US20100111787A1 - Method of recovering valuable metals from the vrds spent catalyst - Google Patents

Method of recovering valuable metals from the vrds spent catalyst Download PDF

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Publication number
US20100111787A1
US20100111787A1 US12/530,743 US53074308A US2010111787A1 US 20100111787 A1 US20100111787 A1 US 20100111787A1 US 53074308 A US53074308 A US 53074308A US 2010111787 A1 US2010111787 A1 US 2010111787A1
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solution
oxide
sodium
water
filtrate
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Man Joo Kim
Kyung Soo Kim
Kyung Min Kim
Seong Hwan Kim
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    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G31/00—Compounds of vanadium
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G31/00—Compounds of vanadium
    • C01G31/02—Oxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G39/00—Compounds of molybdenum
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G39/00—Compounds of molybdenum
    • C01G39/02—Oxides; Hydroxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G53/00—Compounds of nickel
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
    • 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
    • C22B7/008—Wet processes by an alkaline or ammoniacal leaching
    • 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
    • C22B7/009—General processes for recovering metals or metallic compounds from spent catalysts
    • 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

  • This invention relates to a method of recovering metals, such as vanadium, molybdenum, nickel (hereafter, referred to as “valuable matals”), from the catalysts spent in the ‘Vacuum Residue Desulfurization’ (VRDS) process for desulfurization of pertroleum.
  • metals such as vanadium, molybdenum, nickel (hereafter, referred to as “valuable matals”)
  • the conventonal method comprises removing the soaked oil from the spent catalysts by heating the catalysts over the boiling point of oil and thus evaporating the soaked oil from the catalysts.
  • the spent catalysts are roeated at 400 ⁇ 600° C. in the furnace with air (oxyzen) supplied to oxidize sulfur and metals in the catalysts.
  • air oxygen supplied to oxidize sulfur and metals in the catalysts.
  • the sulfur is oxidized into SO 2
  • the metals, such as molybdenum, vanadium, nickel and cobalt are oxidized into MoO 3 , V 2 O 5 , NiO, and CoO, respectively.
  • the SO 2 is induced into an absober (cap-type tower), and then absorbed in water solution of sodium hydoxide to be converted into solution of sodium sulfite (Na 2 SO3).
  • the solution of sodium sulfite is dained out from the absorber.
  • nickel and cobalt In recovery of nickel and cobalt, the oxides of nickel and cobalt are milled, and then nickel and cobalt are extracted from the miled oxides of the metals in ammonia solution. As the extracted nickel and cobalt contains water soaked therein during the previous extraction process, an additional process of drying the soaked nickel and cobalt is required. This makes the whole processes for recovery of metals complex. Further, ammonium salts of nickel and cobalt are formed in the extraction process and thus make separation of the metals incomplete. Because of the above-mentioned disadvantages, a process for roasting proceeds without recovering nickel and cobalt.
  • the conventional process comprises inducing the oxidized waste catalysts with sodium carbonate (Na 2 CO 3 ) continuously and quantitatively into a rotary kiln, and maintaining the rotary kiln at a temperature of 600° C. to melt the oxides of the metals with the sodium carbonate therein.
  • aluminium may be obtained in a form of mixture such as water-insoluble sodium aluminate.
  • Vanadium and molybdenum are obtained in the form of their sodium salts, such as water-soluble sodium vanadate (NaVO 3 ) and sodium molybdate (Na 2 MoO 4 ).
  • the conventional process further comprises milling the roasted product obtained in the preceeding process, agitating the milled roasted-product in the warm water at a temperature of 80° C. and then leaching the formed sodium salts for one hours, washing the leachates at one or twice, controlling the washing liquid at pH 8.0, and agitating the washing liquids with ammonium chloride (NH 4 cl) mixed therein to precipitate crystals of amonium metavanadate (NH 4 VO 3 ).
  • ammonium chloride NH 4 cl
  • the volume of ammonium chloride is used more than thioretical volume. Further, after separaing the precipiates from the mother solution, pH of the mother solution is lowered at the range of pH 2 ⁇ 3. And then, solution of ammonium chloride is added to the mother solution lowered at pH 2-3 so as to remove sufate ion (SO 4 ⁇ 2 ) therein, and thus calcium sulfate (CaSO 4) is precipitated. After removing the precipitates of calcium sulfate and then increasing pH of the mother solution, solution of calcium chloride is added to the mother solution so as to precipiate calcium molybdate (CaMoO 4 ). molybdenum oxides can be obtained by leaching and washing the precipiated calcium molybdate, and then decompounding the precipiated calcium molybdate with hydrochloric acid.
  • the conventional method has disadvantages as followings.
  • the method requires expensive equipments, such as a rotary Kiln, for roasting at a high temperature (900° C.). Because costs is very high, a recovery of nickel wolud not be performed.
  • the waste catalysts contain aluminum oxide therein at a rate of 65 percentage, the aluminum oxide is discarded in a form of water-insoluble aluminum compound, thereby resulting in waste of resources.
  • the present invention comprises pre-treating the waste catalysts for deoiling and desulfurization; forming sodium aluminate, sodium vanadate and sodium molybdate as water-soluble reactants, and nickel oxide, cobalt oxide as water-insoluble reactants by reacting the pre-treated waste crystals in solution of sodium hydroxide at a temperature of 135 ⁇ 160° C.; and leaching the water-inslouble nickel oxide, cobalt oxide and impurities, thereby remaining the water-soluble sodium aluminate, sodium vanadate and sodium molybdate in the solution.
  • the present invention further comprises heating the filtrate containing the sodium aluminate, sodium vanadate and sodium molybdate so as to increase a temperature of the filtrate over a temerature of 80° C., and agitating the filtrate with adding hydrochloric acid or sulfhuric acid therein so as to maintain pH 9.5; forming aluminum oxide at the temperture over 110° C. with heat of the reaction; and recovering the aluminum oxide by leaching.
  • the present invention comprises forming a solution containing sodium vanadate and sodium molybdate bt treating the waste catalysts; heating the solution with the solution maintained in pH 1.0 ⁇ 1.0; and precipitating molybdenum oxide and vanadium oxide in the solution by aeration thereof.
  • the present invention further comprises adding ammonia water to the solution in which molybdenum oxide and vanadium oxide are precipitated and thus agitating the mixtured solution so as to precipitate amonium metavanadate with ammonium molybdate remaining in the solution; and recovering and separating the crystals of the precipitated amonium metavanadate from the solution.
  • the present invention can increase yield of vanadium and molybdenum from the waste catalyst at lower temperature and further recover aluminum as well as nickel and coblat without additional processes.
  • the present invention can recover valuable matals from the waste catalysts without discharging waste water containing ammonia nitrogen, thereby reducing costs for purifying waster water.
  • the present invention can reduce costs of maunfacturing beecause it does not require expensive equipments, such as a rotary Kiln, for roasting at a high temperature (900° C.).
  • FIG. 1 shows a flow diagram of the process according to the present invention.
  • the waste catalysts used in the ‘Vacuum Residue Desulfurization’ (VRDS) process for desulfurization of pertoleum may be pre-treated by the known various methods. That is, the pre-treatments of the waste catalysts, such as oil-removing, sulphur-removing, and oxidization of metals, are accomplished by generally known processes. For example, oils soaked in the waste catalysts are removed by heating the catalysts at a temperature over the boiling point of oil.
  • the deoiled waste catalysts are maintaining at a temperature of 400° C. with heating in the deoiling process. Before cooling, the waste catalysts are induced into the roasting furnace and roasted with the supplied oxygen at a temperature of 400 ⁇ 600° C.
  • the metals such as molybdenum, vanadium, nickel, cobalt
  • the waste catalysts are oxidized and thus coverted into their oxides, such as MoO 3 , V 2 O 3 , NiO, CoO, and also the sulphur is oxidized and converted into sulphuric acid gas (SO 2 ).
  • the sulphuric acid gas is absorbed in solution of sodium hydroxide (NaOH) and converted into sodium sulfite (Na 2 SO 3 ), which is drained out.
  • the waste catalysts are dissolved in solution of sodium hydroxide and then the solution is agitated.
  • the non-reactants including NiO, Fe2O3 are leached and thus separated from the solution.
  • 80 PBW (Parts By Weight) of and 80 PBW of sodium hydroxide are poured and then mixed in a reactor equipped with an agitator.
  • the sodium hydroxide is dissolved with heat of dissolution.
  • the solution is heated pressurelessly until the temperature of the solution reached at 135 ⁇ 160° C. by adding 100 80 PBW of the oxidized waste catalysts therein.
  • NiO, FeO and CoO would not be dissolved and thus remain in the solution. 400 PBW of water is added so as to prevent reprecipitation of reactants by dilution of the solution. Then, the residues including NiO are leached from the solution. Nickel can be simply recovered from the residues.
  • the filtrate contains sodium aluminate (NaAl(OH) 4 ).
  • NaAl(OH) 4 sodium aluminate
  • the filtrate is stirred with an agitator and heated at a temperature of 85 ⁇ 90° C. and then sulphuric acid or hydrochloric acid (20 ⁇ 30%) is added into the filtrate.
  • the addition of the acid to the solution should be controlled to be maintained at pH 9.5.
  • aluminum oxide Al 2 O 3
  • the aluminum oxide is washed with water until vanadium is not detected in the water.
  • the water in the aluminum oxide is dried with suction of a vacuum pump.
  • the beolw reaction formulas show various products of aluminum oxide according to gradients of temperature at pH 9.5 ⁇ 14.
  • NaAl(OH) 4 +HCl AlO(OH)+NaCl+2H2O (80° C. ⁇ 95° C.) ⁇ circle around (2) ⁇
  • the reactant, Al(OH) 3 can not be separted by leaching. Accordingly, a rotary kiln should be required for recovery of aluminum in the condition of the reaction ⁇ circle around (1) ⁇ .
  • the reactant, AlO(OH) by the reaction ⁇ circle around (2) ⁇ may remain but may also be leached. Therefore, the condition of reaction temperatures in the reaction ⁇ circle around (3) ⁇ is accepatable. When the reaction proceeds at a temperature over 80° C., the temperature get increased over 110° C. by the heat of reaction.
  • the above process of recovering aluminum is required to be proceeded at a temperature over 110° C. because the reactant, Al(OH) 3 is not produced at the temperature.
  • the temperature of the reaction is not liminted by the upper limit but preferably maintained at a temperature of 100° C.
  • solution of HCl is added to the filtrate of pH 9 ⁇ 14.
  • sole Al 2 O 3 may be obtained by removing sodium oxide (Na 2 O) from the filtrate.
  • sodium vanadate (NaVO 3 ) and sodium molybdate (Na 2 MoO 4 ) in the filtrate from which Al2O3 is removed.
  • the filtrate is agitated below pH 1 (pH ⁇ 1.0) at 85° C. until the reaction is completed.
  • the filtrate is agitated below pH 1 at 85 ⁇ 100° C. and further aetated therein continuously or periodically.
  • mixtures of molybdenum oxide and vanadium oxide are precipitated in the solution.
  • the precipitated molybdenum oxide and vanadium oxide may be obtained by leaching.
  • acid solution should be used to maintain the solution below pH 2, preferably below pH 1 at a temperature of 80° C. This temperature of reaction is dominantly lower than that of the conventional procsess, which makes heating equipments of high price to be useless.
  • the present invention may further comprise adding ammonia water to the solution in which molybdenum oxide (MoO 3 ) and vanadium oxide (V 2 O 5 ) are precipitated, agitating the mixtured solution and thus precipitating amonium metavanadate (NH 4 VO 3 ) and ammonium molybdate ((NH 4 )2MoO4) by using diiference of solubilty thereof; and recovering and separating the crystals of the precipitated amonium metavanadate and ammonium molybdate from the solution.
  • MoO 3 molybdenum oxide
  • V 2 O 5 vanadium oxide
  • ammonium molybdate (NH 4 )2MoO4)
  • molybdenum oxide (MoO) and vanadium oxide (V 2 O 5 ) are furhter added to the mother solution with amonium water.
  • molybdenum oxide (MoO 3 ) and vanadium oxide (V 2 O 5 ) are dissolved in the mother solution by re-heating, and then amonium metavanadate is obtained by cooling the mother solution.
  • ammonium molybdate and amonium metavanadate of high purity are obtained by minimizing dissoved amonium metavanadate.
  • the specific weight of mother solution may vary as quantity of water or molybdenum in the waste catalyst.
  • the mother solution may be reused as reaction solution.
  • the specific weight is over 2.5, the mother solution becomes ammonium molybdate with 0.0% vanadium by cooling and then removing amonium metavanadate therefrom.
  • Molybdenum oxide and/or vanadium oxide may be obtained by pyrolizing at least one of the amonium metavanadate and ammonium molybdate. Amonia gas generated in the process is converted into amonia water and then reused as a form of amonia water in the process.
  • the present invention can increase yield of vanadium and molybdenum from the waste catalyst at lower temperature and further recover aluminum as well as nickel and coblat without additional processes.
  • the present invention can reduce costs of manunfacturing beecause it does not require expensive equipments, such as a rotary Kiln, for roasting at a high temperature (900° C.).
  • the present invention can recover valuable matals from the waste catalysts without discharging waste water containing ammonia nitrogen, thereby reducing costs for purifying waster water.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Metallurgy (AREA)
  • Manufacturing & Machinery (AREA)
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  • Chemical Kinetics & Catalysis (AREA)
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  • General Life Sciences & Earth Sciences (AREA)
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US12/530,743 2007-03-13 2008-03-13 Method of recovering valuable metals from the vrds spent catalyst Abandoned US20100111787A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
KR10-2007-0025283 2007-03-13
KR20070025283A KR20070043736A (ko) 2007-03-13 2007-03-13 석유의 탈황용 폐촉매에서 저온배소로 귀금속(바나듐,몰리브덴)을 98％이상 회수 분리하는 방법
PCT/KR2008/001412 WO2008111802A1 (fr) 2007-03-13 2008-03-13 Procédé de récupération de métaux précieux à partir des catalyseurs épuisés issus d'un procédé vrds

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US (1) US20100111787A1 (fr)
EP (1) EP2125136A4 (fr)
JP (1) JP2010521286A (fr)
KR (2) KR20070043736A (fr)
CN (1) CN101631598A (fr)
CA (1) CA2679442A1 (fr)
WO (1) WO2008111802A1 (fr)

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CN104384167A (zh) * 2014-09-09 2015-03-04 华电高科（高碑店）环保技术有限公司 一种废弃钛基钒系scr催化剂的综合回收利用方法
US9719031B2 (en) 2010-12-20 2017-08-01 Sachleben Chemie GmbH Titania-supported hydrotreating catalysts
CN111573733A (zh) * 2020-05-14 2020-08-25 大连众智创新催化剂有限公司 一种废催化剂回收利用方法
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Citations (2)

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CN101631598A (zh) 2010-01-20
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