Uop Lcc

Antoine Negiz

Edwin Paul Boldingh

Gregory J Gajda

James E Rekoske

Dean E Rende

Manuela Serban

Kurt M VandenBussche

Christopher P Nicholas

Mark D Moser

Edward M Casey

Paul T Barger

Gregory R Werba

Gregory F Maher

David E Mackowiak

Carl John Stevens

Sergey V Gurevich

Patrick J Silady

Eric J Baker

Bryan K Glover

Paula L Bogdan

David A Wegerer

Andrea G Bozzano

Suheil F Abdo

Robert B James

Robert B Larson

Donald L Mittendorf

Vinayender Kuchana

Hui Wang

Terrence E Deak

Sergio A Pischek

Stanley Joseph Frey

Kurt M Vanden Bussche

Robert L Mehlberg

Vasant P Thakkar

Hayim Abrevaya

Lubo Zhou

Lisa M Knight

Frank S Modica

John Anthony Petri

Richard R Willis

Steven F Zink

David S Lafyatis

Shurong Yang

Nicholas M Brom

Robert Jason Lee Noe

Surgey V Gurevich

Robert B James, Jr

Carl J Stevens

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 reactor comprising a thermal barrier surrounding a combustion zone. The reactor further comprises a cooling jacket inner wall and a binder disposed between the cooling jacket inner wall and the thermal barrier, and a cooling jacket outer wall, wherein the cooling jacket inner wall and the cooling jacket outer wall define a cooling channel. The reactor further comprises an outer reactor wall disposed over the cooling jacket outer wall, wherein the outer reactor wall is impermeable and is configured to contain high pressure gas within the reactor.

Steady state high temperature reactor

A pyrolytic reactor comprising a fuel injection zone, a combustion zone adjacent to the fuel injections zone, an expansion zone adjacent to the combustion zone, a feedstock injection zone comprising a plurality of injection nozzles and disposed adjacent to the expansion zone, a mixing zone configured to mix a carrier stream and feed material and disposed adjacent to the feedstock injection zone, and a reaction zone adjacent to the mixing zone. The plurality of injection nozzles are radially distributed in a first assembly defining a first plane transverse to the feedstock injection zone and in a second assembly transverse to the feedstock injection zone.

Pyrolytic reactor

A method and apparatus for processing hydrocarbons are described. The method includes fractionating a hydrocarbon stream to form at least two fractions. The first fraction is reformed to form a reformate stream, and the reformate stream is introduced into an aromatics processing zone to produce aromatic products. At least a portion of the second fraction is cracked in a fluid catalytic cracking unit. A selectively hydrogenated light naphtha stream is formed by separating the cracked hydrocarbon stream into at least two streams and selectively hydrogenating the light naphtha stream, or selectively hydrogenating the cracked hydrocarbon stream and separating the hydrogenated cracked hydrocarbon stream into at least two streams. Aromatics are extracted from the selectively hydrogenated light naphtha stream forming an extract stream and a raffinate stream. The extract stream is hydrotreated, sent to the aromatics processing zone to produce additional aromatic products.

Process for converting FCC naphtha into aromatics

One exemplary embodiment can be a process for increasing a mole ratio of methyl to phenyl of one or more aromatic compounds in a feed. The process can include reacting an effective amount of one or more aromatic compounds and an effective amount of one or more aromatic methylating agents to form a product having a mole ratio of methyl to phenyl of at least about 0.1:1 greater than the feed.

Process for increasing a mole ratio of methyl to phenyl

A reforming process includes an endpoint reduction zone for converting Ccomponents via selective hydrogenation and hydrodealkylation to lower boiling point aromatics, such as benzene, toluene, and xylene, or their single ring aromatic C-Cprecursors.

Enhanced aromatics production by low pressure end point reduction and selective hydrogenation and hydrodealkylation

A new family of coherently grown composites of TUN and IMF zeotypes has been synthesized and shown to be effective catalysts for aromatic transformation reactions. These zeolites are represented by the empirical formula:NaMTAlESiOwhere 'n' is the mole ratio of Na to (Al+E), M represents at least one meta, 'm' is the mole ratio of M to (Al+E), &#x201c;k&#x201d; is the average charge of the metal or metals M, T is the organic structure directing agent or agents, &#x201c;t&#x201d; is the mole ratio of N from the organic structure directing agent or agents to (Al+E), and E is a framework element such as gallium. The process involves contacting at least a first aromatic with the coherently grown composites of TUN and IMF zeotypes to produce at least a second aromatic.

Aromatic transformation using UZM-39 aluminosilicate zeolite

A process for reforming a hydrocarbon stream is presented. The process involves splitting a naphtha feedstream to at least two feedstreams and passing each feedstream to separation reformers. The reformers are operated under different conditions to utilize the differences in the reaction properties of the different hydrocarbon components. The process utilizes a common catalyst, and common downstream processes for recovering the desired aromatic compounds generated.

Process for increasing benzene and toluene production

Catalysts are disclosed comprising fibrous substrates having silica-containing fibers with diameters generally from about 1 to about 50 microns, which act effectively as 'micro cylinders.' Such catalysts can dramatically improve physical surface area, for example per unit length of a reactor or reaction zone. At least a portion of the silica, originally present in the silica-containing fibers of a fibrous material used to form the fibrous substrate, is converted to a zeolite (e.g., having a SiO/AlOratio of at least about 150) that remains deposited on these fibers. The fibrous substrates possess important properties, for example in terms of acidity, which are useful in hydroprocessing (e.g., hydrotreating or hydrocracking) applications.

Fibrous substrate-based hydroprocessing catalysts and associated methods

A process for selective hydrogenation of hydrocarbons is presented. The process uses a catalyst to selectively hydrogenate acetylenes and diolefins to increase the monoolefins in a product stream. The catalyst in the process includes a layered structure with an inert inner core and an outer layer bonded to the inner core, where the outer layer is a metal oxide and has at least two metals deposited on the outer layer.

Methods for selective hydrogenation performance using a layered sphere catalyst with new formulations

A new family of aluminosilicate zeolites designated UZM-44 has been synthesized. These zeolites are represented by the empirical formula.NaMTAlESiOwhere 'n' is the mole ratio of Na to (Al+E), M represents a metal or metals from zinc, Group 1, Group 2, Group 3 and or the lanthanide series of the periodic table, 'm' is the mole ratio of M to (Al+E), &#x201c;k&#x201d; is the average charge of the metal or metals M, T is the organic structure directing agent or agents, and E is a framework element such as gallium. UZM-44 may be used to catalyze an aromatic transformation process by contacting a feed comprising at least a first aromatic with UZM-44 at hydrocarbon conversion conditions to produce at least a second aromatic.

Aromatic transformation using UZM-44 aluminosilicate zeolite

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Wilmette, IL, United States of America

Antoine Negiz