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Advansix Resins & Chemicals LLC.

Manuela Serban

Kurt M Vanden Bussche

Mark D Moser

Alakananda A Bhattacharyya

Kurt M VandenBussche

David A Wegerer

Antoine Negiz

Christopher P Nicholas

Beckay J Mezza

Mark Paul Lapinski

Warren K Bennion

Ashish Mathur

Matthew C Cole

Joseph A Kocal

Lisa M King

Guanghui Zhu

Ellen Arnold

Clayton Colin Sadler

John Patrick Brady

Jeannie Mee Blommel

Eseoghene Jeroro

Saikrishna Laxmirajam Gosangari

Deng-Yang Jan

Tom N Kalnes

Chunqing Liu

Gregory J Gajda

Charles P Luebke

Luigi Laricchia

David Nathan Myers

Chad R Huovie

Richard K Hoehn

Maureen L Bricker

Christopher D Gosling

Robert B James

Steven Lee Krupa

Michael Jerome Vetter

Joseph A Montalbano

Alan Bart Levy

Christopher D DiGiulio

Mary Jo Wier

Martha Leigh Abrams

Lihao Tang

Gary A Dziabis

Erick J Bennett, Iii

Gregory James Nedohin

Colleen K Costello

Joel S Paustian

Rui De Menezes

Debanjan Chakrabarti

Christopher Procopi

Nicholas M Brom

Massimiliano Cantarelli

Balkrishna Tope

Alan E Cepla

John P Brady

Jr Robert B James

A process for oligomerizing an olefin stream with an oligomerization catalyst to produce an oligomerized olefin stream. Oligomerization may comprise a first stage ethylene oligomerization step followed by a second stage oligomerization of the first stage oligomerized olefin to higher olefins. The oligomerized olefin stream can be separated into jet and diesel fuel streams. The olefin stream may be obtained by converting oxygenates to olefins with an MTO catalyst.

Process for converting olefins to distillate fuels

A process for dehydration of ethanol to produce ethylene is provided. Ethanol is dehydrated to produce ethylene and the subsequent conversion of ethylene to longer chain olefins and then their hydrogenation to produce long chain paraffins. In some embodiments, a split feed is employed to improve efficiency and a caustic wash column is eliminated. The advantages of the process include a lower requirement for steam and a reduction in the combined reactor volume of 30-40% when two reactors are used as compared to a single reactor.

Ethanol to ethylene process

A process for oligomerizing and oligomerizing olefins to distillate fuels which regenerates a first stage oligomerization catalyst bed and/or a second oligomerization catalyst bed in situ by contact with an oxygen gas at elevated temperature. The oligomerization catalyst can be restored to full activity. A regeneration process can enable continuous operation.

Process for converting olefins to distillate fuels with regeneration

A process for oligomerizing olefin streams comprising sending olefin streams comprising a C2− olefin vapor stream and a C3+ olefin liquids stream to a first stage oligomerization reactor containing a solid acid oligomerization catalyst to produce a first stage oligomerized stream; oligomerizing said first-stage oligomerization stream in a second stage oligomerization reactor containing a metal catalyst to provide a second stage oligomerized stream.

Multiphase oligomerization process for converting olefins to jet

An integrated apparatus for hydrogenating olefins wherein the hydrogen stream is generated from the electrolysis of water is described. Water is derived from a first reaction step wherein a first feed stream comprising oxygenated hydrocarbons is reacted to produce a first reacted product stream comprising olefins and a second reacted product stream comprising water. The second reacted product stream is electrolyzed to produce an electrolyzer product stream comprising hydrogen. Hydrogen is used to hydrogenate olefins. A paraffin stream can be obtained from the hydrogenated effluent.

Apparatus for the hydrogenation of olefins

An integrated process for hydrogenating olefins wherein the hydrogen stream is generated from electrolysis of water is described. Water is derived from a first reaction step wherein a first feed stream comprising oxygenated hydrocarbons is reacted to produce a first reacted product stream comprising olefins and a second reacted product stream comprising water. The second reacted product stream is electrolyzed to produce an electrolyzer product stream comprising hydrogen. Hydrogen is used to hydrogenate olefins. A paraffin stream can be obtained from the hydrogenated effluent.

Process for the hydrogenation of olefins

New/fresh catalyst is added to a dehydrogenation unit and aged catalyst is removed from the dehydrogenation unit on a continuous or semi-continuous basis while the dehydrogenation unit is in operation. The conversion achieved by the higher activity catalyst results in the production rate of olefin product being maintained at near start-of-run production for longer, with a slower rate of decline. The higher activity catalyst extends run time, reduces feed consumption for each unit of olefin product, and minimizes fresh catalyst expenses.

Dehydrogenation process having improved run time

Catalysts and processes for a selective conversion of hydrocarbons. The catalyst comprises: a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a modifier selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof; and a support forming a catalyst particle comprising a plurality of pores. The catalyst has a modifier profile index in a range of 1 to 1.4 across the catalyst particle.

Dehydrogenation catalyst with optimum modifier profile index

A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with an average pore diameter between 200 to 350 Angstroms, a porosity of at least 75% and an apparent bulk density between 0.60 and 0.3 g/cc. Also, a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same.

Catalyst and process for the selective conversion of hydrocarbons

Process for regenerating a catalyst for the selective conversion of hydrocarbons

A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with a median diameter between 1.6 mm and 2.5 mm and an apparent bulk density between 0.6 and 0.3 g/cc. Also a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same.

Processes for regenerating a catalyst for the selective conversion of hydrocarbons

Large pill dehydrogenation catalysts and large screens slot width are combined in dehydrogenation units to reduce the pressure drop across the catalyst bed and reactor screens compared to conventional screen and catalyst size combinations. The catalyst has an average pill diameter in the range of 1.6 mm to 3.0 mm, and the slot width of the screen is in the range of about 30% to about 60% of the pill diameter.

Dehydrogenation process

Processes for dehydrogenation of a hydrocarbon feedstock are described. The process can be run at lower H/HC ratios and lower RITs while maintaining coke production at the same level as operation at higher H/HC ratios and higher RITs without decreasing the yield per pass. Acceptable levels of coke were achieved when operating the process at low hydrogen to hydrocarbon molar ratio in the range of 0.01 to 0.40 and reactor inlet temperatures in the range of 500&#xb0;-645&#xb0; C. The process uses a low coke catalyst.

Dehydrogenation process at reduced hydrogen to hydrocarbon ratios

A process for reforming hydrocarbons is presented. The process involves applying process controls over the reaction temperatures to preferentially convert a portion of the hydrocarbon stream to generate an intermediate stream, which will further react with reduced endothermicity. The intermediate stream is then processed at a higher temperature, where a second reforming reactor is operated under substantially isothermal conditions.

Integrated hydrogenation/dehydrogenation reactor in a catalytic reforming process configuration for improved aromatics production

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Glenview, IL, United States of America

Manuela Serban