Abstract: The present disclosure relates to solid phosphoric acid (SPA) catalyst compositions useful in the formation of hydrocarbons, such as the oligomerization of olefins, prepared from formable mixtures that comprise a phosphate source and a siliceous support material source in amounts, for example, such that the ratio of the phosphate source and the siliceous support material source is within the range of about 2.9:1 to about 3.4:1 calculated on a weight basis as H3PO4:SiO2, and a dry particulate material.

Abstract: The present disclosure relates generally to ceramic materials suitable for use as catalyst support materials, catalysts using such materials and methods for using them, such as methods for converting sugars, sugar alcohols, glycerol, and bio-renewable organic acids to commercially-valuable chemicals and intermediates. One aspect of the invention is a ceramic material including zirconium oxide and one or more metal oxides selected from nickel oxide, copper oxide, cobalt oxide, iron oxide and zinc oxide, the ceramic material being at least about 50 wt. % zirconium oxide. In certain embodiments, the ceramic material is substantially free of any binder, extrusion aid or additional stabilizing agent.

Abstract: The present disclosure relates generally to ceramic materials suitable for use as catalyst support materials, catalysts using such materials and methods for using them, such as methods for converting sugars, sugar alcohols, glycerol, and bio-renewable organic acids to commercially-valuable chemicals and intermediates. One aspect of the invention is a ceramic material including zirconium oxide and one or more metal oxides selected from nickel oxide, copper oxide, cobalt oxide, iron oxide and zinc oxide, the ceramic material being at least about 50 wt. % zirconium oxide. In certain embodiments, the ceramic material is substantially free of any binder, extrusion aid or additional stabilizing agent.

Abstract: The present invention relates to solid phosphoric acid (SPA) catalysts, processes for making the catalysts, and processes for conversion of hydrocarbons using the catalysts, such as oligomerization of propylene. In an exemplary embodiment, the catalyst comprises a calcined extrudate of phosphoric acid, diatomaceous earth, and niobic acid. Methods for converting hydrocarbons to olefins comprise contacting a hydrocarbon feedstock with the catalyst at hydrocarbon conversion conditions.

Abstract: A process for removing mercury from a gas or liquid phase, wherein the gas or liquid phase containing mercury is placed in contact with a composition comprising a precipitated metal sulfide. The precipitated metal sulfide may be made by the process of combining a metal source, sulfide source, and modifier to form the precipitated metal sulfide. The metal source may comprise iron, cobalt, nickel, copper, zinc, zirconium, molybdenum, silver, or gold salts. The metal salt may be selected from metal nitrate, metal sulfate, metal phosphate, metal acetate, metal carbonate, metal hydroxide, metal ammonium carbonate, and metal hydroxycarbonate. The sulfide source is selected from hydrogen sulfide (H2S), carbonyl sulfide (COS), salts of sulfide (S2-), salts of hydrosulfide (HS—), and salts of polysulfide (Sn2-). The modifier may be selected from alumina, silica, aluminosilicate, clay, zeolites, carbon, cement, titania, zirconia.

Abstract: A hydrodeoxygenation catalyst comprises a metal catalyst, an acid promoter, and a support. The metal catalyst is selected from platinum, palladium, ruthenium, rhenium rhodium, osmium, iridium, nickel, cobalt, molybdenum, copper, tin, or mixtures thereof. The support is a promoted-zirconium material including texture promoters and acid promoters. The hydrodeoxygenation catalyst may be used for hydrodeoxygenation (HDO) of sugar or sugar alcohol in an aqueous solution. In one embodiment the HDO catalyst may be used for HDO of fatty acids such as fatty acid methyl esters (FAME), triglycerols (in plant oil and animal fat), pyrolysis oil, or lignin. The hydrodeoxygenation catalyst for fatty acid process does not require the use of an acid promoter, it is optional.

Abstract: Ethylene glycol and propylene glycol may be made by hydrogenolysis of a polyol comprising the steps of reacting a polyol with hydrogen in the presence of a hydrogenolysis catalyst. The hydrogenolysis comprises nickel, one or more promoter, and one or more support. The promoter is selected from bismuth, silver, tin, antimony, gold, lead, thallium, cerium, lanthanum, and manganese. The support is selected from zirconia and carbon. A zirconia support comprises a zirconia textual promoter, which is selected from Cr, Mo, W, Nb, Ce, Ca, Mg, La, Pr, Nd, Al, and P. If the support comprises carbon, then the promoter is selected from bismuth and antimony. In another embodiment, if the support comprises carbon, then both the promoter is selected from bismuth and antimony, and the catalyst comprises copper. In another embodiment, the catalyst additionally comprises copper.

Abstract: The present disclosure relates generally to ceramic materials suitable for use as catalyst support materials, catalysts using such materials and methods for using them, such as methods for converting sugars, sugar alcohols, glycerol, and bio-renewable organic acids to commercially-valuable chemicals and intermediates. One aspect of the invention is a ceramic material including zirconium oxide and one or more metal oxides selected from nickel oxide, copper oxide, cobalt oxide, iron oxide and zinc oxide, the ceramic material being at least about 50 wt. % zirconium oxide. In certain embodiments, the ceramic material is substantially free of any binder or additional stabilizing agent.

Abstract: The present disclosure relates generally to catalyst support materials, catalysts and methods for using them, such as methods for converting sugars, sugar alcohols, glycerol, and bio-renewable organic acids to commercially-valuable chemicals and intermediates. One aspect of the invention is catalyst support material including ZrO2 and one or more oxides of manganese (MnOx), the catalyst support material being at least about 50 wt % ZrO2 and MnOx. In certain embodiments, the weight ratio of ZrO2 to MnOx is within the range of about 1:1 to about 30:1; and/or the catalyst support material is substantially free of any binder, extrusion aid or additional stabilizing agent.

Abstract: The present disclosure relates generally to catalyst support materials, catalysts and methods for using them, such as methods for converting sugars, sugar alcohols, glycerol, and bio-renewable organic acids to commercially-valuable chemicals and intermediates. One aspect of the invention is catalyst support material including ZrO2 and one or more oxides of manganese (MnOx), the catalyst support material being at least about 50 wt % ZrO2 and MnOx. In certain embodiments, the weight ratio of ZrO2 to MnOx is within the range of about 1:1 to about 30:1; and/or the catalyst support material is substantially free of any binder, extrusion aid or additional stabilizing agent.

Abstract: A process for removing mercury from a gas or liquid phase, wherein the gas or liquid phase containing mercury is placed in contact with a composition comprising a precipitated metal sulfide. The precipitated metal sulfide may be made by the process of combining a metal source, sulfide source, and modifier to form the precipitated metal sulfide. The metal source may comprise iron, cobalt, nickel, copper, zinc, zirconium, molybdenum, silver, or gold salts. The metal salt may be selected from metal nitrate, metal sulfate, metal phosphate, metal acetate, metal carbonate, metal hydroxide, metal ammonium carbonate, and metal hydroxycarbonate. The sulfide source is selected from hydrogen sulfide (H2S), carbonyl sulfide (COS), salts of sulfide (S2?), salts of hydrosulfide (HS?), and salts of polysulfide (Sn2?). The modifier may be selected from alumina, silica, aluminosilicate, clay, zeolites, carbon, cement, titania, zirconia.

Abstract: A process for converting a sugar, sugar alcohol, or glycerol to a valuable chemical is described. The process may use a support comprising zirconium oxide promoted by a polyacid or promoter material. A catalytically active metal may be impregnated on the polyacid-promoted zirconium oxide support and the catalyst may then be introduced the sugar, sugar alcohol, or glycerol a source of hydrogen under reaction conditions. At least 40 wt % of the sugar, sugar alcohol or glycerol may be converted to a polyol and/or a shorter carbon-chain alcohol that may include at least one of propylene glycol, ethylene glycol, glycerin, methanol, ethanol, propanol and butandiols. Specific processes for converting glycerin having a selectivity for propylene glycol and for converting sorbitol with a selectivity for propylene glycol, ethylene glycol, and/or glycerin are also described.

Abstract: Ethylene glycol and propylene glycol may be made by hydrogenolysis of a polyol comprising the steps of reacting a polyol with hydrogen in the presence of a hydrogenolysis catalyst. The hydrogenolysis comprises nickel, one or more promoter, and one or more support. The promoter is selected from bismuth, silver, tin, antimony, gold, lead, thallium, cerium, lanthanum, and manganese. The support is selected from zirconia and carbon. A zirconia support comprises a zirconia textual promoter, which is selected from Cr, Mo, W, Nb, Ce, Ca, Mg, La, Pr, Nd, Al, and P. If the support comprises carbon, then the promoter is selected from bismuth and antimony. In another embodiment, if the support comprises carbon, then both the promoter is selected from bismuth and antimony, and the catalyst comprises copper. In another embodiment, the catalyst additionally comprises copper.

Abstract: A process for removing mercury from a gas or liquid phase, wherein the gas or liquid phase containing mercury is placed in contact with a composition comprising a precipitated metal sulfide. The precipitated metal sulfide may be made by the process of combining a metal source, sulfide source, and modifier to form the precipitated metal sulfide. The metal source may comprise iron, cobalt, nickel, copper, zinc, zirconium, molybdenum, silver, or gold salts. The metal salt may be selected from metal nitrate, metal sulfate, metal phosphate, metal acetate, metal carbonate, metal hydroxide, metal ammonium carbonate, and metal hydroxycarbonate. The sulfide source is selected from hydrogen sulfide (H2S), carbonyl sulfide (COS), salts of sulfide (S2-), salts of hydrosulfide (HS—), and salts of polysulfide (Sn2-).

Abstract: A hydrodeoxygenation catalyst comprises a metal catalyst, an acid promoter, and a support. The metal catalyst is selected from platinum, palladium, ruthenium, rhenium rhodium, osmium, iridium, nickel, cobalt, molybdenum, copper, tin, or mixtures thereof. The support is a promoted-zirconium material including texture promoters and acid promoters. The hydrodeoxygenation catalyst may be used for hydrodeoxygenation (HDO) of sugar or sugar alcohol in an aqueous solution. In one embodiment the HDO catalyst may be used for HDO of fatty acids such as fatty acid methyl esters (FAME), triglycerols (in plant oil and animal fat), pyrolysis oil, or lignin. The hydrodeoxygenation catalyst for fatty acid process does not require the use of an acid promoter, it is optional.

Abstract: The present invention relates to solid phosphoric acid (SPA) catalysts, processes for making the catalysts, and processes for conversion of hydrocarbons using the catalysts, such as oligomerization of propylene. In an exemplary embodiment, the catalyst comprises a calcined extrudate of phosphoric acid, diatomaceous earth, and niobic acid. Methods for converting hydrocarbons to olefins comprise contacting a hydrocarbon feedstock with the catalyst at hydrocarbon conversion conditions.

Abstract: A process for converting a sugar, sugar alcohol, or glycerol to a valuable chemical is described. The process may use a support comprising zirconium oxide promoted by a polyacid or promoter material. A catalytically active metal may be impregnated on the polyacid-promoted zirconium oxide support and the catalyst may then be introduced the sugar, sugar alcohol, or glycerol a source of hydrogen under reaction conditions. At least 40 wt % of the sugar, sugar alcohol or glycerol may be converted to a polyol and/or a shorter carbon-chain alcohol that may include at least one of propylene glycol, ethylene glycol, glycerin, methanol, ethanol, propanol and butandiols. Specific processes for converting glycerin having a selectivity for propylene glycol and for converting sorbitol with a selectivity for propylene glycol, ethylene glycol, and/or glycerin are also described.

Abstract: A polyacid-promoted, zirconia catalyst or catalyst support having a high crush strength, surface area and pore volume is described. The polyacid-promoted, zirconia catalyst or catalyst support may be made by combining a zirconium compound with a polyacid/promoter material that includes the group 6 metals (i.e., chromium (Cr), molybdenum (Mo), tungsten (W)), as well as phosphoric acids, sulfuric acids, and polyorganic acids. The zirconyl-promoter precursor may be extruded in the absence of any binder or extrusion aid. The polyacid-promoted, zirconia catalyst or catalyst support is hydrothermally stable in aqueous phase hydrogenation or hydrogenoloysis reactions.

Abstract: The present invention relates to a solid phosphoric acid catalyst and a process for conversion of hydrocarbons using a solid phosphoric acid catalyst. The solid phosphoric acid catalyst comprises silicon orthophosphate, and has a silicon orthophosphate to silicon pyrophosphate ratio of at least about 5:1. The total pore volume of the solid phosphoric acid catalyst is at least about 0.17 cm3 per gram of catalyst, of which at least about 0.15 cm3 per gram is contributed by pores with diameter of at least about 10,000 ?.

Abstract: The present invention relates to a solid phosphoric acid catalyst and a process for conversion of hydrocarbons using a solid phosphoric acid catalyst. The solid phosphoric acid catalyst comprises silicon orthophosphate, and has a silicon orthophosphate to silicon pyrophosphate ratio of at least about 5:1. The total pore volume of the solid phosphoric acid catalyst is at least about 0.17 cm3 per gram of catalyst, of which at least about 0.15 cm3 per gram is contributed by pores with diameter of at least about 10,000 ?.