WO2023152655A1 - Procédé hydrométallurgique pour la récupération sélective de vanadium, de molybdène et d'autres métaux de base à partir de divers types de déchets industriels - Google Patents

Procédé hydrométallurgique pour la récupération sélective de vanadium, de molybdène et d'autres métaux de base à partir de divers types de déchets industriels Download PDF

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Publication number
WO2023152655A1
WO2023152655A1 PCT/IB2023/051122 IB2023051122W WO2023152655A1 WO 2023152655 A1 WO2023152655 A1 WO 2023152655A1 IB 2023051122 W IB2023051122 W IB 2023051122W WO 2023152655 A1 WO2023152655 A1 WO 2023152655A1
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iii
solution
naoh
hydrogen peroxide
sodium hydroxide
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PCT/IB2023/051122
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English (en)
Inventor
Ionela BIRLOAGA
Pietro ROMANO
Francesco VEGLIÒ
Alfredo Mancini
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Orim S.P.A.
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Publication of WO2023152655A1 publication Critical patent/WO2023152655A1/fr

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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
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0407—Leaching processes
    • 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
    • C22B21/00—Obtaining aluminium
    • C22B21/0015—Obtaining aluminium by wet processes
    • C22B21/0023—Obtaining aluminium by wet processes from waste materials
    • C22B21/003—Obtaining aluminium by wet processes from waste materials from spent catalysts
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0407—Leaching processes
    • C22B23/0446—Leaching processes with an ammoniacal liquor or with a hydroxide of an alkali or alkaline-earth metal
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00—Obtaining nickel or cobalt
    • C22B23/04—Obtaining nickel or cobalt by wet processes
    • C22B23/0453—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B23/0461—Treatment or purification of solutions, e.g. obtained by leaching by chemical methods
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/26—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
    • C22B34/00—Obtaining refractory metals
    • C22B34/20—Obtaining niobium, tantalum or vanadium
    • C22B34/22—Obtaining vanadium
    • C22B34/225—Obtaining vanadium from spent catalysts
    • 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
    • C22B34/00—Obtaining refractory metals
    • C22B34/30—Obtaining chromium, molybdenum or tungsten
    • C22B34/34—Obtaining molybdenum
    • C22B34/345—Obtaining molybdenum from spent catalysts
    • 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
    • C22B7/006—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

Definitions

  • the present invention relates to a hydrometallurgical process whose main purpose is recovery ofthe metalsV,Mo,Niand Co from many typesofindustrialwaste.
  • the proposed process is economical, easily manageable and innovativesincetheprocesseshithertoreportedin theliteratureconsist ofeither thermalprocesses or a combination ofthermaland aqueous processes,oreven hydrometallurgicalprocesses,butwith theuseofacid leaching solutions.
  • Also,one ofthe process solutions proposed in the present invention takes place under atmospheric pressure and at a temperatureofnomorethan 60°C,which isveryadvantageousin terms ofoperation andin particularin termsofenergy used.
  • the proposed process is very flexible and can easily be adapted to differenttypes ofwaste withoutmajor modificationsto the processschemeandplantlayout.
  • Catalystsareusedin awiderangeofindustrialapplications such as oil refining, petrochemical production, polymer processing, environmental protection reactions and chemical synthesis.
  • catalysts are indispensable in the conventional production ofgasoline,diesel,heavy hydrocarbons,plastics,etc.
  • PatentKR 10-1189183 describes a pyrometallurgicalprocess in which V,Ni and Mo can be recovered from spent HPR catalysts as ferroalloys.
  • TheFe-V-Ni-Moalloy obtained isthen treated atabout1200°C in thepresenceofoxygen and iron oxidefortheselectiveoxidation ofV.
  • the resultingsludgeisthen subjected toan alumino-thermalreduction processtoproduceFe-V alloy.
  • hydrometallurgical processes Compared to pyrometallurgical processes, hydrometallurgical processes have the advantagethatthey can be controlled and managed much more easily; moreover, most of them have no emissions of substances that are hazardousto humans and the environmentand generally require less investment.
  • US8287618B2 describes a processforthe recovery ofNi,Mo,V, Co and Al using a combination of heat treatment and a hydrometallurgical process.
  • the process starts with de-oiling of the catalyst in toluene or naphtha solution.It is then ground and the resultingpowderissubjected tothe removalofcoke and sulfurspecies by means of a thermal process carried out at around 500°C.
  • CN105274344A discloses a process in which the catalyst undergoestworoasting stages.Thefirstisperformed toremovecarbon and oilata temperature of500-600°C. The second isperformed in the presenceofsodium carbonateat600-850°C.Thetreatedcatalystisthen ground and leached with water athigh temperature to recover soluble molybdenum andvanadium salts.
  • US 2007/025899 discloses a hydrometallurgicalprocess for the recoveryofV,MoandNi.Theprocessinvolveswashingthecatalystwith an organicsolventsuch asToluene,XyleneorKerosene (othersolvents may alsobeused)underpressure orathigh temperatures.Leaching of thewashed catalysttakesplacewith NH 3 and O 2 athigh temperatures. In this way V is directly precipitated as NH 4 VO 3 .Niis recovered by solventextractionwhileMoisrecoveredlastas(NH 4 ) 2 MoO 4 bychanging thepH.
  • an organicsolvent such asToluene,XyleneorKerosene (othersolvents may alsobeused)underpressure orathigh temperatures.
  • Leaching of thewashed catalyst takesplacewith NH 3 and O 2 athigh temperatures. In this way V is directly precipitated as NH 4 VO 3 .Niis recovered by solventextractionwhileMoisrecoveredlastas(NH 4
  • Thepresentinvention relatestoahydrometallurgicalprocessthat enablesV,Mo,Niand Cotoberecovered from many typesofindustrial waste.
  • wastes that can be treated are the various wastes from the petroleum industry such as LC-Fining type catalysts (LCF, Lummus-Cities expanded-bed process) or sludge from the petroleum refining process;in addition,waste from the pharmaceuticalindustry such asMo-based catalystscan alsobetreated.
  • the treatmentprocess according to the invention comprisesthe followingmain steps:
  • step II-A Drying of the solid obtained in step I) and grinding with a planetary ballmill,where grinding may also carried outbefore step I), ifnecessary;
  • step V Mixing of the solution and wash water from step IV), neutralisation with HCl or H 2 SO 4 and selective precipitation of molybdenum (Mo)with theaddition ofacationicpolyelectrolytesolution forsolutionsfrom LCF catalysttreatmentand sludge;forthe solution from Mo catalysttreatment (step III-A)),afterthe acid neutralisation step,ammonium chloride orammonium sulfateisadded toprecipitate Mo asammonium molybdate((NH 4 ) 2 MoO 4 );theprecipitateobtainedis recoveredfrom thesolution byfiltration;
  • Mo molybdenum
  • stepVI) Theleachingsolutionfrom stepVI)issenttothenickel(Ni)and/or cobalt(Co)recovery step;Nirecovery can becarried outby electrolysis orprecipitation while Co recovery can be carried outby precipitation.
  • Precipitation forboth elements is carried outby neutralisation ofthe solution with sodium hydroxide and subsequent addition of sodium carbonate(Na 2 CO 3 )oroxalicacid(C 2 H 2 O 4 );inthecaseofjointtreatment of Ni-Mo and Co-Mo catalysts,solvent extraction may be used,for example using di-(2-ethylhexyl)phosphoricacid (D2EHPA)or CIANEX in an organicdiluentsuch asn-heptane;
  • D2EHPA di-(2-ethylhexyl)phosphoricacid
  • CIANEX organicdiluent
  • step V) for the treatment ofLCF or refining sludgeistreated with an organicsolventtoremove residualMo andV ions The solution from step V)for the treatment ofLCF or refining sludgeistreated with an organicsolventtoremove residualMo andV ions.
  • step II-B Roastingofthe solid obtained in step I)inside a rotary kiln with subsequentgrindingwith aplanetaryballmill,wheregrindingmayalso carriedoutbeforestep I));
  • step III-B Leaching ofthe solid (obtained from step II-B)) to dissolve V and/orMo with an aqueous alkaline sodium hydroxide solution (H 2 O- NaOH) or ozone (O 3 )as described for step III-A)to oxidise the metals remainingassulfidesduringstep II-B).
  • H 2 O- NaOH aqueous alkaline sodium hydroxide solution
  • O 3 ozone
  • Figure 1 showsablock diagram ofthehydrometallurgicalprocess relatingtothepresentinvention.
  • Thediagram refersin particulartothe treatmentofLCF catalyst,butcan easilybeadaptedtoalltypesofwaste by followingwhatwassaid earlierin thisdocument.
  • LCF istreated using alternativeA,afterthewashingin step I)thereis air drying,grinding which may also be carried outprior to step I and basic leaching with hydrogen peroxide and sodium hydroxide III- A), whereozone(O 3 )may alsobeusedasdescribedabove.
  • step II-B rotary kiln
  • step I a calcination which may also be carried outbefore step I,and leaching iscarried outwith sodium hydroxide (step III-B)).
  • Mo-based catalyst grindingandleachingiscarried outasdescribed in step III-A)).
  • Figure2 shows theeffectofremovingtheorganiccomponent(step I))on theestimatedheatprofileinsidetherotary kiln in step II-B).
  • the LCF catalyst iswashedwith apolarsolvent such asacetone or ethanol,or a surfactant,either as an alternative to the solvent or consecutively,for 15-45 minutesata solid concentration of10-30% w/v.
  • apolarsolvent such asacetone or ethanol
  • surfactant either as an alternative to the solvent or consecutively,for 15-45 minutesata solid concentration of10-30% w/v.
  • Theuseofaveryvolatilesolvent such asacetoneorethanolallows thesolventtobealmostcompletelyrecoveredwith relativelylow energy consumption, unlike the various solvents used in other similar processes.
  • the washed catalyst undergoes drying at a temperature of25- 60°C,followedby grindingwith aplanetary ballmillto a solid particle size oflessthan 200 pm (step II-A)).Grinding can also be carried out beforethewashingstep (step I).
  • Leaching is performed at a solid concentration of 10-20% for a timeof1-4 hoursatroom temperature,with orwithoutstirring.Ozone (O 3 ) may be used as an oxidant instead of or in combination with hydrogen peroxide.By continuously feeding gaseous ozone into the reaction environment,itispossible to solubilise the gas in the liquid phase.In this way,oxidation of the various metals present can be achieved by reducingtheamountofhydrogen peroxiderequired forthe reaction, and the hydrogen peroxide can be completely replaced by ozone.Attheendofthereactiontheresidualsolidisfilteredandwashed with water.
  • step III-A iscarried outdirectly by leachingwith the aqueous solution ofsodium hydroxide and hydrogen peroxidementioned forthe treatmentofLCF.
  • Step IV)ofthepresentinvention relatestotheselectiverecovery ofvanadium by meansofaprecipitation step.
  • Theleachingsolution and the wash water from Step III-A) are mixed and,once purified from elements such as arsenic and phosphorus, are neutralised with an inorganicacid (i.e.sulfuricacid orhydrochloricacid)untilthepH value is in the range 6-8.
  • an inorganicacid i.e.sulfuricacid orhydrochloricacid
  • ammonium chlorideorammonium sulfate isadded in therange2-3in excessofthe stoichiometric amountrequired for reaction with the vanadium in the solution.
  • Selective precipitation ofV iscarried outata temperature of almost40°C ( ⁇ 5°C)for 1-2 hours.Finally,the precipitate is separated from the solution by filtration and then washed with an ammonium chloride orammonium sulfate solution ata concentration of
  • the metavanadate iswashed to replace the solution in the cake and recoverthesolublemolybdenum presentin it.
  • Ammonium metavanadate can be heated above 450°C in an oxidisingatmosphere.ThisdecomposesintogranularV 2 O 5 and gaseous ammonia.GranularV 2 O 5 can bemelted and reduced toflakes.
  • the leaching solution is neutralised to pH 1.5-3 with HCI.
  • HCI ammonium molybdate
  • ammonium chlorideisaddedtoaconcentration 10-30g/l.
  • stepVI) theresidualsolidfrom theleachingprocessin step III- A)forLCF catalystisleachedwith sulfuricacid and hydrogen peroxide in thefollowingconcentrations: - 1-2M sulfuricacid;
  • Leaching takes place over a period of 2-4 hours, at a solid concentration of5-15%.Theprocessiscarried outatroom temperature. At the end ofthe reaction, the residual solid is separated from the solution by filtration andthen washedwith water.
  • step VI) The solution from step VI)issentto step VII)fortherecovery of Ni and/orCo.Nican berecovered by electrolysisorprecipitation while Co can berecoveredbyprecipitation.Both elementsareprecipitatedout by neutralising the solution with sodium hydroxide and then adding sodium carbonate (Na 2 CO 3 )oroxalicacid (C 2 H 2 O 4 ).
  • the aqueoussolution from themolybdicacidprecipitation section described in step V) is suitably neutralised to a pH of 2.0-2.5 and subjected to an oxidation processwith hydrogen peroxide to bring the vanadium toitshigheroxidised form.
  • the solution isthen treated with an organic solution containing a quaternary amine asin step VIII)to extracttheresidualmolybdenum and vanadium and obtain a raffinate free ofthese elements.
  • the extraction process isvery fast,and the Mo and V ions,present as anions,are captured by the extractant in the organicphaseunderacid conditions.
  • Theextraction yield isnot100% in a single stage,so severalstages are required to recover allthe ionsof interest.Thisoperation isperformed in mixersand settlersin seriesor in countercurrentliquid-liquid extraction columns.
  • the organic solution (extract) is brought into contact with an alkaline stripping solution that counter-extracts Mo and V (again as anions) in several stages.
  • This basic solution is recycled before the arsenicand phosphorusprecipitation step in step IV).
  • the regenerated organic solution is stored and then reused for a further solvent extraction process,with theaddition ofa smallamountofmake-up.
  • the oxidant is oxygen,which is reacted with the material inside a rotary kiln at a temperature of approximately 800-900°C.Reducing the amountoforganic substances presenton thecatalystisessentialtoavoidan uncontrolledtemperature rise in the furnace resulting in sintering ofthe alumina.Thisleadsto difficultiesin the oxygenation and complexation ofthe materialwith a consequentdecreasein theextraction yield ofmetalsofinterestduring leaching.In some processes described in the literature,the organic materialis reduced through an initialroasting in a rotary kiln and subsequentcalcination.
  • step I)in alternative B allows much of the organic component to be removed, with a significant reduction in gaseous emissions compared to the various processes described in the literatureewhich havedoubleheattreatment.
  • Figure 2 shows the effecton thethermalprofile along thewhole axis ofthe rotary kiln due to the percentage ofthe organiccomponent stillpresenton thewashed catalyst.
  • Step III-B) involves leaching of the pre-treated and ground catalystasin step II-B).Leachingisperformedwith an alkalinesolution ofwater and sodium hydroxide (H 2 O-NaOH)with a sodium hydroxide concentration of0.5-4M,atasolid concentration of10-20% foratimeof 2-3hoursatroom temperaturewith orwithoutstirring.Itispossibleto use ozone (O 3 ) as described for step III-A) to oxidise the metals remaining assulfidesduring step II-B).In thiscase,ozoneisfed tothe leaching reactor in quantities that differ from those in step III-A): additions ofthe reagents are optimised flexibly using redox potential- typesensorsorspecificstandardconditionsmanagedbysoftware.Atthe end ofthereaction theresidualsolidisfiltered andwashedwith water.
  • the furnacein step II-B) maybeofdifferenttypes.However,itis preferabletouse a rotary kiln forgreaterefficiency in oxygenation and complexation ofthe solid phase.
  • the furnace may be either electric or fuel-fired;in the case of a fuel-fired furnace, a configuration using hydrogen rather than methane hasbeen considered to further reduce the gaseousemissionsrelatedtothisthermalstep.
  • the process according to the invention is carried outatatemperaturenotexceeding60°C.
  • A.Washing isperformed with acetone,according to the invention.
  • the process may also be performed without roasting.
  • the first leaching is with caustic soda only;without roasting,leaching involvesthe use ofNaOH and H 2 O 2 ,possibly with ozone(O 3 )insteadoforin combination with H 2 O 2 .
  • the washed solid wasdried in airand a weightlossofabout8% was estimated.Subsequently,the solid was ground using a planetary mill with a stainless steel container and metal balls to reduce the particlesizebelow 200 pm.Themillwasprogrammed ata speed of600 rpm for10minutes.
  • Theleachingreaction wasconducted atroom temperatureand at atmosphericpressure for about3 hourswithoutstirring.
  • the residual solid wasthen separatedfrom thesolutionbyfiltration andwashedwith 12 mlofwater (30% vol./vol.oftheinitialsolution).
  • the residualsolid was dried in an oven at 60°C for 24 hours and the weight loss was determinedtobeabout27% andthemoisturecontentofthesolidbefore dryingabout30%.
  • Thefinalsolution andwashwater were analysesdtodeterminethe concentrationsofvanadium and molybdenum.Vanadium recovery was achieved with a yield ofabout80% and molybdenum recovery with a yieldofabout85%.
  • the precipitation reaction was conducted at 40°C and atmosphericpressureforabout2hoursat200rpm.
  • Thesolidprecipitate was filtered and dried.
  • the recovery yield obtained for vanadium precipitation wasover70%.
  • the leaching reaction was conducted at room temperature and atmosphericpressurefor1houratamixingspeed of200rpm. Atthe end ofthe reaction the residualsolid wasseparated from the solution by filtration and washed with 15 mlofwater (30% vol.of theinitialsolution).Theresidualsolidwasdriedin an oven at60°C for 24 hoursand theweightlosswasdetermined tobe about35% and the moisturecontentofthesolidbeforedryingabout34%.
  • the alkaline aqueous solution obtained from the leaching step was subjectedtoaselectivemolybdenum precipitation step.98mlofthe solution obtained as described above was neutralised to pH 1.5 with 7.2 ml of 37% w/w HCl. NH 4 CI was added to the solution to a concentration of20g/1.
  • the precipitation reaction was conducted at room temperature andatmosphericpressureforabout30minwith astirringspeedofabout 200 rpm.
  • the solid precipitate was separated from the solution by filtration andwashedwith 12mlofwater.Finally,thesolidprecipitate was driedin an oven at105°C for48hours.
  • Molybdenum wasrecoveredasmolybdenum trioxideMoO 3 with a recoveryyield ofover98% and apurity ofabout95%.
  • the leaching reaction was conducted for 3 hours at room temperatureand astirringspeed ofapproximately 250rpm.Attheend ofthe reaction,filtration was performed and the residual solid was washedwith 30mlofwater(30% vol/volratioofwashwatertosolution).
  • Vanadium was recovered in excess of 65% yield in a single leaching stage.An increasein temperatureand hydrogen peroxidewas foundtoincreasetheextraction yield above90%.
  • Vanadium wasrecoveredwith arecovery yieldofover90% and a purity ofabout95%.
  • Vanadium was recovered in excess of 70% yield in a single leaching stage,whilemolybdenum wasrecoveredin excessof95% yield.
  • HyVent.Availableonline http://www.hyvent.nl/spent%20catalyst.html.

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Abstract

Procédé hydrométallurgique dont le but principal est la récupération des métaux V, Mo, Ni et Co à partir de nombreux types de déchets industriels.
PCT/IB2023/051122 2022-02-11 2023-02-08 Procédé hydrométallurgique pour la récupération sélective de vanadium, de molybdène et d'autres métaux de base à partir de divers types de déchets industriels WO2023152655A1 (fr)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN117403055A (zh) * 2023-10-17 2024-01-16 广东诚一环保科技有限公司 一种废渣中稀有金属回收处理的方法

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US4721606A (en) * 1982-08-20 1988-01-26 Union Oil Company Of California Recovery of metal values from spent catalysts
US20070025899A1 (en) * 2005-07-29 2007-02-01 Chevron U.S.A. Inc. Process for metals recovery from spent catalyst
US8287618B2 (en) * 2010-11-10 2012-10-16 Kuwait Institute For Scientific Research Method or process for recovering Mo, V, Ni, Co and Al from spent catalysts using ultrasonic assisted leaching with EDTA
CN105274344A (zh) * 2015-11-23 2016-01-27 刘楚玲 一种从废石油催化剂中回收钒和钼的方法

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US4721606A (en) * 1982-08-20 1988-01-26 Union Oil Company Of California Recovery of metal values from spent catalysts
US20070025899A1 (en) * 2005-07-29 2007-02-01 Chevron U.S.A. Inc. Process for metals recovery from spent catalyst
US8287618B2 (en) * 2010-11-10 2012-10-16 Kuwait Institute For Scientific Research Method or process for recovering Mo, V, Ni, Co and Al from spent catalysts using ultrasonic assisted leaching with EDTA
CN105274344A (zh) * 2015-11-23 2016-01-27 刘楚玲 一种从废石油催化剂中回收钒和钼的方法

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Title
CHEN Y ET AL: "Investigations on the extraction of molybdenum and vanadium from ammonia leaching residue of spent catalyst", INTERNATIONAL JOURNAL OF MINERAL PROCESSING, ELSEVIER SCIENCE PUBLISHERS, AMSTERDAM, NL, vol. 79, no. 1, 1 April 2006 (2006-04-01), pages 42 - 48, XP027881491, ISSN: 0301-7516, [retrieved on 20060401] *
PARK K H ET AL: "Hydrometallurgical processing and recovery of molybdenum trioxide from spent catalyst", INTERNATIONAL JOURNAL OF MINERAL PROCESSING, ELSEVIER SCIENCE PUBLISHERS, AMSTERDAM, NL, vol. 80, no. 2-4, 1 September 2006 (2006-09-01), pages 261 - 265, XP027881545, ISSN: 0301-7516, [retrieved on 20060901] *
PARK K H ET AL: "Selective recovery of molybdenum from spent HDS catalyst using oxidative soda ash leach/carbon adsorption method", JOURNAL OF HAZARDOUS MATERIALS, ELSEVIER, AMSTERDAM, NL, vol. 138, no. 2, 16 November 2006 (2006-11-16), pages 311 - 316, XP027885121, ISSN: 0304-3894, [retrieved on 20061116] *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN117403055A (zh) * 2023-10-17 2024-01-16 广东诚一环保科技有限公司 一种废渣中稀有金属回收处理的方法
CN117403055B (zh) * 2023-10-17 2024-06-07 广东诚一环保科技有限公司 一种废渣中稀有金属回收处理的方法

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