Abstract: According to one or more embodiments described herein, a method for dehydrogenating hydrocarbons may include contacting a feed stream including one or more hydrocarbons with a particulate solid, which may include an oxygen-carrier material, to form hydrogen and one or more products. At least a portion of the hydrogen may be reacted with oxygen from the oxygen-carrier material to form water and reduce the oxygen content in the oxygen-carrier material. The process may include passing the particulate solid from the dehydrogenation reactor to a processing zone. In the processing zone, a fuel may be injected into the processing zone, and at least a portion of the fuel may react with oxygen from the oxygen-carrier material of the particulate solid. The gases in the processing zone may include less than or equal to 1 mol. % O2.

Abstract: According to one or more embodiments described herein, a method for dehydrogenating hydrocarbons may include passing a hydrocarbon feed comprising one or more alkanes or alkyl aromatics into a fluidized bed reactor, contacting the hydrocarbon feed with a dehydrogenation catalyst in the fluidized bed reactor to produce a dehydrogenated product and hydrogen, and contacting the hydrogen with an oxygen-rich oxygen carrier material in the fluidized bed reactor to combust the hydrogen and form an oxygen-diminished oxygen carrier material. In additional embodiments, a dual-purpose material may be utilized which has dehydrogenation catalyst and oxygen carrying functionality.

Abstract: A process for oxidative dehydrogenation of a hydrocarbon to produce an olefin and water may include contacting, in a fluidized bed, the hydrocarbon with a particulate material, which may include at least one oxygen transfer agent (OTA) and at least one fluidization enhancing additive. During at least a portion of contacting the hydrocarbon with the particulate material, the fluidized bed may be at a temperature at or above a melting point of one or more materials of the oxygen transfer agent. Further, during at least a portion of contacting the hydrocarbon with the particulate material, a surface of at least a portion of the OTA may comprise a molten layer. The fluidization enhancing additive may not undergo reduction in the fluidized bed during contacting the hydrocarbon with the particulate material and may be present in an amount that maintains sufficient fluidization of the particulate material.

Abstract: A process for preparing C2 to C4 hydrocarbons includes introducing a feed stream into a reaction zone of a reactor, the feed stream comprising hydrogen gas and carbon monoxide. An additional stream is introduced into the reaction zone of the reactor, the additional stream comprising carbon dioxide. A combined stream that includes the feed stream and the additional stream is converted into a product stream comprising C2 to C4 hydrocarbons in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst includes a mixed metal oxide catalyst component, and a microporous catalyst component. The process operates at a gas hourly space velocity in excess of 2500 hr?1 and effectively yields a net carbon dioxide selectivity of less than 5.0% and a productivity of C2-C4 hydrocarbons greater than 75 g hydrocarbons per kilogram of catalyst per hour.

Abstract: According to one or more embodiments described herein, a method for dehydrogenating hydrocarbons may include passing a hydrocarbon feed comprising one or more alkanes or alkyl aromatics into a fluidized bed reactor, contacting the hydrocarbon feed with a dehydrogenation catalyst in the fluidized bed reactor to produce a dehydrogenated product and hydrogen, and contacting the hydrogen with an oxygen-rich oxygen carrier material in the fluidized bed reactor to combust the hydrogen and form an oxygen-diminished oxygen carrier material. In additional embodiments, a dual-purpose material may be utilized which has dehydrogenation catalyst and oxygen carrying functionality.

Abstract: A method for converting alkanes to olefins includes contacting a feed stream comprising alkanes with an oxidative dehydrogenation that does not comprise tellurium catalyst in a reaction zone and dehydrogenating the alkanes without a co-feed of oxygen to yield a product stream having olefins. The oxidative dehydrogenation catalyst has the formula: MovVwNbyAzOx, where v is 1.0, w is from 0.1 to 0.5, y is from 0.001 to 0.3, A is Bi, Sb, Pr, or mixtures thereof, z is from 0.01 to 0.3, and x charge-balances the structure. The oxidative dehydrogenation catalyst has a crystallographic structure with Pba2-32 space group, characterized by reflections determined with Cu-K? X-ray diffraction (XRD) as follows.

Abstract: A method of manufacturing a hollow fiber carbon membrane, the method includes heating a polymeric precursor to a pyrolysis temperature that is greater than or equal to 900° C. and less than or equal to 1200° C., and pyrolyzing the polymeric precursor at the pyrolysis temperature in a pyrolysis atmosphere that comprises oxygen in an amount that is greater than 0 ppm and less than 200 ppm.

Abstract: According to one or more embodiments described herein, a method for dehydrogenating hydrocarbons may include passing a hydrocarbon feed comprising one or more alkanes or alkyl aromatics into a fluidized bed reactor, contacting the hydrocarbon feed with a dehydrogenation catalyst in the fluidized bed reactor to produce a dehydrogenated product and hydrogen, and contacting the hydrogen with an oxygen-rich oxygen carrier material in the fluidized bed reactor to combust the hydrogen and form an oxygen-diminished oxygen carrier material. In additional embodiments, a dual-purpose material may be utilized which has dehydrogenation catalyst and oxygen carrying functionality.

Abstract: According to one or more embodiments described herein, a method for dehydrogenating hydrocarbons may include passing a hydrocarbon feed comprising one or more alkanes or alkyl aromatics into a fluidized bed reactor, contacting the hydrocarbon feed with a dehydrogenation catalyst in the fluidized bed reactor to produce a dehydrogenated product and hydrogen, and contacting the hydrogen with an oxygen-rich oxygen carrier material in the fluidized bed reactor to combust the hydrogen and form an oxygen-diminished oxygen carrier material. In additional embodiments, a dual-purpose material may be utilized which has dehydrogenation catalyst and oxygen carrying functionality.

Abstract: A method for operating an integrated system for producing olefins may include contacting a hydrogenation feed with a first hydrogenation catalyst to produce a hydrogenated effluent, the hydrogenation feed including at least a portion of a first process effluent from a first olefin production process and at least a portion of a second process effluent from a second olefin production process. The hydrogenation feed may include at least hydrogen, ethylene, carbon monoxide, acetylene, methyl acetylene, and propadiene, and the first hydrogenation catalyst may be a hydrogenation catalyst having a temperature operating range of at least 40° C. The hydrogenated effluent may include methyl acetylene, propadiene, or both. The method may further include contacting at least a portion of the hydrogenated effluent with a second hydrogenation catalyst, which may cause hydrogenation of at least a portion of the methyl acetylene and propadiene to produce an MAPD hydrogenated effluent.

Abstract: A process for oxidative dehydrogenation of a hydrocarbon to produce an olefin and water may include contacting, in a fluidized bed, the hydrocarbon with a particulate material, which may include at least one oxygen transfer agent (OTA) and at least one fluidization enhancing additive. During at least a portion of contacting the hydrocarbon with the particulate material, the fluidized bed may be at a temperature at or above a melting point of one or more materials of the oxygen transfer agent. Further, during at least a portion of contacting the hydrocarbon with the particulate material, a surface of at least a portion of the OTA may comprise a molten layer. The fluidization enhancing additive may not undergo reduction in the fluidized bed during contacting the hydrocarbon with the particulate material and may be present in an amount that maintains sufficient fluidization of the particulate material.

Abstract: A process for preparing C2 to C4 hydrocarbons includes introducing a feed stream into a reaction zone of a reactor, the feed stream comprising hydrogen gas and carbon monoxide. An additional stream is introduced into the reaction zone of the reactor, the additional stream comprising carbon dioxide. A combined stream that includes the feed stream and the additional stream is converted into a product stream comprising C2 to C4 hydrocarbons in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst includes a mixed metal oxide catalyst component, and a microporous catalyst component. The process operates at a gas hourly space velocity in excess of 2500 hr-1 and effectively yields a net carbon dioxide selectivity of less than 5.0% and a productivity of C2-C4 hydrocarbons greater than 75 g hydrocarbons per kilogram of catalyst per hour.

Abstract: A method for operating an integrated system for producing olefins may include contacting a hydrogenation feed with a first hydrogenation catalyst to produce a hydrogenated effluent, the hydrogenation feed including at least a portion of a first process effluent from a first olefin production process and at least a portion of a second process effluent from a second olefin production process. The hydrogenation feed may include at least hydrogen, ethylene, carbon monoxide, acetylene, methyl acetylene, and propadiene, and the first hydrogenation catalyst may be a hydrogenation catalyst having a temperature operating range of at least 40° C. The hydrogenated effluent may include methyl acetylene, propadiene, or both. The method may further include contacting at least a portion of the hydrogenated effluent with a second hydrogenation catalyst, which may cause hydrogenation of at least a portion of the methyl acetylene and propadiene to produce an MAPD hydrogenated effluent.

Abstract: A process for converting a feed stream having carbon to C2 to C5 olefins, includes introducing a feed stream including methane and oxygen to a first reaction zone, reacting the methane and oxygen in the first reaction zone to form a first reaction zone product stream having a mixture of C2 to C5 alkanes, transporting the mixture of C2 to C5 alkanes to a second reaction zone, introducing a fresh stream of at least one of ethane and propane to the second reaction zone, converting the C2 to C5 alkanes to C2 to C5 olefins in the second reaction zone, producing one or more product streams in the second reaction zone, where a sum of the one or more product streams includes C2 to C5 olefins, and producing a recycle stream comprising hydrogen in the second reaction zone, where the recycle stream is transported to the first reaction zone.

Abstract: According to one or more embodiments described herein, a method for dehydrogenating hydrocarbons may include passing a hydrocarbon feed comprising one or more alkanes or alkyl aromatics into a fluidized bed reactor, contacting the hydrocarbon feed with a dehydrogenation catalyst in the fluidized bed reactor to produce a dehydrogenated product and hydrogen, and contacting the hydrogen with an oxygen-rich oxygen carrier material in the fluidized bed reactor to combust the hydrogen and form an oxygen-diminished oxygen carrier material. In additional embodiments, a dual-purpose material may be utilized which has dehydrogenation catalyst and oxygen carrying functionality.

Abstract: A process for converting a feed stream having carbon to C2 to C5 olefins, includes introducing a feed stream including methane and oxygen to a first reaction zone, reacting the methane and oxygen in the first reaction zone to form a first reaction zone product stream having a mixture of C2 to C5 alkanes, transporting the mixture of C2 to C5 alkanes to a second reaction zone, introducing a fresh stream of at least one of ethane and propane to the second reaction zone, converting the C2 to C5 alkanes to C2 to C5 olefins in the second reaction zone, producing one or more product streams in the second reaction zone, where a sum of the one or more product streams includes C2 to C5 olefins, and producing a recycle stream comprising hydrogen in the second reaction zone, where the recycle stream is transported to the first reaction zone.

Abstract: A process and system for preparing C2 to C5 hydrocarbons includes introducing a feed stream containing hydrogen gas and a carbon-containing gas selected from carbon monoxide, carbon dioxide, and mixtures thereof into a first reaction zone, contacting the feed stream and a hybrid catalyst in the first reaction zone, introducing a reaction zone product stream into a water removal zone that is downstream from the first reaction zone, and introducing a product stream from the water removal zone into a second reaction zone, resulting in a final stream comprising C2 to C5 hydrocarbons. The hybrid catalyst includes a methanol synthesis component and a microporous solid acid component; the microporous solid acid component is a molecular sieve having 8-MR access. The water removal zone removes at least a portion of water from the reaction zone product stream.

Abstract: A process and system for preparing C2 to C5 hydrocarbons includes introducing a feed stream containing hydrogen gas and a carbon-containing gas selected from carbon monoxide, carbon dioxide, and mixtures thereof into a first reaction zone, contacting the feed stream and a hybrid catalyst in the first reaction zone, introducing a reaction zone product stream into a water removal zone that is downstream from the first reaction zone, and introducing a product stream from the water removal zone into a second reaction zone, resulting in a final stream comprising C2 to C5 hydrocarbons. The hybrid catalyst includes a methanol synthesis component and a microporous solid acid component; the microporous solid acid component is a molecular sieve having 8-MR access. The water removal zone removes at least a portion of water from the reaction zone product stream.

Abstract: A process is provided for the chlorination of ethane using chlorine as the chlorinating agent to produce ethylene, hydrogen chloride (HCl) and vinyl chloride monomer (VCM).

Abstract: A process is provided for the chlorination of ethane using chlorine as the chlorinating agent to produce ethylene, hydrogen chloride (HCl) and vinyl chloride monomer (VCM).