Abstract: Hydrodeoxygenating a biorenewable feed that is concentrated in free fatty acids with 10-13 carbon atoms at a moderate hydrodeoxygenation ratio that is less than the ratio of hydrodeoxygenation utilized for traditional biorenewable feeds such as vegetable oil or even mineral feedstocks, normal paraffins in the range desired by the detergents industry can be produced. Either hydroisomerization or an iso-normal separation can be performed to provide green fuel streams. Two reactors are proposed, one for hydrodeoxygenation of the biorenewable feed that is concentrated in free fatty acids with 10-13 carbon atoms and the other for a traditional biorenewable feed or even a mineral feed operated at a higher deoxygenation ratio.

Abstract: Hydrodeoxygenating a biorenewable feed that is concentrated in free fatty acids with 10-13 carbon atoms at a moderate hydrodeoxygenation ratio that is less than the ratio of hydrodeoxygenation utilized for traditional biorenewable feeds such as vegetable oil or even mineral feedstocks, normal paraffins in the range desired by the detergents industry can be produced. Either hydroisomerization or an iso-normal separation can be performed to provide green fuel streams. Two reactors are proposed, one for hydrodeoxygenation of the biorenewable feed that is concentrated in free fatty acids with 10-13 carbon atoms and the other for a traditional biorenewable feed or even a mineral feed operated at a higher deoxygenation ratio.

Abstract: A process for hydrotreating a renewable feedstock with improved carbon monoxide management is disclosed. A mixture of renewable feedstock and hydrocarbon feedstock is treated in a hydrotreating reactor to produce a hydrotreated effluent stream and contacting the hydrotreated effluent stream with a water gas shift catalyst bed to produce a shift reactor effluent stream. The shift reactor effluent stream is passed to a cold separator to recover a cold vapor stream and recycling the cold vapor stream having reduced concentration of carbon monoxide to the hydrotreating zone. The subject matter disclosed provides an improved process and apparatus to reduce the accumulation of CO by converting CO present in the hydrotreated effluent stream to CO2 using the water shift gas reaction.

Abstract: Processes for co-processing a naphtha stream with a light cycle oil stream are disclosed. The processes include hydrocracking the light cycle oil stream under hydrocracking conditions to provide a hydrocracked effluent stream. A naphtha stream is hydrotreated under hydrotreating conditions to provide a hydrotreated effluent stream. The hydrocracked effluent stream and the hydrotreated effluent stream may be passed to a stripping column to recover a stripping bottom stream. The stripping bottom stream may be passed to a main fractionation column to recover an intermediate naphtha stream.

Abstract: Processes for co-processing a naphtha stream with a light cycle oil stream are disclosed. The processes include hydrocracking the light cycle oil stream under hydrocracking conditions to provide a hydrocracked effluent stream. A naphtha stream is hydrotreated under hydrotreating conditions to provide a hydrotreated effluent stream. The hydrocracked effluent stream and the hydrotreated effluent stream may be passed to a stripping column to recover a stripping bottom stream. The stripping bottom stream may be passed to a main fractionation column to recover an intermediate naphtha stream.

Abstract: Processes and apparatus for maximizing production of heavy naphtha from a hydrocarbon stream are provided. The process comprises providing a hydrocarbon feed stream comprising vacuum gas oil to a first hydrocracking reactor. The hydrocarbon feed stream is hydrocracked at first hydrocracking conditions comprising a first hydrocracking pressure to provide a first hydrocracked effluent stream therein. At least a portion of the first hydrocracked effluent stream is fractionated in a fractionation column to provide a heavy naphtha fraction. A kerosene stream is hydrocracked in a second hydrocracking reactor operating at second hydrocracking conditions comprising a second hydrocracking pressure to provide a second hydrocracked effluent stream. In an aspect, the first hydrocracking pressure can be greater than the second hydrocracking pressure by at least about 6895 kPa (g).

Abstract: The present invention discloses a process and apparatus for selectively hydrogenating diolefins in a cracked stream. The method combines a conversion unit and a recovery section. The recovery section includes the diolefin hydrogenation reactor that is used to selectively hydrogenate the diolefins in the cracked naphtha. The diolefin depleted naphtha may be debutanized to separate the stabilized naphtha and liquefied petroleum gas streams.

Abstract: A process for reducing the sulfur content of FCC naphtha is described. The process includes introducing a FCC naphtha feed to a selective hydrogenation zone to form a hydrogenated feed. The hydrogenated feed is separated into light fraction and a heavy fraction. The heavy fraction is introduced into a selective hydrodesulfurization zone to form a desulfurized stream which contains mercaptans. The desulfurized stream is separated into a mercaptan rich stream and a mercaptan lean stream. The mercaptan rich stream is treated with a caustic extraction process, a hydrodesulfurization reaction zone, a selective hydrogenation process, an adsorption process, or an ionic liquid extraction process to remove at least a portion of the mercaptan compounds to form a second mercaptan lean stream.

Abstract: The present invention discloses a process and apparatus for selectively hydrogenating diolefins in a cracked stream. The method combines a conversion unit and a recovery section. The recovery section includes the diolefin hydrogenation reactor that is used to selectively hydrogenate the diolefins in the cracked naphtha. The diolefin depleted naphtha may be debutanized to separate the stabilized naphtha and liquefied petroleum gas streams.