-])=O BWZOPYPOZJBVLQ-UHFFFAOYSA-K 0.000 description 3
- 150000003512 tertiary amines Chemical class 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 235000011149 sulphuric acid Nutrition 0.000 description 2
- MJUVQSGLWOGIOB-UHFFFAOYSA-N 2-[(Z)-hydroxyiminomethyl]-4-nonylphenol Chemical compound OC1=C(C=N/O)C=C(C=C1)CCCCCCCCC MJUVQSGLWOGIOB-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 239000003929 acidic solution Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 150000001991 dicarboxylic acids Chemical class 0.000 description 1
- 150000005690 diesters Chemical class 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 150000002923 oximes Chemical class 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 150000003504 terephthalic acids Chemical class 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
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/02—Apparatus therefor
-
- 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
- C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
-
- 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
-
- 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
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Manufacturing & Machinery (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Extraction Or Liquid Replacement (AREA)
Description
WO 2004/096400 PCT/US2004/010706 TITLE OF THE INVENTION Interlaced Series Parallel Configuration for Metal Solvent Extraction Plants CROSS-REFERENCE TO RELATED APPLICATIONS This application claims the benefit of copending provisional 5 application serial number 60/463,243, filed on April 16, 2003, the entire contents of which is incorporated herein by reference. BACKGROUND OF THE INVENTION Various metals can be recovered from their ores by leaching. Leaching is accomplished by contacting ore-containing rock with an aqueous 10 acidic solution. A metal of choice can be obtained from a body of ore which contains a mixture of metals in addition to the desired metal. The leaching medium dissolves salts of the desired metal and other metals as it trickles through the ore, to provide an aqueous solution of the mixture of metal values. The metal values are usually leached with a sulfuric acid medium, 15 providing an acidic aqueous solution, but can also be leached by ammonia to provide a basic aqueous solution. The aqueous leaching solution is mixed in tanks with an extraction reagent which is dissolved in an organic solvent, e.g., a kerosene. The reagent includes an extractant chemical which forms a metal-extractant 20 complex with the desired metal ions in preference to ions of other metals. The step of forming the complex is called the extraction or loading stage of the solvent extraction process. The nature of the extractant depends upon the metal to be extracted and the nature of the leach solution. For example, zinc can be extracted with di-2-ethylhexylphosphoric acid, uranium using a 1 WO 2004/096400 PCT/US2004/010706 tertiary fatty amine reagent such as ALAMINE® tertiary amine, cobalt as the chloride complex using a tertiary fatty amine reagent such as ALAMINE® tertiary amine, cobalt using an organo phosphonic acid or phosphinic acid, nickel using a carboxylic acid, molybdenum using a tertiary fatty amine 5 reagent such as ALAMINE® tertiary amine. Copper can be extracted with an aldoxime such as 2-hydroxy-5-nonyl benzaldoxime, a ketoxime such as a 2 hydroxy-5-alkylphenyl ketoxime or combinations of aldoximes and ketoximes such as is described in U.S. patent 6,395,062, the entire contents of which are incorporated herein by reference and oximes in combinations with 10 extractant and equilibrium modifiers such as is described in U.S. patents 6,231,784 and 6,177,055, the entire contents of each of which are incorporated herein by reference. New and more economical methods of improving the extraction process are continuously being sought in order to lower costs and improve 15 the quality of the metal produced. BRIEF SUMMARY OF THE INVENTION The present invention is an interlaced series parallel configuration for metal solvent extraction plants. The method is comprised of the steps of: (1) contacting an organic phase comprised of a water insoluble and water 20 immiscible solvent solution of an extraction reagent formulation substantially free of metal values with a first aqueous metal bearing solution to extract at least a portion of the metal into the organic phase to form a metal depleted aqueous raffinate solution and a first partially loaded organic phase wherein the first aqueous metal bearing solution is the raffinate from step (3); (2) 25 contacting the first partially loaded organic phase with a second aqueous 2 WO 2004/096400 PCT/US2004/010706 metal bearing solution to form a metal depleted aqueous raffinate solution and a second partially loaded organic phase having a metal content greater than the first partially loaded organic phase; (3) contacting the second partially loaded organic phase with a third aqueous metal bearing solution to 5 form a partially metal depleted aqueous and a third partially loaded organic phase. A modification of the process according to the invention is a triple interlaced series parallel configuration for metal solvent extraction plants. This method is comprised of the steps of: (1) contacting an organic phase 10 comprised of a water insoluble and water immiscible solvent solution of an extraction reagent formulation substantially free of metal values with a first aqueous metal bearing solution to extract at least a portion of the metal into the organic phase to form a metal depleted aqueous raffinate solution and a first partially loaded organic phase phase wherein the first aqueous metal 15 bearing solution is the raffinate from step (4); (2) contacting the first partially loaded organic phase with a second aqueous metal bearing solution to form a metal depleted aqueous raffinate solution and a second partially loaded organic phase having a metal content greater than the first partially loaded organic phase; (3) contacting the second partially loaded organic phase with 20 a third aqueous metal bearing solution to form a metal depleted aqueous raffinate solution and a third partially loaded organic phase having a metal content greater than the second partially loaded organic phase; (4) contacting the third partially loaded organic phase with a fourth aqueous metal bearing solution to form a partially metal depleted aqueous and a 25 fourth partially loaded organic phase. 3 WO 2004/096400 PCT/US2004/010706 BRIEF DESCRIPTION OF THE SEVERAL VIEWS OF THE DRAWINGS Figure 1 is a flow diagram of a conventional series parallel extraction configuration. Figure 2 is a flow diagram of an interlaced series parallel extraction 5 configuration. Figure 3 is a flow diagram of a conventional series triple parallel extraction configuration. Figure 4 is a flow diagram of an optimized interlaced series parallel special triple extraction configuration. 10 DETAILED DESCRIPTION OF THE INVENTION The process according to the invention can be best understood with reference to the figures. While the process according to the invention can be used in the extraction of any metal including, but not limited to, zinc, uranium, cobalt, nickel, and molybdenum, it will be described with reference 15 to copper, the preferred embodiment. As used herein the abbreviation PLS stands for a copper-rich aqueous leaching solution. The term "partially loaded organic phase" is an organic phase comprised of a water insoluble and water immiscible solvent solution of an extraction reagent formulation containing less than the 20 maximum possible amount of metal values. The term "loaded organic phase" is an organic phase comprised of a water insoluble and water immiscible solvent solution of an extraction reagent formulation containing the maximum possible amount of metal values. The extractant reagent is defined above and, in the case of copper extraction, can include equilibrium modifiers which 25 can be diesters of linear dicarboxylic acids such as linear alcohol esters of 4 WO 2004/096400 PCT/US2004/010706 malonic, adipic, terephthalic acids. The term "stripped organic phase" is an organic phase comprised of a water insoluble and water immiscible solvent solution of an extraction reagent formulation substantially free of copper values. A stripped organic phase is one in which copper values have been 5 removed from a loaded or partially organic phase by contacting the loaded or partially organic phase with aqueous acid thereby transferring substantially all of the copper value from the organic phase to the aqueous phase or it can be fresh, unused organic phase. A raffinate is an aqueous solution which exits an extraction stage and has been at least partially depleted of 10 copper values by an organic phase. Figure 1 depicts a flow diagram for a conventional series parallel extraction line where there is a fixed configuration and the extraction stages are in one row. The PLS is fed to two parallel-connected extraction stages, El and EP. The PLS is extracted in EP by stripped organic and the partially 15 loaded organic is sent to E2 wherein it extracts the raffinate from El. In El, the PLS is extracted and the aqueous from El is fed in series to E2 where it is extracted by the partially loaded organic from EP. The organic from E2 is fed to El where it extracts the PLS. The loaded organic from El is sent to stripping. The PLS is extracted by copper-free organic in EP and by partially 20 loaded organic in El. Figure 2 depicts a flow diagram of an interlaced series parallel extraction line where E2 and EP are juxtaposed. As in the conventional series parallel extraction line, the PLS is fed to two parallel-connected extraction stages, El and EP. In this configuration, the stripped organic is 25 first contacted in E2 by the partially copper depleted aqueous from El. This 5 WO 2004/096400 PCT/US2004/010706 partially loaded organic then advances to the EP stage where it is contacted with a fresh volume of PLS and extracts additional copper. The organic phase then advances to El where it contacts a second stream of fresh PLS to form a fully loaded organic phase. The copper can be recovered from the 5 fully loaded organic by stripping with aqueous acid. The strip aqueous solution resulting from the stripping contains substantially only copper. The pure copper metal can be recovered from the metal loaded stripping solution by electrowinning. This approach results in an overall higher recovery of copper than in the conventional series parallel configuration. This results 10 primarily from the fact that the stripped organic which is a more efficient organic in terms of copper extraction contacts the partially copper depleted aqueous stream coming from El. In a conventional circuit, this stripped organic first passes through the EP stage before entering E2 and extracts a significant amount of copper. It is not as efficient as a stripped organic in 15 terms of achieving a low raffinate in the exiting aqueous raffinate stream. The interlaced series parallel extraction configuration will typically achieve overall recoveries of from about 0.2 to about 5% absolute higher than a conventional series parallel configuration. For a 50,000 metric ton per year plant, a 1% improvement in recovery is equivalent to approximately 20 $1,500,000 in additional revenue at contemporary copper prices. Figure 3 depicts a variation of the conventional series parallel extraction method which is a flow diagram of an series triple parallel extraction configuration having four extraction stages as opposed to three extraction stages depicted in Figure 1. In the series triple parallel extraction 25 configuration, the stripped organic is first contacted in E4 by fresh PLS to 6 WO 2004/096400 PCT/US2004/010706 form a first partially loaded organic and raffinate which is cycled back to the leaching operation. The first partially loaded organic from E4 is then contacted by fresh PLS in E3 to form a second partially loaded organic having a metal value greater than the first partially loaded organic and 5 raffinate which is cycled back to the leaching operation. The second partially loaded organic from E3 is fed to E2 where it is contacted by raffinate from El which is formed by extraction of PLS by the third partially loaded organic from E2. The raffinate from the E2 extraction is cycled back to the leaching operation. 10 Figure 4 depicts a variation of the optimized triple series parallel method which is a flow diagram of an optimized triple series parallel extraction configuration having four extraction stages as opposed to three extraction stages in Figure 2. In the optimized triple series parallel extraction configuration, the stripped organic is first contacted in E4 by the partially 15 copper depleted aqueous from El. This partially loaded organic then advances to the E3 stage where it is contacted with a fresh volume of PLS and extracts additional copper. The organic phase then advances to E2 where it contacts a second stream of fresh PLS and extracts additional copper. The organic phase then advances to El where it contacts a second 20 stream of fresh PLS to form a fully loaded organic phase. The following examples are meant to illustrate but not to limit the invention. EXAMPLE 1 For comparison purposes, a trial was carried out at a copper solvent 25 extraction plant operating with a conventional series-parallel configuration. 7 WO 2004/096400 PCT/US2004/010706 The plant was carefully monitored for a period of time and then the circuit was re-piped to operate with the interlaced series parallel configuration. The operating conditions and overall copper recovery data for each circuit configuration are summarized in the following Tables: 5 EXTRACTION DATA FOR INTERLACED SERIES PARALLEL CONFIGURATION PLS 3.74 g/1l Cu, pH 2.05 10 Total PLS flow 320 m 3 /h PLS flow to El (series) 180 m 3 /h PLS flow to EP (parallel) 140 m 3 /h Organic flow (whole circuit) 180 m 3 /h Reagent concentration 18.4 % (v/v) 15 El semi-raffinate 1.10 g/I Cu EP raffinate (parallel) 0.23 g/I Cu E2 raffinate (series) 0.09 g/I Cu Overall O/A Extraction 1/1 O/A El stage (aq. recycle) 0.85/1 20 Spent electrolyte 31.1 g/I Cu, 175.0 g/I H2SO4 Pregnant electrolyte 44.4 g/I Cu Series recovery 97.6 % Parallel recovery 93.8 % Combined recovery 95.9 % 25 Net copper transfer 0.347 g/I Cu/volume % extractant 8 WO 2004/096400 PCT/US2004/010706 COMPARATIVE EXAMPLE EXTRACTION DATA FOR CONVENTIONAL SERIES PARALLEL CONFIGURATION PLS 3.74 g/l Cu, pH 2.12 5 Total PLS flow 320 m 3 /h PLS flow to El (series) 140 m 3 /h PLS flow to EP (parallel) 180 m 3 /h Organic flow (whole circuit) 180 m 3 /h Reagent concentration 18.4 % (v/v) 10 El semi-raffinate 1.30 g/I Cu E2 raffinate (series) 0.32 g/i Cu EP raffinate (parallel) 0.29 g/l Cu Overall O/A Extraction 1/1 O/A El stage (aq. recycle) 0.85/1 15 Spent electrolyte 30.0 g/l Cu, 180.3 g/I H2SO4 Pregnant electrolyte 43.5 g/l Cu Series recovery 91.4 % Parallel recovery 92.2 % Combined recovery 91.9 % 20 Net copper transfer 0.332 g/I Cu/volume % extractant The plant organic was used in both cases. The majority of the extractant present in the organic was LIX® 984N, a trademark product of Cognis Corporation, Cincinnati, Ohio. 25 While operating in the interlaced series parallel configuration, an additional 4% overall recovery of copper was achieved as compared to operating with the conventional series parallel configuration. 9
Claims (44)
1. A method for extracting and recovering a metal from an aqueous solution containing the metal comprising of the steps of: (1) contacting an 5 organic phase comprised of a water insoluble and water immiscible solvent solution of an extraction reagent formulation substantially free of metal values with a first aqueous metal bearing solution to extract at least a portion of the metal into the organic phase to form a metal depleted aqueous raffinate solution and a first partially loaded organic phase wherein the first 10 aqueous metal bearing solution is the raffinate from step (3); (2) contacting the first partially loaded organic phase with a second aqueous metal bearing solution to form a metal depleted aqueous raffinate solution and a second partially loaded organic phase having a metal content greater than the first partially loaded organic phase; (3) contacting the second partially loaded 15 organic phase with a third aqueous metal bearing solution to form a partially metal depleted aqueous and a third partially loaded organic phase.
2. The method of claim 1 wherein the extraction reagent is a mixture comprised of an aldoxime and a ketoxime. 20
3. The method of claim 2 wherein the mixture is further comprised of an equilibrium modifier.
4. The method of claim 1 wherein the extraction reagent is an aldoxime. 10 WO 2004/096400 PCT/US2004/010706
5. The method of claim 1 wherein the extraction reagent is a ketoxime.
6. The method of claim 1 wherein the metal is zinc. 5
7. The method of claim 1 wherein the metal is uranium.
8. The method of claim 1 wherein the metal is cobalt.
9. The method of claim 1 wherein the metal is molybdenum. 10
10. The method of claim 1 wherein the metal is nickel.
11. The method of claim 1 wherein the metal is copper. 15
12. The method of claim 6 wherein the extraction reagent is di-2 ethylihexylphosphoric acid.
13. The method of claim 7 wherein the extraction reagent is a tertiary fatty amine. 20
14. The method of claim 8 wherein the extraction reagent is a tertiary fatty amine.
15. The method of claim 9 wherein the extraction reagent is a tertiary fatty 25 amine. 11 WO 2004/096400 PCT/US2004/010706
16. The method of claim 10 wherein the extraction reagent is an organo phosphonic acid or phosphinic acid or a carboxylic acid.
17. The method of claim 11 wherein the extraction reagent is an 5 aldoxime, a ketoxime or a combination thereof.
18. A method for extracting and recovering copper from an aqueous solution containing the copper comprising of the steps of: (1) contacting an organic phase comprised of a water insoluble and water immiscible solvent 10 solution of an extraction reagent formulation substantially free of copper values with a first aqueous metal bearing solution to extract at least a portion of the copper into the organic phase to form a copper depleted aqueous raffinate solution and a first partially loaded organic phase wherein the first aqueous copper bearing solution is the raffinate from step (3); (2) contacting 15 the first partially loaded organic phase with a second aqueous copper bearing solution to form a copper depleted aqueous raffinate solution and a second partially loaded organic phase having a copper content greater than the first partially loaded organic phase; (3) contacting the second partially loaded organic phase with a third aqueous copper bearing solution to form a 20 partially copper depleted aqueous and a third partially loaded organic phase.
19. The method of claim 18 wherein the extraction reagent is an aldoxime, a ketoxime or a combination thereof. 12 WO 2004/096400 PCT/US2004/010706
20. The method of claim 19 wherein the mixture is further comprised of an equilibrium modifier.
21. The method of claim 18 further comprising the step of recovering the 5 copper by contacting the third loaded organic phase with an aqueous acid solution wherein the copper is transferred to the aqueous acid solution to form a strip aqueous phase.
22. The method of claim 21 further comprising the step of recovering the 10 copper from the strip aqueous phase by electrowinning.
23. A method for extracting and recovering a metal from an aqueous solution containing the metal comprising of the steps of: (1) contacting an organic phase comprised of a water insoluble and water immiscible solvent 15 solution of an extraction reagent formulation substantially free of metal values with a first aqueous metal bearing solution to extract at least a portion of the metal into the organic phase to form a metal depleted aqueous raffinate solution and a first partially loaded organic phase wherein the first aqueous metal bearing solution is the raffinate from step (3); (2) contacting 20 the first partially loaded organic phase with a second aqueous metal bearing solution to form a metal depleted aqueous raffinate solution and a second partially loaded organic phase having a metal content greater than the first partially loaded organic phase; (3) contacting the second partially loaded organic phase with a third aqueous metal bearing solution to form a metal 25 depleted aqueous raffinate solution and a third partially loaded organic 13 WO 2004/096400 PCT/US2004/010706 phase having a metal content greater than the second partially loaded organic phase; (4) contacting the third partially loaded organic phase with a fourth aqueous metal bearing solution to form a partially metal depleted aqueous and a fourth partially loaded organic phase. 5
24. The method of claim 23 wherein the extraction reagent is a mixture comprised of an aldoxime and a ketoxime.
25. The method of claim 24 wherein the mixture is further comprised of 10 an equilibrium modifier.
26. The method of claim 23 wherein the extraction reagent is an aidoxime. 15
27. The method of claim 23 wherein the extraction reagent is a ketoxime.
28. The method of claim 23 wherein the metal is zinc.
29. The method of claim 23 wherein the metal is uranium. 20
30. The method of claim 23 wherein the metal is cobalt.
31. The method of claim 23 wherein the metal is molybdenum. 25
32. The method of claim 23 wherein the metal is nickel. 14 WO 2004/096400 PCT/US2004/010706
33. The method of claim 23 wherein the metal is copper.
34. The method of claim 28 wherein the extraction reagent is di-2 ethylihexylphosphoric acid. 5
35. The method of claim 29 wherein the extraction reagent is a tertiary fatty amine.
36. The method of claim 30 wherein the extraction reagent is a tertiary 10 fatty amine.
37. The method of claim 31 wherein the extraction reagent is a tertiary fatty amine. 15
38. The method of claim 32 wherein the extraction reagent is an organo phosphonic acid or phosphinic acid or a carboxylic acid.
39. The method of claim 33 wherein the extraction reagent is an aldoxime, a ketoxime or a combination thereof. 20
40. A method for extracting and recovering a copper from an aqueous solution containing the copper comprising of the steps of: (1) contacting an organic phase comprised of a water insoluble and water immiscible solvent solution of an extraction reagent formulation substantially free of copper 25 values with a first aqueous copper bearing solution to extract at least a 15 WO 2004/096400 PCT/US2004/010706 portion of the copper into the organic phase to form a copper depleted aqueous raffinate solution and a first partially loaded organic phase wherein the first aqueous copper bearing solution is the raffinate from step (3); (2) contacting the first partially loaded organic phase with a second aqueous 5 copper bearing solution to form a copper depleted aqueous raffinate solution and a second partially loaded organic phase having a copper content greater than the first partially loaded organic phase; (3) contacting the second partially loaded organic phase with a third aqueous copper bearing solution to form a copper depleted aqueous raffinate solution and a third partially 10 loaded organic phase having a copper content greater than the second partially loaded organic phase; (4) contacting the third partially loaded organic phase with a fourth aqueous copper bearing solution to form a partially copper depleted aqueous and a fourth partially loaded organic phase. 15
41. The method of claim 40 wherein the extraction reagent is an aldoxime, a ketoxime or a combination thereof.
42. The method of claim 41 wherein the mixture is further comprised of 20 an equilibrium modifier.
43. The method of claim 40 further comprising the step of recovering the copper by contacting the fourth partially loaded organic phase with an aqueous acid solution wherein the copper is transferred to the aqueous acid 25 solution to form a strip aqueous phase. 16 WO 2004/096400 PCT/US2004/010706
44. The method of claim 43 further comprising the step of recovering the copper from the strip aqueous phase by electrowinning. 17
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US46324303P | 2003-04-16 | 2003-04-16 | |
| US60/463,243 | 2003-04-16 | ||
| US81636004A | 2004-04-01 | 2004-04-01 | |
| US10/816,360 | 2004-04-01 | ||
| PCT/US2004/010706 WO2004096400A2 (en) | 2003-04-16 | 2004-04-08 | Interlaced series parallel configuration for metal solvent extraction plants |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| AU2004233790A1 true AU2004233790A1 (en) | 2004-11-11 |
Family
ID=33423503
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2004233790A Abandoned AU2004233790A1 (en) | 2003-04-16 | 2004-04-08 | Interlaced series parallel configuration for metal solvent extraction plants |
Country Status (5)
| Country | Link |
|---|---|
| AU (1) | AU2004233790A1 (en) |
| BR (1) | BRPI0409423A (en) |
| MX (1) | MXPA05010879A (en) |
| PE (1) | PE20050213A1 (en) |
| WO (1) | WO2004096400A2 (en) |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6177055B1 (en) * | 1998-09-14 | 2001-01-23 | Henkel Corporation | Process for extracting and recovering copper |
| US6395062B2 (en) * | 2000-02-18 | 2002-05-28 | Cognis Corporation | Process for recovery of metals from metal-containing ores |
| US6632264B2 (en) * | 2001-04-17 | 2003-10-14 | The University Of British Columbia | Gold recovery from thiosulfate leaching |
-
2004
- 2004-04-08 MX MXPA05010879A patent/MXPA05010879A/en active IP Right Grant
- 2004-04-08 AU AU2004233790A patent/AU2004233790A1/en not_active Abandoned
- 2004-04-08 WO PCT/US2004/010706 patent/WO2004096400A2/en active Application Filing
- 2004-04-08 BR BRPI0409423-9A patent/BRPI0409423A/en not_active Application Discontinuation
- 2004-04-14 PE PE2004000371A patent/PE20050213A1/en active IP Right Grant
Also Published As
| Publication number | Publication date |
|---|---|
| WO2004096400A2 (en) | 2004-11-11 |
| BRPI0409423A (en) | 2006-04-25 |
| MXPA05010879A (en) | 2005-11-25 |
| PE20050213A1 (en) | 2005-05-09 |
| WO2004096400A3 (en) | 2005-12-29 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PC1 | Assignment before grant (sect. 113) |
Owner name: COGNIS IP MANAGEMENT GMBH Free format text: FORMER APPLICANT(S): COGNIS CORPORATION |
|
| MK4 | Application lapsed section 142(2)(d) - no continuation fee paid for the application |