Isomerization of normal paraffins to form branched paraffins may be complicated by significant cracking of C.sub.7+ paraffins under isomerization reaction conditions. This issue may complicate upgrading of hydrocarbon feeds having significant quantities of heavier normal paraffins. Cracking selectivity may be decreased by combining one or more naphthenic compounds with a feed mixture comprising at least one C.sub.7+ normal paraffin and/or by utilizing tungstated zirconium catalysts having decreased tungsten loading. Further, C.sub.5 and C.sub.6 normal paraffins may undergo isomerization in the presence of C.sub.7+ normal paraffins. Methods for isomerizing normal paraffins may comprise: providing a feed mixture comprising at least C.sub.5-C.sub.7 normal paraffins and lacking normal paraffins larger than C.sub.8; and contacting the feed mixture with a bifunctional mixed metal oxide catalyst under isomerization reaction conditions effective to form a product mixture comprising one or more branched paraffins formed from each of the C.sub.5-C.sub.7 normal paraffins.

Systems and methods for producing an isomerization product. One or more isomerization reactors comprising a catalyst may be used to process an isomerization feedstock comprising a primary n-paraffin reactant and hydrogen gas, and the isomerization reactor may be operated at a pressure parameter at which the partial pressure of the primary n-paraffin is within about 70% to about 130% of its equilibrium vapor pressure to isomerize the primary n-paraffin reactant.

The present disclosure provides methods for fabricating catalysts for ammonia decomposition. The method may comprise (a) subjecting a catalyst support to one or more physical or chemical processes to optimize one or more pores, morphologies, and/or surface chemistry or property of the catalyst support; (b) depositing a composite support material on the catalyst support, wherein the composite support material comprises a morphology or surface chemistry or property; and (c) depositing one or more active metals on at least one of the composite support material and the catalyst support, wherein the one or more active metals comprise one or more nanoparticles configured to conform to the morphology of the composite support material and/or catalyst support material, thereby optimizing one or more active sites on the nanoparticles for ammonia processing.

The present invention relates to a method for preparing an alumina supported perovskite type oxide composition, to an alumina supported perovskite type oxide composition and to the use of such an alumina supported perovskite type oxide composition in catalytic systems in emission control applications.

A multilayer supported oxidative coupling of methane (OCM) catalyst composition (alpha-Al.sub.2O.sub.3 support, first single oxide layer, one or more mixed oxide layers, optional second single oxide layer) characterized by formula A.sub.aZ.sub.bE.sub.cD.sub.dO.sub.x/alpha-Al.sub.2O.sub.3; A is alkaline earth metal; Z is first rare earth element; E is second rare earth element; D is redox agent/third rare earth element; the first, second, third rare earth element are not the same; a=1.0; b=0.1-10.0; c=0.1-10.0; d=0-10.0; x balances oxidation states; first single oxide layer (Z.sub.b1O.sub.x1, b1=0.1-10.0; x1 balances oxidation states) contacts alpha-Al.sub.2O.sub.3 support and one or more mixed oxide layers; one or more mixed oxide layers (A.sub.a2Z.sub.b2E.sub.c2D.sub.d2O.sub.x2, a2=1.0; b2=0.1-10.0; c2=0.1-10.0; d2=0-10.0; x2 balances oxidation states; A.sub.aZ.sub.bE.sub.cD.sub.dO.sub.x and A.sub.a2Z.sub.b2E.sub.c2D.sub.d2O.sub.x2 are different) contacts first single oxide layer and optionally second single oxide layer, and second single oxide layer (AO), when present, contacts one or more mixed oxide layers and optionally first single oxide layer.

The present invention relates to a method for producing a support at least micrometric in size, photocatalytically active and at least in the visible range, containing nanocrystals each composed of from 80 to 100 mol % of TiO.sub.2 and from 0 to 20 mol % of at least one other metal or semi-metallic oxide, comprising the following steps, from an acidic aqueous reaction medium, at a heating temperature of between 20 and 60° C.: a step of adding the titanium oxide precursor, or a mixture of the titanium oxide precursor and the precursor of the other oxide, in the acidic aqueous reaction medium, and a condensation step on or inside the support, by spraying onto the support or immersing the support in the aqueous reaction medium, for a specific period of condensation, a heating step, the support allowing the nanocrystals to be crystallized, without using surfactant, in the aqueous reaction medium, a step of rinsing with water and a recovery step on the one hand of the support on which the crystallization took place, these nanocrystals being attached by covalent bonds to the support, and on the other hand of a residual solution.

A Ni—Al.sub.2O.sub.3@Al.sub.2O.sub.3—SiO.sub.2 catalyst with coated structure is provided. The catalyst has a specific surface area of 98 m.sup.2/g to 245 m.sup.2/g, and a pore volume of 0.25 cm.sup.3/g to 1.1 cm.sup.3/g. A mass ratio of an Al.sub.2O.sub.3 carrier to active component Ni in the catalyst is Al.sub.2O.sub.3:Ni=100:4˜26, a mass ratio of the Al.sub.2O.sub.3 carrier to an Al.sub.2O.sub.3—SiO.sub.2 coating layer is Al.sub.2O.sub.3:Al.sub.2O.sub.3—SiO.sub.2=100:0.1˜3, and a molar ratio of Al to Si in the Al.sub.2O.sub.3—SiO.sub.2 coating layer is 0.01 to 1. Ni particles are distributed on a surface of the Al.sub.2O.sub.3 carrier in an amorphous or highly dispersed state and have a grain size less than or equal to 8 nm, and the coating layer is filled among the Ni particles.

The present invention relates to a catalyst comprising at least one oxide of vanadium, at least one oxide of tungsten, at least one oxide of cerium, at least one oxide of titanium and at least one oxide of antimony, and an exhaust system containing said oxides.

A method of upcycling polymers to useful hydrocarbon materials. A catalyst with nanoparticles on a substrate selectively docks and cleaves longer hydrocarbon chains over shorter hydrocarbon chains. The nanoparticles exhibit an edge to facet ratio to provide for more interactions with the facets.

Embodiments of the present invention relates to two improved catalysts and associated processes that directly converts carbon dioxide and hydrogen to liquid fuels. The catalytic converter is comprised of two catalysts in series that are operated at the same pressures to directly produce synthetic liquid fuels or synthetic natural gas. The carbon conversion efficiency for CO.sub.2 to liquid fuels is greater than 45%. The fuel is distilled into a premium diesel fuels (approximately 70 volume %) and naphtha (approximately 30 volume %) which are used directly as “drop-in” fuels without requiring any further processing. Any light hydrocarbons that are present with the carbon dioxide are also converted directly to fuels. This process is directly applicable to the conversion of CO.sub.2 collected from ethanol plants, cement plants, power plants, biogas, carbon dioxide/hydrocarbon mixtures from secondary oil recovery, and other carbon dioxide/hydrocarbon streams. The catalyst system is durable, efficient and maintains a relatively constant level of fuel productivity over long periods of time without requiring re-activation or replacement.