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WO2012068621A1 - Procédé d'extraction de zinc et/ou d'oxyde de zinc i - Google Patents

Procédé d'extraction de zinc et/ou d'oxyde de zinc i Download PDF

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Publication number
WO2012068621A1
WO2012068621A1 PCT/AU2011/001508 AU2011001508W WO2012068621A1 WO 2012068621 A1 WO2012068621 A1 WO 2012068621A1 AU 2011001508 W AU2011001508 W AU 2011001508W WO 2012068621 A1 WO2012068621 A1 WO 2012068621A1
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WO
WIPO (PCT)
Prior art keywords
zinc
process according
lixiviant
containing material
leachate
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/AU2011/001508
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English (en)
Inventor
Neal Barr
Ying Liang
Raymond Walter Shaw
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Metallic Waste Solutions Pty Ltd
Original Assignee
Metallic Waste Solutions Pty Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from AU2010905189A external-priority patent/AU2010905189A0/en
Application filed by Metallic Waste Solutions Pty Ltd filed Critical Metallic Waste Solutions Pty Ltd
Publication of WO2012068621A1 publication Critical patent/WO2012068621A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C22B19/00—Obtaining zinc or zinc oxide
    • C22B19/32—Refining zinc
    • 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
    • C22B19/00—Obtaining zinc or zinc oxide
    • C22B19/20—Obtaining zinc otherwise than by distilling
    • C22B19/24—Obtaining zinc otherwise than by distilling with leaching with alkaline solutions, e.g. ammonia
    • 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
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/02—Working-up flue dust
    • 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 generally relates to a process for the recovery of zinc preferably in the form of zinc or zinc oxide.
  • the invention is particularly applicable for recovering zinc from Electric Arc Furnace dust ("EAF") and it will be convenient to hereinafter disclose the invention in relation to that exemplary application.
  • EAF Electric Arc Furnace dust
  • the invention is not limited to that application and could be used to recover zinc from a variety of sources including materials containing zinc oxide and other metal oxides, such as galvanisers' ash, oxidised ores, mineral processing residues, water treatment precipitates, contaminated soils, waste stockpiles and/or, solid waste streams, materials containing mixed-metal oxides including zinc where a "mixed-metal" oxide is a compound composed of zinc, oxygen and at least one other metal (e.g. zinc ferrite, or zinc ferrate) such as oxidised ores, or mineral processing residues.
  • materials containing zinc oxide and other metal oxides such as galvanisers' ash, oxidised ores, mineral processing residues, water treatment precipitates, contaminated soils, waste stockpiles and/or, solid waste streams, materials containing mixed-metal oxides including zinc where a "mixed-metal" oxide is a compound composed of zinc, oxygen and at least one other metal (e.g. zinc ferrite, or zinc ferrate) such
  • EAF dust Electric Arc Furnace dust
  • This dust has to be collected and treated or disposed of in some way. Disposal of EAF dust by stabilization and burial is widely practiced. In many markets this is costly. Economic treatments to recover contained zinc in EAF dust has been a challenge to industry for many years.
  • the zinc in EAF dust is typically in the form of zinc oxide and zinc ferrite.
  • the zinc oxide in EAF dust can be leached by a variety of lixiviants.
  • the associated zinc ferrite has generally proven more difficult.
  • Such zinc ferrite has not been easy to attack by purely hydrometallurgical means.
  • a thermal reduction is performed before leaching to further convert zinc ferrite to zinc oxide to make more zinc amenable to aqueous leaching agents.
  • EAF dust A further problem with EAF dust is that the high iron content in EAF dust is leached by many acidic lixiviants. The removal of this solubilised iron from leach solutions complicates hydrometallurgical processes and flow charts.
  • any metal such as zinc, manganese, lead etc should be understood to include any chemical form (i.e. metal, salts, complexes, chelates, etc) or ionic form.
  • a process for recovering zinc from a zinc containing material including the steps of: leaching the zinc containing material with an alkaline lixiviant which includes an ammonium species, a hydroxide species and a halide species to produce a zinc containing leachate;
  • the process of the present invention therefore uses an alkaline ammonium based lixiviant to selectively leach the zinc from the zinc containing material.
  • the overall process predominantly leaves zinc in solution in the resultant leachate.
  • lixiviant composition By selection of lixiviant composition, a zinc solution can be produced that can have the zinc solubility modified by ammonia stripping which can facilitate recovery of a substantial portion of the contained zinc as basic zinc compounds leaving a zinc depleted ammonium chloride liquor for recycle.
  • the lixiviant composition can comprise any suitable alkaline solution which includes an ammonium species, a hydroxide species and a halide species, and in particular ionic forms of those species.
  • the lixiviant comprises a mixture of an ammonium halide and ammonium hydroxide.
  • suitable lixiviant is an aqueous mixture of ammonium chloride and ammonia.
  • the lixiviant comprises an aqueous solution of 10 to 1000g/L of ammonium chloride, preferably between 100 and 500 g/L, more preferably between 200 and 300 g/L, and most preferably about 280 g/L, and between 5 to 300 g/L total ammonia, preferably between 100 and 200 g/L, most preferably about 150 g/L.
  • an ammonium chloride content of between 200 to 500g/L is preferred when the lixiviant has a temperature of between ambient to 50°C.
  • the lixiviant has a pH > 7.
  • An alkaline lixiviant is less conducive to iron solubilisation and minimizes lead and manganese solubilisation.
  • the addition of ammonia, ammonium hydroxide should be sufficient to make the lixiviant alkaline in terms of normal aqueous chemistry.
  • the lixiviant mixture need not be fully in a solution form at the commencement of its use.
  • the ammonium chloride does not necessarily have to be dissolved at the start of leaching. Heating the lixiviant to above ambient temperatures, preferably greater than 50°C, would assist in dissolution of the ammonium chloride into solution and thereby optimise the ammonium chloride and ammonium hydroxide concentrations.
  • the leaching step is preferably performed in a gas tight environment to prevent loss of ammonia gas to the atmosphere.
  • the amount of lixiviant added to the zinc containing material can be varied depending on the composition of that material because the lixiviant/solids ratio is sensitive to the zinc content and nature of the material to be leached. In some embodiments, the lixiviant/solids ratio is 20 to 1500 g of zinc containing material per L of lixiviant is leached in the leaching step.
  • the leach contact time is variable depending on the composition of the zinc containing material being leached in the leaching step.
  • the contact time can therefore range from minutes to several days. It should however be appreciated that high temperature favours shorter leach times.
  • the leaching step is conducted in temperatures above ambient, the leaching step should be conducted in a pressure vessel designed to withstand at least the vapour pressure of ammonia and water at that operational temperature. Low temperature (ambient temperature(s) and below) leaching steps can be performed in a closed vessel.
  • the leaching step is preferably conducted at a temperature of between -10°C to 150°C, more preferably between 20 to 70 °C.
  • the overall process is preferably set up to predominantly leave zinc in solution.
  • the selected lixiviant is alkaline through the use of ammonia/ammonium hydroxide.
  • a zinc rich leachate can be produced that can have its zinc solubility modified by ammonia stripping. This can recover a substantial portion of the contained zinc as basic zinc compounds leaving a zinc depleted ammonium chloride liquor for recycle.
  • the process of the present invention includes the step of stripping ammonia from the leachate.
  • This stripping step precipitates out basic zinc compounds which can then be recovered.
  • the stripped ammonia can be captured for recycle to the leaching step.
  • This stripping step preferably provides a stripped liquid containing solid zinc product, and the process further includes the step of removing solids from the stripped liquid. Though, this stripped liquor could also be used as an electrolyte for electrowinning.
  • Ammonia stripping can be performed by any number of processes.
  • the step of stripping ammonia from the leachate includes a gas sparging step. Waste heat from a co-located process is preferably used for the gas sparging step.
  • waste heat from the steel plant can be used to heat air for gas sparging.
  • waste heat from the hot dip galvanising furnace can be used in the ammonia stripping step.
  • the zinc can be extracted from the process in various forms including zinc hydroxide, zinc hydroxychloride, zinc oxide, or zinc dichlorodiammine or combinations thereof.
  • the composition of the lixiviant can be modified to control the composition of the final stripped liquor composition, which in turn assists in the selection of the dominant product.
  • Zinc oxide is favoured by stripping followed by neutralization by caustic soda.
  • the process of the present invention can therefore further include a neutralisation step following the ammonia stripping step including adding sodium hydroxide to the stripped liquid.
  • the zinc can be extracted from the stripped liquor substantially as zinc dichlorodiammine.
  • Zinc dichlorodiammine crystallization is favoured from hot leach liquors derived from the preferred ammonium chloride lixiviant loadings.
  • the process then preferably further includes a hydrolysis step.
  • the hydrolysis step typically includes a step of reacting the solid zinc containing material product with water to convert the zinc dichlorodiammine to Zn(OH) 2 .
  • the step of stripping ammonia can promote the precipitation of large amounts of Zinc dichlorodiammine without the need for excessive heating and cooling to drive solubility.
  • Subsequent hydrolysis of Zinc dichlorodiammine avoids the need to dilute the leach liquor prior to crystallization.
  • Zinc oxide can then be produced by heating the hydrolysis product (substantially Zn(OH) 2 ) to drive off water.
  • the "zinc containing material” can be any material including material containing zinc species are such as: [0023] Materials containing zinc oxide and other metal oxides such as galvanisers' ash, EAF dust, oxidised ores, mineral processing residues, water treatment precipitates, contaminated soils, waste stock-piles, or solid waste streams.
  • a "mixed- metal” oxide is a compound composed of zinc oxygen and at least one other metal (e.g. zinc ferrite, or zinc ferrate, such as EAF dust, oxidised ores or the like; or
  • the zinc containing material is substantially particulate.
  • Recovery of the zinc from the leachate preferably includes one or more process steps which separate solids from the leachate, removal procedures for other metal species which may be present in the leachate such as lead, manganese, copper and cadmium and/or process steps to separate the zinc from the leachate.
  • the separation of solid and liquid can be performed using any suitable method.
  • the process may include at least one filtering step to remove solids from the leachate.
  • the zinc containing material may also include at least one of manganese, lead, copper or cadmium. Other trace elements, species or impurities may also be present.
  • the process of the present invention therefore can include steps of removing any lead, manganese, copper or cadmium from the leachate.
  • the zinc containing material includes lead
  • these can be removed using selective removal processes. Firstly, it should be appreciated that lead(ll) is leached in the leaching step while lead(IV) is not leached. Those lead leached from the zinc containing material are preferably returned to the leached solids by oxidation to an insoluble form.
  • Controlled oxidation preferentially oxidizes lead before any manganese which may be present in the zinc containing material.
  • any lead can be isolated before manganese.
  • the lead removal step is preferably conducted prior to any solids/liquid separation of leachate after the leaching step. However, in some embodiments, lead can be removed and separated after a liquid solids separation step and collected separately.
  • the zinc containing material includes manganese
  • these can be removed using selective removal processes. Firstly, it should be appreciated that manganese in oxidation states less than +4 is leached in the leaching process but manganese(IV) is not leached.
  • the manganese leached from the zinc containing material is preferably returned to the leached solids by oxidation to an insoluble form.
  • the manganese removal step is preferably conducted prior to any solids/liquid separation of leachate after the leaching step.
  • manganese can be removed and separated after a liquid solids separation step and collected separately.
  • lead it is preferable to conduct the controlled oxidation of lead prior to manganese so lead can be optionally isolated before manganese then removed and manganese subsequently oxidized to manganese dioxide and separated.
  • Each of the lead and manganese removal steps can comprise chemical oxidation using one of peroxide or chlorine and/or chloride based oxidants such as hypochlorite or chloramine. Air oxidation may also be used to remove these metals. Alternatively, electrochemical oxidation may also be used.
  • the zinc containing material includes copper and cadmium
  • these can be removed by the well established process of cementation on zinc.
  • the manganese leached from the zinc containing material is preferably removed using a cementation process which includes the step of adding zinc metal to the leachate.
  • the zinc containing material also includes manganese, lead, copper and cadmium.
  • the process preferably includes the steps of:
  • the lead, manganese, copper and cadmium can be removed using various processes.
  • the steps of removing the lead, manganese, copper and cadmium from the leachate to produce a modified leachate and cementation solids; and separating the modified leachate and cementation solids include the steps of
  • a plant which includes a process according to the first aspect of the present invention.
  • This plant preferably includes a pressure vessel able to present the lixiviant solution and particulate material(s) to ammonia saving confinement for the purpose of the leaching out of the zinc.
  • the present invention also provides a zinc containing material produced from a process according to the first aspect of the present invention.
  • a process for recovering zinc from a zinc containing material including the steps of:
  • an alkaline lixiviant which includes an ammonium species, a hydroxide species and a chloride species to produce a zinc containing leachate
  • Figure 1 is a flow diagram showing the process steps for one preferred embodiment of the process according to the present invention.
  • Figure 2 shows flow diagram of one preferred embodiment of the process according to the present invention for producing zinc oxide from EAF dust.
  • the process of the present invention relates to the recovery of zinc from a zinc containing material.
  • the "zinc containing material” can be any material including material containing zinc species are such as galvanisers' ash, EAF dust, oxidised ores, mineral processing residues, water treatment precipitates, contaminated soils, waste stock-piles, or solid waste streams.
  • Such zinc containing material typically also includes manganese, lead, copper and cadmium which can also be solubilised in a lixiviant applied during a leaching step.
  • the applicant has designed the leaching and step of recovering the zincs of the process of the present invention to take advantage of the equilibrium which is established between the soluble and insoluble metal complexes of the oxides and mixed metal oxides in such a zinc containing material when leached by a lixiviant.
  • the particular lixiviant of the present invention provides a mix of ligands which facilitate this equilibrium.
  • Ammonium, ammonia chloride, hydroxide and water are all available for metal complex formation.
  • iron(lll) is not solubilised to any great extent as its solubility is controlled by the solubility product of iron(lll) hydroxide which is an equilibrium species in the leach mixture. This is effective in keeping iron out of solution.
  • the major risk of iron contamination of leach liquors is the formation of colloidal iron hydroxide.
  • Lead(IV) and manganese(IV) are either not leached or leached and returned to the solid phase in a similar manner to iron(lll).
  • Both manganese(ll) and lead(ll) are soluble in the lixiviant but are easily oxidized to the less soluble manganese(IV) and lead(IV) oxides. They can be returned to the solids in the leach by oxidation or subsequently removed after primary solids separation by oxidation and filtration. Cadmium and copper, being generally soluble in the lixiviant mix can be removed to low levels by cementation on zinc.
  • the overall process thus predominantly leaves zinc in solution.
  • a zinc solution can be produced that can have the zinc solubility modified by ammonia stripping in order to recover a substantial portion of the contained zinc as basic zinc compounds leaving a zinc depleted ammonium chloride liquor for recycle.
  • This zinc in this zinc solution can be recovered using a variety of recovery processes.
  • this zinc solution may be suitable for zinc electrowin in a divided electrowin cell.
  • FIG. 1 there is shown a flow diagram showing the basic steps in recovering the zinc for a zinc containing material using a leaching step in accordance with a preferred embodiment of the present invention.
  • the zinc containing material treated in the process includes zinc, manganese, lead, copper and cadmium.
  • the zinc containing material is leached with an alkaline lixiviant.
  • the lixiviant composition comprises an aqueous mixture of ammonium chloride and ammonia mixed to provide a pH > 7.
  • An alkaline lixiviant is less conducive to iron solubilisation and minimizes lead and manganese solubilisation.
  • the lixiviant mixture need not be fully in a solution form at the commencement of its use. Heating the lixiviant to above ambient temperatures assists in dissolution of the ammonium chloride into solution and thereby optimises the ammonium chloride and ammonium hydroxide concentrations.
  • the lixiviant/solids ratio for this leaching step is between 20 to 1500 g of zinc containing material per L of lixiviant.
  • the leach contact time is variable depending on the composition of the zinc containing material being leached in the leaching step.
  • the leaching step produces a leachate substantially including the zinc.
  • the leachate also includes solubilised manganese, lead, copper and cadmium.
  • a leached solid content is also present.
  • this mixture can either be filtered to remove the leached solids, or undergo a process step where the lead and manganese are removed from the leachate.
  • the lead and manganese removal step is however preferably conducted prior to any solids/liquid separation of leachate after the leaching step.
  • each of the lead and manganese removal steps can comprise a controlled oxidation step. This can be chemical oxidation using one of peroxide or chlorine and/or chloride based oxidants such as hypochlorite or chloramine. Air oxidation may also be used to remove these metals. Alternatively, electrochemical oxidation may also be used. Controlled oxidation preferentially oxidizes lead before any manganese which may be present in the zinc containing material. Thus, any lead can be isolated before manganese.
  • the resulting liquor is then passed through a separation step, typically a filtration step to separate the leachate and leached solids.
  • the resulting liquor then undergoes a process step where the copper and cadmium are removed from that liquor.
  • This step is typically conducted by the well established process of cementation on zinc to produce a modified leachate and cementation solids.
  • other processes could be used, for example electrolytic separation process.
  • the resulting liquor is then passed through a separation step, typically a filtration step to separate the liquor and cementation solids.
  • the resultant filtered liquor predominantly includes the zinc in solution.
  • This filtered liquor can optionally be treated with alkali such as sodium hydroxide, diluted and ammonia stripped to precipitate zinc compounds and produce a disposal salt solution of low zinc content. This is useful for ammonia recycle when a lixiviant has reached the end of its recycle life due to build up of contaminants such as calcium and magnesium.
  • the zinc rich leachate is normally passed directly into an ammonia stripping step in order to modify the solubility of zinc in that solution.
  • This stripping step precipitates out basic zinc compounds producing a stripped liquid containing solid zinc product.
  • the stripped ammonia is captured for recycle to the leaching step.
  • Ammonia stripping can be performed by any number of processes, for example gas sparging. Waste heat from a co-located process can be used for the gas sparging step.
  • the zinc can be extracted from the process in various forms including zinc hydroxide, zinc hydroxychloride, zinc oxide, or zinc dichlorodiammine or combinations thereof.
  • the composition of the lixiviant can be modified to control the composition of the final stripped liquor composition, which in turn assists in the selection of the dominant product.
  • zinc oxide is favoured by stripping followed by neutralization by caustic soda.
  • Zinc dichlorodiammine crystallization is favoured from hot leach liquors derived from high ammonium chloride lixiviant loadings.
  • Zinc hydroxychloride and Zn(OH) 2 are favoured by dilution of the leach liquor with water prior to the precipitation.
  • the isolated zinc containing solid product can be treated by any suitable means to produce zinc compounds or zinc metal. For example:
  • Zinc hydroxide can be heated at temperatures above 150°C to produce zinc oxide.
  • Zinc dichlorodiammine can be hydrolysed in water to form zinc oxide and/or Zn(OH) 2 and recycle liquor bearing ammonium chloride.
  • Zinc oxide or hydroxide can be fed to a conventional sulphate electrowin cell for production of zinc metal.
  • Zinc dichlorodiammine and zinc hydroxychloride are suitable feeds for zinc ammonium chloride based chemicals.
  • Zinc dichlorodiammine and zinc hydroxychloride are suitable feeds for zinc metal electrowin in divided chloride electrowin cells.
  • the final solution undergoes a filtration step to recover the solid product.
  • the liquor can be recycled.
  • FIG 2 shows flow diagram of one preferred embodiment of the process according to the present invention for producing zinc oxide from EAF dust.
  • EAF dust typically includes zinc, manganese, lead, copper and cadmium. Other trace elements may also be present. The process therefore follows the same basic steps as illustrated in Figure 1 .
  • the EAF dust is leached with an alkaline lixiviant comprising an aqueous mixture of ammonium chloride and ammonia.
  • the leaching step produces a leachate substantially including the zinc with solubilised manganese, lead, copper and cadmium. A leached solids content is also present.
  • the leached mixture is then filtered to remove the leached solids.
  • the resulting leach liquor then passed through a controlled oxidation step to remove the lead and manganese from the liquor, followed by a cementation step where the copper and cadmium are removed by cementation on zinc. Further filtration steps may be used after the controlled oxidation step and/or cementation step to separate out the solid content from the liquor.
  • the resultant liquor predominantly includes the zinc in solution.
  • This zinc rich leachate is then passed into a hot ammonia stripping step which results in basic zinc compounds precipitating out into the stripped solution. In this case, zinc dichlorodiammine crystals are predominantly formed.
  • This stripping step produces a stripped liquid containing solid zinc product. Again, the stripped ammonia is captured for recycle to the leaching step.
  • the stripped liquid is then passed through a separation stage to separate the zinc compound precipitate from the liquor.
  • the resulting separated liquor is then recycled for use in the leaching step.
  • the separation stage also includes a solids wash cycle.
  • the separated the zinc dichlorodiammine precipitate is then hydrolysed with hot water to form a hydrolysis product (typically Zn(OH) 2 ), which is then heated to drive off water to form a zinc oxide product.
  • the hydrolysis step preferably includes a hot dilution step, however this could be conducted at any temperature, hot or cold.
  • the liquor bearing ammonium chloride from this step is also recycled for use in the leaching step.
  • the zinc oxide product is then dried.
  • the leach examples hereafter have treated EAF dust with the content of Table 1 .
  • the mixture was then kept in the closed plastic bottle for 2 days at 23°C.
  • the same procedures of filtering, rinsing and measurements as described above were followed.
  • the zinc solubilised was calculated as 0.71 g representing 0.34 % of the zinc contained in the sample of EAF dust. Thus, the total zinc extraction was 77 %.

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Abstract

L'invention concerne un procédé d'extraction de zinc à partir d'une matière contenant du zinc, ce procédé comprenant les étapes qui consistent à: lixivier la matière contenant du zinc à l'aide d'un lixiviant alcalin qui comprend une espèce d'ammonium, une espèce d'hydroxyde et une espèce d'halogénure afin de produire un lixiviat contenant du zinc; extraire par stripage l'ammoniac du lixiviat pour produire une liqueur épurée qui contient un précipité contenant du zinc; et extraire le zinc de la liqueur épurée.
PCT/AU2011/001508 2010-11-23 2011-11-23 Procédé d'extraction de zinc et/ou d'oxyde de zinc i Ceased WO2012068621A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2010905189 2010-11-23
AU2010905189A AU2010905189A0 (en) 2010-11-23 Process for recovering zinc and/or zinc oxide l

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WO2012068621A1 true WO2012068621A1 (fr) 2012-05-31

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2814993A4 (fr) * 2012-02-15 2015-10-21 Metallic Waste Solutions Pty Ltd Procédé pour la production d'oxyde de zinc à partir de minerai
RU2623519C1 (ru) * 2016-08-30 2017-06-27 Игорь Олегович Цой Способ выделения оксидов цинка и меди
CN109182749A (zh) * 2018-08-01 2019-01-11 昆明理工大学 一种氧化锌矿碱性浸出剂及其浸出方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU1712433A1 (ru) * 1990-01-18 1992-02-15 Нижегородский политехнический институт Способ выделени оксидов цинка и меди из водно-аммиачных растворов
CN1093418A (zh) * 1993-04-09 1994-10-12 广州市新技术应用研究所 络合物电解制锌
WO1998048066A1 (fr) * 1995-05-11 1998-10-29 Metals Recycling Technologies Corp. Procede d'utilisation du reglage du ph dans la recuperation de metaux et de produits chimiques utiles provenant de flux de dechets industriels

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU1712433A1 (ru) * 1990-01-18 1992-02-15 Нижегородский политехнический институт Способ выделени оксидов цинка и меди из водно-аммиачных растворов
CN1093418A (zh) * 1993-04-09 1994-10-12 广州市新技术应用研究所 络合物电解制锌
WO1998048066A1 (fr) * 1995-05-11 1998-10-29 Metals Recycling Technologies Corp. Procede d'utilisation du reglage du ph dans la recuperation de metaux et de produits chimiques utiles provenant de flux de dechets industriels

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2814993A4 (fr) * 2012-02-15 2015-10-21 Metallic Waste Solutions Pty Ltd Procédé pour la production d'oxyde de zinc à partir de minerai
AU2013220926B2 (en) * 2012-02-15 2016-10-06 Steel Dynamics Investments, LLC Process for zinc oxide production from ore
RU2623519C1 (ru) * 2016-08-30 2017-06-27 Игорь Олегович Цой Способ выделения оксидов цинка и меди
CN109182749A (zh) * 2018-08-01 2019-01-11 昆明理工大学 一种氧化锌矿碱性浸出剂及其浸出方法

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