Abstract: A process for preparing C2 to C4 hydrocarbons includes introducing a feed stream including hydrogen gas and a carbon-containing gas selected from the group consisting of carbon monoxide, carbon dioxide, and mixtures thereof into a reaction zone of a reactor, and converting the feed stream into a product stream including C2 to C4 hydrocarbons in the reaction zone in the presence of a formed hybrid catalyst. The formed hybrid catalyst includes a metal oxide catalyst component including gallium oxide and zirconia, a microporous catalyst component that is a molecular sieve having 8-MR (Membered Ring) pore openings, and a binder including alumina, zirconia, or both.

Abstract: According to one or more embodiments of the present disclosure, a catalyst system useful for dehydrogenation includes from 98 vol. % to 99.95 vol. % of a catalyst and from 0.05 vol. % to 2 vol. % of a combustion additive. The catalyst may include from 1 ppmw to 150 ppmw platinum, gallium, and a support material. The combustion additive may include from 150 ppmw to 1,000 ppmw platinum, gallium, and a support material. The combustion additive may include at least 1.1 times greater platinum than the catalyst.

Abstract: According to one or more embodiments of the present disclosure, a method for producing olefins includes contacting a hydrocarbon-containing feed with a catalyst in a reactor portion of a reactor system to form an olefin-containing effluent, separating at least a portion of the olefin-containing effluent from the catalyst, passing the catalyst to a catalyst-processing portion of the reactor system and processing the catalyst to produce a processed catalyst and a combustion gas, passing the processed catalyst from the catalyst-processing portion to the reactor portion, and introducing a combustion additive to the reactor system when the combustion gas comprises one or more hydrocarbons in an amount greater than 5% of an LFL of the combustion gas at a temperature and pressure of the catalyst processing portion. The catalyst may include from 1 ppmw to 150 ppmw platinum. The combustion additive may include from 150 ppmw to 1,000 ppmw platinum.

Abstract: A hybrid catalyst including a metal oxide catalyst component comprising chromium, zinc, and at least one additional metal selected from the group consisting of aluminum and gallium, and a microporous catalyst component that is a molecular sieve having 8-MR pore openings. The metal oxide catalyst component includes anatomic ratio of chromium:zinc (Cr:Zn) from 0.35 to 1.00, and the at least one additional metal is present in an amount from 25.0 at % to 40.0 at %. A process for preparing C2 and C3 olefins comprising: a) introducing a feed stream comprising hydrogen gas and a carbon-containing gas selected from the group consisting of carbon monoxide, carbon dioxide, and mixtures thereof into a reaction zone of a reactor; and b) converting the feed stream into a product stream comprising C2 and C3 olefins in the reaction zone in the presence of said hybrid catalyst.

Abstract: A method for separating CO2 from C2 to C5 alkanes includes introducing a first stream including C2 to C5 alkanes and CO2 into a first separation zone, the first separation zone including a hydrocarbon solvent, and separating the first stream into a recycle stream and a second stream in the first separation zone. The recycle stream including CO2 and one or more of CO, H2, and CH4, and the second stream including C2 to C5 alkanes. The method further includes introducing the second stream into a second separation zone, and separating the second stream into a third stream and a fourth stream, wherein the third stream includes C2 alkanes and the fourth stream includes C3 to C5 alkanes.

Abstract: Embodiments of the present disclosure are directed to methods of producing a hydrogen-selective oxygen carrier material comprising combining one or more core material precursors and one or more shell material precursors to from a precursor mixture and heat-treating the precursor mixture at a treatment temperature to form the hydrogen-selective oxygen carrier material. The treatment temperature is greater than or equal to 100° C. less than the melting point of a shell material, and the hydrogen-selective oxygen carrier material comprises a core comprising a core material and a shell comprising the shell material. The shell material may be in direct contact with at least a majority of an outer surface of the core material.

Abstract: A method for operating an acetylene hydrogenation unit in an integrated steam cracking-fluidized catalytic dehydrogenation (FCDh) system may include separating a cracked gas from a steam cracking system and an FCDh effluent from an FCDh system into a hydrogenation feed and an acetylene-depleted stream, the hydrogenation feed comprising at least hydrogen, CO, and acetylene. During normal operating conditions, at least 20% of the CO in the hydrogenation feed is from the cracked gas. The method may include contacting the hydrogenation feed with an acetylene hydrogenation catalyst to hydrogenate at least a portion of the acetylene in the hydrogenation feed to produce a hydrogenated effluent. The steam cracking is operated under conditions that increase CO production such that a concentration of CO in the cracked gas is great enough that when a flowrate of the FCDh effluent is zero, a CO concentration in the hydrogenation feed is at least 100 ppmv.

Abstract: A method for operating an acetylene hydrogenation unit of a steam cracking system that integrates a fluidized catalytic dehydrogenation (FCDh) effluent from a fluidized catalytic dehydrogenation (FCDh) system may include separating a cracked gas from the steam cracking system into at least a hydrogenation feed comprising at least acetylene, CO, and hydrogen, introducing the FCDh effluent to the separation system, combining the FCDh effluent with the cracked gas upstream of the separation system, or both. The method may include hydrogenating acetylene in the hydrogenation feed. Elevated CO concentration in the hydrogenation feed due to the FCDh effluent may reduce a reaction rate of acetylene hydrogenation. The acetylene hydrogenation unit may operate at an elevated temperature relative to normal operating temperatures when the portion of the FCDh effluent is not integrated, such that a concentration of acetylene in the hydrogenated effluent is less than a threshold acetylene concentration.

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 preparing C2 to C3 hydrocarbons may include introducing a feed stream including hydrogen gas and a carbon-containing gas comprising carbon monoxide, carbon dioxide, and mixtures thereof into a reaction zone of a reactor, and converting the feed stream into a product stream comprising C2 to C3 hydrocarbons in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst may include a metal oxide catalyst component and a microporous catalyst component comprising 8-MR pore openings and may be derived from a natural mineral, the product stream comprises a combined C2 and C3 selectivity greater than 40 carbon mol%.

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 preparing C2 to C3 hydrocarbons may include introducing a feed stream including hydrogen gas and a carbon-containing gas comprising carbon monoxide, carbon dioxide, and mixtures thereof into a reaction zone of a reactor, and converting the feed stream into a product stream comprising C2 to C3 hydrocarbons in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst may include a metal oxide catalyst component and a microporous catalyst component comprising 8-MR pore openings less than or equal to 5.1 A and a cage defining ring size less than or equal to 7.45 A, where a C2/C3 carbon molar ratio of the product stream is greater than or equal to 0.7.

Abstract: A process for preparing C2 to C4 olefins includes introducing a feed stream of hydrogen gas and a carbon-containing gas into a reaction zone of a reactor and converting the feed stream into a product stream including C2 to C4 olefins in the reaction zone in the presence of a hybrid catalyst and in a non-oxidative atmosphere. The hybrid catalyst includes a metal oxide catalyst component comprising gallium oxide and zirconia, and a microporous catalyst component having an 8 membered ring structure. The process also includes periodically introducing an oxidative atmosphere into the reaction zone.

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 process for preparing C2 to C5 paraffins includes introducing a feed stream comprising hydrogen gas and a carbon-containing gas into a reaction zone of a reactor, and converting the feed stream into a product stream comprising C2 to C5 paraffins in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst includes a metal oxide catalyst component and a microporous catalyst component. The metal oxide catalyst component satisfies: an atomic ratio of Cu/Zn from 0.01 to 3.00; an atomic ratio of Cr/Zn from 0.01 to 1.50; and percentage of (Al+Cr) from greater than 0.0 at % to 50.0 at % based on a total amount of metal in the metal oxide catalyst component.

Abstract: A process for preparing C2 to C5 hydrocarbons includes introducing a feed stream into a reaction zone of a reactor, the feed stream including hydrogen gas and carbon monoxide. An additional stream is introduced into the reaction zone of the reactor, the additional stream comprising water, carbon dioxide, or mixtures thereof. A combined stream that includes the feed stream and the additional stream is converted into a product stream comprising C2 to C5 hydrocarbons in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst includes a metal oxide catalyst component, and a microporous catalyst component.

Abstract: A process for preparing C2 to C5 olefins includes introducing a feed stream comprising hydrogen and at least one carbon-containing component selected from the group consisting of CO, CO2, and mixtures thereof into a reaction zone. The feed stream is contacted with a hybrid catalyst in the reaction zone, and a product stream is formed that exits the reaction zone and includes C2 to C5 olefins. The hybrid catalyst includes a methanol synthesis component and a solid microporous acid component that is selected from molecular sieves having 8-MR access and having a framework type selected from the group consisting of CHA, AEI, AFX, ERI, LTA, UFI, RTH, and combinations thereof. The methanol synthesis component comprises a metal oxide support and a metal catalyst. The metal oxide support includes titania, zirconia, hafnia or mixtures thereof, and the metal catalyst includes zinc.

Abstract: A hybrid catalyst including a metal oxide catalyst component comprising chromium, zinc, and at least one additional metal selected from the group consisting of iron and manganese, and a microporous catalyst component that is a molecular sieve having 8-MR pore openings. The at least one additional metal is present in an amount from 5.0 at % to 20.0 at %.

Abstract: A method for separating CO2 from C2 to C5 alkanes includes introducing a first stream including C2 to C5 alkanes and CO2 into a first separation zone, the first separation zone including a hydrocarbon solvent, and separating the first stream into a recycle stream and a second stream in the first separation zone. The recycle stream including CO2 and one or more of CO, H2, and CH4, and the second stream including C2 to C5 alkanes. The method further includes introducing the second stream into a second separation zone, and separating the second stream into a third stream and a fourth stream, wherein the third stream includes C2 alkanes and the fourth stream includes C3 to C5 alkanes.

Abstract: A method for operating an acetylene hydrogenation unit of a steam cracking system that integrates a fluidized catalytic dehydrogenation (FCDh) effluent from a fluidized catalytic dehydrogenation (FCDh) system may include separating a cracked gas from the steam cracking system into at least a hydrogenation feed comprising at least acetylene, CO, and hydrogen, introducing the FCDh effluent to the separation system, combining the FCDh effluent with the cracked gas upstream of the separation system, or both. The method may include hydrogenating acetylene in the hydrogenation feed. Elevated CO concentration in the hydrogenation feed due to the FCDh effluent may reduce a reaction rate of acetylene hydrogenation. The acetylene hydrogenation unit may operate at an elevated temperature relative to normal operating temperatures when the portion of the FCDh effluent is not integrated, such that a concentration of acetylene in the hydrogenated effluent is less than a threshold acetylene concentration.