Abb Lummus Global Inc.

Lummus Technology Inc.

Infineum International Limited

University of Massachusetts

Catalytic Distillation Technologies

Thomas Skourlis

Robert J Gartside

Hassan Kaleem

Jacob I Emert

Philip Dimitrov

Richard Joseph Severt

Jeremy Weber

Rudolf Faust

Charles Sumner

Robert E Trubac

Robert I Haines

Richard J Severt

Richard Severt

A method for producing highly reactive olefin polymers wherein at least 50 mol. % of the polymer chains have terminal double bonds, from an impurity-containing isobutylene or a mixed Chydrocarbyl feedstock containing isobutylene in which the water content of the feedstock is controlled to be at least equal to the content of polar impurities in the feedstock, and less than the concentration at which the water causes a decrease in vinylidene end-group selectivity.

Polymerization initiating system and method to produce highly reactive olefin functional polymers

A method for producing highly reactive olefin polymers wherein at least 50 mol. % of the polymer chains have terminal double bonds, from an isobutylene or a mixed Chydrocarbyl feedstock containing isobutylene. To achieve a viable process, water is added to the catalyst stream or the feedstock in the overall range of 0.05 mM to less than 5 mM per liter of feedstock.

This invention relates to thioetherification processes for the removal of mercaptans in charge gas streams. In particular, the invention relates to thioetherification processes for the removal of mercaptans using a catalyst comprising palladium and silver.

Thioetherification processes for the removal of mercaptans from gas streams

An apparatus is described for the preferential conversion to 2-butene of a stream containing C4 compounds including 1-butene and 2-butene involving mixing the C4 stream with a first hydrogen stream to form a feed stream, hydroisomerizing the feed stream in the presence of a first hydroisomerization catalyst in order to convert at least a portion of the 1-butene to 2-butene, thereby producing a hydroisomerization effluent, passing the hydroisomerization effluent through a fractionation column to form a top stream comprising isobutane and isobutylene and a bottoms stream comprising 2-butene, withdrawing a recycle stream from said fractionation column at a location above the feed point at which the weight ratio of 1-butene to 2-butene is high, and combining the recycle stream with at least one of the C4 stream and the feed stream upstream from the hydroisomerization catalyst.

Apparatus for the double bond hydroisomerization of butenes

A process is disclosed for the preferential conversion to 2-butene of a C4 stream containing 1-butene and 2-butene. The process involves mixing the C4 stream with a first hydrogen stream to form a feed stream, hydroisomerizing the feed stream in the presence of a first hydroisomerization catalyst in order to convert at least a portion of the 1-butene to 2-butene, thereby producing a hydroisomerization effluent, separating the hydroisomerization effluent in a fractionation column having an upper end and a lower end to form a 1-butene mixture at the upper end, a top effluent stream containing isobutane and isobutylene and a bottoms stream containing 2-butene, and hydroisomerizing the 1-butene mixture at the upper end of the column using a second hydroisomerization catalyst. A corresponding apparatus also is disclosed.

Double bond hydroisomerization of butenes

A process is disclosed for the preferential conversion to 2-butene of a stream containing C4 compounds including 1-butene and 2-butene. The process involves mixing the C4 stream with a first hydrogen stream to form a feed stream, hydroisomerizing the feed stream in the presence of a first hydroisomerization catalyst in order to convert at least a portion of the 1-butene to 2-butene, thereby producing a hydroisomerization effluent, passing the hydroisomerization effluent through a fractionation column to form a top stream comprising isobutane and isobutylene and a bottoms stream comprising 2-butene, withdrawing a recycle stream from said fractionation column at a location above the feed point at which the weight ratio of 1-butene to 2-butene is high, and combining the recycle stream with at least one of the C4 stream and the feed stream upstream from the hydroisomerization catalyst. A corresponding apparatus also is disclosed.

Process for the double bond hydroisomerization of butenes

A process for the selective hydrogenation of one or more alkyne and/or one or more diene in an olefin-containing hydrocarbon feed includes contacting the hydrocarbon feed with a catalyst under selective hydrogenation conditions, the catalyst including from about 0.01 to about 0.1 weight percent palladium and from about 0.005 to about 0.6 weight percent of at least one Group IB metal incorporated into an inorganic support, wherein the surface area of the support is from about 2 to about 20 m/g, the pore volume is greater than about 0.4 cc/g, at least about 90% of the pore volume is contained in pores with pore diameters larger than about 500 &#x212b;, and the pore volume of the pores with a pore diameter from about 500 to about 1,000 &#x212b; comprise from about 1% to about 2% of the total pore volume.

Process for the selective hydrogenation of alkynes and/or dienes in an olefin-containing hydrocarbon stream

Presented is an improvement to a previous invention involving the catalytic hydrogenation of the C to C and heavier acetylenes and dienes in a thermally cracked feed stream without significantly hydrogenating the C and C olefins. The improvement involves the use of a fixed bed hydrogenation reactor system in combination with a modified version of the catalytic distillation unit used in the prior art. The modification to the catalytic distillation unit involves improvement of the liquid recycle scheme. The fixed bed reactors combined with the modified catalytic distillation allows for 100% conversion of acetylene and helps to maintain high conversion of the other dienes and acetylenes with no ethylene or propylene conversion under a variety of conditions. These condition variations include but are not limited to the feed diene and acetylene composition, the mol % carbon monoxide in the feed, and catalyst deactivation. With catalytic distillation alone, complete conversion of the acetylene as stated above can not be achieved without ethylene loss, nor would satisfactory operation and control be possible under the variety of conditions experienced during a commercial operation.

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Basking Ridge, NJ, United States of America

Thomas Skourlis