Alkyl-demethylation of C2+-hydrocarbyl substituted aromatic hydrocarbons can be utilized to treat one or more of a heavy naphtha reformate stream, a hydrotreated SCN stream, a C8 aromatic hydrocarbon isomerization feed stream, a C9+ aromatic hydrocarbon transalkylation feed stream, and similar hydrocarbon streams to produce additional quantity of xylene products.

Catalyst compositions comprising an inorganic porous material with pore diameters of at least 2 nm and of crystals of molecular sieve, characterized in that the crystals of molecular sieve have an average diameter, measured by scanning electron microscopy, not bigger than 50 nm, and in that the catalyst composition presents a concentration of acid sites ranges from 50 to 1200 mol/g measured by TPD NH3 adsorption; and the XRD pattern of said catalyst composition is the same as the X ray diffraction pattern of said inorganic porous material.

Catalyst compositions comprising an inorganic porous material with pore diameters of at least 2 nm and of crystals of molecular sieve, characterized in that the crystals of molecular sieve have an average diameter, measured by scanning electron microscopy, not bigger than 50 nm, and in that the catalyst composition presents a concentration of acid sites ranges from 50 to 1200 mol/g measured by TPD NH3 adsorption; and the XRD pattern of said catalyst composition is the same as the X ray diffraction pattern of said inorganic porous material.

The present disclosure relates to a method and an apparatus for decomposing a phenolic by-product generated in a bisphenol A preparation process, the method including: a step (S10) of feeding the phenolic by-product to a multistage reactive distillation column; a step (S20) of separating the phenolic by-product into an upper discharge stream containing an active component, a side discharge stream containing acetophenone, and a bottom discharge stream containing tar by the multistage reactive distillation column; and a step (S30) of mixing the side discharge stream discharged from the multistage reactive distillation column and the bottom discharge stream discharged from the multistage reactive distillation column to form a mixed discharge stream.

The present disclosure relates to a method and an apparatus for decomposing a phenolic by-product generated in a bisphenol A preparation process, the method including: a step (S10) of feeding the phenolic by-product to a multistage reactive distillation column; a step (S20) of separating the phenolic by-product into an upper discharge stream containing an active component, a side discharge stream containing acetophenone, and a bottom discharge stream containing tar by the multistage reactive distillation column; and a step (S30) of mixing the side discharge stream discharged from the multistage reactive distillation column and the bottom discharge stream discharged from the multistage reactive distillation column to form a mixed discharge stream.

The present disclosure relates to a process for producing a mono-alkylated aromatic compound, such as, for example, ethylbenzene or cumene, in which an alkylatable aromatic compound stream, such as, for example, benzene, and an alkylation agent stream, such as, for example, poly-ethylbenzene or poly-isopropylbenzene, are contacted in the presence of a transalkylation catalyst and under at least partial liquid phase transalkylation conditions. The transalkylation catalyst comprises a zeolite having a framework structure selected from the group consisting of FAU, BEA*, MOR, MWW and mixtures thereof. The zeolite has a silica-alumina molar ratio in a range of 10 to 15. The transalkylation catalyst composition has an external surface area/volume ratio in the range of 30 cm.sup.1 to 85 cm.sup.1.

The present disclosure relates to a process for producing a mono-alkylated aromatic compound, such as, for example, ethylbenzene or cumene, in which an alkylatable aromatic compound stream, such as, for example, benzene, and an alkylation agent stream, such as, for example, poly-ethylbenzene or poly-isopropylbenzene, are contacted in the presence of a transalkylation catalyst and under at least partial liquid phase transalkylation conditions. The transalkylation catalyst comprises a zeolite having a framework structure selected from the group consisting of FAU, BEA*, MOR, MWW and mixtures thereof. The zeolite has a silica-alumina molar ratio in a range of 10 to 15. The transalkylation catalyst composition has an external surface area/volume ratio in the range of 30 cm.sup.1 to 85 cm.sup.1.

A process for producing cumene comprising converting plastics to hydrocarbon liquid and pyrolysis gas; feeding hydrocarbon liquid to hydroprocessor to yield hydrocarbon product and first gas stream; feeding hydrocarbon product to reforming unit to produce reforming product, second gas stream, and hydrogen; separating reforming product into non-aromatics recycle stream and second aromatics stream (C.sub.6+ aromatics); recycling non-aromatics recycle stream to reforming unit; separating second aromatics stream into benzene, C.sub.7, C.sub.8, C.sub.9, C.sub.10, and C.sub.11+ aromatics; contacting C.sub.7, C.sub.9, and/or C.sub.10 aromatics with a disproportionation&transalkylation catalyst/H2 to yield benzene&xylenes; conveying C.sub.11+ aromatics to hydroprocessor; introducing pyrolysis gas, first and/or second gas stream to first separator to produce first propylene stream, first C.sub.2&C.sub.4 unsaturated stream, and saturated gas (H.sub.2 and C.sub.1-4 saturated hydrocarbons); introducing first C.sub.2&C.sub.4 unsaturated stream to metathesis reactor to produce second propylene stream; and feeding benzene, and first and/or second propylene stream to alkylation unit to produce cumene.

A process for producing cumene comprising converting plastics to hydrocarbon liquid and pyrolysis gas; feeding hydrocarbon liquid to hydroprocessor to yield hydrocarbon product and first gas stream; feeding hydrocarbon product to reforming unit to produce reforming product, second gas stream, and hydrogen; separating reforming product into non-aromatics recycle stream and second aromatics stream (C.sub.6+ aromatics); recycling non-aromatics recycle stream to reforming unit; separating second aromatics stream into benzene, C.sub.7, C.sub.8, C.sub.9, C.sub.10, and C.sub.11+ aromatics; contacting C.sub.7, C.sub.9, and/or C.sub.10 aromatics with a disproportionation&transalkylation catalyst/H2 to yield benzene&xylenes; conveying C.sub.11+ aromatics to hydroprocessor; introducing pyrolysis gas, first and/or second gas stream to first separator to produce first propylene stream, first C.sub.2&C.sub.4 unsaturated stream, and saturated gas (H.sub.2 and C.sub.1-4 saturated hydrocarbons); introducing first C.sub.2&C.sub.4 unsaturated stream to metathesis reactor to produce second propylene stream; and feeding benzene, and first and/or second propylene stream to alkylation unit to produce cumene.

Catalyst compositions comprising a zeolite and a mesoporous support or binder are disclosed. The mesoporous support or binder comprises a mesoporous metal oxide having a particle diameter of greater than or equal to 20 m at 50% of the cumulative pore size distribution (d50). Also disclosed are processes for producing a mono-alkylated aromatic compound (e.g., ethylbenzene or cumene) which exhibit improved yield of the mono-alkylated aromatic compound using alkylation catalysts comprising one or more of these catalyst compositions.