Catalytic methods for synthesis of super linear alkenyl arenes and alkyl arenes are provided. The methods are capable of synthesizing super linear alkyl and alkenyl arenes from simple arene and olefin starting materials and with high selectivity for linear coupling. Methods are also provided for making a 2,6-dimethylnapthalene (DMN) or 2,6-methylethylnapthalene (MEN).

Catalytic methods for synthesis of super linear alkenyl arenes and alkyl arenes are provided. The methods are capable of synthesizing super linear alkyl and alkenyl arenes from simple arene and olefin starting materials and with high selectivity for linear coupling. Methods are also provided for making a 2,6-dimethylnapthalene (DMN) or 2,6-methylethylnapthalene (MEN).

The present invention relates to a reactor for non-oxidative direct conversion of methane and a method of manufacturing ethylene and an aromatic compound using the same. More particularly, the present invention relates to a reactor for non-oxidative direct conversion of methane in which a catalytic reaction velocity is maximized, the production of coke is minimized, and a high conversion rate of methane and a high yield of ethylene and an aromatic compound are ensured when ethylene and the aromatic compound are manufactured from methane, and a method of manufacturing ethylene and an aromatic compound using the same.

Disclosed are processes for rejuvenating catalysts comprising at least one Group 10 metal and a microporous crystalline metallosilicate, and hydrocarbon conversion processes including such rejuvenation processes. In an aspect, the rejuvenation process comprises contacting a deactivated catalyst comprising at least one Group 10 metal and a microporous crystalline metallosilicate with an oxygen-containing gaseous stream under conditions comprising a temperature ranging from about 250° C. to about 375° C. and a pressure of up to about 100 bar. In a further aspect, the rejuvenation process comprises contacting a deactivated catalyst comprising at least one Group 10 metal, at least one rare earth metal, and a microporous crystalline metallosilicate with an oxygen-containing gaseous stream under conditions comprising a temperature ranging from about 250° C. to about 500° C. and a pressure of up to about 100 bar.

Disclosed are a catalytic method and system for producing aromatic hydrocarbons from aliphatic hydrocarbons or light naphtha. In an aspect, the process comprises adding a diluent comprising a heavy aromatic hydrocarbon (for example, C.sub.7-C.sub.9+) to a reactor feedstock comprising aliphatic hydrocarbons (for example, C.sub.6-C.sub.8) or light naphtha to form a reactor feed stream, such that the heat capacity of reactor feed stream is higher than the heat capacity of feedstock. The reactor feed stream is heated and contacting with a catalyst under conditions sufficient to aromatize at least a portion of the aliphatic hydrocarbons and form a product stream comprising a primary aromatic hydrocarbon product and a heavy aromatic hydrocarbon product. In an aspect, the diluent can comprise a heavy aromatic hydrocarbon having at least one carbon atom more than the primary aromatic hydrocarbon product.

The present disclosure relates to processes that catalytically convert a hydrocarbon feed stream predominantly comprising both isopentane and n-pentane to yield upgraded hydrocarbon products that are suitable for use either as a blend component of liquid transportation fuels or as an intermediate in the production of other value-added chemicals. The hydrocarbon feed stream is isomerized in a first reaction zone to convert at least a portion of the n-pentane to isopentane, followed by catalytic-activation of the isomerization effluent in a second reaction zone with an activation catalyst to produce an activation effluent. The process increases the conversion of the hydrocarbon feed stream to olefins and aromatics, while minimizing the production of C1-C4 light paraffins. Certain embodiments provide for further upgrading of at least a portion of the activation effluent by either oligomerization or alkylation.

The present disclosure relates to processes that catalytically convert a hydrocarbon feed stream predominantly comprising both isopentane and n-pentane to yield upgraded hydrocarbon products that are suitable for use either as a blend component of liquid transportation fuels or as an intermediate in the production of other value-added chemicals. The hydrocarbon feed stream is isomerized in a first reaction zone to convert at least a portion of the n-pentane to isopentane, followed by catalytic-activation of the isomerization effluent in a second reaction zone with an activation catalyst to produce an activation effluent. The process increases the conversion of the hydrocarbon feed stream to olefins and aromatics, while minimizing the production of C1-C4 light paraffins. Certain embodiments provide for further upgrading of at least a portion of the activation effluent by either oligomerization or alkylation.

A method for converting an alcohol to a jet-diesel hydrocarbon fraction, comprising contacting the alcohol with a pillared two-dimensional zeolite catalyst at a temperature of at least 200 C. and up to 500 C. to convert the alcohol to hydrocarbons comprising: (a) a first mixed olefin fraction containing a mixture of C.sub.2-C.sub.5 olefins; (b) a first paraffin fraction containing C.sub.3-C.sub.5 paraffins; and (c) a gasoline fraction containing C.sub.6.sup.+ hydrocarbons; and the conversion of the alcohol is energy neutral or exothermic. The first mixed olefin fraction may be subjected to an oligomerization process to result in a second paraffin fraction containing C.sub.3-C.sub.6 paraffins along with a C.sub.7.sup.+ partially unsaturated fraction, and the first and second paraffin fractions combined into a total C.sub.3-C.sub.6 paraffin fraction, which can in turn be subjected to a dehydrogenation or aromatization process with hydrogen gas as byproduct, and the hydrogen gas recycled for use in producing the jet-diesel fraction.

A method for converting an alcohol to a jet-diesel hydrocarbon fraction, comprising contacting the alcohol with a pillared two-dimensional zeolite catalyst at a temperature of at least 200 C. and up to 500 C. to convert the alcohol to hydrocarbons comprising: (a) a first mixed olefin fraction containing a mixture of C.sub.2-C.sub.5 olefins; (b) a first paraffin fraction containing C.sub.3-C.sub.5 paraffins; and (c) a gasoline fraction containing C.sub.6.sup.+ hydrocarbons; and the conversion of the alcohol is energy neutral or exothermic. The first mixed olefin fraction may be subjected to an oligomerization process to result in a second paraffin fraction containing C.sub.3-C.sub.6 paraffins along with a C.sub.7.sup.+ partially unsaturated fraction, and the first and second paraffin fractions combined into a total C.sub.3-C.sub.6 paraffin fraction, which can in turn be subjected to a dehydrogenation or aromatization process with hydrogen gas as byproduct, and the hydrogen gas recycled for use in producing the jet-diesel fraction.

Methods for producing supported catalysts containing a transition metal and a bound zeolite base are disclosed. These methods employ a step of impregnating the bound zeolite base with the transition metal, fluorine, and high loadings of chlorine. The resultant high chlorine content supported catalysts have improved catalyst activity in aromatization reactions.