Abstract: A renewable feed that is concentrated linear C10-C13 paraffins is produced by hydrodeoxygenating a renewable feedstock is produced by first hydrotreating the feedstock to remove heteroatoms followed by use of a Group VI or VIII catalyst producing a 10-13 carbon atom product having a high level of linearity. Normal paraffins in the range desired by the detergents industry can be produced.

Abstract: A de-hydrogenation catalyst and its use in dehydrogenation of hydrocarbons. The catalyst has low cracking activity and comprises gallium or gallium and platinum on an essentially non-acidic and amorphous alumina-phosphate or silica-alumina-phosphate support with an empirical chemical composition of [Al2O3][SiO2]Y[P2O5]Z, wherein Y is between 0 and 0.2 and Z is between 0.01 and 1.1, with a BET surface area above 50 m2/g, as measured by N2 adsorption experiment.

Abstract: A biorenewable feed that is concentrated in free fatty acids is produced by hydrodeoxygenating a biorenewable feedstock is produced by use of a Group VIII catalyst producing a 10-13 carbon atom product having a high level of linearity. Normal paraffins in the range desired by the detergents industry can be produced. Either isomerization or an iso-normal separation can be performed to provide green fuel streams.

Abstract: A fluidized catalytic reactor system cycles from 0.05-5% of catalyst at a time through a rejuvenation unit to be heated in the presence of oxygen to maintain catalyst activity. The use of the rejuvenation unit that may be 2% of the size of the main catalyst regeneration unit allows for reduction in equipment size and in catalyst inventory. The catalyst that is sent to the rejuvenation unit may be spent catalyst but may be partially or fully regenerated catalyst. The rejuvenation unit may be heated by combusting fuel or by hot flue gas.

Abstract: A fluidized reforming process comprising a two stage fluidized reforming reactor is described. A naphtha stream flows upward through the two fluidized stages and contacts the catalyst forming a product stream and spent catalyst. The spent catalyst is separated from the product stream and the naphtha feed stream. Some of the spent catalyst is regenerated by contact with an oxygen-containing regeneration fluid to heat and reactivate the catalyst. The heated, regenerated catalyst forms at least a port of the catalyst stream for the process. A process for cyclizing paraffins or isomerizing cyclopentanes is also described. The process uses a chloride-free Pt/Ga-containing catalyst to form a cyclic aliphatic hydrocarbon or isomerizing a cyclopentane in the presence of the chloride-free Pt/Ga-containing catalyst to form a cyclohexane.

Abstract: A fluidized catalytic reactor decouples the catalyst regenerator temperature from the catalyst reactor residence time. Regenerated catalyst is cooled before it contacts reactant feed. The regenerated catalyst may be cooled by heat exchange with oxygen supply gas, spent catalyst or other materials. The process and apparatus are especially useful for fluidized endothermic catalytic reactions.

Abstract: A de-hydrogenation catalyst and its use in dehydrogenation of hydrocarbons. The catalyst has low cracking activity and comprises gallium or gallium and platinum on an essentially non-acidic and amorphous alumina-phosphate or silica-alumina-phosphate support with an empirical chemical composition of [Al2O3][SiO2]Y[P2O5]Z, wherein Y is between 0 and 0.2 and Z is between 0.01 and 1.1, with a BET surface area above 50 m2/g, as measured by N2 adsorption experiment.

Abstract: A process is provided for dehydrogenating a paraffinic hydrocarbon comprising sending the paraffinic hydrocarbon to a fluidized bed reactor to be contacted at dehydrogenation reaction conditions with a catalyst composition comprising less than about 0.0999 wt % platinum and about 0.05-2.5 wt % Group I or Group II elements or a mixture thereof. The catalytic composition is prepared without addition of tin, gallium, indium, germanium or lead.

Abstract: A fluidized catalytic reactor system cycles from 0.05-5% of catalyst at a time through a rejuvenation unit to be heated in the presence of oxygen to maintain catalyst activity. The use of the rejuvenation unit that may be 2% of the size of the main catalyst regeneration unit allows for reduction in equipment size and in catalyst inventory. The catalyst that is sent to the rejuvenation unit may be spent catalyst but may be partially or fully regenerated catalyst. The rejuvenation unit may be heated by combusting fuel or by hot flue gas.

Abstract: A process for regenerating spent catalyst by combusting coke and fuel gas together in the presence of enriched oxygen restores activity to the catalyst to bring back to adequate activity level while reducing or obviating the need for the oxygen treatment step. The oxygen concentration in the oxygen supply gas should be greater than 21 vol %.

Abstract: A trialkylphosphonium haloaluminate compound having a formula: where R1, R2, and R3 are the same or different and each is independently selected from C1 to C8 hydrocarbyl; and X is selected from F, Cl, Br, I, or combinations thereof is described. An ionic liquid catalyst composition incorporating the trialkylphosphonium haloaluminate compound, methods of making the trialkylphosphonium haloaluminate compound, and alkylation processes incorporating the trialkylphosphonium haloaluminate compound are also described.

Abstract: The process for producing light olefins comprises the steps of contacting a feed stream comprising C4 to C11 hydrocarbons having at least 10 wt % paraffins and at least 15 wt % alkylaromatics with an acidic catalyst to form a cracked product comprising light olefins and aromatics. The catalyst comprises about 30 to about 80 wt-% of a crystalline zeolite and a low-acidic binder and may be regenerated.

Abstract: A process utilizing a micro-emulsion is described. The micro-emulsion formed by contacting an ionic liquid, a co-solvent, a hydrocarbon, an optional surfactant, and an optional catalyst promoter to form the micro-emulsion. The micro-emulsion comprises a hydrocarbon component comprising the hydrocarbon and an ionic liquid component comprising the ionic liquid. The ionic liquid comprises a halometallate anion and a cation. The co-solvent has a polarity greater than a polarity of the hydrocarbon. The ionic liquid is present in an amount of 0.05 wt % to 40 wt % of the micro-emulsion. A product mixture comprising a product is produced in a process zone containing the micro-emulsion.

Abstract: A micro-emulsion and a method of making the micro-emulsion are described. The micro-emulsion includes a hydrocarbon component, an ionic liquid component, and a co-solvent. The ionic liquid comprises a halometallate anion and a cation. The micro-emulsion can optionally include a surfactant, and a catalyst promoter. The co-solvent has a polarity greater than the polarity of the hydrocarbon. The ionic liquid is present in an amount of about 0.05 wt % to about 40 wt % of the micro-emulsion.

Abstract: A hydrocarbon conversion process is described. The process involves contacting a hydrocarbon feed with a non-cyclic amide or thioamide based ionic liquid catalyst in a reaction zone under reaction conditions to form a mixture comprising reaction products, and the non-cyclic amide or thioamide based ionic liquid catalyst. Typical hydrocarbon conversion processes include alkylation, oligomerization, isomerization, disproportionation, and reverse disproportionation.

Abstract: Non-cyclic amide or thioamide based ionic liquids and methods of making them are disclosed.

Abstract: A trialkylphosphonium haloaluminate compound having a formula: where R1, R2, and R3 are the same or different and each is independently selected from C1 to C8 hydrocarbyl; and X is selected from F, Cl, Br, I, or combinations thereof is described. An ionic liquid catalyst composition incorporating the trialkylphosphonium haloaluminate compound, methods of making the trialkylphosphonium haloaluminate compound, and alkylation processes incorporating the trialkylphosphonium haloaluminate compound are also described.

Abstract: A process utilizing an ionic liquid is described. The process includes contacting a hydrocarbon feed with an ionic liquid component, the ionic liquid component comprising a mixture of a first ionic liquid and a viscosity modifier, wherein a viscosity of the ionic liquid component is at least about 10% less than a viscosity of the first ionic liquid.

Abstract: A naphtha cracking feed stream is taken, heated and passed to a cracking reactor. Hydrogen is added to the cracking reactor to mitigate catalyst deactivation. The aliphatic compounds are selectively cracked and at least a portion of the alkyl groups on the aromatic compounds are selectively dealkylated in the presence of a cracking catalyst to produce a cracked effluent stream comprising aromatic compounds and cracked olefins.

Abstract: A process utilizing a micro-emulsion is described. The micro-emulsion formed by contacting an ionic liquid, a co-solvent, a hydrocarbon, an optional surfactant, and an optional catalyst promoter to form the micro-emulsion. The micro-emulsion comprises a hydrocarbon component comprising the hydrocarbon and an ionic liquid component comprising the ionic liquid. The ionic liquid comprises a halometallate anion and a cation. The co-solvent has a polarity greater than a polarity of the hydrocarbon. The ionic liquid is present in an amount of 0.05 wt % to 40 wt % of the micro-emulsion. A product mixture comprising a product is produced in a process zone containing the micro-emulsion.