Uop Lcc

Cytec Industries Inc.

Susie C Martins

Alakananda A Bhattacharyya

Douglas A Nafis

Erin Marie Broderick

Avram Michael Buchbinder

Stuart Smith

Kaitlin M DeSalvo

Paul T Barger

Trung S Pham

Kurt A Detrick

Christopher P Nicholas

Tom N Kalnes

Paula L Bogdan

Bryan K Glover

Zhanping Xu

Robert J Schmidt

David A Wegerer

Stuart R Miller

Suheil F Abdo

Hayim Abrevaya

Maureen L Bricker

Lisa M Knight

Paul Olson

Richard R Willis

Wharton Sinkler

Wei Pan

Joel T Walenga

David E Mackowiak

Carl John Stevens

Gregory B Kuzmanich

Dana K Sullivan

Praneeth Dayanthe Edirisinghe

Donato Nucciarone

Sean Glennon Thomas Mueller

Michael Brendel

Melanie Timmons Schaal

Alakananda Bhattacharyya

A hydroprocessing catalyst with improved performance has been produced that involves an intimately mixed unsupported metal oxide with a zeolite or other acid function. The intimate mixing allows an intimate interaction between the unsupported metal oxide and the acid function. The hydroprocessing catalyst may be used alone or may be incorporated with a portion of a conventional hydrocracking catalyst.

High activity and high distillate yield hydrocracking catalysts with intimate interaction between unsupported metal oxide and zeolite

A process for sulfuric acid catalyzed alkylation involving the use of surfactants which form bi-continuous micro-emulsions with the sulfuric acid and the hydrocarbon is described. The bi-continuous phase facilitates and improves the sulfuric acid catalyzed alkylation reactions. The concentration of the surfactant is selected based on the type of olefin feed. Easy to alkylate feeds, such as 2-butene, use lower concentrations of surfactant, while feeds which are harder to alkylate, such as propene or isobutene, use higher concentrations of the surfactant. In addition, increasing the concentration of sulfuric acid when a surfactant is included resulted in higher calculated RON. The use of a surfactant and a high concentration of sulfuric acid can provide a calculated RON over 100 and close to theoretical yields.

Sulfuric acid catalyzed alkylation process

A trialkylphosphonium haloaluminate compound having a formula: where R, R, and Rare the same or different and each is independently selected from Cto Chydrocarbyl; and X is selected from F, Cl, Br, I, or combinations thereof is described. An ionic liquid catalyst composition incorporating the trialkylphosphonium haloaluminate compound, methods of making the trialkylphosphonium haloaluminate compound, and alkylation processes incorporating the trialkylphosphonium haloaluminate compound are also described.

Trialkylphosphonium ionic liquids, methods of making, and alkylation processes using trialkylphosphonium ionic liquids

An integrated process for gasoline production is described. The process includes introducing a feed comprising n-Chydrocarbons into a disproportionation reaction zone in the presence of a disproportionation catalyst to form a disproportionation mixture comprising iso-Cand Cdisproportionation products and unreacted n-Chydrocarbons. An iso-Chydrocarbon stream and an olefin feed are introduced into an alkylation reaction zone in the presence of an alkylation catalyst to produce an alkylation mixture comprising alkylate and unreacted iso-Cparaffins. The disproportionation mixture and the alkylation mixture are combined, and the combined mixture is separated into at least a stream comprising the alkylate product, an iso-Cstream, and an unreacted n-Chydrocarbon stream. The iso-Cstream is recycled to the alkylation reaction zone, and the unreacted n-Chydrocarbon stream is recycled to the disproportionation reaction zone. The stream comprising the alkylate product is recovered.

Integrated process for gasoline production

A process utilizing an ionic liquid is described. The process includes contacting a hydrocarbon feed with an ionic liquid component, the ionic liquid component comprising a mixture of a first ionic liquid and a viscosity modifier, wherein a viscosity of the ionic liquid component is at least about 10% less than a viscosity of the first ionic liquid.

Viscosity modifiers for decreasing the viscosity of ionic liquids

A process in which the conductivity of an ionic liquid catalyst used in a continuous reaction process is measured in order to determine the amount of conjunct polymer associated with the ionic liquid catalyst. The conductivity may be used to control: an amount of spent ionic liquid catalyst passed back to the reaction zone; an amount of spent ionic liquid catalyst passed to a regeneration zone; an amount of spent ionic liquid catalyst removed from the continuous reaction process; an amount of fresh ionic liquid catalyst passed to the reaction zone; an amount of regenerated ionic liquid catalyst passed to the reaction zone; or combinations thereof.

Process for controlling an ionic liquid catalyst regeneration using a conductivity measurement

Alkylation processes are described. The processes utilize ionic liquid catalysts having a kinematic viscosity range of about 50 cSt to about 100 cSt at 25&#xb0; C. Catalysts within this range produce alkylate having higher octane than catalysts outside this range, especially at higher process temperatures which are preferable from an operating cost standpoint. The alkylate can have one or more of a research octane number of at least about 93, a selectivity of Cof at least about 65%, and a mole ratio of trimethylpentane to dimethylhexane of greater than about 7:1.

Process for alkylation using ionic liquid catalysts

An alkylation process utilizing less than 10 vol % of a halometallate based ionic liquid catalyst is described. By decreasing the catalyst volume fraction, the level of subsequent undesirable reactions may be minimized. The total residence time is typically in the range of about 1 min to about 30 min. The alkylate typically has a research octane number of at least about 93, and the olefin conversion is typically at least about 96%.

Process for alkylation using low ionic liquid volume fraction

One or more processes for recovering entrained ionic liquid from a hydrocarbon phase containing droplets of ionic liquid are described. The processes includes contacting the hydrocarbon phase containing the droplets of ionic liquid with a retaining material in a separation zone. The droplets of ionic liquid are retained by the retaining material. The ionic liquid may be recovered from the retaining material with a solvent or desorbent. The retaining material may be regenerated and the ionic liquid may be reactivated. The retaining material may be used in a wash vessel to retain or remove contaminant solids within the reactor or other vessels.

Processes for removing entrained ionic liquid from a hydrocarbon phase

A method for regenerating deactivated acidic ionic liquid is described. The method involves reducing a level of free hydrochloric acid in the deactivated acidic ionic liquid in a removal zone using at least one of heat, a stripping fluid, reduced pressure, and liquid-liquid extraction to form a deactivated acidic ionic liquid having a reduced level of free hydrochloric acid; and regenerating the deactivated acidic ionic liquid having the reduced level of free hydrochloric acid.

Hydrochloric acid stripping process for ionic liquid regeneration process

An integrated hydrocarbon conversion process is described. The process includes contacting a heavy hydrocarbon feedstock with a hydrocarbon cracking catalyst in a fluidized reactor zone to produce light olefins to form a fluid catalytic cracker (FCC) effluent stream comprising a range of hydrocarbons. The FCC effluent stream is separated to form at least a stream rich in Chydrocarbons which comprises isobutane and 1-butene. The stream rich in Chydrocarbons is introduced into an alkylation reaction zone where the isobutane and the 1-butene are alkylated to form a reaction product mixture comprising dimethylhexanes and Chydrocarbons. The reaction product mixture is dehydrocyclized to form a stream rich in xylenes.

Integrated fluid catalytic cracking and alkylation process

A method of quantifying an amount of Br&#xf8;nsted acid sites in an aluminum chloride-containing catalyst is described. The method involves adding a known amount of at least one silane or borane compound to the aluminum chloride-containing catalyst being analyzed. The Br&#xf8;nsted acid sites in the aluminum chloride-containing catalyst react with the silane or borane compound to form a silyl boryl compound, resulting in a catalyst phase and a hydrocarbon phase which contains the silyl or boryl compound. The amount of silyl or boryl compound in the hydrocarbon phase is measured. From the measured amount of silyl or boryl compound formed, the amount of Br&#xf8;nsted acid sites can be determined.

Method for quantitation of acid sites in acidic catalysts using silane and borane compounds

A method of quantifying an amount of Br&#xf8;nsted acid sites in an acidic ionic liquid is described. The method involves adding a known amount of at least one silane or borane compound to the acidic ionic liquid being analyzed. The Br&#xf8;nsted acid sites in the acidic ionic liquid react with the silane or borane compound to form a silyl or boryl compound, resulting in an ionic liquid phase and a hydrocarbon phase which contains the silyl or boryl compound. The amount of silyl or boryl compound in the hydrocarbon phase is measured. From the measured amount of silyl or boryl compound formed, the amount of Br&#xf8;nsted acid sites can be determined.

Method for quantitation of acid sites in acidic ionic liquids using silane and borane compounds

A hydrocarbon conversion process is described. The process involves contacting a hydrocarbon feed with a lactamium based ionic liquid catalyst in a reaction zone under reaction conditions to form a mixture comprising reaction products, and the lactamium based ionic liquid catalyst. Typical hydrocarbon conversion processes include alkylation, oligomerization, isomerization, disproportionation, and reverse disproportionation.

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Carol Stream, IL, United States of America

Susie C Martins