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Avram Michael Buchbinder

Susie C Martins

Alakananda A Bhattacharyya

Erin Marie Broderick

Douglas A Nafis

Hayim Abrevaya

Kurt A Detrick

Stanley Joseph Frey

Gavin Paul Towler

Zhanping Xu

Trung S Pham

Stuart Smith

Wei Pan

Paul T Barger

Robert J Schmidt

David A Wegerer

John Joseph Senetar

Robert L Mehlberg

Timothy A Brandvold

Richard A Johnson, Ii

Nancy E Iwamoto

Paul Olson

John A Karch

Joel T Walenga

Karl Z Steigleder

Wolfgang A Spieker

Sean G Mueller

J W Adriaan Sachtler

Nina I Kuznetsova

Phuong T M Do

David S Lafyatis

Praneeth Dayanthe Edirisinghe

Raymond Shih

Xi Zhao

Kaitlin M DeSalvo

Donato Nucciarone

Falaah Falih

Michael Brendel

Sean Glennon Thomas Mueller

Evan B Jorgenson

Tatsamai Jarusiripipat

A de-hydrogenation catalyst and its use in dehydrogenation of hydrocarbons. The catalyst has low cracking activity and comprises gallium or gallium and platinum on an essentially non-acidic and amorphous alumina-phosphate or silica-alumina-phosphate support with an empirical chemical composition of [Al2O3][SiO2][P2O5], wherein Y is between 0 and 0.2 and Z is between 0.01 and 1.1, with a BET surface area above 50 m/g, as measured by N2 adsorption experiment.

Catalyst for propane dehydrogenation to propylene

A fluidized catalytic reactor system cycles from 0.05-5% of catalyst at a time through a rejuvenation unit to be heated in the presence of oxygen to maintain catalyst activity. The use of the rejuvenation unit that may be 2% of the size of the main catalyst regeneration unit allows for reduction in equipment size and in catalyst inventory. The catalyst that is sent to the rejuvenation unit may be spent catalyst but may be partially or fully regenerated catalyst. The rejuvenation unit may be heated by combusting fuel or by hot flue gas.

Regeneration of a dehydrogenation catalyst slip-stream

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

The process for producing light olefins comprises the steps of contacting a feed stream comprising Cto Chydrocarbons having at least 10 wt % paraffins and at least 15 wt % alkylaromatics with an acidic catalyst to form a cracked product comprising light olefins and aromatics. The catalyst comprises about 30 to about 80 wt-% of a crystalline zeolite and a low-acidic binder and may be regenerated.

Process to convert aliphatics and alkylaromatics to light olefins with acidic catalyst

A process utilizing a micro-emulsion is described. The micro-emulsion formed by contacting an ionic liquid, a co-solvent, a hydrocarbon, an optional surfactant, and an optional catalyst promoter to form the micro-emulsion. The micro-emulsion comprises a hydrocarbon component comprising the hydrocarbon and an ionic liquid component comprising the ionic liquid. The ionic liquid comprises a halometallate anion and a cation. The co-solvent has a polarity greater than a polarity of the hydrocarbon. The ionic liquid is present in an amount of 0.05 wt % to 40 wt % of the micro-emulsion. A product mixture comprising a product is produced in a process zone containing the micro-emulsion.

Hydrocarbon processes using halometallate ionic liquid micro-emulsions

A micro-emulsion and a method of making the micro-emulsion are described. The micro-emulsion includes a hydrocarbon component, an ionic liquid component, and a co-solvent. The ionic liquid comprises a halometallate anion and a cation. The micro-emulsion can optionally include a surfactant, and a catalyst promoter. The co-solvent has a polarity greater than the polarity of the hydrocarbon. The ionic liquid is present in an amount of about 0.05 wt % to about 40 wt % of the micro-emulsion.

Halometallate ionic liquid micro-emulsions

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

Hydrocarbon conversion processes using non-cyclic amide and thioamide based ionic liquids

Non-cyclic amide or thioamide based ionic liquids and methods of making them are disclosed. The non-cyclic amide or thioamide based ionic liquid comprises a cation and an anion and has the formula: 

Synthesis of non-cyclic amide and thioamide based ionic liquids

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 naphtha cracking feed stream is taken, heated and passed to a cracking reactor. Hydrogen is added to the cracking reactor to mitigate catalyst deactivation. The aliphatic compounds are selectively cracked and at least a portion of the alkyl groups on the aromatic compounds are selectively dealkylated in the presence of a cracking catalyst to produce a cracked effluent stream comprising aromatic compounds and cracked olefins.

Aliphatic cracking and dealkylation with hydrogen diluent

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

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Chicago, IL, United States of America

Avram Michael Buchbinder