Abstract: A conditioning process that is employed with a high selectivity catalyst (HSC) during an initial phase (i.e., start-up) of the epoxidation process is provided. The HSC conditioning process of the present disclosure ensures that the heat release from a catalyst bed containing an HSC during a start-up operation is less than 2000 kJ/Kgcat·hr. The HSC containing catalyst bed that has been conditioned by the process of the present disclosure exhibits improved performance (i.e., EO selectivity) and reduced hot spots.

Abstract: A conditioning process that is employed with a high selectivity catalyst (HSC) during an initial phase (i.e., start-up) of the epoxidation process is provided. The HSC conditioning process of the present disclosure ensures that the heat release from a catalyst bed containing an HSC during a start-up operation is less than 2000 kJ/Kgcat·hr. The HSC containing catalyst bed that has been conditioned by the process of the present disclosure exhibits improved performance (i.e., EO selectivity) and reduced hot spots.

Abstract: A phenol alkylation catalyst exhibiting a desirable combination of activity, selectivity, and regenerability is prepared from a catalyst precursor that includes specific amounts of magnesium oxide, copper oxide or a copper oxide precursor, a hydrous magnesium aluminosilicate-containing binder, a pore-former, a lubricant, and water. Methods of forming and regenerating the catalyst, as well as a phenol alkylation method, are described.

Abstract: Methods for producing butadiene by the oxidative dehydrogenation of butene are provided. Methods for producing butadiene from a feed stream including oxygen and butene in a molar ratio of oxygen to butene (O2/C4H8) from about 0.9 to about 1.5 can include introducing the feed stream to a catalyst in the presence of steam. The molar ratio of steam to butene (H2O/C4H8) can be from about 10 to about 20. Methods can further include reacting the butene to generate a product stream therefrom comprising butadiene and water. Methods can further include separating water from the product stream to generate a butadiene stream including greater than about 85 wt-% butadiene.

Abstract: A phenol alkylation catalyst exhibiting a desirable combination of activity, selectivity, and regenerability is prepared from a catalyst precursor that includes specific amounts of magnesium oxide, copper oxide or a copper oxide precursor, a hydrous magnesium aluminosilicate-containing binder, a pore-former, a lubricant, and water. Methods of forming and regenerating the catalyst, as well as a phenol alkylation method, are described.

Abstract: Methods for producing butadiene by the oxidative dehydrogenation of butene are provided. Methods for producing butadiene from a feed stream including oxygen and butene in a molar ratio of oxygen to butene (O2/C4H8) from about 0.9 to about 1.5 can include introducing the feed stream to a catalyst in the presence of steam. The molar ratio of steam to butene (H2O/C4H8) can be from about 10 to about 20. Methods can further include reacting the butene to generate a product stream therefrom comprising butadiene and water. Methods can further include separating water from the product stream to generate a butadiene stream including greater than about 85 wt-% butadiene.

Abstract: In one embodiment, a process for the purification of CO2 from chlorinated and non-chlorinated hydrocarbons, comprising: contacting a CO2 stream with a metal oxide catalyst, wherein the stream comprises the CO2 and impurities comprising the non-chlorinated hydrocarbons and the chlorinated hydrocarbons; interacting the impurities with the catalyst to form additional CO2 and metal chloride; and regenerating the catalyst by contacting the metal chloride with an oxygen containing gas stream.

Abstract: The present disclosure provides methods for the hydrogenation of carbon dioxide. In one non-limiting exemplary embodiment, the presently disclosed subject matter provides a method for the hydrogenation of carbon dioxide to form syngas that includes contacting a feedstream that contains hydrogen and carbon dioxide with a catalyst at a temperature of about 650° C. in an Inconel alloy reactor to produce a syngas mixture that includes hydrogen and carbon monoxide.

Abstract: In one embodiment, a process for the purification of CO2 from chlorinated and non-chlorinated hydrocarbons, comprising: contacting a CO2 stream with a metal oxide catalyst, wherein the stream comprises the CO2 and impurities comprising the non-chlorinated hydrocarbons and the chlorinated hydrocarbons; interacting the impurities with the catalyst to form additional CO2 and metal chloride; and regenerating the catalyst by contacting the metal chloride with an oxygen containing gas stream.

Abstract: In an embodiment, a process for producing ethylene comprising: introducing a methane stream comprising methane, oxygen, and water to a methane coupling zone; reacting the methane, the oxygen, and the water in the methane coupling zone via a methane oxidative coupling reaction to produce a first product stream; introducing the first product stream to a pyrolysis zone; and pyrolyzing ethane in the first product stream in the pyrolysis zone to produce a second product stream comprising ethylene. A heat from the methane coupling reaction is used in the pyrolysis reaction.

Abstract: A dehydrogenation catalyst is formed by forming a mixture comprising a bayerite aluminum hydroxide (Al(OH)3), a lanthanum (La) source, a cerium (Ce) source, a barium (Ba) source, a zirconium (Zr) source, and water into a shaped body. The shaped body is calcined at a temperature of at least 750° C. to form a catalyst support. The catalyst support is treated with a dehydrogenation catalyst component to form a treated catalyst support containing the dehydrogenation catalyst component. The treated catalyst support is then calcined. The resulting catalyst composition may be used by contacting a paraffin hydrocarbon feed with a catalyst within a reactor in the presence of steam under dehydrogenation reaction conditions suitable to form dehydrogenated hydrocarbon products.

Abstract: The invention relates to a catalyst and process for making syngas mixtures including hydrogen, carbon monoxide and carbon dioxide. The process comprises contacting a gaseous feed mixture containing carbon dioxide and hydrogen with the catalyst, where the catalyst comprises Mn oxide and an auxiliary metal oxide selected from the group consisting of La, Ca, K, W, Cu, Al and mixtures or combinations thereof. The process enables hydrogenation of carbon dioxide into carbon monoxide with high selectivity, and good catalyst stability over time and under variations in processing conditions. The process can be applied separately, but can also be integrated with other processes, both up-stream and/or down-stream including methane reforming or other synthesis processes for making products like alkanes, aldehydes, or alcohols.

Abstract: Dialkyl carbonate and diol products are prepared in an integrated process performed by reacting an alkylene oxide with carbon dioxide in the presence of a non-halide-containing homogeneous carbonation catalyst in a first reaction zone to form a crude cyclic carbonate product. The crude cyclic carbonate product is introduced along with an aliphatic monohydric alcohol to a second reaction zone containing a transesterification catalyst. The transesterification catalyst is comprised of a strongly basic Type I ion exchange resin in gel having a particular form. The cyclic carbonate product and monohydric alcohol are reacted to form the dialkyl carbonate and diol products. In another aspect, dialkyl carbonate and diol products are prepared in an integrated process wherein a halide-containing homogeneous carbonation catalyst is used to form a crude cyclic carbonate product that is then used in a transesterification reaction.

Abstract: A method of forming a cyclic carbonate product is carried out by reacting an alkylene oxide, such as ethylene oxide, with carbon dioxide in the presence of a metal organic framework (MOF) catalyst with less than 0.5 mol % of any potassium or quaternary ammonium salts present based on moles of alkylene oxide feed in a reaction zone under reaction conditions to form a cyclic carbonate product. The cyclic carbonate product may be optionally fed as a crude carbonate product that does not undergo any purification or separation, other than the optional removal of any portion of unreacted alkylene oxide, carbon dioxide, and light hydrocarbon gases, to a second reaction zone containing a transesterification catalyst along with an aliphatic monohydric alcohol. The cyclic carbonate product and monohydric alcohol are allowed to react under reaction conditions to form the dialkyl carbonate and diol products.

Abstract: A method of forming a cyclic carbonate product is carried out by reacting an alkylene oxide, such as ethylene oxide, with carbon dioxide in the presence of a metal organic framework (MOF) catalyst with less than 0.5 mol % of any potassium or quaternary ammonium salts present based on moles of alkylene oxide feed in a reaction zone under reaction conditions to form a cyclic carbonate product. The cyclic carbonate product may be optionally fed as a crude carbonate product that does not undergo any purification or separation, other than the optional removal of any portion of unreacted alkylene oxide, carbon dioxide, and light hydrocarbon gases, to a second reaction zone containing a transesterification catalyst along with an aliphatic monohydric alcohol. The cyclic carbonate product and monohydric alcohol are allowed to react under reaction conditions to form the dialkyl carbonate and diol products.

Abstract: Dialkyl carbonate and diol products are prepared in an integrated process performed by reacting an alkylene oxide with carbon dioxide in the presence of a non-halide-containing homogeneous carbonation catalyst in a first reaction zone to form a crude cyclic carbonate product. The crude cyclic carbonate product is introduced along with an aliphatic monohydric alcohol to a second reaction zone containing a transesterification catalyst. The transesterification catalyst is comprised of a strongly basic Type I ion exchange resin in gel having a particular form. The cyclic carbonate product and monohydric alcohol are reacted to form the dialkyl carbonate and diol products. In another aspect, dialkyl carbonate and diol products are prepared in an integrated process wherein a halide-containing homogeneous carbonation catalyst is used to form a crude cyclic carbonate product that is then used in a transesterification reaction.

Abstract: A method for making a syngas mixture is accomplished by introducing a gaseous feed mixture containing carbon dioxide and hydrogen into a reactor containing a non-zinc catalyst. The catalyst contacts the gaseous feed mixture to form syngas mixture reaction products. The reaction takes place in the presence of nickel-containing and/or iron-containing materials. The gaseous feed mixture is introduced into the reactor at a reactor inlet temperature of from 700° C. to 800° C., with the reaction being carried out at substantially adiabatic conditions or wherein the syngas mixture reaction products are removed from the reactor at a reactor outlet temperature of from 500° C. to 600° C.

Abstract: A catalyst for oxidative dehydrogenation of organic compounds is provided by forming a solution of catalyst precursor components comprised of Fe+3 and Zn+2 cations and at least one other modifier element cation in water to form an aqueous solution of the catalyst precursor components. The modifier element cation has a standard reduction potential of from greater than about ?2.87 E° (V) to less than about ?0.036 E° (V) with a valence of +2. A base is separately and simultaneously added to the aqueous solution in amounts to maintain the pH of the aqueous solution at a pH of from about 8.5 to about 9.5 as the catalyst precursor components. The catalyst precursor components are allowed to react and precipitate out of solution as a precipitate. The resulting precipitate is calcined to form a modified zinc ferrite catalyst compound.

Abstract: Dialkyl carbonate and diol products are prepared in an integrated process performed by reacting an alkylene oxide with carbon dioxide in the presence of a non-halide-containing homogeneous carbonation catalyst in a first reaction zone to form a crude cyclic carbonate product. The crude cyclic carbonate product is introduced along with an aliphatic monohydric alcohol to a second reaction zone containing a transesterification catalyst. The transesterification catalyst is comprised of a strongly basic Type I ion exchange resin in gel having a particular form. The cyclic carbonate product and monohydric alcohol are reacted to form the dialkyl carbonate and diol products. In another aspect, dialkyl carbonate and diol products are prepared in an integrated process wherein a halide-containing homogeneous carbonation catalyst is used to form a crude cyclic carbonate product that is then used in a transesterification reaction.

Abstract: A method of forming a cyclic carbonate product is carried out by reacting an alkylene oxide, such as ethylene oxide, with carbon dioxide in the presence of a metal organic framework (MOF) catalyst with less than 0.5 mol % of any potassium or quaternary ammonium salts present based on moles of alkylene oxide feed in a reaction zone under reaction conditions to form a cyclic carbonate product. The cyclic carbonate product may be optionally fed as a crude carbonate product that does not undergo any purification or separation, other than the optional removal of any portion of unreacted alkylene oxide, carbon dioxide, and light hydrocarbon gases, to a second reaction zone containing a transesterification catalyst along with an aliphatic monohydric alcohol. The cyclic carbonate product and monohydric alcohol are allowed to react under reaction conditions to form the dialkyl carbonate and diol products.