WO2008039192A1 - Dispositifs et procédés d'extraction de cuivre - Google Patents

Dispositifs et procédés d'extraction de cuivre Download PDF

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Publication number
WO2008039192A1
WO2008039192A1 PCT/US2006/037747 US2006037747W WO2008039192A1 WO 2008039192 A1 WO2008039192 A1 WO 2008039192A1 US 2006037747 W US2006037747 W US 2006037747W WO 2008039192 A1 WO2008039192 A1 WO 2008039192A1
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WIPO (PCT)
Prior art keywords
copper
metal
concentration
iron
ion
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PCT/US2006/037747
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English (en)
Inventor
Darron R. Brackenbury
Chulheung Bae
Brian J. Dougherty
Stephen J. Harrison
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Everclear Solutions, Inc.
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Application filed by Everclear Solutions, Inc. filed Critical Everclear Solutions, Inc.
Priority to PCT/US2006/037747 priority Critical patent/WO2008039192A1/fr
Priority to PCT/US2007/020739 priority patent/WO2008039478A2/fr
Priority to US12/311,407 priority patent/US20100089763A1/en
Publication of WO2008039192A1 publication Critical patent/WO2008039192A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
    • C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
    • C25C1/12—Electrolytic production, recovery or refining of metals by electrolysis of solutions of copper
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/46104—Devices therefor; Their operating or servicing
    • C02F1/46176—Galvanic cells
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/68—Treatment of water, waste water, or sewage by addition of specified substances, e.g. trace elements, for ameliorating potable water
    • C02F1/683—Treatment of water, waste water, or sewage by addition of specified substances, e.g. trace elements, for ameliorating potable water by addition of complex-forming compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/20—Heavy metals or heavy metal compounds

Definitions

  • the field of the invention is remediation of aqueous media, and especially remediation of water contaminated with copper and optionally other metals.
  • the Berkeley open pit copper mine ceased operations in 1982 and since then, groundwater from the surrounding basin leaked into the pit.
  • the sulfuric acid content of the water increased and leached heavy metals and other contaminants from the earth, accumulating to over 17 billion gallons of wastewater.
  • arsenic, cadmium, and zinc are present in substantial quantities, and copper was measured to be above 180 ppm.
  • such wastewater is now considered a resource.
  • copper can be recovered from solution by precipitation, adsorption, or electrowinning.
  • Copper precipitation is typically relatively simple, and several processes are known in the art. As most of such processes rely on hydroxide formation, enormous quantities of base are required where the wastewater is acidic. Moreover, as copper is often present in relatively dilute form in such wastewaters, mixing and separation of the precipitate are impractical in most cases. Other known processes, for example, employ ferric and ferrous iron as reagents to promote formation of copper ferrite precipitate (see e.g., U.S. Pat. No.
  • copper can also be bound or complexed using adsorbent media, and there are many adsorbent media known in the art.
  • copper can be complexed with sulfides, or organic chelating agents (e.g., EDTA, various thiocarbamates) to either form a precipitate or to be adsorbed by a secondary sorbent (e.g., activated charcoal).
  • organic chelating agents e.g., EDTA, various thiocarbamates
  • secondary sorbent e.g., activated charcoal
  • Polymeric adsorbents typically avoid difficulties otherwise associated with complexing agents as they may act as a sold phase carrier or adsorbing filter.
  • the polymeric materials are polyethyleneimine-based and may or may not include functional groups as described in U.S. Pat.
  • electrochemical recovery of copper is achieved by plating elemental copper from an aqueous solution.
  • plating efficiency is critically dependent on the copper concentration and is therefore not practicable in most configurations.
  • spouted bed cathodes can be employed as described by Spiegel et al in U.S. Pat. No. 6,298, 996.
  • carbon felt cathodes were employed for copper plating in specific configurations as taught by Sunderland in U.S. Pat. No. 5,690,806. While such cathodes typically increase current efficiency, numerous difficulties nevertheless remain.
  • the present invention is directed to configurations and methods for metal recovery, and especially for copper recovery from aqueous solutions where other non-copper metals are also present (most typically, non-copper metals include ferric and ferrous iron, zinc, and/or manganese).
  • non-copper metals include ferric and ferrous iron, zinc, and/or manganese.
  • the copper-containing solution is first subjected to a redox reaction to reduce presence of metals with valences that would interfere with enrichment and/or plating. Copper is then selectively concentrated from the treated medium to produce a copper enriched solution from which copper is plated onto a flow through electrode.
  • contemplated configurations and methods allow for selective copper enrichment from low to moderate concentrations without significant interference from non-copper metals.
  • high current efficiencies and high copper purity are achieved while producing a copper depleted solution that may be further used for recovery of remaining metals (e.g., zinc and manganese).
  • a method of removing copper from an aqueous medium includes a step of providing an aqueous medium comprising copper and a second metal, wherein the copper and the second metal are in an ionic form.
  • a redox reaction is performed in the aqueous medium under conditions that change valence of the second metal, and in yet another step, copper is selectively enriched relative to the second metal to thereby produce a copper enriched solution from which copper is electrolytically deposited on a flow-through electrode.
  • the second metal is ferric iron (Fe-III), and the aqueous medium also includes ferrous iron (Fe-II), and optionally at least one of a zinc ion and a manganese ion.
  • the redox reaction comprises electrolytic reduction of the second metal, and the reduction is performed to achieve a ferric iron concentration of less than 30% of total iron ionic species. It is also preferred that the reduction is performed under conditions that do not change the valence of the copper.
  • an ion exchange resin is used to selectively enrich the copper to produce a copper enriched solution with copper at a concentration of at least 3000 ppm.
  • a remediation system will include a redox reactor configured to receive an aqueous medium comprising copper and a second metal, wherein the copper and the second metal are in an ionic form, and wherein the redox reactor is further configured to perform a redox reaction in the aqueous medium under conditions that change valence of the second metal.
  • a concentration system is fluidly coupled to the redox reactor and configured to selectively enrich copper relative to the second metal to thereby produce a copper enriched solution
  • a first electrochemical cell is fluidly coupled to the concentration system, wherein the cell is further configured to include a flow- through electrode onto which copper is platable.
  • the copper ion is a cupric ion
  • the second metal is ferric iron (Fe-III)
  • the aqueous medium may further comprise ferrous iron (Fe-II), and optionally comprise at least one of a zinc ion and a manganese ion.
  • the redox reactor preferably comprises a second electrochemical cell that may advantageously be configured to reduce ferric iron to ferrous iron without reducing the cupric ion to elemental copper.
  • the concentration system comprises an ion exchange resin, wherein the exchange resin preferentially binds ferric iron relative to ferrous iron.
  • the concentration system is configured to provide a copper depleted eluent that is enriched in the second metal, and/or the redox reactor is configured to increase selectivity in the concentration system.
  • the first electrochemical cell may be configured to provide a copper depleted eluent to the concentration system.
  • Figure 1 is a schematic illustration of an exemplary copper removal process according to the inventive subject matter.
  • Figure 2 is a schematic illustration of an exemplary electrochemical cell for copper plating according to the inventive subject matter.
  • Figure 3 is a graph showing the binding capacity of an exemplary resin for selected metal ions.
  • Figure 4 is a graph showing the cell voltage and Fe 3+ and Cu 2+ concentration profiles during copper plating.
  • Figure 5 is a graph depicting overall current efficiency in copper plating according to the inventive subject matter.
  • Figure 6 is a graph depicting Fe 3+ concentration in the initial samples over consecutive cycles of plating.
  • Figure 7 is a graph depicting energy consumption to recover 1 kg of copper at selected Cu 2+ concentrations over consecutive cycles of plating.
  • Figure 8 is a graph depicting required electrode area for copper plating over consecutive cycles of plating.
  • the inventors have unexpectedly discovered that various metals, and especially metals at low to moderate concentrations (e.g., less than 1000 ppm) can be effectively and selectively recovered from an aqueous medium in which other metals are present by using a process that employs a redox reaction to reduce enrichment and/or plating interference from other metals, that selectively enriches the target metal to form a enriched medium, and that then plates the target metal from the enriched medium in a flow through electrode.
  • low to moderate concentrations e.g., less than 1000 ppm
  • Contemplated configurations and methods are particularly desirable for treatment of copper containing acid mine drainage solutions and has been shown to produce high quality copper in a current efficient and economical manner. Such achievement is particularly notable as mine waste solutions are often richer in iron, zinc, and sulfuric acid than the target metal copper, and may further have significant buffering capacity (e.g., due to calcium, magnesium, and aluminum sulfates).
  • Berkeley Pit water served as the source of acid mine drainage water (which is known to comprise thousands of tons of copper, zinc, iron, manganese, and smaller amounts of other metals).
  • This water is acidic at a pH of about 2.8, has a sulfate concentration of about 10,000 ppm, with a copper concentration of 178 ppm, manganese of 240 ppm, zinc of 600 ppm, and iron of 1000 ppm.
  • the buffering capacity of this water was determined have a combined load of about 1270 ppm of calcium, magnesium, and aluminum salts. Using known processes, it would seem highly improbable that copper could be recovered from this mixture in an economical manner.
  • the terms "copper” and "metal” as used herein refers to both the ionic species as well uncharged elements (plated element).
  • electrochemical capture of metals on the cathode of an electrochemical cell is usually inefficient. This is particularly true where the metal concentrations are relatively low (e.g., below 1000 ppm, more problematic below 500 ppm, and even more problematic below 200 ppm), and where additional metals with redox states in aqueous solution (e.g., iron) will act as shuttle species between the anode and cathode and compete with the plating process (Fe +2 - e " at the anode -> Fe +3 ; Fe +3 + e " at the cathode -_> Fe +2 ).
  • Conventional tank electolyzers as used in the industry for electrowinning of copper/zinc will not properly operate under such circumstances and low metal concentration as the shuttle species and the anodes and cathodes are in the same electrolyte.
  • FIG. 1 illustrates a schematic overlook of the devices and methods presented herein.
  • a solution containing copper ions, ferric iron, ferrous iron, zinc ions and manganese ions is first subjected to a redox reaction to electrolytically reduce ferric iron to ferrous iron, preferably without reducing the copper ions (and other non-copper metal ions) as indicated in box 110.
  • the so treated solution is then passed through a cation exchange column that binds copper ions preferentially over other metal ions as indicated in box 120.
  • a cation exchange column that binds copper ions preferentially over other metal ions as indicated in box 120.
  • Copper ion depleted eluent 122 may then be stored for further processing (e.g., to remove the non-copper metal ions).
  • the resin with the bound copper ions is then treated with eluent to remove the copper ions from the resin as depicted in box 130.
  • the eluent is preferentially enriched in copper ions (typically at least 10-fold in concentration) while at the same time non-copper metal ions are removed into the copper depleted eluent 122.
  • concentration of non-copper ions in the copper ion-enriched elution will be significantly reduced ⁇ e.g., at least 5 -fold, more typically at least 10-fold in concentration) and also include significantly reduced ⁇ e.g., at least 5-fold, more typically at least 10-fold in concentration) concentrations of ionic species that may interfere ⁇ e.g., as redox shuttle) with the subsequent electroplating in box 140.
  • Electroplating is preferably performed in a flow through electrode, which most preferably includes carbon felt as cathode material.
  • the copper ion depleted solution after electroplating is then stored or routed for further use as eluent in the ion exchange column of box 120.
  • the plated elemental copper can then be further refined to desired purity as depicted in box 142.
  • the inventors contemplate a method of removing copper from an aqueous medium in which in one step an aqueous medium comprising copper and a second metal is provided, wherein the copper and the second metal are in an ionic form.
  • a redox reaction is performed in the aqueous medium under conditions that changes valence of the second metal, and in yet another step, copper is electrolytically deposited as elemental copper on a flow-through electrode.
  • a remediation system that includes a redox reactor that is configured to receive an aqueous medium comprising copper and a second metal, wherein the copper and the second metal are in an ionic form, wherein the redox reactor is further configured to perform a redox reaction in the aqueous medium under conditions that change valence of the second metal.
  • a concentration system is fluidly coupled to the redox reactor and is further configured to selectively enrich copper relative to the second metal to thereby produce a copper enriched solution.
  • Contemplated systems also include a first electrochemical cell that is fluidly coupled to the concentration system and that is further configured to include a flow-through electrode onto which copper is platable.
  • target metals i.e., metals that are plated in contemplated configurations and methods
  • metals other than copper include various noble metals (gold, silver, platinum, etc.), various heavy metals (cadmium, chromium, etc.), uranium, etc., all of which may be in various oxidation states.
  • the metals have at least a single positive charge.
  • Suitable target metals may be present as dissolved salts (i.e., as free ions), in complex with one or more ligands, or as organo-metallic compound.
  • contemplated aqueous solutions will vary substantially, and may include various wastewaters (e.g., from circuit board manufacture, mine drainage, landfill, etc.), process fluids (e.g., semiconductor manufacture, chemical plant, etc.), contaminated well water, and all other aqueous media that have at least one metal ion in a concentration of less than 2000 ppm, more typically of less than 1000 ppm, even more typically of less than 500 ppm, and most typically between about 100 ppb and 300 ppm.
  • wastewaters e.g., from circuit board manufacture, mine drainage, landfill, etc.
  • process fluids e.g., semiconductor manufacture, chemical plant, etc.
  • contaminated well water e.g., contaminated well water
  • all other aqueous media that have at least one metal ion in a concentration of less than 2000 ppm, more typically of less than 1000 ppm, even more typically of less than 500 ppm, and most typically between about 100 ppb and 300 ppm.
  • second metal may vary considerably, and it should be appreciated that the second metal may be present in various oxidation states, and/or that additional metals may be present.
  • suitable second metals include iron, chromium, zinc, molybdenum, nickel, cadmium, silver, etc.
  • second metals include those that will act as shuttle species in a plating process of the target metal and/or that will co-enrich in an enrichment process of the target metal.
  • especially contemplated second metals include ferric iron (Fe-III) and ferrous iron (Fe-II), which may be accompanied by zinc ion and/or a manganese ions (such metal composition is typical for various acid mine drainage solutions).
  • Second metal ions will typically be present in total concentrations of between 1 ppm and 300 ppm, more typically between 300 ppm and 500 ppm, even more typically between 500 ppm and 1000 ppm, and most typically between 1000 ppm and 3000 ppm, and even higher.
  • suitable reactions include electrochemical reactions on an anode and/or cathode, and chemical reactions with a reductant and/or oxidizing agent.
  • particularly preferred processes comprise electrolytic reduction of the second metal.
  • chemical reaction with a redox reagent may also be employed.
  • copper is to be isolated in an aqueous solution that includes both ferric and ferrous iron, it is typically preferred to reduce ferric iron to ferrous iron to a final ferric iron concentration of less than 30%, more preferably less than 20%, even more preferably less than 10%, and most preferably less than 5% of total iron ionic species.
  • the redox reactor is configured and/or operated to increase selectivity in the concentration system. Most typically, reduction (chemical or electrolytic) will be performed under conditions that do not change the valence of the copper ion (or other target metal).
  • the target metal e.g., copper
  • particularly preferred options employ an ion exchange resin that binds the target ion preferably at a higher affinity than non-target metals.
  • the target metal is enriched at least 3 -fold, more preferably at least 5-fold, even more preferably at least 10-fold, and most preferably at least 20-fold in absolute concentration whereas non-target metals are enriched to lesser degree, and most preferably depleted by at least 2-fold, more preferably at least 5 -fold, even more preferably at least 10- fold, and most preferably at least 20-fold in absolute concentration.
  • suitable ion exchange resins will preferentially bind ferric iron relative to ferrous iron.
  • ferric to ferrous iron will dramatically reduce overall iron ion concentration in the copper enriched exchange eluent.
  • the target metal may also be selectively enriched using various known processes, including membrane filtration (which may or may not be assisted by complexation or chelation of target or non-target ions) and/or precipitation.
  • membrane filtration which may or may not be assisted by complexation or chelation of target or non-target ions
  • precipitation for example, non-target metals may be removed by an increase in pH (ferric iron precipitates above pH 3.5 while ferrous iron remains dissolved).
  • copper may be enriched by ferrite precipitation.
  • Preferred enrichment processes will generate aqueous media with target metal (e.g., copper) concentrations of at least 1000 ppm, more typically at least at least 2000 ppm, even more typically at least 3000 ppm, and most typically at least 4000 ppm, while the total non- target metal concentration is preferably below 3000 ppm, more preferably below 2000 ppm, and most preferably below 1000 ppm.
  • target metal e.g., copper
  • the concentration system is configured to provide a copper depleted eluent or other process fluid that is enriched in the second metal, wherein valuable second metals especially include zinc, chromium, molybdenum, and arsenic.
  • Contemplated electrochemical cells include all known electrochemical cells in which anolyte and catholyte are separated by a separator and in which copper can be plated from a copper containing solution. Therefore, suitable electrochemical cells may be closed and static systems in which electrolyte is loaded prior to reduction of the metal or open dynamic cells in which electrolyte is circulated (or recirculated) from catholyte and/or anolyte tanks. However, particularly preferred systems include open dynamic cells. It should be noted that electrolyte (re)circulation can be acomplished with pumps and other equipment well known in the art. Similarly, there are numerous electrode configurations and materials known in the art, and all configurations and materials are deemed suitable for use herein.
  • anode configurations include flat panel electrodes or flat mesh electrodes. It is still further preferred that the anode is disposed in the anode compartment such that space between the anode and the separator defines a relatively narrow anolyte flow path. Viewed from a different perspective, it is generally preferred that the anode is as close as possible to the separator.
  • Anode materials are preferably corrosion resistant and will include platinum coated titanium mesh, Magnelli phase titanium suboxide, etc.
  • suitable anolytes it should be noted that all anolytes known for electrowinning of metals are deemed suitable, and that the choice of suitable anolyte is well within the scope of a person of ordinary skill in the art.
  • contemplated cathode materials are corrosion resistant to the catholyte and will provide a relatively large surface area to allow efficient copper plating at even relatively low copper concentrations. Therefore, especially contemplated cathode materials include carbon-based materials, and particularly carbon felt, glassy carbon, and carbon fiber, all of which may be partially pyrolyzed, activated, or otherwise treated.
  • carbon felt refers to a textile material that predominantly comprises randomly oriented and intertwined carbon fibers, which are typically fabricated by carbonization of organic felts (see e.g., IUPAC Compendium of Chemical Terminology 2nd Edition (1997)).
  • organic textile fibrous felts are subjected to pyrolysis at a temperature of at least 1200 0 K, more typically 1400 0 K, and most typically 1600 0 K in an inert atmosphere, resulting in a carbon content of the residue 90 wt%, more typically 95 wt%, and most typically 99 wt%.
  • contemplated carbon felts will have a surface area of at least about 0.01-100 m 2 /g, and more typically 0.1-5 m 2 /g, most typically 0.3-3 m 2 /g, and where the carbon felt is activated, will have a surface area (BET) of more than 100-500 m 2 /g, more typically at least about 500-800 m 2 /g, even more typically at least about 800-1200 m 2 /g, and most typically at least about 1200-1500 m Ig, or even more.
  • BET surface area
  • the carbon felt may be graphitic, amorphous, have partial diamond structures (added or formed by carbonization), or a mixture thereof.
  • reticulated or vitreous (glassy) carbon is formed from carbonized thermosetting organic polymer foams that generally have a non- fibrous, open or closed cellular architecture. While not preferred as high surface area material in conjunction with the teachings presented herein, reticulated or vitreous (glassy) carbon may also be used.
  • the carbon felt is prepared from carbonized organic textile fibrous felts and has a surface area of about 0.1-5 m /g to about 1200 m 2 /g and even higher (where the carbon felt is activated).
  • the exact configuration is of the carbon felt may be variable, it is typically preferred that the carbon felt will have a thickness to allow for a flow path from one side to the other of the felt of between 0.1 cm and 10 cm, and even more preferably between 0.5 cm and 5 cm.
  • Especially preferred cathodes are configured such that at least 50%, more typically at least 75%, even more typically at least 90%, and most typically at least 95% of the catholyte flow from one side of the cathode through the volume of the cathode to the other side of the cathode (which is proximal to the separator).
  • especially preferred cathodes are flow through cathodes.
  • Current can be fed to the flow through material of the cathode in numerous manners, and all known manners are deemed suitable for use herein.
  • the separator maintains the anolyte separate from the catholyte and only allows charged species to cross.
  • the charged species are limited to proton exchange, and therefore, all known proton exchange membranes are deemed suitable for use herein (e.g., NATIONTM [perfluorosulphonate cation exchange membrane commercially available from Dupont]) may be advantageously employed in contemplated electrochemical cells as such membrane has desirable resistance to the catholyte and anolyte.
  • the cell is configured and operated such that the target metal is substantially completely plated onto the cathode.
  • the target metal is copper
  • the inventors contemplate an electrochemical cell that is configured to provide a copper depleted eluent to the concentration system.
  • copper was recovered from controlled aqueous solutions and Berkely pit acid mine water in a process that included a reduction step to convert ferric to ferrous iron, a selective enrichment step that increase copper concentration, and a plating step that almost completely removed any copper from the treated and concentrated solution. It should be particularly appreciated that the processes and devices presented herein allow for an economic and conceptually simple recovery of copper without interference of non-copper metals at concentrations originally significantly higher than copper.
  • FIG. 2 schematically depicts an exemplary electrowinning cell 200 in which the cell body is formed from HDPE plates 210 (typically high-density polyethylene or other corrosion resistant material) in which flow channels are formed to allow entry and exit of catholyte and anolyte.
  • the cathode compartment 212 and anode compartment 214 are separated by NAFION membrane 220.
  • anolyte flows (arrows) across the anode 230, which is coupled to spacer block 232 to reduce the space between the anode 230 and the separator 220.
  • the anode 230 is preferably a platinum coated titanium mesh.
  • the cathode 240 in the cathode compartment 212 is preferably a graphite felt 242 that is mounted on a titanium current feeder 244.
  • Graphite felt 242 is preferably held in place by plastic mesh 246. It should be especially noted that the catholyte flows (arrows) into the cathode compartment 212 and from there through the graphite felt 242 before entering the space defined by the separator 220, felt 242, and catholyte entry and exit ports. Therefore, the flow of the electrolyte and the current are parallel.
  • the inventors decided to selectively concentrate copper in the wastewater, preferably via ion exchange.
  • copper concentration by ion exchange was expected to also enrich other non-copper metals (which typically occur in higher concentrations), resins with selectivity for copper needed to be identified.
  • suitable resins should provide enrichment of copper without concentration of iron, zinc, and manganese.
  • cation exchange resins were tested with large samples of Berkeley pit water, and selected commercially available resins were identified as binding copper with desirable affinity.
  • Amberlite IRT 7481 as particularly suitable as copper eluted other ions like Zn +2 , Fe +2 , and Mn +2 .
  • the ion exchange resin became almost completely occupied with copper.
  • Amberlite IRT 7481 bound Fe +3 , the least abundant state of iron in Berkeley Pit waters, with significant affinity. It was thus necessary to ensure that as much iron as possible was in the reduced ferrous state prior to reaching the ion exchange resin.
  • ferric iron acts as a shuttle species in an electrochemical cell.
  • various options for reducing ferric iron to ferrous iron are available: Chemical treatment (e.g., with sulfur dioxide, hydrazine sulfate, sodium metabisulfite etc.), or electrochemical reduction.
  • sodium metabisulfite Na 2 S 2 O 5
  • One mole of sodium metabisulfite reduces 4 moles of Fe + .
  • the speciation of iron was done via titration with Ce 4+ .
  • sodium metabisulfite was used in excess, it was successful in reducing Fe 3+ , however when the salt was added to BP water a dark orange color was formed which inhibited its use in an ion exchange column.
  • Berkeley Pit water is treated first to convert Fe +3 to Fe +2 , and to feed the so treated wastewater to an ion exchange bed that strips the wastewater of copper until breakthrough occurs.
  • the treated water is collected for zinc and manganese recovery, which can be performed using numerous manners known in the art.
  • the copper rich solution stripped from the ion exchange column is then treated in the carbon felt cell to plate the copper. When copper reaches the prescribed thickness the electrode is removed and the copper removed mechanically from the cathode. The copper free solution is then used to further strip more copper from the next batch of ion exchange resin.
  • Ferric iron contents in Berkley Pit are 25% to 30% of the total 1000 ppm. This ratio had increased in the samples received due to oxidation.
  • BP water was reduced electrochemically to 30% Fe(III) and was used in a beaker test with IRC 7481 under a nitrogen blanket to prevents oxidation.
  • the resin captured 60% of total copper, 14% of total iron, and 8% of total zinc. More detailed results and further experiments are provided below.
  • the first set of beaker tests were performed on DOWEX® M4195 and the following AMBERLITE® resins: IRC 747, IRC 7481, and GT73. It was found that DOWEX® M4195 and IRC 7481 had higher copper capacities than GT73. AMBERLITE® resin IRC 747 did not have a high capacity for copper. Figure 3 shows the equilibrium capacity of each resin for copper, iron, and zinc respectively (in the presence or absence of ascorbic acid as reductant). Among the resins tested, DOWEX® M4195 had the highest capacity for zinc.
  • An electrochemical cell as depicted in Figure 2 was employed to plate copper from the regenerant of the IRC 7481 ion exchange resin column.
  • Pt/Ti mesh and carbon felt were used as anode and cathode, respectively.
  • the Pt/Ti mesh electrode was bent and spot welded onto a Ti plate as shown in the Figure 2 and a HDPE plastic block was inserted between the Pt/Ti mesh and Ti plate current feeder to give less space between the anode and a separator.
  • a 10 cm thick carbon felt cathode was threaded onto a Ti mesh current feeder together with a plastic mesh which pushed the felt electrode against the Ti mesh current feeder (resulting in better contact between the felt electrode and current feeder).
  • the projected area of the carbon felt electrode was 11 x 9.5 cm 2 .
  • the anodic and cathodic compartments were separated with an ion exchange membrane (Nafion® 450), and 10% H 2 SO 4 and the regenerant were utilized as anolyte and catholyte, respectively. Both electrolytes entered at the bottom of the cell and left at the top of the cell.
  • the catholyte flow process is in "flow-through" mode where flow of solution and current are parallel.
  • the catholyte was fed from the cathode surface which faced the Ti mesh current feeder towards the ion exchange membrane as seen in Figure 2. It should be appreciated that the catholyte flow path was made in this way in order to suppress the fast copper dendrite growth on the surface of the carbon felt facing the membrane during the plating process. From the preliminary experiments with opposite catholyte flow path, it was observed that the copper dendrite grew fast on the side of the carbon felt electrode facing the membrane since that side was nearer to the positive electrode and less copper ions were sent to the other side of the felt electrode resulting in poorer copper plating along the whole depth of the carbon felt electrode. Between each cell part, Tygon gaskets were situated for better sealing.
  • a peristaltic pump (Masterflex L/STM, Cole-Parmer Instrument company model 7552-02) was employed to circulate the electrolytes with two pump heads (Masterflex® Easy-Load) giving same flow rate to both compartments.
  • the electrolyte flow rate was adjusted by the pump controller (Masterflex ® Wash-Dow Modular controller, Cole- Parmer Instrument company model 7552-71) and it was fixed at 20 ml sec-1, which for a flow channel past the electrode of width 11 cm and height 9.5 cm corresponds to a linear flow velocity of 18.18 x 10 "2 cm sec "1 .
  • the electrolytes were fed into the electrochemical cell from the 2 L plastic bottle reservoirs through the Tygon tubings and sent back to the reservoirs.
  • the catholyte tubings in the cathodic reservoir were immersed into the electrolyte to prevent any Fe 2+ ions in the catholyte from contacting the oxygen in the air and being oxidized to Fe 3+ which can possibly oxidize the plated copper on the felt electrode as well as consume charges for its reduction back to Fe 2+ causing poorer charge efficiency during the copper plating process.
  • a pressure gauge was connected near the catholyte inlet at the bottom of the cell to monitor the pressure drop before and after the copper plating. Copper plating was performed under constant current at 30 Amp using a Maccor unit (computerized battery charger) which also monitored the cell voltage and energy consumption during the experiments.
  • the regenerant was filtered to remove copper debris and the filtered regenerant was immediately used to regenerate the successively loaded ion exchange resin column. From 5th cycle concentrated acid was added to the regenerant prior to the next regeneration to adjust the acid concentration. After each experiment, the electrochemical cell was taken apart and all of the cell components were washed with de-ionized water. The used carbon felt electrode was replaced with a fresh felt for each copper plating experiment.
  • the regenerant includes Fe 3+ ions which reduction to Fe 2+ occurs at higher potential compared to Cu 2+ reduction to Cu resulting in the competition between the two species at the beginning of the experiments.
  • Figure 4 shows the cell voltage, Fe 3+ and Cu 2+ concentration profiles during the 1st copper plating from the regenerant.
  • Fe 3+ and Cu 2+ concentration decrease for the first 3 minutes but Fe 3+ concentration change gives steeper slope than Cu 2+ indicating that Fe 3+ reduction consumes more electrical charges than Cu deposition during that time.
  • Fe 3+ concentration remains at 550 ppm for the rest of the experiment while Cu 2+ concentration starts decreasing faster and the cell voltage slightly increases until 9 minutes showing that Cu plating mainly occurs during this period of time.
  • the Cu 2+ concentration drops much slower and the cell voltage rapidly increases indicating that the hydrogen evolution commences.
  • Eff. is efficiency, n is the number of electrons involved in the reaction, F is the Faraday's constant (96485) [C mol "1 ], ⁇ C is the concentration difference (Cl-C2)[mol/1], V is the volume of the solution [1], I is the supplied current [Amp], and 11 the time spent between Cl and C2 [sec].
  • Overall current efficiency was employed, which is accumulative current efficiency. As shown in Figure 5, maximum overall current efficiency was obtained from 1st cycle at 78 %, decreasing until 4th copper plating. From 4th to 8th cycles the overall current efficiencies are similar with around 70% maximum current efficiency. The decrease in overall current efficiency until 4th plating can be explained with the initial Fe 3+ concentration in the regenerant for each experiment.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Organic Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
  • Electrolytic Production Of Metals (AREA)
  • Treatment Of Water By Ion Exchange (AREA)
  • Removal Of Specific Substances (AREA)

Abstract

La présente invention concerne des dispositifs et des procédés permettant une extraction efficace de cuivre de matières aqueuses par concentration sélective de cuivre au cours d'une première opération, des ions métalliques en compétition subissant une réaction d'oxydoréduction visant à augmenter la concentration sélective. Le cuivre est ensuite déposé dans un flux qui traverse une électrode à partir d'une solution de cuivre relativement concentrée qui est pauvre en métaux différents du cuivre en compétition. Dans des modes de réalisation préférés de l'invention, la première opération fait intervenir un effluent pauvre en cuivre comprenant du zinc et/ou du manganèse, pour extraction ultérieure.
PCT/US2006/037747 2006-09-26 2006-09-26 Dispositifs et procédés d'extraction de cuivre WO2008039192A1 (fr)

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PCT/US2006/037747 WO2008039192A1 (fr) 2006-09-26 2006-09-26 Dispositifs et procédés d'extraction de cuivre
PCT/US2007/020739 WO2008039478A2 (fr) 2006-09-26 2007-09-26 Dispositifs et procédés d'extraction de cuivre
US12/311,407 US20100089763A1 (en) 2006-09-26 2007-09-26 Devices and methods of copper recovery

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017172007A (ja) * 2016-03-24 2017-09-28 田中貴金属工業株式会社 金属回収装置
EP4007824A4 (fr) * 2019-08-01 2023-09-27 Aqua Metals Inc. Récupération de métaux à partir d'électrolytes contenant du plomb

Citations (3)

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US4159366A (en) * 1978-06-09 1979-06-26 The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration Electrochemical cell for rebalancing redox flow system
JPS56139193A (en) * 1980-12-25 1981-10-30 Kosaku:Kk Treatment of waste copper plating solution
US5690806A (en) * 1993-09-10 1997-11-25 Ea Technology Ltd. Cell and method for the recovery of metals from dilute solutions

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US4378275A (en) * 1981-12-03 1983-03-29 Saudi-Sudanese Red Sea Joint Commission Metal sulphide extraction

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Publication number Priority date Publication date Assignee Title
US4159366A (en) * 1978-06-09 1979-06-26 The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration Electrochemical cell for rebalancing redox flow system
JPS56139193A (en) * 1980-12-25 1981-10-30 Kosaku:Kk Treatment of waste copper plating solution
US5690806A (en) * 1993-09-10 1997-11-25 Ea Technology Ltd. Cell and method for the recovery of metals from dilute solutions

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"AMBERLITE IRC748", product pamphlet from Rohm and Haas Company, October 2001 *

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017172007A (ja) * 2016-03-24 2017-09-28 田中貴金属工業株式会社 金属回収装置
WO2017164271A1 (fr) * 2016-03-24 2017-09-28 田中貴金属工業株式会社 Dispositif de récupération de métal
EP4007824A4 (fr) * 2019-08-01 2023-09-27 Aqua Metals Inc. Récupération de métaux à partir d'électrolytes contenant du plomb

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