Uop Lcc

Cytec Industries Inc.

Douglas A Nafis

Susie C Martins

Alakananda A Bhattacharyya

Erin Marie Broderick

Avram Michael Buchbinder

Kaitlin M DeSalvo

Ralph D Gillespie

Lynn H Rice

Trung S Pham

Gregory F Maher

Stuart Smith

Kurt A Detrick

Michelle J Cohn

William D Schlueter

David S Lafyatis

Eric Leeton

Tom N Kalnes

Paul T Barger

Bryan K Glover

Zhanping Xu

David A Wegerer

Robert L Mehlberg

Huping Luo

Hye Kyung Timken

Paul Olson

Bong-Kyu Chang

Matthew Lippmann

Sean G Mueller

Michael John Girgis

Elizabeth Carter

Gregory J Schrad

Donato Nucciarone

Michael Brendel

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

Processes for regenerating ionic liquid catalyst by contacting the ionic liquid catalyst with hydrogen gas in a regeneration reactor. The amount of hydrogen is less than 550 SCF/BBL (97.96 m/m) of spent ionic liquid catalyst, or less than 500 SCF/BBL (89.05 m/m) of spent ionic liquid catalyst, or between 550 and 45 SCF/BBL (97.96 and 8.015 m/m) of spent ionic liquid catalyst, or between 500 and 50 SCF/BBL (89.05 and 8.905 m/m) of spent ionic liquid catalyst. Alkylation processes are also disclosed.

Ionic liquid catalyst regeneration with reduced hydrogen amounts

A process for treating an ionic liquid containing waste stream is described. If there is a liquid waste stream, the liquid waste stream is introduced into a liquid treatment zone. The ionic liquid in the liquid waste stream is neutralized. The concentration of the ionic liquid in the liquid waste stream is determined, and the allowed concentration of the ionic liquid in the liquid waste stream is determined. The concentration of the ionic liquid in the neutralized liquid waste stream is reduced to the allowed concentration, and the liquid waste stream having the allowed concentration is released. If there is a vapor waste stream, the vapor waste stream is introduced into a vapor treatment zone. The vapor waste stream is treated to form a treated vapor waste stream, and the treated vapor waste stream is released to a plant vapor treatment zone.

Ionic liquid waste handling system

The present invention involves processes and equipment for handling chloride in an ionic liquid alkylation system. The processes involve not only breaking down the organic chloride to active HCl for ionic liquid activation, but also recovering HCl in the effluent downstream to maintain the HCl requirements while also reducing HCl emissions. This equipment may be used in conjunction with an isomerization reaction zone which is integrated into the ionic liquid alkylation process to further isomerize n-paraffins to isoparaffins for recycle to the alkylation reaction zone.

Chloride management in ionic liquid alkylation processes

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

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

A method of controlling a hydrocarbon conversion process is described. The method involves introducing a reactant into a reaction zone containing an ionic liquid catalyst. The reaction zone has at least two zones. The mass transfer resistance in the second zone is greater than the mass transfer resistance in the first zone.

Selectivity of ionic liquid alkylation

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 process for making an alkylate is presented. The process includes mixing an isoparaffin stream with an olefin stream in an alkylation reactor. The alkylation reactor includes a catalyst for performing the reaction. The catalyst is an ionic liquid that is a quaternary chloroaluminate based ionic liquid, and the reaction is performed at or near ambient temperatures.

Alkylation process using phosphonium-based ionic liquids

A hydrocarbon conversion process is described. The process includes contacting a hydrocarbon feed with an acidic catalyst under hydrocarbon conversion conditions in a hydrocarbon conversion zone. The hydrocarbon feed reacts to form a mixture comprising reaction products, the acidic catalyst, and deactivated acidic catalyst containing conjunct polymer. The mixture is separated into at least two streams, a first stream comprising the reaction products and a second stream comprising the deactivated acidic catalyst. The reaction products are recovered. The deactivated acidic catalyst is contacted with at least one silane or borane compound in a regeneration zone under regeneration conditions, the conjunct polymer reacting with the at least one silane or borane compound resulting in a catalyst phase and an organic phase containing the conjunct polymer and at least one silyl or boryl compound.

Hydrocarbon conversion process including catalyst regeneration

A method of regenerating an acidic catalyst is described. A borane compound is contacted with an acidic catalyst that contains conjunct polymer, which releases the conjunct polymer from the acidic catalyst. The acidic catalyst can then be re-activated with acid. The conjunct polymer can be separated from the borane compound, and the borane compound can be recycled.

Regeneration of an acidic catalyst by borane addition

A process for making an alkylate is presented. The process includes mixing an isoparaffin stream with an olefin stream in an alkylation reactor. The alkylation reactor includes a catalyst for performing the reaction. The catalyst is an ionic liquid that is a quaternary phosphonium based ionic liquid, and the reaction is performed at or near ambient temperatures.

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Mount Prospect, IL, United States of America

Douglas A Nafis