Abstract: A process for dehydration of an ethanol feed stream comprising sending said ethanol feed stream and steam to a radial flow reactor to contact a catalyst under reaction conditions and produce an effluent comprising ethylene. The use of a radial flow reactor eliminates concerns about pressure drops that may occur with conventional fixed bed downflow reactors.

Abstract: A process for dehydration of ethanol to produce ethylene is provided. Ethanol is dehydrated to produce ethylene and the subsequent conversion of ethylene to longer chain olefins and then their hydrogenation to produce long chain paraffins. In some embodiments, a split feed is employed to improve efficiency and a caustic wash column is eliminated. The advantages of the process include a lower requirement for steam and a reduction in the combined reactor volume of 30-40% when two reactors are used as compared to a single reactor.

Abstract: Provided herein is an alkane dehydrogenation catalyst, a method of manufacturing an alkane dehydrogenation catalyst, and a method of converting alkanes to alkenes.

Abstract: Provided herein is an alkane dehydrogenation catalyst, a method of manufacturing an alkane dehydrogenation catalyst, and a method of converting alkanes to alkenes.

Abstract: A modified UZM-14 zeolite is described. The modified UZM-14 zeolite has a Modification Factor of 6 or more. The modified UZM-14 zeolite may have one or more of: a Si/Al2 ratio of 14 to 30; a total pore volume in a range of 0.5 to 1.0 cc/g; at least 5% of a total pore volume being mesopores having a diameter of 10 nm of less; a cumulative pore volume of micropores and mesopores having a diameter of 100 ? or less of 0.25 cc/g or more; or a Collidine IR Bronsted acid site distribution greater than or equal to an area of 3/mg for a peak in a range of 1575 to 1700 cm?1 after desorption at 150° C. Processes of making the modified UZM-14 zeolite and transalkylation processes using the modified UZM-14 zeolite are also described.

Abstract: A catalyst suitable for the conversion of aromatic hydrocarbons is described. The catalyst comprises UZM-54 zeolite; a mordenite zeolite; a binder comprising alumina, silica, or combinations, thereof; and a metal selected from one or more of: Groups VIB(6) VIIB(7), VIII(8-10) and IVA(14) of the Periodic Table. A process for transalkylation using the catalyst is also described.

Abstract: Toluene disproportionation processes utilizing treated UZM-39 zeolites are described. The processes produce effluent streams comprising para-xylene and benzene. The molar ratio of benzene to xylene (Bz/X) in the effluent stream can be in a range of about 1.00 to about 1.14, the molar ratio of para-xylene to xylene (pX/X) in the effluent stream can be in a range of about 0.80 to about 1.0, and the conversion of toluene can be about 20% to about 40%.

Abstract: Toluene disproportionation processes utilizing treated UZM-44 zeolites are described. The processes produce effluent streams comprising para-xylene and benzene. The molar ratio of benzene to xylene (Bz/X) in the effluent stream can be in a range of about 1.00 to about 1.14, the molar ratio of para-xylene to xylene (pX/X) in the effluent stream can be in a range of about 0.80 to about 1.0, and the conversion of toluene can be about 20% to about 40%.

Abstract: Toluene disproportionation processes utilizing treated UZM-44 zeolites are described. The processes produce effluent streams comprising para-xylene and benzene. The molar ratio of benzene to xylene (Bz/X) in the effluent stream can be in a range of about 1.00 to about 1.14, the molar ratio of para-xylene to xylene (pX/X) in the effluent stream can be in a range of about 0.80 to about 1.0, and the conversion of toluene can be about 20% to about 40%.

Abstract: Toluene disproportionation processes utilizing treated UZM-39 zeolites are described. The processes produce effluent streams comprising para-xylene and benzene. The molar ratio of benzene to xylene (Bz/X) in the effluent stream can be in a range of about 1.00 to about 1.14, the molar ratio of para-xylene to xylene (pX/X) in the effluent stream can be in a range of about 0.80 to about 1.0, and the conversion of toluene can be about 20% to about 40%.

Abstract: A catalyst suitable for the conversion of aromatic hydrocarbons is described. The catalyst comprises UZM-54 zeolite; a mordenite zeolite; a binder comprising alumina, silica, or combinations, thereof; and a metal selected from one or more of: Groups VIB(6) VIIB(7), VIII(8-10) and IVA(14) of the Periodic Table. A process for transalkylation using the catalyst is also described.

Abstract: A modified UZM-14 zeolite is described. The modified UZM-14 zeolite has a Modification Factor of 6 or more. The modified UZM-14 zeolite may have one or more of: a Si/Al2 ratio of 14 to 30; a total pore volume in a range of 0.5 to 1.0 cc/g; at least 5% of a total pore volume being mesopores having a diameter of 10 nm of less; a cumulative pore volume of micropores and mesopores having a diameter of 100 ? or less of 0.25 cc/g or more; or a Collidine IR Bronsted acid site distribution greater than or equal to an area of 3/mg for a peak in a range of 1575 to 1700 cm?1 after desorption at 150° C. Processes of making the modified UZM-14 zeolite and transalkylation processes using the modified UZM-14 zeolite are also described.

Abstract: A modified UZM-14 zeolite is described. The modified UZM-14 zeolite has a Modification Factor of 6 or more. The modified UZM-14 zeolite may have one or more of: a Si/Al2 ratio of 14 to 30; a total pore volume in a range of 0.5 to 1.0 cc/g; at least 5% of a total pore volume being mesopores having a diameter of 10 nm of less; a cumulative pore volume of micropores and mesopores having a diameter of 100 ? or less of 0.25 cc/g or more; or a Collidine IR Bronsted acid site distribution greater than or equal to an area of 3/mg for a peak in a range of 1575 to 1700 cm?1 after desorption at 150° C. Processes of making the modified UZM-14 zeolite and transalkylation processes using the modified UZM-14 zeolite are also described.

Abstract: A modified UZM-14 zeolite is described. The modified UZM-14 zeolite has a Modification Factor of 6 or more. The modified UZM-14 zeolite may have one or more of: a Si/Al2 ratio of 14 to 30; a total pore volume in a range of 0.5 to 1.0 cc/g; at least 5% of a total pore volume being mesopores having a diameter of 10 nm of less; a cumulative pore volume of micropores and mesopores having a diameter of 100 ? or less of 0.25 cc/g or more; or a Collidine IR Bronsted acid site distribution greater than or equal to an area of 3/mg for a peak in a range of 1575 to 1700 cm?1 after desorption at 150° C. Processes of making the modified UZM-14 zeolite and transalkylation processes using the modified UZM-14 zeolite are also described.