Disclosed herein is a method for converting cannabidiol (CBD) into a composition comprising Δ.sup.9-tetrahydrocannabinol (Δ.sup.9-THC) and Δ.sup.8-tetrahydrocannabinol (Δ.sup.8-THC) in which the composition has a Δ.sup.9-THC:Δ.sup.8-THC ratio of greater than 1.0:1.0. The method comprises contacting the CBD with a Lewis-acidic heterogeneous reagent under reaction conditions comprising: (i) an aprotic-solvent system; (ii) a reaction temperature that is less than a threshold reaction temperature for the Lewis-acidic heterogeneous reagent and the aprotic-solvent system; and (iii) a reaction time that is less than a threshold reaction time for the Lewis-acidic heterogeneous reagent, the aprotic-solvent system, and the reaction temperature. Methods for converting CBD into a composition comprising Δ.sup.9-THC and Δ.sup.8-THC in which the composition has a Δ.sup.9-THC:Δ.sup.8-THC ratio of greater than 1.0:1.0 under neat reaction conditions are also provided.

Disclosed herein is a method for converting cannabidiol (CBD) into a composition comprising Δ.sup.9-tetrahydrocannabinol (Δ.sup.9-THC) and Δ.sup.8-tetrahydrocannabinol (Δ.sup.8-THC) in which the composition has a Δ.sup.9-THC:Δ.sup.8-THC ratio of greater than 1.0:1.0. The method comprises contacting the CBD with a Lewis-acidic heterogeneous reagent under reaction conditions comprising: (i) an aprotic-solvent system; (ii) a reaction temperature that is less than a threshold reaction temperature for the Lewis-acidic heterogeneous reagent and the aprotic-solvent system; and (iii) a reaction time that is less than a threshold reaction time for the Lewis-acidic heterogeneous reagent, the aprotic-solvent system, and the reaction temperature. Methods for converting CBD into a composition comprising Δ.sup.9-THC and Δ.sup.8-THC in which the composition has a Δ.sup.9-THC:Δ.sup.8-THC ratio of greater than 1.0:1.0 under neat reaction conditions are also provided.

Disclosed are a bifunctional catalyst and a preparation method therefor, the bifunctional catalyst being suitable to produce high-value aromatic hydrocarbons by subjecting alkylaromatic hydrocarbons to a disproportionation/transalkylation/dealkylation reaction while suppressing aromatic loss or subjecting C8 aromatic hydrocarbons to an isomerization reaction while suppressing xylene loss.

Systems and methods are provided for conversion of methanol to gasoline in an integrated system that can also upgrade light paraffins generated by the methanol conversion process to aromatics. In some aspects, the integrated configuration can include integration of the stage for upgrading of light paraffins to aromatics into the product separation sequence for processing of the methanol conversion effluent. In other aspects, the integrated configuration can further include sharing a common catalyst between the methanol conversion stage and the stage for upgrading light paraffins to aromatics.

A process for producing olefins from the hydrocarbon feed includes introducing the hydrocarbon feed into a Solvent Deasphalting Unit (SDA) to remove asphaltene from the hydrocarbon feed producing a deasphalted oil stream, wherein the SDA comprises a solvent that reacts with the hydrocarbon feed, and the deasphalted oil stream comprises from 0.01 weight percent (wt. %) to 18 wt. % asphaltenes; introducing the deasphalted oil stream into a steam catalytic cracking system; steam catalytically cracking the deasphalted oil stream in the steam catalytic cracking system in the presence of steam and a nano zeolite cracking catalyst to produce a steam catalytic cracking effluent; and separating the olefins from the steam catalytic cracking effluent.

A process for producing olefins from the hydrocarbon feed includes introducing the hydrocarbon feed into a Solvent Deasphalting Unit (SDA) to remove asphaltene from the hydrocarbon feed producing a deasphalted oil stream, wherein the SDA comprises a solvent that reacts with the hydrocarbon feed, and the deasphalted oil stream comprises from 0.01 weight percent (wt. %) to 18 wt. % asphaltenes; introducing the deasphalted oil stream into a steam catalytic cracking system; steam catalytically cracking the deasphalted oil stream in the steam catalytic cracking system in the presence of steam and a nano zeolite cracking catalyst to produce a steam catalytic cracking effluent; and separating the olefins from the steam catalytic cracking effluent.

A process for producing olefins from the hydrocarbon feed includes introducing the hydrocarbon feed into a Solvent Deasphalting Unit (SDA) to remove asphaltene from the hydrocarbon feed producing a deasphalted oil stream, wherein the SDA comprises a solvent that reacts with the hydrocarbon feed, and the deasphalted oil stream comprises from 0.01 weight percent (wt. %) to 18 wt. % asphaltenes; introducing the deasphalted oil stream into a steam catalytic cracking system; steam catalytically cracking the deasphalted oil stream in the steam catalytic cracking system in the presence of steam and a nano zeolite cracking catalyst to produce a steam catalytic cracking effluent; and separating the olefins from the steam catalytic cracking effluent.

A process for producing olefins from the hydrocarbon feed includes introducing the hydrocarbon feed into a Solvent Deasphalting Unit (SDA) to remove asphaltene from the hydrocarbon feed producing a deasphalted oil stream, wherein the SDA comprises a solvent that reacts with the hydrocarbon feed, and the deasphalted oil stream comprises from 0.01 weight percent (wt. %) to 18 wt. % asphaltenes; introducing the deasphalted oil stream into a steam catalytic cracking system; steam catalytically cracking the deasphalted oil stream in the steam catalytic cracking system in the presence of steam and a nano zeolite cracking catalyst to produce a steam catalytic cracking effluent; and separating the olefins from the steam catalytic cracking effluent.

A catalyst structure includes a porous support structure, where the support structure includes an aluminosilicate material. Any two or more metals are loaded in the porous support structure, the two or more metals selected from the group consisting of Ga, Ag, Mo, Zn, Co and Ce, where each metal loaded in the porous support structure is present in an amount from about 0.1 wt % to about 20 wt %. In example embodiments, the catalyst structure includes three or more of the metals loaded in the porous support structure. The catalyst structure is used in a hydrocarbon upgrading process that is conducted in the presence of methane, nitrogen or hydrogen.

The present disclosure relates to a method that includes pyrolyzing a biomass to produce a pyrolysis oil and upgrading the pyrolysis oil to yield a first upgraded pyrolysis oil, where the pyrolysis oil is in at least one of a liquid phase and/or a vapor phase, the pyrolyzing is performed in a pyrolysis reactor at a first temperature between 400° C. and 600° C., the biomass has a residence time of less than five seconds in the pyrolysis reactor, the upgrading is performed in a fluidized bed reactor, and the upgrading is catalyzed using a zeolite.