US3656888A - Liquid phase oxidation process - Google Patents

Liquid phase oxidation process Download PDF

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US3656888A
US3656888A US863197A US3656888DA US3656888A US 3656888 A US3656888 A US 3656888A US 863197 A US863197 A US 863197A US 3656888D A US3656888D A US 3656888DA US 3656888 A US3656888 A US 3656888A
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molybdenum disulfide
molybdenum
reaction
slurry
percent
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Henry F Barry
Calvin J Hallada
Robert W Mcconnell
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Cyprus Amax Minerals Co
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American Metal Climax Inc
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    • 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
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/80—Compositional purity

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  • LIQUID PHASE OXIDATION PROCESS [72] Inventors: Henry F. Barry; Calvin J. Hallada, both of Ann Arbor; Robert W. McConnell, South Lyon, all of Mich.
  • ABSTRACT A process for effecting an aqueous liquid phase oxidation of molybdenum disulfide to molybdenum oxide by agitating, at elevated temperature, a slurry of molybdenum disulfide particles in water, under pressure, in the presence of oxygen for a period of time sufficient to effect the conversion of at least a portion of the molybdenum disulfide to molybdenum oxide,
  • Such ore beneficiaation processes conventionally comprise a grinding operation by which the ore is reduced to a particle size usually less than about 200 mesh and wherein the particles are subjected to a flotation extraction operation using a hydrocarbon oil, such as pine oil or petroleum oil, in combination with wetting agents to effect a separation of the molybdenum disulfide constituent from the gangue.
  • a hydrocarbon oil such as pine oil or petroleum oil
  • molybdenum disulfide While some of the molybdenum disulfide, after further purification, is employed directly in the compounding of lubricants, the predominant portion is converted to the oxide form in which it is employed as an alloying constituent in various metal alloys or is further reduced from the oxide form to the pure metallic state for special uses.
  • the present invention provides for an improved oxidation process for effecting a conversion of molybdenum disulfide to the corresponding oxide whereby the sulfur by-product constituent can be recovered as a sulfate and the molybdenum constituent is recovered as the trioxide.
  • this improved process it is now economically feasible to effect a liquid phase oxidation of molybdenum disulfide to provide molybdenum trioxide of high purity and in commercially acceptable yields.
  • aqueous slurry consisting of finely particulated particles containing molybdenum disulfide dispersed in water which is heated to a temperature preferably in excess of about 80 C. under an atmosphere containing free oxygen at an oxygen partial pressure of preferably at least about 50 psi.
  • the slurry is subjected to agitation sufficient to maintain a substantially uniformdispersion of the particles through the aqueous medium and to further effect entrainment and dissolving of the free oxygen in the aqueous medium for reaction with the surfaces of the molybdenum disulfide particles.
  • reaction progresses, sulfur oxides are formed, which in turn form sulfuric acid that effect a progressive reduction in the pH of the reaction medium as the reaction continues.
  • the reaction is continued for a period of time, normally about one to six hours, depending on the specific temperature-pressureparticle size conditions employed, whereafter the molybdenum trioxide product can be separated from the acidic aqueous medium, such as by filtration.
  • the extracted solids it is usually preferred to subject the extracted solids to a wash with ammonium hydroxide, effecting a conversion of the molybdenum oxide to ammonium molybdate and leaving a solid residue consisting of unreacted molybdenum disulfide and other insoluble impurities such as the gangue.
  • the solid residue if desired, can be subjected to further liquid phase oxidation to effect conversion of the balance of the molybdenum disulfide to molybdenum oxide.
  • the resultant ammonium molybdate solution can be concentrated, such as in an evaporator, and the crystals can thereafter be subjected to calcination, providing a relatively pure grade of molybdenum trioxide.
  • the drawing comprises a diagrammatic flow sheet of the process for effecting a liquid phase oxidation of molybdenum disulfide to molybdenum oxide in accordance with the preferred embodiments of the present invention.
  • the molybdenum disulfide starting material may comprise a concentrate as derived from flotation extraction operations in which molybdenum disulfide is usually present in amounts in excess of percent by weight and is in the form of finely divided particles of a size usually less than 200 mesh.
  • Concentrates of the foregoing type derived directly from the ore beneficiaation process are in the form of wet oily masses which usually contain up to about 5 percent water and up to about 7 percent of the hydrocarbon flotation oils employed in the flotation extraction operation.
  • Such concentrates ordinarily require no pretreatment prior to oxidation in accordance with the practice of the present invention, although in some situations, it has been found advantageous to remove the predominant portion of the flotation oils to provide for increased efiiciency in the oxidation reaction. This is particularly true when only a single-pass liquid phase oxidation reaction is employed.
  • the removal of the flotation oils or a reduction in the quantity thereof can be achieved, for example, by retorting the concentrate, efiecting a volatilization and/or thermal degradation and decomposition of the oils, providing a resultant substantially dry concentrate usually containing less than about 0.5 percent oil and, more usually, less than about 0. 1 percent.
  • the retorting operation is conventionally carried out at a temperature of about 1,200 F which also effects a corresponding reduction in the water content of the concentrate.
  • the concentrate can be subjected to solvent washing for removing the flotation oils followed by filtration to recover the de-oiled molybdenite.
  • molybdenite concentrates consist predominantly of molybdenum disulfide, about 5 percent to about 10 percent silica is also normally present.
  • Other metals are also present in minimal quantities such as lead, copper, zinc, iron, aluminum, calcium, magnesium, etc.
  • the presence of such contaminating metals, which are present in amounts of less than 1 percent, does not detract from the efficiency of the liquid phase oxidation process comprising the present invention.
  • the concentrate can be subjected to further leaching so as to effect an extraction of one or more of such metals with any one of a variety of techniques well known in the art.
  • the concentrate as derived from the mine, or as derived after further pretreatment is of an average particle size of less than about 200 mesh and can be employed directly in forming an aqueous dispersion without further comminution. While particle sizes of less than about 200 mesh are satisfactory for the practice of the process of the present invention, it is generally preferred that the concentrate have an average particle size of less than about 20 microns, and preferably less than about 5 microns, due to the increased surface area which further promotes the efiiciency of the oxidation reaction. Particles of such smaller size also facilitate the formation and maintenance of a substantially uniform aqueous dispersion and are usually preferred for this purpose.
  • the molybdenum disulfide concentrate is discharged from a storage hopper 2 into a dispersion tank 4 provided with an agitator 6 for effecting the formation of an aqueous dispersion or slurry which is intermittently or continuously transferred by means of a pump 8 into the inlet side of an autoclave 10.
  • a dispersion tank 4 provided with an agitator 6 for effecting the formation of an aqueous dispersion or slurry which is intermittently or continuously transferred by means of a pump 8 into the inlet side of an autoclave 10.
  • slurries which contain up to about 40 percent by weight of molybdenum disulfide based on the total weight of the slurry can be formed.
  • the liquid phase oxidation in the autoclave 10 can be carried out batchwise and also, preferably, in a continuous manner as shown.
  • batch operations it is convenient to form the dispersion directly in the autoclave, while in continuous operation, it is preferred to form the dispersion exteriorly of the autoclave employing a dispersion tank 4, as shown in the drawing, from which the slurry is continuously added to the inlet side of the autoclave and passes in a serpentine manner, as provided by the baffles 12, to the outlet side thereof.
  • the autoclave 10 is further provided with an agitator 14 of the mechanical mixing type for maintaining a substantially uniform dispersion of the particles in the aqueous medium.
  • agitation devices can be satisfactorily employed in lieu of the mechanical propellertype agitator 14, illustrated in the drawing, including, for example, sparger-type agitators through which the free oxygencontaining gas is admitted under pressure into the autoclave in the form of a stream of bubbles, imparting turbulence to the aqueous medium, as well as effecting a contact of the free oxygen with the surfaces of the molybdenum disulfide particles.
  • the provision of free oxygen in the autoclave 10 can be accomplished by introducing pure oxygen gas through a supply line 16 or, alternatively, can be provided by air or a mixture of the two. Additional free oxygen is continuously or intermittently supplied to the autoclave to replenish that consumed during the oxidation reaction. When air is employed as the source of free oxygen replenishment, it is preferred to provide a vent line 18 in the upper portion of the autoclave for continuously and/or intermittently withdrawing gas from the upper portion of the autoclave to avoid the formation of an atmosphere which is excessively rich in nitrogen.
  • oxygen partial pressures at or about atmospheric pressure At oxygen pressures at or about atmospheric pressure, the oxidation reaction has been observed to be very slow and totally impractical from a commercial standpoint. It has been discovered that as the partial pressure of the free oxygen is increased to above about 50 p.s.i., a marked improvement in the rate of reaction and in the product yield takes place. Particularly satisfactory results are attained employing oxygen partial pressures of from about 300 p.s.i. up to about 600 p.s.i. or above. While oxygen partial pressures in excess of about 600 p.s.i. have been found to provide for further improvements in the reaction rate, the increases in reaction rate at these higher levels become progressively smaller and are not significantly greater than that attained at pressures at or about 600 p.s.i. Additionally, oxygen partial pressures in excess of about 600 p.s.i. require that the processing equipment employed be of substantially greater structural strength, and it is because of the foregoing considerations that the use of such higher pressures is not ordinarily economically justified.
  • the liquid phase reaction medium preferably comprises an aqueous dispersion containing from about 10 percent up to about 30 percent by weight of molybdenum disulfide particles of an average particle size of less than about 200 mesh which is vigorously agitated at a temperature preferably ranging from about l50 C. to about 250 C. in contact with free oxygen present at a partial pressure of from about 300 p.s.i. to about 600 p.s.i.
  • substantially complete reaction and conversion of the molybdenum disulfide to the corresponding oxide takes place within about one to about six hours.
  • the acid aqueous slurry is withdrawn from the autoclave and is transferred, as shown in the drawing, to a filter 20 for effecting a separation of the molybdenum trioxide reaction product from the filtrate.
  • the filter cake also contains unreacted molybdenum disulfide particles and any other solid contaminating material such as the gangue present in the original concentrate which is predominantly in the form of silica.
  • the aqueous filtrate which is acidic due to the presence of the sulfuric acid formed during the oxidation reaction also contains some dissolved molybdenum in the form of molybdenyl sulfate.
  • the acidity of the filtrate conventionally ranges from a pH of about 0 to a pH of about 2.0, depending upon the concentration of molybdenum disulfide in the original slurry charge and the extent to which the conversion reaction has taken place.
  • the filtrate discharged from the filter 20 is preferably transferred, as shown in the drawing, to a neutralizer 22 in which an alkaline compound, such as caustic, is added and causes precipitation of the dissolved molybdenum trioxide.
  • the precipitated molybdenum oxide can be recovered in a flter 24.
  • the neutralized filtrate from the filter 24 can be suitably discharged to storage and subsequently utilized as a source of sulfate.
  • a portion of the filtrate from the filter 20 can be recycled back to the autoclave or to the tank 4 used for preparing the slurry prior to charging the autoclave.
  • the recycling of such acidic filtrate causes the initial slurry charge to be slightly on the acid side, resulting in an increased acidity of the reacted slurry as withdrawn at the output end of the autoclave. For this reason, while a recycling of a portion of the filtrate from the filter can be accomplished, generally the quantity recycled is small.
  • all of the filtrate is directly transferred to the neutralizer 22.
  • the filter cake derived from the filter 20 consists of a precipitated molybdenum trioxide product in combination with unreacted molybdenum disulfide and a small proportion of inert contaminants, such as silica, originally introduced with the molybdenum disulfide concentrate.
  • An extraction of the molybdenum trioxide product from the filter cake is conveniently achieved by transferring the filter cake to a wash treatment 26, in which it is subject to an aqueous ammonium hydroxide wash solution prepared in a make-up tank 28.
  • the aqueous ammonium hydroxide wash solution may range in concentration from about 1 to about 12 normal (N), and preferably, concentrations of about 10 to 12 N are used in order to minimize water dilution of the resultant molybdate solution.
  • the quantity of wash solution employed is designed to provide a molar ratio of ammonia to molybdenum of preferably at least 2.3 up to about 3.0.
  • the wash solution effects a dissolving of the molybdenum oxide by converting it to ammonium molybdate.
  • the unreacted molybdenum disulfide and solid contaminants are thereafter removed in a filter and the filtrate containing the dissolved ammonium molybdate can be concentrated, such as by evaporation or in a crystalizer 32, as shown in the drawing.
  • the solid ammonium molybdate derived from the crystalizer can be employed as a product in that form or, alternatively, can be transferred to a calciner 34 in which it is heated, effecting an evolution of ammonium gas which is recycled back to the ammonium hydroxide make-up tank 28.
  • the resultant molybdenum trioxide product is of high purity.
  • the filter cake derived from the filter 30 containing unreacted molybdenum disulfide in combination with inert contaminants is preferably accumulated and thereafter charged to a second autoclave 36 in which an aqueous slurry is formed and a further oxidation reaction is carried out in accordance with the reaction as previously described in connection with the autoclave It).
  • the autoclave 36 similarly is provided with appropriate agitation and means for introducing oxygen under pressure to effect a conversion of the residual molybdenum disulfide to the corresponding oxide with a formation of sulfuric acid in accordance with the reaction equation as hereinbefore set forth.
  • the reacted slurry is transferred from the autoclave 36 to a filter 38 in which the precipitated molybdenum trioxide particles are removed in combination with the contaminating inert particles along with any residual unreacted molybdenum disulfide.
  • the filtrate from the filter 38 may conveniently be transferred to the neutralizer 22 at which it is treated with caustic in a manner as previously described.
  • the resultant filter cake from the filter 38 similarly is washed with an aqueous ammonium hydroxide solution, effecting a dissolving of the molybdenum trioxide product in a treating tank 40, whereafter it is transferred to a filter 42 for removal of the undissolved solids which comprise essential inert contaminating materials originally present in the molybdenum disulfide concentrate.
  • the filtrate from the filter 42 is conveniently transferred and is mixed with the filtrate from the filter 30 for further concentration in the crystalizer 32 in a manner as previously described.
  • the efficiency of conversion can be further improved by employing a multiple-phase reaction as exemplified by the continuous autoclave 10 and wherein any residual unreacted molybdenum disulfide is subsequently substantially completely converted to the oxide form using an auxiliary autoclave 36.
  • EXAMPLE 1 A regular grade molybdenum disulfide concentrate derived from an oil flotation extracted molybdenite ore from Climax, Colo., having an average particle size of less than 200 mesh was employed for the liquid phase oxidation reaction. The concentrate was washed 6 times with acetone to remove the residual oils and was thereafter dried for several hours at a temperature of C. The chemical analysis of the de-oiled concentrate revealed that it contained 52.44 percent molybdenum and 35.54 percent sulfur with a sulfur to molybdenum mole ratio of 2.03:1.
  • a l-liter capacity autoclave equipped with a magnetically driven agitator was employed for the liquid phase oxidation reaction.
  • a slurry was prepared by mixing 50 grams of the molybdenum disulfide concentrate with 450 grams of water and charging the resultant slurry into the autoclave.
  • the autoclave was pressurized with oxygen and thereafter heated, during agitation, to the operating temperature. Heating was continued to provide a substantially constant operating temperature of about 177 C. (350 F.) with a total vapor pressure of 750 p.s.i. gauge of which the calculated oxygen partial pressure was about 615 p.s.i.
  • the charge was cooled and filtered through a Buchner funnel and the filter cake was dried for several hours at 110 C.
  • the filtrate, at the completion of the reaction, was at a pH of less than zero.
  • Thirty grams of the dry filter cake thereafter was stirred with 250 milliliters of 5 N ammonium hydroxide for 30 minutes at room temperature, effecting a dissolving of the molybdenum oxide and the charge was thereafter filtered and the residue again dried at 1 10 C. and weighed.
  • the yield of molybdenum oxide was calculated based on the original filter cake recovered and the weight loss of the ammonium hydroxide-washed filter cake which revealed a conversion of about 88.4 percent of the molybdenum disulfide to molybdenum trioxide.
  • EXAMPLE II A second test was conducted employing the same concentrate and equipment as previously described in connection with Example I. The same procedure utilizing the same temperature and reaction conditions, but a total pressure of 350 p.s.i.g., was used, providing a calculated oxygen partial pressure of 215 p.s.i. The resultant filtrate had a pH of 0.12 and an analysis of the reaction residue revealed a conversion of molybdenum disulfide to molybdenum trioxide of about 81 percent based on the original charge.
  • EXAMPLE Ill A third test was conducted employing the same concentrate and equipment as previously described in connection with Example The same procedure utilizing the same temperature and reaction conditions were used but a total pressure of 1,500 p.s.i.g. was employed so as to provide a calculated oxygen partial pressure of 1,365 p.s.i. The resultant filtrate obtained had a pH of less than zero and analysis of the reaction residue revealed that 89.8 percent of the molybdenum disulfide present in the original charge was converted to molybdenum trioxide.
  • a process for converting molybdenum disulfide to molybdenum oxide which comprises the steps. of dispersing a particulated molybdenum disulfide-bearing material having an average particle size less than about 20 microns in water forming an aqueous slurry containing up to about 40 percent by weight of said material, heating said slurry to a temperature of at least about C. and agitating said slurry while in contact with an atmosphere containing free oxygen at an oxygen partial pressure of at least about 215 p.s.i.

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Cited By (31)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4165362A (en) * 1977-04-08 1979-08-21 Engelhard Minerals & Chemicals Corporation Hydrometallurgical processing of molybdenite ore concentrates
US4342728A (en) * 1981-01-19 1982-08-03 Amax Inc. Process for digesting tungsten ores containing organic matter
US4379127A (en) * 1981-07-22 1983-04-05 Gfe Gesellschaft Fur Elektrometallurgie Mbh Method of recovering molybdenum oxide
US4414060A (en) * 1980-12-16 1983-11-08 Nalco Chemical Method for sulfite pulping using water-soluble molybdenum containing compounds
US4432947A (en) * 1981-07-31 1984-02-21 Uranium Pechiney Ugine Kuhlmann Process for obtaining molybdenum as a useful product from molybdeniferous solutions containing alkali metal carbonate, sulphate, hydroxide or hydrogen carbonate and possibly uranium
US4512958A (en) * 1983-10-28 1985-04-23 Gfe Gesellschaft Fur Elektrometallurgie Mbh Method of recovering molybdenum oxide
US4523948A (en) * 1984-02-14 1985-06-18 Amax Inc. Roasting of molybdenite concentrates containing flotation oils
DE3443806A1 (de) * 1984-11-27 1986-06-05 Eberhard Priv. Doz. Prof. Dr.-Ing. 1000 Berlin Gock Verfahren zur herstellung von reinem moo(pfeil abwaerts)3(pfeil abwaerts) ueber die extraktion von molybdaen aus sulfatloesungen
US4657745A (en) * 1986-03-31 1987-04-14 Chemical & Metal Industries, Inc. Value recovery from spent alumina-base catalyst
WO1996012675A1 (fr) * 1994-10-24 1996-05-02 Kennecott Corporation Procede d'oxydation sous pression pour la production de trioxyde de molybdene a partir de molybdenite
US5804151A (en) * 1997-09-16 1998-09-08 Cyprus Amax Minerals Company Process for autoclaving molybdenum disulfide
US5820844A (en) * 1997-01-29 1998-10-13 Cyprus Amax Minerals Company Method for the production of a purified MoO3 composition
US5985236A (en) * 1998-06-09 1999-11-16 Cyprus Amax Minerals Company Ammonium octamolybdate composition and method for producing the same
US6451088B1 (en) 2001-07-25 2002-09-17 Phelps Dodge Corporation Method for improving metals recovery using high temperature leaching
US6451089B1 (en) 2001-07-25 2002-09-17 Phelps Dodge Corporation Process for direct electrowinning of copper
WO2002090263A1 (fr) * 2001-05-09 2002-11-14 H. C. Starck Gmbh Mecanismes de commande d'autoclave pour oxydation de molybdenite sous pression
US6497745B2 (en) 2000-07-25 2002-12-24 Phelps Dodge Corporation Method for processing elemental sulfur-bearing materials using high temperature pressure leaching
US6676909B2 (en) 2000-07-25 2004-01-13 Phelphs Dodge Corporation Method for recovery of metals from metal-containing materials using medium temperature pressure leaching
US6680034B2 (en) 2000-07-25 2004-01-20 Phelps Dodge Corporation Method for recovering metal values from metal-containing materials using high temperature pressure leaching
US20050109163A1 (en) * 2001-07-25 2005-05-26 Phelps Dodge Corporation Process for multiple stage direct electrowinning of copper
US20050126923A1 (en) * 2001-07-25 2005-06-16 Phelps Dodge Corporation Process for recovery of copper from copper-bearing material using medium temperature pressure leaching, direct electrowinning and solvent/solution extraction
US20060144717A1 (en) * 2004-10-29 2006-07-06 Phelps Dodge Corporation Process for recovery of copper from copper-bearing material using pressure leaching, direct electrowinning and solvent/solution extraction
RU2302997C2 (ru) * 2001-05-09 2007-07-20 Х.К. Штарк Гмбх Способ получения высокочистого димолибдата аммония (его варианты)
US20080023342A1 (en) * 2004-10-29 2008-01-31 Phelps Dodge Corporation Process for recovery of copper from copper-bearing material using pressure leaching, direct electrowinning and solution extraction
US20080124269A1 (en) * 2006-11-16 2008-05-29 Albemarle Netherlands B.V. Purified molybdenum technical oxide from molybdenite
US20080166280A1 (en) * 2006-11-16 2008-07-10 Albemarle Netherlands B.V. Purification Of Molybdenum Technical Oxide
US20090071839A1 (en) * 2004-10-29 2009-03-19 Phelps Dodge Corporation Process for multiple stage direct electrowinning of copper
RU2398902C1 (ru) * 2009-03-30 2010-09-10 Российская Федерация, от имени которой выступает государственный заказчик-Государственная корпорация по атомной энергии "Росатом" Способ гидрометаллургической переработки ренийсодержащего молибденитового концентрата
WO2011024164A1 (fr) * 2009-08-24 2011-03-03 Metal Tech Ltd. Procédé pour la séparation de multiples métaux issus de matières premières et système de mise en œuvre du procédé
US8753591B2 (en) 2012-03-23 2014-06-17 Kennecott Utah Copper Llc Process for the conversion of molybdenite to molydenum oxide
CN106745262A (zh) * 2016-12-12 2017-05-31 郑州大学 一种利用氧化少层硫化钼制备非晶氧化钼纳米片的方法

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US3353908A (en) * 1961-10-24 1967-11-21 Knapsack Ag Process for the manufacture of dicalcium phosphate

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Cited By (55)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4165362A (en) * 1977-04-08 1979-08-21 Engelhard Minerals & Chemicals Corporation Hydrometallurgical processing of molybdenite ore concentrates
US4414060A (en) * 1980-12-16 1983-11-08 Nalco Chemical Method for sulfite pulping using water-soluble molybdenum containing compounds
US4342728A (en) * 1981-01-19 1982-08-03 Amax Inc. Process for digesting tungsten ores containing organic matter
WO1982002540A1 (fr) * 1981-01-19 1982-08-05 Inc Amax Oxydation par voie humide de matieres organiques
US4379127A (en) * 1981-07-22 1983-04-05 Gfe Gesellschaft Fur Elektrometallurgie Mbh Method of recovering molybdenum oxide
US4432947A (en) * 1981-07-31 1984-02-21 Uranium Pechiney Ugine Kuhlmann Process for obtaining molybdenum as a useful product from molybdeniferous solutions containing alkali metal carbonate, sulphate, hydroxide or hydrogen carbonate and possibly uranium
US4512958A (en) * 1983-10-28 1985-04-23 Gfe Gesellschaft Fur Elektrometallurgie Mbh Method of recovering molybdenum oxide
US4523948A (en) * 1984-02-14 1985-06-18 Amax Inc. Roasting of molybdenite concentrates containing flotation oils
DE3443806A1 (de) * 1984-11-27 1986-06-05 Eberhard Priv. Doz. Prof. Dr.-Ing. 1000 Berlin Gock Verfahren zur herstellung von reinem moo(pfeil abwaerts)3(pfeil abwaerts) ueber die extraktion von molybdaen aus sulfatloesungen
US4657745A (en) * 1986-03-31 1987-04-14 Chemical & Metal Industries, Inc. Value recovery from spent alumina-base catalyst
EP0241149A3 (en) * 1986-03-31 1989-07-12 Chemical & Metal Industries, Inc. Value recovery from spent alumina-base catalysts
WO1996012675A1 (fr) * 1994-10-24 1996-05-02 Kennecott Corporation Procede d'oxydation sous pression pour la production de trioxyde de molybdene a partir de molybdenite
US6149883A (en) * 1994-10-24 2000-11-21 Kennecott Utah Copper Corporation Pressure oxidation process for the production of molybdenum trioxide from molybdenite
US5820844A (en) * 1997-01-29 1998-10-13 Cyprus Amax Minerals Company Method for the production of a purified MoO3 composition
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FR2064092B1 (fr) 1973-12-21
AT305211B (de) 1973-02-12
NL7014530A (fr) 1971-04-06
CA935623A (en) 1973-10-23
DE2043874A1 (fr) 1971-04-15
FR2064092A1 (fr) 1971-07-16
NL141841B (nl) 1974-04-16
DE2043874B2 (de) 1972-08-31
LU61791A1 (fr) 1971-06-18
BE756944A (fr) 1971-03-16
SE352613B (fr) 1973-01-08

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