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 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: 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.