A method of forming C.sub.6-C.sub.8 aromatics may include selectively dealkylating a Fluid Catalytic Cracking (FCC) heavy cut naphtha that has at least C.sub.9+ aromatics to selectively crack C.sub.2+ alkyl chains from the C.sub.9+ aromatics, thereby forming the C.sub.6-C.sub.8 aromatics. The selectively de-alkylated heavy cut naphtha is then combined with a FCC middle cut naphtha, and aromatics including the C.sub.6-C.sub.8 aromatics are separated from the combined stream. A system for forming C.sub.6-C.sub.8 aromatics may include a fluid catalytic cracking unit for producing a FCC heavy cut naphtha comprising at least C.sub.9+ aromatics; a de-alkylation reactor for selectively cracking C.sub.2+ alkyl chains from the C.sub.9+ aromatics, thereby forming the C.sub.6-C.sub.8 aromatics; and an aromatic extraction unit for extracting at least a portion of the C.sub.6-C.sub.8 aromatics.

A method of forming C.sub.6-C.sub.8 aromatics may include selectively dealkylating a Fluid Catalytic Cracking (FCC) heavy cut naphtha that has at least C.sub.9+ aromatics to selectively crack C.sub.2+ alkyl chains from the C.sub.9+ aromatics, thereby forming the C.sub.6-C.sub.8 aromatics. The selectively de-alkylated heavy cut naphtha is then combined with a FCC middle cut naphtha, and aromatics including the C.sub.6-C.sub.8 aromatics are separated from the combined stream. A system for forming C.sub.6-C.sub.8 aromatics may include a fluid catalytic cracking unit for producing a FCC heavy cut naphtha comprising at least C.sub.9+ aromatics; a de-alkylation reactor for selectively cracking C.sub.2+ alkyl chains from the C.sub.9+ aromatics, thereby forming the C.sub.6-C.sub.8 aromatics; and an aromatic extraction unit for extracting at least a portion of the C.sub.6-C.sub.8 aromatics.

A process for the treatment of a light naphtha feedstock that comprises normal paraffins and iso-paraffins may include separating the feedstock into a first iso-paraffin stream and a normal paraffin stream. The separating may be performed with 5A molecular sieves, a pressure of about 1-3 bars, and a temperature of 100-260° C. A product stream may be provided by subjecting the normal paraffin stream to at least one of steam cracking, isomerizing, and aromatizing.

A process for producing benzene and xylenes comprising introducing hydrocarbon liquid stream to hydroprocessor to yield first gas stream and hydrocarbon product (C.sub.5+); optionally introducing hydrocarbon product to first aromatics separating unit to produce saturated hydrocarbons (C.sub.5+) and first aromatics stream (C.sub.6+); feeding hydrocarbon product and/or saturated hydrocarbons to reformer to produce reformer product, second gas stream, and hydrogen stream; introducing reformer product to second aromatics separating unit to produce a non-aromatics recycle stream and second aromatics stream comprising C.sub.6+ aromatics; recycling non-aromatics recycle stream to reformer; introducing first aromatics stream and/or second aromatics stream to third aromatics separating unit to produce first C.sub.6 aromatics (benzene), C.sub.7 aromatics (toluene), C.sub.8 aromatics (xylenes&ethylbenzene), C.sub.9 aromatics, C.sub.10 aromatics, and C.sub.11+ aromatics; introducing C.sub.7 aromatics, C.sub.9 aromatics, C.sub.10 aromatics, or combinations thereof to disproportionation and transalkylation unit to yield third aromatics stream (benzene and xylenes); and conveying C.sub.11+ aromatics to hydroprocessor.

Systems and methods include an aromatics complex (ARC), the ARC in fluid communication with a naphtha reforming unit (NREF) and operable to receive a reformate stream produced by the NREF, and the ARC further operable to separate the reformate stream into a gasoline pool stream, an aromatics stream, and an aromatic bottoms stream; and a hydrodearylation unit operable to receive heavy, non-condensed, alkyl-bridged, multi-aromatic compounds from the aromatic bottoms stream, the hydrodearylation unit further operable to hydrogenate and hydrocrack the heavy, non-condensed, alkyl-bridged, multi-aromatic compounds to produce a stream suitable for recycle to the NREF or the reformate stream, where the hydrodearylation unit is further operable to receive hydrogen produced in the NREF.

The present disclosure relates to processes that catalytically convert a hydrocarbon feed stream predominantly comprising both isopentane and n-pentane to yield upgraded hydrocarbon products that are suitable for use either as a blend component of liquid transportation fuels or as an intermediate in the production of other value-added chemicals. The hydrocarbon feed stream is isomerized in a first reaction zone to convert at least a portion of the n-pentane to isopentane, followed by catalytic-activation of the isomerization effluent in a second reaction zone with an activation catalyst to produce an activation effluent. The process increases the conversion of the hydrocarbon feed stream to olefins and aromatics, while minimizing the production of C1-C4 light paraffins. Certain embodiments provide for further upgrading of at least a portion of the activation effluent by either oligomerization or alkylation.

The present disclosure relates to processes that catalytically convert a hydrocarbon feed stream predominantly comprising both isopentane and n-pentane to yield upgraded hydrocarbon products that are suitable for use either as a blend component of liquid transportation fuels or as an intermediate in the production of other value-added chemicals. The hydrocarbon feed stream is isomerized in a first reaction zone to convert at least a portion of the n-pentane to isopentane, followed by catalytic-activation of the isomerization effluent in a second reaction zone with an activation catalyst to produce an activation effluent. The process increases the conversion of the hydrocarbon feed stream to olefins and aromatics, while minimizing the production of C1-C4 light paraffins. Certain embodiments provide for further upgrading of at least a portion of the activation effluent by either oligomerization or alkylation.

A process for treatment of PFO from a steam cracking zone includes hydrodealkylating PFO or a portion thereof for conversion of polyaromatics compounds contained in the PFO into hydrodealkylated aromatic compounds with one benzene ring, a hydrodealkylated BTX+ stream. In addition, a naphtha reformer is integrated, so that the hydrodealkylated BTX+ stream and a reformate stream are separated into BTX compounds.

A process for treatment of PFO from a steam cracking zone includes selectively hydrogenating PFO or a portion thereof for conversion of polyaromatics compounds contained in the PFO into aromatic compounds with one benzene ring to produce a selectively hydrogenated stream. The selectively hydrogenated stream is reacted in a fluid catalytic cracking reactor for selective ring opening and dealkylation to produce fluid catalytic cracking including light cycle oil. In addition, a naphtha reformer is integrated, so that light cycle oil and a reformate stream are separated into BTX compounds. Optionally the PFO is separated into a first stream containing C9+ aromatics compounds with one benzene ring, and a second stream containing C10+ aromatic compounds, whereby the first stream containing C9+ aromatics compounds with one benzene ring is passed to the fluid catalytic cracking reactor, and the feed to the selective hydrogenation step comprises all or a portion of the second stream containing C10+ aromatic compounds.

A process for treatment of PFO from a steam cracking zone includes selectively hydrogenating PFO or a portion thereof for conversion of polyaromatics compounds contained in the PFO into aromatic compounds with one benzene ring to produce a selectively hydrogenated stream. The selectively hydrogenated stream is selectively hydrocracked for selective ring opening and dealkylation to produce a selectively hydrocracked BTX+ stream. In addition, a naphtha reformer is integrated, so that the selectively hydrocracked BTX+ stream and a reformate stream are separated into BTX compounds. Optionally the PFO is separated into a first stream containing C9+ aromatics compounds with one benzene ring, and a second stream containing C10+ aromatic compounds, whereby the first stream containing C9+ aromatics compounds with one benzene ring is passed to the selective hydrocracking step, and the feed to the selective hydrogenation step comprises all or a portion of the second stream containing C10+ aromatic compounds.