US3770414A - Recovery of rhenium and molybdenum values from molybdenite concentrates - Google Patents

Recovery of rhenium and molybdenum values from molybdenite concentrates Download PDF

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US3770414A
US3770414A US00101784A US3770414DA US3770414A US 3770414 A US3770414 A US 3770414A US 00101784 A US00101784 A US 00101784A US 3770414D A US3770414D A US 3770414DA US 3770414 A US3770414 A US 3770414A
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oxygen
rhenium
sulfur dioxide
concentrate
oxidation
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J Lake
M Goldenberg
M Vojkovic
J Litz
R Coleman
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Continental Ore Corp
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Continental Ore Corp
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    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01F—MAGNETS; INDUCTANCES; TRANSFORMERS; SELECTION OF MATERIALS FOR THEIR MAGNETIC PROPERTIES
    • H01F10/00—Thin magnetic films, e.g. of one-domain structure
    • H01F10/08—Thin magnetic films, e.g. of one-domain structure characterised by magnetic layers
    • H01F10/10—Thin magnetic films, e.g. of one-domain structure characterised by magnetic layers characterised by the composition
    • 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
    • C01G47/00—Compounds of rhenium
    • 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
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/02—Roasting 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
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/14—Agglomerating; Briquetting; Binding; Granulating
    • C22B1/16—Sintering; Agglomerating
    • C22B1/20—Sintering; Agglomerating in sintering machines with movable grates
    • 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
    • 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
    • C22B61/00—Obtaining metals not elsewhere provided for in this subclass
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B21/00—Open or uncovered sintering apparatus; Other heat-treatment apparatus of like construction
    • F27B21/06—Endless-strand sintering machines
    • 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

Definitions

  • the molybdenite is usually separated from the bulk of the copper minerals and is recovered as a flotation concentrate containing from 40% to 55% molybdenum. Then the molybdenum sulfide concentrate is roasted to produce an oxide product containing a minimum of sulfur, the chief objective of prior art processes being the ultimate recovery of molybdenum. The rhenium is volatilized during roasting and generally was not recovered.
  • a process directed to the recovery from molybdenite concentrate of rhenium along with molybdenum is disclosed in US. Pat. No. 2,579,107 to Bertolus.
  • the present invention is directed to the recovery from molybdenite of a high yield of rhenium either as a high grade intermediate product or as a high grade metal along with a metallurgical quality molybdic oxide calcine containing a minimum of copper and sulfur impurities, all with an efficient use of heat and materials.
  • the normal practice for the recovery of rhenium from molybdenite concentrates consists of roasting the concentrate in air utilizing a multiple hearth-type roaster. A portion of the rhenium as rhenium oxide is volatilized and is collected as a fume with the dust in a scrubber where it is dissolved in water. Recoveries of rhenium from the concentrate normally are in the 55% to 65% range.
  • An authoratative opinion by those skilled in the art is that a conventional plant operated primarily for the recovery of rhenium in accordance with prior art procedure could effect a net recovery of 77% of the rhenium.
  • a principal feature of the process is the provision of a reaction zone in which finely divides molybdenite is effectively dispersed and moves vertically and Countercurrent to an upwardly traveling stream of pure hot oxygen, oxygen-enriched air or an oxygensulfur dioxide mixture emanating from a concentrate roasting furnace, the result being a highly effective oxi dation of the sulfur content of the concentrate to sulfur dioxide, of rhenium and molybdenum to their higher oxides, and volatilization of rhenium oxide.
  • the process begins with roasting a preheated molybdenite concentrate in an oxygen or mixed oxygensulfur dioxide atmosphere in a vertical flash roaster.
  • Sulfur dioxide is formed from the oxidation of sulfur and will mix with the oxygen introduced or it may be added with the oxygen to control oxidation rate.
  • the oxidizing gases and the molybdenum sulfide particles pass countercurrently in the vertical section of the flash roaster to provide maximum surface contact between the particles and gases.
  • the length of time of the concentrate particles in the vertical section in countercurrent contact with oxidizing gases is regulated to initiate the oxidation of each of the particles of molybdenum sulfide, such that each of the particles will have a layer of molybdenum trioxide on its outer surface.
  • the particles pass downwardly through the vertical section onto a rotating horizontal hearth where they are annealed for a period of time at approximately 550 to 680C. in an oxygen or oxygen-sulfur dioxide atmosphere.
  • This annealing step permits complete oxidation of molybdenum to molybdenum trioxide.
  • the major portion of the rhenium is volatilized while the concentrate particles are roasted and annealed, and pass out of the roasting and annealing furnace with the off-gases which contain the excess oxygen, the sulfur dioxide formed and added during roasting, and a small quantity of dust which is incompletely roasted.
  • An improvement of the invention is the partial control of the rate of oxidation of sulfides in the reaction zone and thereby the temperature of the zone to keep it below that at which molybdic oxide volatilizes or melts with resultant inhibition of the volatilization of rhenium oxide.
  • Part of the heat is due to the oxidation of the sulfides, the rate of this oxidation being controlled by the gas stream composition and the stoichiometric ratio of available oxygen to concentrate in the reaction zone.
  • This oxidation rate and the heat generated thereby are controlled by varying the stoichiometric ratio of oxygen to concentrate using the ratio of sulfur dioxide to oxygen gases in the exhaust gas as a measure of this ratio existing in the reaction area.
  • Other parameters affecting the operation of the process may be varied, these being preheat temperature, height of reactor column and heat dissipation from the column.
  • FIG. 1 is a partial schematic sectional view of the combined roaster and vertical column comprising the flash roaster of the invention.
  • FIG. 2 is a flow diagram illustrating the operation of the flash roasting process of the invention.
  • the numeral 10 indicates a conventional rotating hearth furnace used for roasting concentrates.
  • the furnace is illustrative of the type concentrate roasting furnace which is constructed to provide for the introduction and passage of hot gases over the material in the roasting area.
  • Other conventional furnaces of this type are moving horizontal conveyor (sintering machine), circular rabbled hearth (single or multiple), longitudinal rabbled'hearth (Edwards style roaster) and horizontal kilns. Beyond this feature of the invention is not limited to any type furnace.
  • a furnace in which a water cooling system is used for temperature control is preferred. If the furnace is air-cooled, the air is not passed through the reaction zone of the flash roaster.
  • the furnace may be operated under negative or positive pressure.
  • the furnace comprises the rotating hearth 12 rotatably supported by wheels 14 on platform 16 which moves vertically along the interior surfaces of main support legs 17.
  • Central support member 18, which supports platform 16, is mounted for raising and lowering by hydraulic cylinder 20 to correspondingly raise and lower the rotating furnace 12 and the platform 16.
  • the bed of the rotating hearth upon which the concentrate rests is indicated at 22.
  • a water cooling system for the rotating hearth by which water enters the inlet 24 and leaves through the outlet 26 is indicated generally at 28.
  • the furnace is provided with the usual cutter assembly 30 to periodically break crusts which form as the concentrate is roasted.
  • Circumferentially-spaced inlets 32 permit the introduction of gases, such as oxidizing gases, into the hearth area formed by the bed of the hearth and roof 34.
  • gases may be introduced under positive pressure, or reduced pressure generated at the outlet pipe 42.
  • the hearth l2' rotates in liquid seals indicated at 35 to provide a gastight hearth area.
  • A.conventional drive unit 36 is provided for rotating the hearth.
  • a hollow reactor column 38 is mounted vertically on the furnace 10 so that its bottom end opens into the hearth area as shown.
  • The-vertical reactor column may be constructed of refractory or insulated material or heat conducting material provided with a cooling or heat transfer media.
  • the reactor column may be made vertically adjustable by constructing it in spool sections or otherwise. For support, it is secured to the top of lbeam 39 by means of a conventional flange and bolt arrangement as shown, the l-beam being attached to support 17.
  • the outer casing of the vertical reactor column 38 forms an inner chamber 40 which is the reaction zone of the vertical column.
  • the reaction zone 40 is provided with an outlet 42 for gases, fumes, dust, etc., including rhenium oxide. Since its bottom end opens into the enclosed area above the rotating hearth 12, gas introduced into inlets 32 passes over the hearth bed 22 and upwardly through the reaction zone 40 and out the outlet 42.
  • a concentrate preheater unit 44 is mounted above the reaction zone 40 by supports, not shown, and is connected to delivery pipe 46 so that preheated concentrate may be introduced downwardly from the pre-
  • the preheater unit 44 is a conventional heater and need not be mounted above the reaction zone as heated concentrate from the preheater located elsewhere can be transferred to the upper end of delivery pipe 46.
  • a finely divided molybdenite concentrate is introduced into the preheater 44 in an inert atmosphere and brought to a minimum temperature in the neighborhood of about 500C.
  • hot gas is introduced into'the preheat port 56 and circulated through the reaction zone 40 as a start-up procedure.
  • Oxygen gas may also be introduced at this time through inlet ports 32 and circulated through the area above rotating hearth bed 22 and out the outlet port 42.
  • reaction zone 40 When the reaction zone 40 has reached the required temperature, preferably between about 550 an d-
  • the hearth bed 22 is rotating and the calcine contin- I uously leaves the hearth through an outlet, not shown, preceded by a scraper, where it is collected and subsequently processed to recover metal values from it.
  • the water cooling system 28 is used as necessary to control the temperature of the material on rotating hearth 22.
  • sulfur dioxide is formed by oxidation of sulfides present in the molybdenite concentrate.
  • This hot sulfur dioxide gas is mixed with the upwardly traveling hot oxygen and passes out the exit 42 into the scrubbers along with the other gases, fumes and dust. where some of it unites with water in the scrubbers to'form sulfurous acid and the remainder is collected.
  • the sulfur dioxide produced normally occupies from about 30-50% of the volume of the exhaust gases. Excess oxygen which has not been consumed in the reaction zone passes through the outlet 42 and may be collected for recirculation through the system.
  • rhenium oxide is formed by roasting rhenium sulfide in the presence of oxygen at a temperature between 200 and 300C; however, this reaction does not readily proceed in the presence of molybdenum sulfide. After the major part of the sulfur has been driven off as sulfur dioxide in the reaction zone, rhenium and molybdic oxides are formed in the temperature range of about 500 to 650C.
  • the reaction zone temperature during the oxidation of sulfides must be kept below that at which molybdic oxide volatilizes or melts with resultant inhibition of the volatilization of rhenium oxide.
  • the rhenium oxide passes to the scrubbers while the molybdic oxide particles fall by gravity to the rotating hearth 22.
  • Some of the unoxidized sultides will also reach the rotating hearth as well as impurities in the form of compounds of copper, iron, etc. Some of these latter impurities, along with some molybdenum sulfide, also pass to the scrubbers.
  • FIG. 11 gives a condensed showing of the process described.
  • the molybdenum and rhenium may be separated and recovered from solution by conventional means.
  • a preferred method is disclosed in co-pending patent application Ser. No. 94,268 filed Dec. 2, 1970, now US. Pat. No. 3,681,016.
  • the calcine from the roaster is leached to remove impurities and the leach solution filtered with technical grade molybdic oxide being recovered.
  • An atmosphere free of oxygen is maintained in the preheater at all times.
  • an atmosphere of nitrogen is used.
  • Preheating of the concentrate before it reaches the reaction chamber greatly accelerates oxidation between the hot sulfides and hot oxygen. ltalso shortens the required time in the reaction zone 44]? for completion of the chemical reactions involved and, accordingly, enables a shorter vertical column to be used. This also reduces the volume of gas necessary in the reaction zone MD at all times.
  • oxygen-enriched air can be used but this creates the problem of removing introduced nitrogen from the system.
  • oxidation reactions are occurring continuously through contact of oxygen with the hot calcines on the rotating hearth.
  • the gaseous oxidation products are carried by the oxygen up through the reaction zone and to the scrubbers.
  • These products are principally sulfur dioxide, rhenium oxides and molybdenum oxides.
  • Vertical orientation of the reaction zone is preferable in that it makes feasible complete dispersion of the molybdenite concentrate particles above the reaction zone and before the particles enter the reaction zone.
  • the oxygen updraft further disperses the falling particles.
  • the effective dispersion of the hot particles in the hot reaction zone gives maximum surface contact of the particles with the oxygen to provide complete oxidation thereof. This feature is referred to as flash roasting.
  • a further important feature of the invention is the use of sulfurous acid formed in the scrubbers for leaching of the molybdic oxide concentrate in the recovery of the remaining rhenium from the molybdic oxide calcine. This feature contributes to the economy of the system. Other leaching agents may be used.
  • the efficiency of the system may be increased by reroasting the calcine.
  • the molybdenum trioxide produced in the flash roaster may not be completely oxidized and may contain some sulfur in addition to any copper which may have been in the feed.
  • the sulfur is more completely oxidized by re-roasting the calcines in air at 600C. for thirty minutes.
  • This second roast also insures almost complete oxidation of the copper. It was found most convenient to perform the reroast in an externally heated kiln using a small air flow to complete the oxidation.
  • An addition portion of rhenium is also volatilized during the re-roast and can be collected by scrubbing the off-gas in a second scrubber.
  • the oxidation process in the vertical column is to a degree self-regulating by the variation occurring in the sulfur dioxide to oxygen ratio of the gas stream.
  • the sulfur dioxide concentration increases and the oxygen concentration decreases, resulting in a suppression of the reaction rate.
  • the ratio of sulfur dioxide to oxygen in the exhaust gas is, in effect, a measure of the efficiency of the process when the most desirable ratio is known.
  • the process was operated at various ratios of sulfur dioxide to oxygen in the exhaust gas, and high volatilization of rhenium oxide with high recovery of molybdenum in the calcine occurred when operating at sulfur dioxide percentages by volume of 30 and 35 .in the exhaust gas.
  • These volumes are, of course, related to the ratio of sulfur dioxide to oxygen,
  • the sulfur dioxide-oxygen ratio in the exhaust stream can be partially controlled to provide the optimum value, if necessary, by the introduction of sulfur dioxide gas with the oxygen.
  • the ratios reflected by 3035% volume of sulfur dioxide are by no means critical, but its use to provide favorable reaction zone conditions illustrates the effectiveness of this method of control.
  • the preheat temperature is readily controlled by adjusting the heat input to the indirect-fired preheat furnace.
  • the height of the reactor column determines the dwell time of the sulfide particles in the reaction zone for complete oxidation and for formation and volatilization ofrhenium oxide.
  • the optimum height for a given operation is developed by calculations and measurements derived from pilot plant operation. For example, in a continuous pilot plant operation excellent results were obtained using a vertical column 44 inches in height and 6 inches in diameter with a rotating hearth 3 feet in diameter. These dimensional relationships are not critical and would change with change in other variables, such as, concentrate characteristics, composition of feed gases, rate of gas injection, etc.
  • the heat dissipated from the vertical column is controlled by design, and construction materials used.
  • the construction can be varied'from highly insulated construction to high conductivity construction with a cooling media.
  • the radiation and convection loss of heat generated for a metal conducting material and a given feed rate can be readily calculated. Additional heat may be removed from the column by water cooling or other heat exchange media.
  • Table 1 shows some material balances obtained in roasting tests performed on molybdenite concentrate.
  • Table 1 shows the variability of the rhenium content of the product produced at somewhat similar conditions. With careful control, a molybdenum product may be produced which contains only 5% of the feed rhenium, demonstrating that the process is effective to provide high yields of both molybdenum and rhenium.
  • Table 3 shows the results from re-roasting a number of calcines:
  • the leached residue is separated from the leach solution by filtration and after drying is ready for packaging for sale.
  • the leach solution joins the solutions from the scrubbers on the flash roaster and re-roaster.
  • the reduced volume of exhaust gas also results in a much higher concentration of rhenium oxide in the exhaust gas than is obtained in conventional processes.
  • recovery of substantially all of the rhenium is far more feasible and economical than in present prosesses using air with resultant large volumes of exhaust gas to be processed for recovery of the rhenium oxide.
  • a method forrecovering rhenium and molybdic oxide from molybdenite concentrate which comprises:
  • rare-heating particles of said concentrate in an oxygen-free atmosphere to a temperature not in excess of about "150C to raise the temperature of the particles to promote flash oxidation of the molybdenite when the particles are introduced into a flash oxidation zone,
  • reaction rate is controlled by adjusting the relative feed rate of oxygen and molybdenite concentrate to the first oxidation zone to control the stoichiometric ratio of oxygen to metal sulfides introduced therein.

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US00101784A 1970-12-28 1970-12-28 Recovery of rhenium and molybdenum values from molybdenite concentrates Expired - Lifetime US3770414A (en)

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Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3941867A (en) * 1974-09-04 1976-03-02 Canadian Patents And Development Limited Production of molybdenum trioxide from molybdenite in a fluidized bed
US4523948A (en) * 1984-02-14 1985-06-18 Amax Inc. Roasting of molybdenite concentrates containing flotation oils
US4687647A (en) * 1987-01-08 1987-08-18 Lloyd Berg Conversion of molybdenite to molybdenum dioxide using petroleum or coal tar pitches
DE3710725A1 (de) * 1987-03-31 1988-10-13 Gock Eberhard Verfahren zur direkten aufarbeitung von rheniumhaltigen molybdaensulfiden mit ammoniak
US20030049182A1 (en) * 2000-05-01 2003-03-13 Christopher Hertzler System and method for abatement of dangerous substances from a waste gas stream
US20030219361A1 (en) * 2002-05-25 2003-11-27 Unisem Co., Ltd. Apparatus and method for pretreating effluent gases in a wet environment
US20090277305A1 (en) * 2008-05-06 2009-11-12 Sd Lizenzverwertungsgesellschaft Mbh & Co. Kg Recovery of rhenium
US20110229366A1 (en) * 2010-03-16 2011-09-22 Luederitz Eberhard Method for recovering rhenium and other metals from rhenium-bearing materials
US8753591B2 (en) 2012-03-23 2014-06-17 Kennecott Utah Copper Llc Process for the conversion of molybdenite to molydenum oxide
CN104017987A (zh) * 2014-06-20 2014-09-03 大冶有色金属有限责任公司 一种从含铼钼精矿中分离钼和铼的方法
CN104313329A (zh) * 2014-10-31 2015-01-28 罗旭 辐射解离铼气钼气电极还原金属铼钼的装置
US8956582B2 (en) 2009-03-13 2015-02-17 Maritime House Metals Inc. Rhenium recovery
US20150114181A1 (en) * 2012-12-28 2015-04-30 Pan Pacific Copper Co., Ltd. Method for producing aqueous solution of perrhenic acid from rhenium sulfide
US20150267581A1 (en) * 2014-03-24 2015-09-24 Michael Patrick Ware, JR. In-situation scr catalyst cleaning process
CN105087962A (zh) * 2015-09-09 2015-11-25 中南大学 从含铼低品位钼精矿中高效提取钼和铼的方法
US9631259B2 (en) 2012-12-28 2017-04-25 Pan Pacific Copper Co., Ltd. Method for producing aqueous solution of perrhenic acid from rhenium sulfide

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EA002417B1 (ru) * 1998-08-21 2002-04-25 Оао "Институт Гинцветмет" Способ переработки сульфидного молибденового концентрата
RU2222626C1 (ru) * 2002-05-07 2004-01-27 Государственное унитарное предприятие "Всероссийский научно-исследовательский институт химической технологии" Способ извлечения рения и других элементов
CN102703715B (zh) * 2012-06-26 2013-09-18 西部鑫兴金属材料有限公司 一种从含铼钼精矿焙烧烟道灰中回收铼和钼的方法

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US1970467A (en) * 1932-10-28 1934-08-14 Otavi Minen Und Eisenbahngesel Process for working up ferrovanadium containing products
US2234378A (en) * 1938-07-12 1941-03-11 Loring Peter Francis Process for the extraction of the valuable contents from antimonial, arsenical, and other complex ores
US2345067A (en) * 1939-08-17 1944-03-28 Osann Bernhard Method of and apparatus for operating shaft furnaces for roasting and the like
US2579107A (en) * 1948-03-03 1951-12-18 Marcel M Bertolus Industrial process for extracting rhenium
US2809092A (en) * 1955-04-11 1957-10-08 Kennecott Copper Corp Extraction of rhenium incidental to manufacture of mol ybdenum oxide
US3117860A (en) * 1958-04-11 1964-01-14 Ferrolegeringar Trollhetteverk Methods of removing copper and related metals from sulfidic molybdenum ores and molybdenum-containing materials
US3196004A (en) * 1963-04-01 1965-07-20 Sherritt Gordon Mines Ltd Molybdenum recovery process
US3348942A (en) * 1965-03-08 1967-10-24 Chase Brass & Copper Co Recovery of rhenium values
US3455677A (en) * 1967-04-27 1969-07-15 Union Carbide Corp Process for recovering copper and molybdenum from ore concentrates
US3458277A (en) * 1966-07-21 1969-07-29 Kennecott Copper Corp Process for the recovery of molybdenum values as high purity ammonium paramolybdate from impure molybdenum-bearing solution,with optional recovery of rhenium values if present
US3579328A (en) * 1967-05-31 1971-05-18 Christiania Spigerverk Process for the production of ferro-vanadium directly from slag obtained from vanadium-containing pig iron
GB1265486A (enExample) * 1968-05-21 1972-03-01

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1970467A (en) * 1932-10-28 1934-08-14 Otavi Minen Und Eisenbahngesel Process for working up ferrovanadium containing products
US2234378A (en) * 1938-07-12 1941-03-11 Loring Peter Francis Process for the extraction of the valuable contents from antimonial, arsenical, and other complex ores
US2345067A (en) * 1939-08-17 1944-03-28 Osann Bernhard Method of and apparatus for operating shaft furnaces for roasting and the like
US2579107A (en) * 1948-03-03 1951-12-18 Marcel M Bertolus Industrial process for extracting rhenium
US2809092A (en) * 1955-04-11 1957-10-08 Kennecott Copper Corp Extraction of rhenium incidental to manufacture of mol ybdenum oxide
US3117860A (en) * 1958-04-11 1964-01-14 Ferrolegeringar Trollhetteverk Methods of removing copper and related metals from sulfidic molybdenum ores and molybdenum-containing materials
US3196004A (en) * 1963-04-01 1965-07-20 Sherritt Gordon Mines Ltd Molybdenum recovery process
US3348942A (en) * 1965-03-08 1967-10-24 Chase Brass & Copper Co Recovery of rhenium values
US3458277A (en) * 1966-07-21 1969-07-29 Kennecott Copper Corp Process for the recovery of molybdenum values as high purity ammonium paramolybdate from impure molybdenum-bearing solution,with optional recovery of rhenium values if present
US3455677A (en) * 1967-04-27 1969-07-15 Union Carbide Corp Process for recovering copper and molybdenum from ore concentrates
US3579328A (en) * 1967-05-31 1971-05-18 Christiania Spigerverk Process for the production of ferro-vanadium directly from slag obtained from vanadium-containing pig iron
GB1265486A (enExample) * 1968-05-21 1972-03-01

Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3941867A (en) * 1974-09-04 1976-03-02 Canadian Patents And Development Limited Production of molybdenum trioxide from molybdenite in a fluidized bed
US4523948A (en) * 1984-02-14 1985-06-18 Amax Inc. Roasting of molybdenite concentrates containing flotation oils
US4687647A (en) * 1987-01-08 1987-08-18 Lloyd Berg Conversion of molybdenite to molybdenum dioxide using petroleum or coal tar pitches
DE3710725A1 (de) * 1987-03-31 1988-10-13 Gock Eberhard Verfahren zur direkten aufarbeitung von rheniumhaltigen molybdaensulfiden mit ammoniak
US20030049182A1 (en) * 2000-05-01 2003-03-13 Christopher Hertzler System and method for abatement of dangerous substances from a waste gas stream
US20030219361A1 (en) * 2002-05-25 2003-11-27 Unisem Co., Ltd. Apparatus and method for pretreating effluent gases in a wet environment
US20090277305A1 (en) * 2008-05-06 2009-11-12 Sd Lizenzverwertungsgesellschaft Mbh & Co. Kg Recovery of rhenium
US7763096B2 (en) 2008-05-06 2010-07-27 Sd Lizenzverwertungsgesellschaft Mbh & Co. Kg Recovery of rhenium
US8956582B2 (en) 2009-03-13 2015-02-17 Maritime House Metals Inc. Rhenium recovery
US20110229366A1 (en) * 2010-03-16 2011-09-22 Luederitz Eberhard Method for recovering rhenium and other metals from rhenium-bearing materials
US8383070B2 (en) 2010-03-16 2013-02-26 World Resources Company Method for recovering rhenium and other metals from rhenium-bearing materials
US8753591B2 (en) 2012-03-23 2014-06-17 Kennecott Utah Copper Llc Process for the conversion of molybdenite to molydenum oxide
US20150114181A1 (en) * 2012-12-28 2015-04-30 Pan Pacific Copper Co., Ltd. Method for producing aqueous solution of perrhenic acid from rhenium sulfide
US9624561B2 (en) * 2012-12-28 2017-04-18 Pan Pacific Copper Co., Ltd. Method for producing aqueous solution of perrhenic acid from rhenium sulfide
US9631259B2 (en) 2012-12-28 2017-04-25 Pan Pacific Copper Co., Ltd. Method for producing aqueous solution of perrhenic acid from rhenium sulfide
US20150267581A1 (en) * 2014-03-24 2015-09-24 Michael Patrick Ware, JR. In-situation scr catalyst cleaning process
CN104017987A (zh) * 2014-06-20 2014-09-03 大冶有色金属有限责任公司 一种从含铼钼精矿中分离钼和铼的方法
CN104017987B (zh) * 2014-06-20 2016-01-20 大冶有色金属有限责任公司 一种从含铼钼精矿中分离钼和铼的方法
CN104313329A (zh) * 2014-10-31 2015-01-28 罗旭 辐射解离铼气钼气电极还原金属铼钼的装置
CN105087962A (zh) * 2015-09-09 2015-11-25 中南大学 从含铼低品位钼精矿中高效提取钼和铼的方法
CN105087962B (zh) * 2015-09-09 2017-11-10 中南大学 从含铼低品位钼精矿中高效提取钼和铼的方法

Also Published As

Publication number Publication date
IT961042B (it) 1973-12-10
FR2119951B1 (enExample) 1976-04-30
GB1364934A (en) 1974-08-29
AU442132B2 (en) 1973-11-15
CA955754A (en) 1974-10-08
AU3568971A (en) 1973-05-24
DE2159219B2 (de) 1973-07-05
DE2159219A1 (de) 1972-07-13
FR2119951A1 (enExample) 1972-08-11

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