Amax Incorporated

Gte Sylvania Incorporated

John M Laferty, Jr

Joseph E Ritsko

Dale K Huggins

David J Port

Roger F Sebenik

Paul B Queneau

Leo W Beckstead

Malcolm T Hepworth

Cvetko B Nikolic

William A May

Kent H Carpenter

John D Bruno

Dennis L Howe

Lawrence F McHugh

Pablo P LaValle

A process is provided for converting MoS.sub.2 to MoO.sub.2 wherein, MoS.sub.2 in particulate form is fed into a reactor while flowing MoO.sub.3 vapor therein to effect reaction thereof with MoS.sub.2 to form MoO.sub.2. The temperature in the reactor is maintained at a level sufficient to cause the reaction to go forward. A portion of the MoO.sub.2 is removed from the reactor as a product and the remainder is selectively oxidized at a temperature sufficient to generate gaseous MoO.sub.3 which is recycled to the reactor relative to the flow of MoS.sub.2 therein to convert the MoS.sub.2 to MoO.sub.2.

Process for the production of molybdenum dioxide

A process is provided for producing ammonium metatungstate comprising fluid bed roasting ammonium paratungstate at a temperature over the range of about 275.degree. C. to 305.degree. C. for a time at least sufficient to provide a roasted product in the form of a precursor of ammonium metatungstate, forming an aqueous slurry of the precursor and digesting the precursor at a pH of about 3 to 4 for a time at least sufficient to effect substantially complete dissolution of said precursor, filtering the digested slurry to produce a clear filtrate, and further processing the clear filtrate by evaporation to provide crystals of substantially pure ammonium metatungstate.

Process for producing ammonium metatungstate

A process is provided for recovering metal values from spent hydrodesulfurization catalyst, the process comprising forming in a pressure reactor an aqueous slurry of finely divided spent catalyst and sodium carbonate, the spent catalyst containing by weight about 2 to 10% Mo, up to about 12% V (e.g., about 2 to 10%), about 0.5 to 4% Co, up to about 10% Ni (e.g., about 0.5 to 5%), occluded oil, coke, sulfide sulfur and the balance essentially alumina. The amount of sodium carbonate employed is at least sufficient under oxidizing conditions to convert molybdenum and any vanadium present to soluble Na.sub.2 MoO.sub.4 and NaVO.sub.3 and to neutralize SO.sub.3 produced during oxidation, the amount of sodium carbonate being at least that required stoichiometrically. The slurry is heated to a temperature of about 200.degree. C. to 350.degree. C. (e.g., 275.degree. C. to 325.degree. C.) and a pressure of about 800 psig to 2500 psig (e.g., about 1500 psig to 2500 psig) for a time at least sufficient to solubilize the molybdenum and vanadium present, the amount of oxygen employed being over about 1.1 times the stoichiometric amount sufficient to oxidize the metal values and sulfur to the maximum oxidized state, and to oxidize the oil and free carbon to CO.sub.2 and H.sub.2 O. The solubilized Mo and V are thereafter separated from each other.

Recovery of metal values from spent hydrodesulfurization catalysts

A process for stripping tungsten values from a tungsten-bearing acidic liquid organic phase into a basic aqueous ammoniacal stripping solution comprises mixing the organic phase and the stripping solution with a high-shear mixing device to maximize the pH gradient between the organic phase and the aqueous solution whereby growth of any precipitated ammonium paratungstate crystals is minimized and the dissolution thereof is maximized and to strip the tungsten values from the organic phase into the stripping solution.

Ammonium hydroxide stripping of tungsten from organic solvents

A hydrometallurgical process is provided for the recovery of molybdenum values from a molybdenum disulfide concentrate containing copper. The process comprises forming an aqueous slurry of finely divided molybdenum concentrate of carbonates and hydroxides of alkali metals, and pressure leaching the slurry in the presence of oxygen at an elevated temperature and pressure for a time sufficient to effect conversion of the contained molybdenum values to alkali metal molybdate and provide a residue containing copper oxide or basic copper carbonate from which copper is later recovered. The molybdenum values are recovered from solution by solvent extraction and the solvent thereafter stripped of the molybdenum as ammonium molybdenum using ammonium hydroxide. The molybdenum is recovered as crystals of ammonium molybdate by crystallization, e.g., by evaporating the stripping solution.

Process for recovering molybdenum and copper from sulfide concentrates

Molybdenum is recovered from an ammonium molybdate solution containing phosphate anions by digesting in an ammonium molybdate solution at least one water-soluble compound of at least one metal selected from the group consisting of aluminum, calcium, iron and magnesium in small but effective amounts to precipitate at least about 50% of the phosphate anions for a time sufficient to precipitate the phosphate anion, separating the phosphate precipitate from the ammonium molybdate solution, then acidifying the ammonium molybdate solution with at least one mineral acid selected from the group consisting of sulfuric acid and nitric acid to lower the pH value of the solution to between about 2.5 and about 4.5 to precipitate ammonium polymolybdate, and calcining the ammonium polymolybdate at a temperature below about 750.degree. C. to produce a molybdenum trioxide product.

Production of molybdenum oxide from ammonium molybdate solutions

Free flowing powders, such as for flame spray applications, are produced by spray drying a slurry of finely divided particles of the metal in a solvent-binder system to produce agglomerates, wherein the binder is a soluble compound of the metal. These agglomerates possess sufficient green strength to be screened and exhibit higher apparent densities than comparable powders agglomerated with conventional organic binders. When these powders are heated in a reducing atmosphere above the decomposition temperature of the binder, the binder converts to base metal and harmless by-products, such as nitrogen and water thus avoiding contamination of the product, equipment and work area usually associated with conventional organic binders.

Free flowing powder and process for producing it

Selenium is removed from copper electrolytes by adding a substance selected from the group consisting of metals above copper in the electromotive series, excluding alkali metals, such as nickel powder, cobalt powder and iron powder. Sodium sulfide can also be used along with a subsequent addition of ferric sulfate. The amount of the reactive substance added should be sufficient to reduce the selenium content to below 2 ppm.

Growing community of inventors

Wheat Ridge, CO, United States of America

John M Laferty, Jr