Abstract: A process for the production of olefins from at least one of an alcohol and ether, the process including: contacting at least one alcohol or ether with a hydrofluoric acid-treated amorphous synthetic alumina-silica catalyst under decomposition conditions to produce an olefin.

Abstract: A process for the production of olefins from at least one of an alcohol and ether, the process including: contacting at least one alcohol or ether with a hydrofluoric acid-treated amorphous synthetic alumina-silica catalyst under decomposition conditions to produce an olefin.

Abstract: A process for the production of olefins from at least one of an alcohol and ether, the process including: contacting at least one alcohol or ether with a hydrofluoric acid-treated amorphous synthetic alumina-silica catalyst under decomposition conditions to produce an olefin.

Abstract: Processes for producing diaryl carbonates are disclosed, where such processes may provide for the production of diaryl carbonates from green house gases, such as carbon dioxide. The processes disclosed advantageously integrate diethyl carbonate and diaryl carbonate production, eliminating the need for solvent-based extractive distillation, as is commonly required when producing diaryl carbonates from dimethyl carbonate, providing for the integration of separation equipment and raw material usage, and reducing the operating and capital requirements for such processes. In some embodiments, processes disclosed herein may be operated essentially closed-loop with respect to ethanol usage, for example.

Abstract: A process for the production of ethylene, the process including: feeding hydrogen, a heavy solvent, a light solvent, and acetylene to a down-flow reactor comprising at least one reaction zone comprising a hydrogenation catalyst; concurrently in the down-flow reactor: contacting acetylene and hydrogen in the presence of the hydrogenation catalyst to convert at least a portion of the acetylene to ethylene; boiling at least a portion of the light solvent from a liquid phase to a vapor phase; recovering a reactor effluent comprising heavy solvent, light solvent, and ethylene; condensing at least a portion of the light solvent in the vapor phase; recovering a solvent fraction comprising the heavy solvent and the light solvent; recovering a product fraction comprising ethylene.

Abstract: Processes for the alcoholysis, inclusive of transesterification and/or disproportionation, of reactants are disclosed. The alcoholysis process may include feeding reactants and a trace amount of soluble organometallic compound to a reactor comprising a solid alcoholysis catalyst, wherein the soluble organometallic compound and the solid alcoholysis catalyst each independently comprise a Group II to Group VI element, which may be the same element in various embodiments. As an example, diphenyl carbonate may be continuously produced by performing transesterification over a solid catalyst followed by disproportionation, where a trace amount of soluble organometallic compound is fed to the transesterification reactor.

Abstract: A process for the production of olefins from at least one of an alcohol and ether, the process including: contacting at least one alcohol or ether with a hydrofluoric acid-treated amorphous synthetic alumina-silica catalyst under decomposition conditions to produce an olefin.

Abstract: Processes for the alcoholysis, inclusive of transesterification and/or disproportionation, of reactants are disclosed. The alcoholysis process may include feeding reactants and a trace amount of soluble organometallic compound to a reactor comprising a solid alcoholysis catalyst, wherein the soluble organometallic compound and the solid alcoholysis catalyst each independently comprise a Group II to Group VI element, which may be the same element in various embodiments. As an example, diphenyl carbonate may be continuously produced by performing transesterification over a solid catalyst followed by disproportionation, where a trace amount of soluble organometallic compound is fed to the transesterification reactor.

Abstract: A process for the production of olefins from at least one of an alcohol and ether, the process including: contacting at least one alcohol or ether with a hydrofluoric acid-treated amorphous synthetic alumina-silica catalyst under decomposition conditions to produce an olefin.

Abstract: Processes for producing diaryl carbonates are disclosed, where such processes may provide for the production of diaryl carbonates from green house gases, such as carbon dioxide. The processes disclosed advantageously integrate diethyl carbonate and diaryl carbonate production, eliminating the need for solvent-based extractive distillation, as is commonly required when producing diaryl carbonates from dimethyl carbonate, providing for the integration of separation equipment and raw material usage, and reducing the operating and capital requirements for such processes. In some embodiments, processes disclosed herein may be operated essentially closed-loop with respect to ethanol usage, for example.

Abstract: Processes for the alcoholysis, inclusive of transesterification and/or disproportionation, of reactants are disclosed. The alcoholysis process may include feeding reactants and a trace amount of soluble organometallic compound to a reactor comprising a solid alcoholysis catalyst, wherein the soluble organometallic compound and the solid alcoholysis catalyst each independently comprise a Group II to Group VI element, which may be the same element in various embodiments. As an example, diphenyl carbonate may be continuously produced by performing transesterification over a solid catalyst followed by disproportionation, where a trace amount of soluble organometallic compound is fed to the transesterification reactor.

Abstract: Processes for producing diaryl carbonates are disclosed, where such processes may provide for the production of diaryl carbonates from green house gases, such as carbon dioxide. The processes disclosed advantageously integrate diethyl carbonate and diaryl carbonate production, eliminating the need for solvent-based extractive distillation, as is commonly required when producing diaryl carbonates from dimethyl carbonate, providing for the integration of separation equipment and raw material usage, and reducing the operating and capital requirements for such processes. In some embodiments, processes disclosed herein may be operated essentially closed-loop with respect to ethanol usage, for example.

Abstract: Processes for the alcoholysis, inclusive of transesterification and/or disproportionation, of reactants are disclosed. The alcoholysis process may include feeding reactants and a trace amount of soluble organometallic compound to a reactor comprising a solid alcoholysis catalyst, wherein the soluble organometallic compound and the solid alcoholysis catalyst each independently comprise a Group II to Group VI element, which may be the same element in various embodiments. As an example, diphenyl carbonate may be continuously produced by performing transesterification over a solid catalyst followed by disproportionation, where a trace amount of soluble organometallic compound is fed to the transesterification reactor.

Abstract: Processes for the alcoholysis, inclusive of transesterification and/or disproportionation, of reactants are disclosed. The alcoholysis process may include feeding reactants and a trace amount of soluble organometallic compound to a reactor comprising a solid alcoholysis catalyst, wherein the soluble organometallic compound and the solid alcoholysis catalyst each independently comprise a Group II to Group VI element, which may be the same element in various embodiments. As an example, diphenyl carbonate may be continuously produced by performing transesterification over a solid catalyst followed by disproportionation, where a trace amount of soluble organometallic compound is fed to the transesterification reactor.

Abstract: Processes for the alcoholysis, inclusive of transesterification and/or disproportionation, of reactants are disclosed. The alcoholysis process may include feeding reactants and a trace amount of soluble organometallic compound to a reactor comprising a solid alcoholysis catalyst, wherein the soluble organometallic compound and the solid alcoholysis catalyst each independently comprise a Group II to Group VI element, which may be the same element in various embodiments. As an example, diphenyl carbonate may be continuously produced by performing transesterification over a solid catalyst followed by disproportionation, where a trace amount of soluble organometallic compound is fed to the transesterification reactor.

Abstract: Processes for the alcoholysis, inclusive of transesterification and/or disproportionation, of reactants are disclosed. The alcoholysis process may include feeding reactants and a trace amount of soluble organometallic compound to a reactor comprising a solid alcoholysis catalyst, wherein the soluble organometallic compound and the solid alcoholysis catalyst each independently comprise a Group II to Group VI element, which may be the same element in various embodiments. As an example, diphenyl carbonate may be continuously produced by performing transesterification over a solid catalyst followed by disproportionation, where a trace amount of soluble organometallic compound is fed to the transesterification reactor.

Abstract: A supported catalyst for selective hydrogenation of acetylenes comprising 3-15 wt. % Ni promoted with 0.005-0.2 Pd on a support. The catalyst is prepared by depositing nickel promoted with palladium on a support, containing one or more optional elements from copper, silver, Group IA (Li, Na, K, Rb, Cs, Fr) and Group IIA (Be, Mg, Ca, Sr, Ba, Ra) and B (Zn, Cd,) of the periodic table of elements and characterized as: Component Range of component Preferably wt. % wt. % Ni 3-15 ?4-11 Cu 0-I?? 0.0-0.6 Pd 0.005-0.2?? 0.01-0.1? Ag 0-10 0-5 Group IA ?0-2.5 ??0-1.5 Group IIA & B 0-25 0.1-5.

Abstract: Processes for producing diaryl carbonates are disclosed, where such processes may provide for the production of diaryl carbonates from green house gases, such as carbon dioxide. The processes disclosed advantageously integrate diethyl carbonate and diaryl carbonate production, eliminating the need for solvent-based extractive distillation, as is commonly required when producing diaryl carbonates from dimethyl carbonate, providing for the integration of separation equipment and raw material usage, and reducing the operating and capital requirements for such processes. In some embodiments, processes disclosed herein may be operated essentially closed-loop with respect to ethanol usage, for example.

Abstract: More selective and efficient Ni hydrotreating catalysts are those which contain more than about 60% of the Ni content on the peripheral surface of porous supports, such as extruded alumina, which may be obtained by spraying an atomized solution of a Ni compound onto the support and drying it at a temperature in the range of from 200 to 600° C. When used, for example, to remove acetylenic compounds from butadiene streams, higher recovery of the desired butadiene with lower acetylenic content and low heavy polymer deposition is obtained than was possible with prior catalysts.

Abstract: More selective and efficient Ni hydrotreating catalysts are those which contain more than about 60% of the Ni content on the peripheral surface of porous supports, such as extruded alumina, which may be obtained by spraying an atomized solution of a Ni compound onto the support and drying it at a temperature in the range of from 200 to 600° C. When used, for example, to remove acetylenic compounds from butadiene streams, higher recovery of the desired butadiene with lower acetylenic content and low heavy polymer deposition is obtained than was possible with prior catalysts.