Abstract: Methods, apparatuses, and systems for the conversion of bioalcohol to renewable diesel fuel are disclosed.

Abstract: Methods, apparatuses, and systems for the conversion of bioethanol to renewable jet fuel are disclosed. In an example embodiment, a method for converting bioethanol to renewable jet fuel includes providing an olefin process stream comprising olefins to a hydrogenation reaction zone, converting at least a portion of the olefin process stream to a product stream comprising jet-range compatible hydrocarbons, determining, in the hydrogenation reaction zone, an iso-to-normal ratio of a portion of the product stream via one or more online analyzers, in an instance wherein the determined iso-to-normal ratio fails to satisfy a predetermined iso-to-normal threshold ratio, determine at least one additive and an amount of the at least one additive to be added to the product stream, the at least one additive configured to adjust a freeze point of the product stream, and adding the at least one additive to the product stream prior to the product stream exiting the hydrogenation reaction zone.

Abstract: Methods, apparatuses, and systems for the conversion of bioethanol to renewable jet fuel are disclosed. In an example embodiment, a method for converting bioethanol to renewable jet fuel includes providing an olefin process stream comprising olefins to a hydrogenation reaction zone, converting at least a portion of the olefin process stream to a product stream comprising jet-range compatible hydrocarbons, determining, in the hydrogenation reaction zone, an iso-to-normal ratio of a portion of the product stream via one or more online analyzers, in an instance wherein the determined iso-to-normal ratio fails to satisfy a predetermined iso-to-normal threshold ratio, determine at least one additive and an amount of the at least one additive to be added to the product stream, the at least one additive configured to adjust a freeze point of the product stream, and adding the at least one additive to the product stream prior to the product stream exiting the hydrogenation reaction zone.

Abstract: A process for hydroprocessing a biorenewable feedstock is disclosed. The process comprises hydrotreating the biorenewable feed stream in a hydrotreating reactor to hydrodeoxygenate the biorenewable feed stream to provide a hydrotreated stream. A hydrocracking feed stream taken from the hydrotreated stream is hydrocracked in a hydrocracking reactor to provide a hydrocracked stream. A hydroisomerization feed stream taken from the hydrotreated stream is hydroisomerized in a hydroisomerization reactor to provide a hydroisomerized stream. The hydroisomerized stream is separated to provide a jet fuel stream and a diesel stream. The diesel stream is separated into a first recycle diesel stream and a second recycle diesel stream. The first recycle diesel stream is passed to the hydrocracking reactor and the second recycle diesel stream is passed to the hydroisomerization reactor.

Abstract: A process for dimerizing and oligomerizing olefins to distillate fuels which subjects oligomerized product to hydrocracking and hydroisomerization in a single reactor to convert heavier oligomers to jet fuel range oligomers. A jet fuel product stream may be taken from a side of a stripping column which produces a heavy drag stream from a bottom of the stripping column to ensure an end point boiling specification is achieved.

Abstract: An integrated process for maximizing recovery of aromatics is provided. The process comprises passing at least a portion of a xylene column bottoms stream to a heavy aromatics column to provide a heavy aromatics column bottoms stream comprising C9+ aromatics and a heavy aromatics column overhead stream. The heavy aromatics column bottoms stream is passed to a second stage hydrocracking reactor of a two-stage hydrocracking reactor. In the second stage hydrocracking reactor, the heavy aromatics column bottoms stream is hydrocracked in the presence of a hydrocracking catalyst and hydrogen to provide a hydrocracked effluent stream.

Abstract: An integrated process for maximizing recovery of aromatics is provided. The process comprises passing at least a portion of a xylene column bottoms stream to a heavy aromatics column to provide a heavy aromatics column bottoms stream comprising C9+ aromatics and a heavy aromatics column overhead stream. The heavy aromatics column bottoms stream is passed to a second stage hydrocracking reactor of a two-stage hydrocracking reactor. In the second stage hydrocracking reactor, the heavy aromatics column bottoms stream is hydrocracked in the presence of a hydrocracking catalyst and hydrogen to provide a hydrocracked effluent stream.

Abstract: An integrated process for maximizing recovery of hydrogen is provided. The process comprises: providing a hydrocarbonaceous feed comprising naphtha, and a hydrogen stream to a reforming zone, wherein the hydrogen stream is obtained from at least one of a hydrocracking zone, a transalkylation zone, and an isomerization zone. The hydrocarbonaceous feed is reformed in the reforming zone in the presence of the hydrogen stream and a reforming catalyst to provide a reformate effluent stream. At least a portion of the reformate effluent stream is passed to a debutanizer column of the reforming zone to provide a net hydrogen stream and a fraction comprising liquid petroleum gas (LPG). At least a portion of the net hydrogen stream is recycled to the reforming zone as the hydrogen stream.

Abstract: An integrated process for maximizing recovery of LPG is provided. The process comprises providing a hydrocarbonaceous feed comprising naphtha, and a hydrogen stream to a reforming zone. The hydrocarbonaceous feed is reformed in the reforming zone in the presence of the hydrogen stream and a reforming catalyst to provide a reformate effluent stream. At least a portion of the reformate effluent stream and at least one stream comprising C6? hydrocarbons from one or more of a hydrocracking zone, an isomerization zone, and a transalkylation zone is passed to a debutanizer column of the reforming zone to provide a fraction comprising liquid petroleum gas (LPG) and a debutanizer column bottoms stream.

Abstract: An integrated process for maximizing recovery of hydrogen is provided. The process comprises: providing a hydrocarbonaceous feed comprising naphtha, and a hydrogen stream to a reforming zone, wherein the hydrogen stream is obtained from at least one of a hydrocracking zone, a transalkylation zone, and an isomerization zone. The hydrocarbonaceous feed is reformed in the reforming zone in the presence of the hydrogen stream and a reforming catalyst to provide a reformate effluent stream. At least a portion of the reformate effluent stream is passed to a debutanizer column of the reforming zone to provide a net hydrogen stream and a fraction comprising liquid petroleum gas (LPG). At least a portion of the net hydrogen stream is recycled to the reforming zone as the hydrogen stream.

Abstract: An integrated process for maximizing recovery of LPG is provided. The process comprises providing a hydrocarbonaceous feed comprising naphtha, and a hydrogen stream to a reforming zone. The hydrocarbonaceous feed is reformed in the reforming zone in the presence of the hydrogen stream and a reforming catalyst to provide a reformate effluent stream. At least a portion of the reformate effluent stream and at least one stream comprising C6? hydrocarbons from one or more of a hydrocracking zone, an isomerization zone, and a transalkylation zone is passed to a debutanizer column of the reforming zone to provide a fraction comprising liquid petroleum gas (LPG) and a debutanizer column bottoms stream.

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: A process for hydrotreating coker kerosene is described. Instead of a post treat reactor, a smaller trim reactor zone which operates at a lower pressure than the post treat reactor is used downstream of the product stripper. The trim reactor uses a noble metal catalyst to reduce the BI of the stripped product to less than about 150, and desirably in the range of about 50 to about 100.

Abstract: Embodiments of apparatuses and methods for treating a vacuum gas oil (VGO) hydrotreating feed are provided. In one example, a method comprises contacting the VGO hydrotreating feed with a first hydrotreating catalyst in the presence of hydrogen at first hydroprocessing conditions effective to form a first hydrotreated effluent. The first hydrotreated effluent is separated to form a hydrotreated VGO-containing stream and a hydrotreated diesel-containing stream. The hydrotreated VGO-containing stream is stripped and fractionated to form a VGO product stream. The hydrotreated diesel-containing stream is combined with a hydrotreated diesel-, naphtha-containing stream to form a combined stream. The combined stream is stripped to form a diesel product stream.

Abstract: A process for hydrotreating coker kerosene is described. Instead of a post treat reactor, a smaller trim reactor zone which operates at a lower pressure than the post treat reactor is used downstream of the product stripper. The trim reactor uses a noble metal catalyst to reduce the BI of the stripped product to less than about 150, and desirably in the range of about 50 to about 100.

Abstract: Embodiments of apparatuses and methods for treating a vacuum gas oil (VGO) hydrotreating feed are provided. In one example, a method comprises contacting the VGO hydrotreating feed with a first hydrotreating catalyst in the presence of hydrogen at first hydroprocessing conditions effective to form a first hydrotreated effluent. The first hydrotreated effluent is separated to form a hydrotreated VGO-containing stream and a hydrotreated diesel-containing stream. The hydrotreated VGO-containing stream is stripped and fractionated to form a VGO product stream. The hydrotreated diesel-containing stream is combined with a hydrotreated diesel-, naphtha-containing stream to form a combined stream. The combined stream is stripped to form a diesel product stream.

Abstract: A method for processing hydrocarbons includes providing a hydrocarbon stream including chlorides from one or more of a crude, vacuum or coker column and contacting the provided hydrocarbon stream with an adsorbent capable of adsorbing the chlorides from the hydrocarbon stream. The dechlorinated hydrocarbon stream is then provided to a hydrotreater reactor.