Uop Lcc

Hayim Abrevaya

Tamotsu Imai

Suheil F Abdo

Bipin Virpal Vora

Anil Rajaram Oroskar

Avram Michael Buchbinder

Joel T Walenga

R Lyle Patton

Alakananda A Bhattacharyya

Stephen T Wilson

Gavin Paul Towler

Paul T Barger

Robert R Frame

Laurence O Stine

Erin Marie Broderick

Deng-Yang Jan

Stanley Joseph Frey

Gregory J Gajda

Michael A Schultz

Jeffery C Bricker

Richard R Willis

Francis Stephen Lupton

Stuart Smith

John E Bauer

Karl Z Steigleder

Julio C Marte

Ben A Wilson

Shurong Yang

Deng Yang Jan

W Patrick Dennler

Christopher P Nicholas

Tom N Kalnes

Antoine Negiz

Andrea G Bozzano

Timothy A Brandvold

Susan C Koster

Lubo Zhou

Christopher D Gosling

Lisa M Knight

John Anthony Petri

Nancy E Iwamoto

Susie C Martins

Gregory R Werba

Wharton Sinkler

David E Mackowiak

Mary Jo Wier

Thomas A Verachtert

Phuong T M Do

Raymond Shih

Lance Lyle Jacobsen

Lisa M Lane

William M Targos

Rodrigo J Lobo

Suleyman M Ozmen

Falaah Falih

Robert L Zhou

Den-Yang Jan

A process is provided of treating a feed comprising polyethylene terephthalate comprising dissolving said feed in a polar solvent at a temperature between about 100 to 250&#xb0; C. to produce a dissolved feed; then adding an anti-solvent that is less polar than said polar solvent followed by cooling a resulting mixture resulting in precipitation of purified polyethylene terephthalate and then separation of solid purified polyethylene terephthalate from remaining liquids.

Solvent based approach to post-consumer recycling of polyethylene terephthalate

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 method is provided for synthesizing an aromatic carboxylic acid compound comprising providing an aromatic compound or an aromatic compound with at least one carboxylic group; providing a metal hydroxide and at least one carboxylate to produce a mixture; and adding carbon dioxide to the mixture under pressures from about atmospheric to 1000 psig and sufficient heat for a time sufficient to produce aromatic carboxylic acid compounds. The aromatic carboxylic acid compounds may include terephthalic acid, naphthalic acid, thiophene dicarboxylic acid, pyridine dicarboxylic acid, carbazole dicarboxylic acid, and dibenzothiophene dicarboxylic acid.

Process for the synthesis of aromatic dicarboxylic acids

A process is provided for making a polymer comprising providing a mixture of at least one furandicarboxylic acid, at least one diol, and at least one C2-C3 dicarboxlic acid, ester derivatives of C2-C3 dicarboxylic acid, hydroxy fatty acid or ester derivative of a hydroxy fatty acid; adding a catalyst and processing said mixture at reaction conditions until a polymer product is produced. The polymer consists of random units based upon the starting materials that are used.

Polymers containing aromatic dicarboxylic acid

A process and apparatus for making aromatics are described. The process includes reforming a naphtha stream in a reforming zone to form a reformer effluent comprising aromatic compounds and non-aromatic compounds, wherein at least a portion of the aromatic compounds contain alkyl groups. The reformer effluent is heated and passed directly to an acid cracking reaction zone. The non-aromatic compounds are selectively cracked and at least a portion of the alkyl groups on the aromatic compounds are selectively dealkylated in the presence of an acid cracking catalyst to form a cracked reformer effluent comprising the aromatic compounds and cracked olefins.

Olefin and BTX production using aliphatic cracking reactor

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 catalyst composition comprising a support comprising a mixture of amorphous silica-alumina and non-zeolitic alumina comprising no more than 75 wt % amorphous silica-alumina and having a ratio of moles of silicon to moles of aluminum in the range of about 0.05 to about 0.50. A first hydrogenation metal comprising platinum, a second hydrogenation metal from Group VIIB or Group VIII of the Periodic Table other than platinum and an optional third metal from Group IA of the Periodic Table may be deposited on the support. The ratio of moles of silicon to the moles of the first hydrogenation metal, the second hydrogenation metal and the optional third metal on the support may be between about 15 and about 75.

Composition for opening polycyclic rings in hydrocracking

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

Processes and apparatuses for the production of propylene are provided. In an embodiment, a process is provided for production of propylene from an oxygenate feed comprising passing the oxygenate feed to an oxygenate-to-olefin reactor to contact the oxygenate feed with a catalyst to provide an effluent stream comprising olefins comprising ethylene, propylene and butylene. The effluent stream is separated in a product separation zone to generate a propylene product stream, an ethylene stream and a C+ stream. The ethylene stream is reacted in an ethylene dimerization or oligomerization reactor in presence of a dimerization or oligomerization catalyst to provide a first process stream. The C+ stream and the first process stream are cracked in a cracking reactor under cracking conditions to provide a cracked stream comprising additional amounts of ethylene and propylene. Finally, the cracked stream is passed to the product separation zone to recover additional amounts of propylene.

Processes and apparatuses for production of polypropylene

A flexible process for gasoline refineries is described. The process can vary depending on the available feedstock and the desired products. At one time, the process can involve disproportionating pentanes to a product mixture including isobutane and isohexane. At other times, by switching the feedstock and operating conditions, the process can convert a mixture of Cand Cparaffins to a low aromatic blendstock with suitable octane and a vapor pressure lower than butanes. The process can be performed in separate stand-alone units operated at different times, or a single unit can be operated according to one process at one time and according to the other process at another time.

Flexible gasoline process using multiple feedstocks

A process of making terephthalic acid or a derivative of terephthalic acid is described. The process includes reacting a derivative of 2,5-dimethylfuran, with a dienophile containing an unsaturated 2-carbon unit, in the presence of a catalyst having Br&#xf6;nsted acidity to form a para-xylene derivative; and optionally reacting the para-xylene derivative to terephthalic acid.

Processes and catalysts for conversion of 2,5-dimethylfuran derivatives to terephthalate

A reverse disproportionation reaction of two hydrocarbon feeds allows production of a reaction mixture containing products with intermediate carbon numbers. The amount of at least one of the products with intermediate carbon numbers is equal to or greater than the amount formed from disproportionation of the hydrocarbon alone. A reverse disproportionation reaction mixture is also described.

Catalytic reverse disproportionation of paraffins using ionic liquids

The present invention comprises a hydrocarbon-conversion process using an improved MgMxAPSO-31 molecular sieve which demonstrates a favorable combination of conversion and selectivity in aromatics conversion. The sieve comprises at least two divalent elements with narrow specific concentration limits in the framework structure having defined crystal characteristics. The element Mx may comprise one or more of manganese, cobalt, nickel, iron and zinc.

Hydrocarbon conversion using an improved molecular sieve

A process for forming a zeolite beta dielectric layer onto a substrate such as a silicon wafer has been developed. The zeolite beta is characterized in that it has an aluminum concentration from about 0.1 to about 2.0 wt. %, and has crystallites from about 5 to about 40 nanometers. The process involves first dealuminating a starting zeolite beta, then preparing a slurry of the dealuminated zeolite beta followed by coating a substrate, e.g. silicon wafer with the slurry, heating to form a zeolite beta film and treating the zeolite beta with a silylating agent.

Process for preparing a dielectric interlayer film containing silicon beta zeolite

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Kenilworth, IL, United States of America

Hayim Abrevaya