Uop Lcc

Jennifer S Holmgren

Blaise J Arena

Jeffery C Bricker

Ralph D Gillespie

Leonid B Galperin

Gregory J Gajda

Timothy A Brandvold

Joseph J Alcaraz

Edwin Paul Boldingh

Laszlo T Nemeth

Santi Kulprathipanja

Stephen T Wilson

Joseph A Kocal

Paul T Barger

Thomas P Malloy

Beth McCulloch

Richard R Willis

Stanley A Gembicki

Michael W Schoonover

Peter K Nickl

Barret A Ferm

Douglas B Galloway

Edith M Flanigen

Paula L Bogdan

Robert J Schmidt

Susan C Koster

Christopher D Gosling

Robert L Patton

Paul R Kurek

David A Lesch

Richard E Marinangeli

Michelle J Cohn

Thomas M Reynolds

Michael H Quick

John I Hammerman

Paul George Blommel

Lyle E Monson

Cara Moy Roeseler

An improved catalytic composite and process are disclosed for the selective disproportionation of toluene. The process uses a layered composite comprising a catalytically active core which comprises a zeolitic aluminosilicate having a SiO:AlOratio of 8 to 50 and a relatively inactive protective mantle which preferably comprises boralite. Optionally, the composite is selectively precoked prior to toluene disproportionation. The composite and process provide improved selectivity for the production of paraxylene.

Selective disproportionation catalyst and process

A zeolitic catalyst useful in the selective disproportionation and transalkylation of toluene comprises a molecular sieve having a pore diameter of about 5 to 8 &angst;, a refractory inorganic oxide and a reduced weak non-framework metal which is believed to provide Lewis acidity.

Selective aromatics disproportionation/transalkylation catalyst

An improved process is disclosed for the selective disproportionation of toluene. The process uses a zeolitic catalyst which is oil-dropped in an amorphous aluminum phosphate binder and optionally is selectively precoked prior to toluene disproportionation. The catalyst and process provide enhanced selectivity for the production of paraxylene.

Selective aromatics disproportionation process

A process for the carbonylation of saturated hydrocarbons to give an oxygenated saturated hydrocarbon is disclosed and claimed. The process involves using an acidic ionic liquid catalyst to catalyze the carbon monoxide addition to the saturated hydrocarbon at reaction conditions to form an oxygenate. The acidic ionic liquid comprises a Lewis or Bronsted acid in combination with a quaternary nitrogen-containing compound. A specific example is a mixture of aluminum chloride and n-butylpyridinium chloride.

Direct carbonylation of paraffins using an ionic liquid catalyst

An improved catalyst and process are disclosed for the selective disproportionation of toluene. The process uses a zeolitic catalyst which is oil-dropped in an aluminum phosphate binder and has an X-ray diffraction pattern showing characteristic intensities at specified Bragg angles. Optionally, the catalyst is selectively precoked prior to toluene disproportionation. The catalyst and process provide improved selectivity for the production of paraxylene.

A process for separating one chiral compound from a mixture of chiral compounds is disclosed. The separation process involves using a chiral stationary phase (CSP) which comprises a chiral organic material deposited on an amorphous silica support having a unimodal distribution of pore sizes in the range of about 300 .ANG. to about 25,000 .ANG. and a surface area of less than about 30 m.sup.2 /g.

Process for separating chiral compounds using a unimodal large pore

An improved process is disclosed for the selective disproportionation and transalkylation of toluene. The process uses a zeolitic catalyst, preferably comprising a binder, containing a weak metal in a defined reduced state which is believed to provide Lewis acidity in the catalyst. The catalyst and process provide improved selectivity for the production of paraxylene.

Selective aromatics disproportionation/transalkylation

A hydrothermal process for preparing a modified amorphous silica has been prepared. The process involves mixing a slurry of a silica with a mineralizer such as sodium hydroxide or sodium carbonate at a temperature of about 85.degree. C. to about 300.degree. C. for a time of about 4 hours to about 10 days. The silica thus produced has a unimodal pore distribution with pores in the range of about 300 .ANG. to about 25,000 .ANG..

Hydrothermal process for preparing a unimodal large pore silica

This invention is drawn to a process for isomerizing a non-equilibrium mixture of xylenes and ethylbenzene using a silicoaluminophosphate molecular sieve which is enriched in framework silicon at the surface, resulting in a greater yield of para-xylene compared to prior-art processes.

Aromatic isomerization using a modified silicoaluminophosphate

The need for silicas with large pore sizes can be met by hydrothermal treatment of a silica powder with a mineralizing agent. Pore sizes in the range 300-25,000 angstroms, and more particularly in the range up to 10,000 angstroms, are readily obtained using mineralizing agents such as hydroxide, carbonate, and fluoride at temperatures in the range 85-300.degree. C. A narrow, unimodal distribution of pores is typical.

Unimodal, large-pore silicas by hydrothermal treatment of silicia powders

Chiral stationary phases perform well when the underlying support for the chiral organic material is coated onto a silica pore widened by a hydrothermal treatment. The resulting silica is amorphous with a unimodal distribution of large pores. A variety of chiral stationary phases perform well and are distinguished, inter alia, by the treatment, if any, prior to coating the chiral organic material.

Chiral separation using a unimodal, large-pore silica as the support

A method of continuously promoting the activity of solid strong acid catalysts used in acid catalyzed reactions by adding or generating water in the reaction mixture has been developed. The solid strong acid catalyst may be a sulfated metal oxide, a tungstated metal oxide, or a molybdated metal oxide. The metal oxides are oxides, hydroxides, oxyhydroxides, or oxide-hydrates of Group IV-A, Group III-A, Group III-B, and Group V-A metals. The catalyst may also contain a Group VIII metal, or when the metal oxide is a hydroxide, oxide, oxyhydroxide, or oxide-hydrate of the Group IV-A, Group III-A, or Group III-B metals, the catalyst may also contain an oxide, hydroxide, oxyhydroxide or oxide-hydrate of a Group V-A, Group V-B, Group VI-B, or Group VII-B metal as a promoter. The acid catalyzed reactions where the activity promotion method may be applied include catalytic cracking, catalytic reforming, hydrodesulfurization, isomerization, alkylation of aliphatic and aromatic hydrocarbons, polymerization, and oligomerization. The amount of water added to or generated in the reaction mixture may be from about 0.1 ppm to about 500 ppm water.

Method of promoting the activity of solid strong acid catalysts

A process combination is disclosed to selectively upgrade naphtha in accordance with expected trends leading to more-aliphatic gasolines. Such gasolines contain lower concentrations of aromatics and have lower end points with concomitant reduced harmful automotive emissions. The present process combination converts the higher-boiling portion of the naphtha, yields isobutane and other isoparaffins which are particularly suitable for upgrading or blending, and reduces cyclics in intermediate processing steps.

Production of aliphatic gasoline

A process for removing sulfur containing compounds from various hydrocarbon streams is disclosed and claimed. The process involves contacting the feedstream with an adsorbent such as nickel exchanged zeolite X or Y, or a smectite layered clay having a surface area of at least 150 m.sup.2 /g, thereby adsorbing the sulfur compounds onto the adsorbent.

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Bloomingdale, IL, United States of America

Jennifer S Holmgren