Mobil Oil Corporation

Other

Jorge L Soto

Amos A Avidan

Margaret Nemet-Mavrodin

Hartley Owen

Samuel A Tabak

David L Johnson

Kenneth J Del Rossi

Tai-Sheng Chou

Sergei Yurchak

Francis P Ragonese

The present invention provides a Lewis acid-catalyzed isoparaffin/olefin alkylation process in which acid consumption and energy costs are decreased by employing an acid sorption stage to separate the Lewis acid catalyst from the alkylate product stream, or from a selected fraction of the alkylate product stream, and desorbing the Lewis acid from the sorption stage with an isoparaffin-containing alkylation process feedstream.

Isoparaffin/olefin alkylation

Yield is improved in a fluid-bed catalytic paraffin aromatization process by tailoring heat transfer to match the endothermic heat load within the fluid bed.

Fluid bed paraffin aromatization

A fluid bed catalytic paraffin upgrading process is disclosed. By closely controlling catalyst particle size distribution and density, together with feedstock superficial vapor velocity, the fluid bed is maintained in a turbulent flow regime. Surprisingly, maintaining the fluid bed in a turbulent flow regime shifts the product selectivity away from methane and ethane and toward the more valuable products hydrogen, light olefins and C.sub.5 + gasoline. In the most preferred embodiment, the catalyst contains a dehydrogenation metal component such as gallium, zinc, platinum or rhenium to provide a C.sub.5+ gasoline product rich in aromatics. Catalysts useful in the inventive process include zeolites as well as layered siliceous materials.

Turbulent fluid bed paraffin conversion process

A process is disclosed for the conversion of C.sub.2 -C.sub.12 paraffinic hydrocarbons to more valuable petrochemical feedstocks including C.sub.2 -C.sub.4 olefins and C.sub.6 -C.sub.8 aromatics in the presence of a composite catalyst comprising a binder and at least one zeolite having a Constraint Index of between about 1 and 12, said composite catalyst having an alpha value of of greater than 5 and less than 33. It has been found that yields of valuable C.sub.2 -C.sub.4 olefins and C.sub.6 -C.sub.8 aromatics are increased by maintaining the composite catalyst alpha value within the claimed range.

Process for the conversion of C.sub.2 -C.sub.12 paraffinic hydrocarbons

A fluidized bed catalytic process for conversion of propene-rich light olefinic gas feedstock comprising at least 2 mol % ethene and having a C.sub.3 :C.sub.2 molar ratio of at least about 2:1 to produce hydrocarbons rich in C.sub.4.sup.+ aliphatics and aromatics, comprising maintaining a turbulent fluidized bed in a reactor operating at a moderate pressure in the range from about 400 to 2500 kPa, and temperature of about 315.degree. to 510.degree. C., the catalyst having an apparent particle density of about 0.9 to 1.6 g/cm.sup.3, a size range of about 1 to 150 microns, and average catalyst particle size of about 20 to 100 microns containing about 10 to 25 weight percent of fine particles having a particle size less than 32 microns, by passing hot feedstock vapor upwardly through the fluidized catalyst bed at a superficial fluid velocity of about 0.3 to 2 meters per second. Hydrocarbon product is recovered containing a major amount of C.sub.5.sup.+ hydrocarbons and containing C.sub.3 -C.sub.5 alkanes and alkenes in the ratio of about 0.1:1 to 200:1 and preferably at a reaction severity index (R.I.) of about 0.2:1 to 5:1.

Upgrading propene-ethene mixtures in a turbulent fluidized catalyst bed

A fluidized bed catalytic process for conversion of light olefinic gas feedstock containing ethene to produce hydrocarbons rich in C.sub.5.sup.+ liquids, comprising the steps of maintaining a fluidized bed of zeolite catalyst particles in a turbulent reactor bed at a temperature of about 315.degree. to 510.degree. C., said catalyst having an apparent particle density of about 0.9 to 1.6 g/cm.sup.3 and a size range of about 1 to 150 microns, and average catalyst particles size of about 20 to 100 microns containing about 10 to 25 weight percent of fine particles having a particle size less than 32 microns; passing hot feedstock vapor upwardly through the fluidized catalyst bed under turbulent flow conditions; maintaining turbulent fluidized bed conditions through the reactor bed between transition velocity and transport velocity at a superficial fluid velocity of about 0.3 to 2 meters per second; and recovering hydrocarbon product containing a major amount of C.sub.5.sup.+ hydrocarbons and containing C.sub.3 -C.sub.5 alkanes and alkenes in the ratio of about 0.2:1 to 5:1.

Growing community of inventors

Sewell, NJ, United States of America

Jorge L Soto