A process for processing plastic waste comprising converting plastic waste to hydrocarbon liquid and a first C.sub.1-4 gas; contacting hydrocarbon liquid with a first hydroprocessing catalyst in hydroprocessing unit to yield a second C.sub.1-4 gas and a first hydrocarbon product comprising C.sub.5+ liquid hydrocarbons; introducing the first hydrocarbon product to a first separating unit to produce treated hydrocarbon stream comprising C.sub.5-8 hydrocarbons and a first heavies stream comprising C9+ hydrocarbons; contacting the first heavies stream with a second hydroprocessing catalyst in hydrodealkylating unit to yield a second hydrocarbon product comprising C.sub.5+ liquid hydrocarbons and a third C.sub.1-4 gas; conveying the second hydrocarbon product to the first separating unit; feeding treated hydrocarbon stream to steam cracker to produce steam cracker product; separating steam cracker product into olefin gas, saturated hydrocarbons gas, aromatics, and a second heavies stream; and conveying the second heavies stream to hydroprocessing unit.

Provided here are systems and methods that integrate a hydrodearylation process and a transalkylation process into an aromatic recovery complex. Various other embodiments may be disclosed and claimed.

The invention relates to a process for producing benzene comprising the steps of: (a) providing a hydrocracking feed stream comprising C.sub.5-C.sub.12 hydrocarbons, (b) contacting the hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst under process conditions including a temperature of 425-580 C., a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 3-30 h.sup.1 to produce a hydrocracking product stream comprising BTX and (c) separating the BTX from the hydrocracking product stream, wherein the hydrocracking catalyst comprises a shaped body comprising a zeolite and a binder and a hydrogenation metal deposited on the shaped body, wherein the amount of the hydrogenation metal is 0.010-0.30 wt-% with respect to the total catalyst and wherein the zeolite is ZSM-5 having a silica (SiO.sub.2) to alumina (Al.sub.2O.sub.3) molar ratio of 25-75.

Embodiments include processes and systems for maximizing the production of benzene and para-xylene from heavy reformate. Embodiments include a C9 dealkylation reactor, a transalkylation reactor, and a C10+ dealkylation reactor. The process and system for producing benzene and para-xylene may be configured to additionally produce alkanes in the presence of hydrogen or olefins in the absence of hydrogen. Embodiments may include an aromatic extraction unit to separate non-aromatics from aromatics.

Embodiments include processes and systems for maximizing the production of benzene and para-xylene from heavy reformate. Embodiments include a C9 dealkylation reactor, a transalkylation reactor, and a C10+ dealkylation reactor. The process and system for producing benzene and para-xylene may be configured to additionally produce alkanes in the presence of hydrogen or olefins in the absence of hydrogen. Embodiments may include an aromatic extraction unit to separate non-aromatics from aromatics.

A process for producing xylene from C.sub.9+ aromatic hydrocarbons comprises contacting a first feedstock comprising C.sub.9+ aromatic hydrocarbons with a first catalyst in the presence of 0 wt. % or more of hydrogen under effective vapor phase dealkylation conditions to dealkylate part of the C.sub.9+ aromatic hydrocarbons and produce a first product comprising benzene, toluene and residual C.sub.9+ aromatic hydrocarbons. A second feedstock comprising C.sub.9+ aromatic hydrocarbons and benzene and/or toluene is contacted with a second catalyst under effective liquid phase C.sub.9+ transalkylation conditions to transalkylate at least part of the C.sub.9+ aromatic hydrocarbons and produce a second product comprising xylenes.

A process for producing xylene from C.sub.9+ aromatic hydrocarbons comprises contacting a first feedstock comprising C.sub.9+ aromatic hydrocarbons with a first catalyst in the presence of 0 wt. % or more of hydrogen under effective vapor phase dealkylation conditions to dealkylate part of the C.sub.9+ aromatic hydrocarbons and produce a first product comprising benzene, toluene and residual C.sub.9+ aromatic hydrocarbons. A second feedstock comprising C.sub.9+ aromatic hydrocarbons and benzene and/or toluene is contacted with a second catalyst under effective liquid phase C.sub.9+ transalkylation conditions to transalkylate at least part of the C.sub.9+ aromatic hydrocarbons and produce a second product comprising xylenes.

An integrated process for forming a combined feedstock stream comprising catalytically cracking a first hydrocarbon feedstock to form a full range cracked full naphtha stream and a first light olefins stream, steam cracking a second hydrocarbon feedstock to form a pyrolysis gasoline stream and a second light olefins stream mixing at least a portion of each of the full range cracked naphtha stream and the pyrolysis gasoline stream to form a combined stream, hydro-processing the combined stream to form a hydro-processed combined stream splitting the hydro-processed combined stream into a C.sub.5/C.sub.6 stream, and a first aromatic rich stream, splitting the first aromatic rich stream into a second aromatic rich stream and a heavy oil stream.

An integrated process for forming a combined feedstock stream comprising catalytically cracking a first hydrocarbon feedstock to form a full range cracked full naphtha stream and a first light olefins stream, steam cracking a second hydrocarbon feedstock to form a pyrolysis gasoline stream and a second light olefins stream mixing at least a portion of each of the full range cracked naphtha stream and the pyrolysis gasoline stream to form a combined stream, hydro-processing the combined stream to form a hydro-processed combined stream splitting the hydro-processed combined stream into a C.sub.5/C.sub.6 stream, and a first aromatic rich stream, splitting the first aromatic rich stream into a second aromatic rich stream and a heavy oil stream.

Toluene disproportionation and C9/C10 transalkylation are a significant source of xylenes in a modern aromatics complex. Methods and apparatuses for improving the energy efficiency of these disproportionation and transalkylation processes are provided.