Abstract: The invention relates to renewable hydrocarbons, and more particularly to biomass-based diesel fuel produced in a process including hydrodeoxygenation (HDO) of phenolic lipids. The process may generally include combining a phenolic lipid and a hydrocarbon diluent to provide a hydrocarbon-diluted phenolic lipid then subjecting the hydrocarbon-diluted phenolic lipid to hydrodeoxygenation in a reactor to provide a reactor effluent including a hydrodeoxygenated phenolic lipid. The hydrodeoxygenated phenolic lipid is separated from the reactor effluent.

Abstract: Methods that increase production of a liquid transportation fuel blend component by utilizing C5 hydrocarbon streams taken from both a refinery naphtha stream and an NGL fractionator pentanes plus stream. A high vapor pressure pentane fraction from the NGL fractionator is separated to remove isopentane and produce lower vapor pressure commodity natural gasoline. A refinery naphtha stream (that is optionally an FCC naphtha stream) is separated to produce a C5 olefins stream that is then oligomerized to produce an upgraded stream having lower vapor pressure and higher octane rating, then combined with the remainder of the naphtha stream as well as the isopentane stream to produce a gasoline blend component that meets specifications for vapor pressure and octane rating.

Abstract: The invention relates to renewable hydrocarbons, and more particularly to biomass-based diesel fuel produced in a process including hydrodeoxygenation (HDO) of phenolic lipids. The process may generally include combining a phenolic lipid and a hydrocarbon diluent to provide a hydrocarbon-diluted phenolic lipid then subjecting the hydrocarbon-diluted phenolic lipid to hydrodeoxygenation in a reactor to provide a reactor effluent including a hydrodeoxygenated phenolic lipid. The hydrodeoxygenated phenolic lipid is separated from the reactor effluent.

Abstract: The disclosed process relates to removal of benzene from a reformate stream and in turn providing gasoline and diesel products along with commodity chemicals (such as cyclohexylbenzene). The disclosed process further relates to the upgrading of heart-cut reformate benzene to higher value products.

Abstract: Methods that increase production of a liquid transportation fuel blend component by utilizing C5 hydrocarbon streams taken from both a refinery naphtha stream and an NGL fractionator pentanes plus stream. A high vapor pressure pentane fraction from the NGL fractionator is separated to remove isopentane and produce lower vapor pressure commodity natural gasoline. A refinery naphtha stream (that is optionally an FCC naphtha stream) is separated to produce a C5 olefins stream that is then oligomerized to produce an upgraded stream having lower vapor pressure and higher octane rating, then combined with the remainder of the naphtha stream as well as the isopentane stream to produce a gasoline blend component that meets specifications for vapor pressure and octane rating.

Abstract: A process and system for the conversion of a feedstock comprising C3-C5 light alkanes to a C5+ hydrocarbon product, for example, a BTX-rich hydrocarbon product, by performing the alkane activation (first-stage) and the oligomerization/aromatization (second-stage) in separate stages, which allows each conversion process to occur at optimal reaction conditions thus increasing the overall hydrocarbon product yield. The alkane activation or first-stage is operated at a higher temperature than the second-stage since light alkanes are much less reactive than light olefins. Since aromatization of olefins is more efficient at higher pressure, the second-stage is maintained at a higher pressure than the first-stage. Further, fixed-bed catalysts are used in each of the first-stage and the second-stage.

Abstract: A process and system for the conversion of a feedstock comprising C3-C5 light alkanes to a C5+ hydrocarbon product, for example, a BTX-rich hydrocarbon product, by performing the alkane activation (first-stage) and the oligomerization/aromatization (second-stage) in separate stages, which allows each conversion process to occur at optimal reaction conditions thus increasing the overall hydrocarbon product yield. The alkane activation or first-stage is operated at a higher temperature than the second-stage since light alkanes are much less reactive than light olefins. Since aromatization of olefins is more efficient at higher pressure, the second-stage is maintained at a higher pressure than the first-stage. Further, fixed-bed catalysts are used in each of the first-stage and the second-stage.

Abstract: Processes relating to thermal activation (or cracking) of ethane to an intermediate, low purity raw ethylene stream in a first stage. This stream is then mixed with a stream of biomass-derived ethanol that may contain four volume percent or more of water. The resulting mixture is reacted over a suitable catalyst at temperatures and pressures suitable to produce gasoline-range and diesel-range blend stock.

Abstract: A process for converting ethane to liquid fuels may involve directing an ethane stream into an ethane cracking unit to produce an intermediate hydrocarbon stream and a raw ethylene stream; fractionating the intermediate hydrocarbon stream into a gasoline fraction and a diesel fraction; introducing the raw ethylene stream into an oligomerization unit; contacting the raw ethylene stream with an oligomerization catalyst to produce a liquid hydrocarbon stream and an off-gas stream; recycling an off-gas recycle stream from an off-gas stream of the oligomerization unit separation unit to an inlet of the oligomerization reactor; introducing at least part of the off-gas stream into a hydrogenation reactor to remove unconverted olefins; separating a hydrogen component and a plurality of light paraffin components in a post hydrogenation reactor separation unit using a PSA technology or membrane technology; and recycling the light paraffins stream into the ethane cracking unit.

Abstract: Converting ethane may include directing a gaseous stream from a gas well into a fractionator for fractionating and producing a post-fractionator ethane stream, which is directed into a thermal activation unit for heating and raising the temperature of the post-fractionator ethane stream thereby creating an activated ethane stream, which is directed into a quench tower thereby creating a quenched stream, which may be converted in a catalytic conversion unit to a mixed product stream containing hydrogen and C1-C15 hydrocarbons; directing the mixed product stream into a first separation unit forming a stream of C4+ hydrocarbon product and a stream of C1-C3 hydrocarbons; directing the stream of C1-C3 hydrocarbons into a catalytic hydrogenation reactor thereby imparting hydrogen into a post-hydrogenation reactor stream, which is directed directly into a second separation unit thereby creating a light hydrocarbons recycle stream, which may be recycled into the thermal activation unit, and a hydrogen and methane str

Abstract: Systems relating to thermal activation (or cracking) of ethane to an intermediate, low purity raw ethylene stream in a first stage. The system then mixes this stream with a stream of raw biomass-derived ethanol that may contain more than four volume percent of water. The resulting mixture is reacted over a suitable catalyst at temperatures and pressures suitable to produce gasoline-range and diesel-range blend stock.

Abstract: A process for converting ethane to liquid fuels may involve directing an ethane stream into an ethane cracking unit to produce an intermediate hydrocarbon stream and a raw ethylene stream; fractionating the intermediate hydrocarbon stream into a gasoline fraction and a diesel fraction; introducing the raw ethylene stream into an oligomerization unit; contacting the raw ethylene stream with an oligomerization catalyst to produce a liquid hydrocarbon stream and an off-gas stream; recycling an off-gas recycle stream from an off-gas stream of the oligomerization unit separation unit to an inlet of the oligomerization reactor; introducing at least part of the off-gas stream into a hydrogenation reactor to remove unconverted olefins; separating a hydrogen component and a plurality of light paraffin components in a post hydrogenation reactor separation unit using a PSA technology or membrane technology; and recycling the light paraffins stream into the ethane cracking unit.

Abstract: Systems relating to thermal activation (or cracking) of ethane to an intermediate, low purity raw ethylene stream in a first stage. The system then mixes this stream with a stream of raw biomass-derived ethanol that may contain more than four volume percent of water. The resulting mixture is reacted over a suitable catalyst at temperatures and pressures suitable to produce gasoline-range and diesel-range blend stock.

Abstract: Converting ethane may include directing a gaseous stream from a gas well into a fractionator for fractionating and producing a post-fractionator ethane stream, which is directed into a thermal activation unit for heating and raising the temperature of the post-fractionator ethane stream thereby creating an activated ethane stream, which is directed into a quench tower thereby creating a quenched stream, which may be converted in a catalytic conversion unit to a mixed product stream containing hydrogen and C1-C15 hydrocarbons; directing the mixed product stream into a first separation unit forming a stream of C4+ hydrocarbon product and a stream of C1-C3 hydrocarbons; directing the stream of C1-C3 hydrocarbons into a catalytic hydrogenation reactor thereby imparting hydrogen into a post-hydrogenation reactor stream, which is directed directly into a second separation unit thereby creating a light hydrocarbons recycle stream, which may be recycled into the thermal activation unit, and a hydrogen and methane str

Abstract: Processes relating to thermal activation (or cracking) of ethane to an intermediate, low purity raw ethylene stream in a first stage. This stream is then mixed with a stream of biomass-derived ethanol that may contain four volume percent or more of water. The resulting mixture is reacted over a suitable catalyst at temperatures and pressures suitable to produce gasoline-range and diesel-range blend stock.

Abstract: Processes for the conversion of hydrocarbons boiling in the temperature range of from about 80° F. to about 1000° F. to diesel boiling range hydrocarbons, and processes for increasing the cetane number and amount of n-C17 hydrocarbon products in such processes. Diesel boiling range hydrocarbons may be produced by contacting a hydrocarbon boiling in the above-mentioned boiling range with a triglyceride-containing compound to form a mixture, and then contacting the mixture with a hydrotreating catalyst under suitable reaction conditions.

Abstract: Processes for the conversion of carbohydrates to gasoline boiling range hydrocarbons, and processes for increasing the solubility of carbohydrates used in such processes are disclosed. The solubility of carbohydrates may be increased by contacting the carbohydrate with an ion-exchange resin. The dissolved product may be hydrogenated and reacted in the present of a catalyst to form a reaction product containing non-aromatic and aromatic gasoline boiling range hydrocarbons.