Abstract: In one embodiment, a process for the purification of CO2 from chlorinated and non-chlorinated hydrocarbons, comprising: contacting a CO2 stream with a metal oxide catalyst, wherein the stream comprises the CO2 and impurities comprising the non-chlorinated hydrocarbons and the chlorinated hydrocarbons; interacting the impurities with the catalyst to form additional CO2 and metal chloride; and regenerating the catalyst by contacting the metal chloride with an oxygen containing gas stream.

Abstract: In one embodiment, a process for the purification of CO2 from chlorinated and non-chlorinated hydrocarbons, comprising: contacting a CO2 stream with a metal oxide catalyst, wherein the stream comprises the CO2 and impurities comprising the non-chlorinated hydrocarbons and the chlorinated hydrocarbons; interacting the impurities with the catalyst to form additional CO2 and metal chloride; and regenerating the catalyst by contacting the metal chloride with an oxygen containing gas stream.

Abstract: The invention relates to a catalyst and process for making syngas mixtures including hydrogen, carbon monoxide and carbon dioxide. The process comprises contacting a gaseous feed mixture containing carbon dioxide and hydrogen with the catalyst, where the catalyst comprises Mn oxide and an auxiliary metal oxide selected from the group consisting of La, Ca, K, W, Cu, Al and mixtures or combinations thereof. The process enables hydrogenation of carbon dioxide into carbon monoxide with high selectivity, and good catalyst stability over time and under variations in processing conditions. The process can be applied separately, but can also be integrated with other processes, both up-stream and/or down-stream including methane reforming or other synthesis processes for making products like alkanes, aldehydes, or alcohols.

Abstract: A method for making a syngas mixture is accomplished by introducing a gaseous feed mixture containing carbon dioxide and hydrogen into a reactor containing a non-zinc catalyst. The catalyst contacts the gaseous feed mixture to form syngas mixture reaction products. The reaction takes place in the presence of nickel-containing and/or iron-containing materials. The gaseous feed mixture is introduced into the reactor at a reactor inlet temperature of from 700° C. to 800° C., with the reaction being carried out at substantially adiabatic conditions or wherein the syngas mixture reaction products are removed from the reactor at a reactor outlet temperature of from 500° C. to 600° C.

Abstract: The invention relates to a catalyst and process for making syngas mixtures including hydrogen, carbon monoxide and carbon dioxide. The process comprises contacting a gaseous feed mixture containing carbon dioxide and hydrogen with the catalyst, where the catalyst comprises Mn oxide and an auxiliary metal oxide selected from the group consisting of La, Ca, K, W, Cu, Al and mixtures or combinations thereof. The process enables hydrogenation of carbon dioxide into carbon monoxide with high selectivity, and good catalyst stability over time and under variations in processing conditions. The process can be applied separately, but can also be integrated with other processes, both up-stream and/or down-stream including methane reforming or other synthesis processes for making products like alkanes, aldehydes, or alcohols.

Abstract: Disclosed is a catalyst composition which does not contain antimony or molybdenum for the vapor phase ammoxidation of alkanes of the general empirical formula: VWaBibMcOx wherein M is one or more elements selected from sodium, cesium, magnesium, calcium, barium, boron, yttrium, indium, aluminum, gallium, tin, titanium, silicon, zirconium, germanium, niobium and tantalum, a is 0.2 to 10, b is 0.5 to 5, c is 0 to 10 and x is determined by the valence requirements of the elements present. The catalyst precursor is precipitated from a solution or slurry of compounds of vanadium, tungsten, bismuth and, optionally, M, then separated, dried and calcined to give a phase or combination of phases active in the ammoxidation of low-weight paraffins to the corresponding unsaturated mononitriles. Nitriles may be produced in a gas phase catalytic reaction of alkanes with ammonia and oxygen in the presence of the catalyst.

Abstract: A process for the vapor phase ammoxidation of alkanes and olefins with a catalyst of the general empirical formula: VSbaMbQcOx wherein M is at least one element selected from magnesium, aluminum, zirconium, silicon, hafnium, titanium and niobium, Q is at least one element selected from rhenium, tungsten, molybdenum, tantalum, manganese, phosphorus, cerium, tin, boron, scandium, bismuth, gallium, indium, iron, chromium, lanthanum, yttrium, zinc, cobalt, nickel, cadmium, copper, strontium, barium, calcium, silver, potassium, sodium and cesium, a is 0.5 to 20, b is 2 to 50, c is 0 to 10 and x is determined by the valence requirements of the elements present. The process has a co-feed of gaseous carbon dioxide with an alkane (paraffin) and/or alkene, ammonia and an oxygen-containing gas which react in the presence of the catalyst to form a nitrile and by-products.

Abstract: A catalyst composition for the vapor phase ammoxidation of alkanes and olefins of the general empirical formulae: VSbaMbOx VSbaMbM′b′Ox VSbaMbQcOx VSbaMbQcQ′c′Ox wherein M and M′ are at least one element selected from magnesium, aluminum, zirconium, silicon, hafnium, titanium and niobium, M and M′ being different, Q and Q′ are at least one element selected from rhenium, tungsten, molybdenum, tantalum, manganese, phosphorus, cerium, tin, boron, scandium, bismuth, gallium, indium, iron, chromium, lanthanum, yttrium, zinc, cobalt, nickel, cadmium, copper, strontium, barium, calcium, silver, potassium, sodium and cesium, Q and Q′ being different, a is 0.5 to 20, b is 2 to 50, b′ is 0 to 50, c is 0 to 10, c′ is 0 to 10 and x is determined by the valence requirements of the elements present.

Abstract: A catalyst composition for the vapor phase ammoxidation of alkanes and olefins of the general empirical formulae:

Abstract: A catalyst composition for oxidative dehydrogenation of paraffinic hydrocarbons and other compounds having at least two adjacent carbon atoms each having at least one hydrogen atom. The catalyst composition is represented by the formula AaBbSbcVdAleOx wherein A is an alkali or alkaline earth metal; B is one or more optional elements selected from zinc, cadmium, lead, nickel, cobalt, iron, chromium, bismuth, gallium, niobium, tin and neodymium; a is 0 to 0.3, b is 0 to 5, c is 0.5 to 10, d is 1, e is 3 to 10, 7≦a+b+c+d+e≦25, and x is determined by the valence requirements of the elements present. A process for the oxidative dehydrogenation of paraffins using the catalyst composition.

Abstract: Alkanes are catalytically oxidized in air or oxygen using iron-substituted polyoxoanions (POAs) of the formula:H.sub.e-z ?(n-C.sub.4 H.sub.9).sub.4 N!.sub.z (XM.sub.11 M'O.sub.39).sup.-eThe M' (e.g., iron(III)/iron(II)) reduction potential of the POAs is affected by selection of the central atom X and the framework metal M, and by the number of tetrabutyl-ammonium groups. Decreased Fe(III)/Fe(II) reduction potential has been found to correlate to increased oxidation activity.

Abstract: Alkanes are converted to unsaturated carboxylic acids by contacting an alkane with an oxidizing agent and a heteropolyacid or polyoxoanion comprising (1) at least 9 atoms of a first framework metal or metals comprising molybdenum, tungsten or vanadium or combinations thereof and (2) 1 to 3 atoms of a second framework metal or metals comprising zinc or a transition metal different from the first framework metal.

Abstract: Alkanes are catalytically oxidized using heteropolyacids (HPAs) or polyoxoanions (POAs) deposited on a graphite surface. The HPAs and POAs are framework-substituted with a different metal in place of a metal-oxygen unit.