Mobil Oil Corporation

Exxonmobil Research and Engineering Company

Exxonmobil Chemical Patents Inc.

Exxonmobil Oil Corporation

Government of the United States of America, As Represented by the Secretary of Commerce

Exxonmobil Corporation

Thomas F Degnan

Nai Y Chen

Philip Jay Angevine

David O Marler

Minas R Apelian

Dominick N Mazzone

Terry Eugene Helton

Wieslaw J Roth

Garry W Kirker

Michael E Landis

Stuart S Shih

Ajit Bhaskar Dandekar

Kathleen M Keville

John P McWilliams

Sharon B McCullen

Cynthia T-w Chu

Donald J Klocke

George H Hatzikos

Charles T Kresge

Albin Huss, Jr

Mae K Rubin

Richard F Socha

Brent A Aufdembrink

Anthony S Fung

Grant H Yokomizo

William S Borghard

Clarence D Chang

Quang N Le

Bruce P Pelrine

Robert P Absil

Chaya R Venkat

Jocelyn A Kowalski

Michael Hryniszak

Billy K Huh

Robert T Hanlon

Michael R Stapleton

James C Vartuli

Arthur W Chester

Ernest W Valyocsik

Pochen Chu

Ian A Cody

David S Shihabi

Ivy Dawn Johnson

Paul G Rodewald, Jr

Mohsen Shahmirzadi Yeganeh

Bhupender S Minhas

Kenneth J Del Rossi

Paul B Weisz

Daria N Lissy

Hye Kyung Timken

Henry H Ashjian

Sebastian Carmen Reyes

Charanjit Singh Paur

Augusto Rodolfo Quinones

Leonard R Koenig

Brenda H Rose

Erick D Gamas-Castellanos

Susan C Ardito

Gordon J Kennedy

Don E Stratton

Thomas Mebrahtu

Abhimanyu Onkar Patil

Tsoung Y Yan

Margaret M Wu

Scott S Han

Wenyih Frank Lai

Ralph M Dessau

Jose G Santiesteban

Michel A Daage

Stephen John McCarthy

Dennis E Walsh

Kirk D Schmitt

David Joseph Baillargeon

Satish Bodige

Francis G Dwyer

Randall D Partridge

Robert A Ware

Stephen M Oleck

Roger A Morrison

Philip Varghese

Gary Paul Schleicher

William Joseph Novak

Clinton R Kennedy

Malvina Farcasiu

Richard Charles Dougherty

Michael E Leonowicz

Charles L Baker

Grant G Karsner

Christopher Gordon Oliveri

Yun-Yang Huang

Altaf Husain

Suzzy Chen Hsi Ho

Stephen L Lawton

Krista Marie Prentice

Anil B Ketkar

Ronald A Weiss

Steven Matthew LeCours

George R Landolt

José Guadalupe Santiesteban

Kenneth G Simons, Deceased

A process for generating refrigeration, electricity or work utilizing a sorption system is disclosed. The sorption system includes a sorbent material and a fluid, in which the sorbent material and fluid in combination have a pressure index of at least 1.2.

System using unutilized heat for cooling and/or power generation

A poly(alpha-olefin/alkylene glycol) copolymer of the following formula: wherein R, R, Ra, and Rb are, independently, any of H, a Cto Cnormal or branched alkyl radical, or a Cto Caromatic radical or aromatic-containing alkyl radicals; wherein n and m, are, independently, integers from 1 to 1000; and wherein x is an integer from 0 to 10. There is also a process for making the copolymer. There is also a lubricant formulation having the copolymer.

Poly(alpha-olefin/alkylene glycol) copolymer, process for making, and a lubricant formulation therefor

A sorption system is disclosed that includes a sorbent material and a fluid, in which the sorbent material and fluid in combination have a pressure index of at least 1.2.

An integrated process for producing naphtha fuel, diesel fuel and/or lubricant base oils from feedstocks under sour conditions is provided. The ability to process feedstocks under higher sulfur and/or nitrogen conditions allows for reduced cost processing and increases the flexibility in selecting a suitable feedstock. The sour feed can be delivered to a catalytic dewaxing step without any separation of sulfur and nitrogen contaminants, or a high pressure separation can be used to partially eliminate contaminants. The integrated process includes an initial hydrotreatment, hydrocracking, catalytic dewaxing of the hydrocracking effluent, and an option final hydrotreatment.

Integrated hydrocracking and dewaxing of hydrocarbons

The present invention provides a process for producing an alkylaromatic compound comprising the step of contacting an alkylatable aromatic compound with an alkylating agent under alkylation conditions in the presence of a alkylation catalyst comprising phosphorus and a porous crystalline inorganic oxide material having an X-ray diffraction pattern including the d-spacing maxima at 12.4&#xb1;0.25, 6.9&#xb1;0.15, 3.57&#xb1;0.07 and 3.42&#xb1;0.07 Angstrom.

Aromatics alkylation

The catalyst becomes at least partially deactivated by sorbing catalyst poisons present in the feed during a process for alkylating aromatics by contacting a feed containing benzene, toluene, xylenes, alkylbenzenes, naphthalene or substituted naphthalenes under liquid phase alkylating conditions with C-Colefins in the presence of MCM-22, MCM-36, MCM-49, MCM-56, ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-48, ZSM-50, ZSM-4, ZSM-18, ZSM-20, Zeolite X, Zeolite Y, USY, mordenite or offretite to provide an alkylated aromatic product. The at least partially deactivated catalyst can be treated in situ by contacting with at least one polar compound having a dipole moment of at least 0.05 Debyes and selected from the group consisting of acetic acid, formic acid, water, and carbon monoxide, under conditions of temperature and pressure employed in the liquid phase alkylating conditions which are sufficient to at least partially desorb the catalyst poison from the catalyst.

Process for liquid phase aromatics alkylation comprising in-situ catalyst reactivation with polar compounds

A process for isomerization dewaxing of a hydrocarbon feed which includes contacting the hydrocarbon feed with a large pore size, small crystal size, crystalline molecular sieve and an intermediate pore size, small crystal size, crystalline molecular sieve to produce a dewaxed product with a reduced pour point and a reduced cloud point. In a preferred embodiment, the feed is contacted with the molecular sieves sequentially, first with the large pore sieve followed by the intermediate pore sieve.

Process for isomerization dewaxing of hydrocarbon streams

The present invention relates to the removal of mercury and other heavy metals from a hydrocarbon feedstream. The process involves contacting the hydrocarbon feedstream with a feedstream-soluble sulfur compound and then contacting the hydrocarbon feedstream and solubilized sulfur compound with an adsorbent.

Mercury removal in petroleum crude using H2S/C

Akylation product is contacted with a purification medium in a liquid phase pre-reaction step to remove impurities and form a purified stream. The purified stream may then be further processed by liquid phase transalkylation to convert the polyalkylated aromatic compound to a monoalkylated aromatic compound. The process may use a large pore molecular sieve catalyst such as MCM-22 as the purification medium in the pre-reaction step because of its high reactivity for alkylation, strong retention of catalyst poisons and low reactivity for oligomerization under the pre-reactor conditions. Olefins, diolefins, styrene, oxygenated organic compounds, sulfur containing compounds, nitrogen containing compounds and oligomeric compounds are removed.

Aromatic alkylation process

Petroleum wax feeds are converted to high viscosity index lubricants by a two-step hydrocracking-hydroisomerization process in which the wax feed which exhibits branchingis initially subjected to hydrocracking under mild conditions with a conversion to non-lube range products of no more than about 30 weight percent of the feed. The hydrocracking is carried out at a hydrogen pressure of at least 1000 psig (7000 kPa) using an amorphous catalyst which preferentially removes the aromatic components present in the initial feed. The hydrocracked effluent is then subjected to hydroisomerization in a second step using a low acidity zeolite beta catalyst which effects a preferential isomerization on the paraffin components to less waxy, high VI isoparaffins. The second stage may be operated at high pressure by cascading the first stage product into the second stage or at a lower pressure, typically from 200 to 1000 psig. The second stage catalyst is preferably a noble metal containing zeolite beta catalyst which contains boron as a framework component of the zeolite to give a low alpha value, typically below 10 while maintaining an isomerizaiton selectiveity of no less than 48%. The second stage is carried out at relatively low temperature, typically from 600&deg; to 650&deg; F. with a 650&deg; F.&plus; conversion in the range of 10 to 20 weight percent of the second stage feed but with high selectivity for isomerization of the paraffins. A final dewaxing step to target pour point may be used with relatively low loss, typically no more than 15 weight percent, during this dewaxing. The final products typically have VI values in excess of 140 and usually in the range of 143 to 147 and are characterized by exceptional stability.

Production of high viscosity index lubricants

Petroleum waxes are converted to high viscosity index lubricants by a hydroisomerization process in which the wax feed is subjected to hydroisomerization over a low acidity molecular sieve isomerization catalyst (the molecular sieve being preferably a zeolite) which effects a preferential isomerization on the paraffin components in the feed to less waxy, high VI isoparaffins. The hydroisomerization is operated at high pressure, at least 1000 psig hydrogen partial pressure (reactor inlet) using a zeolite catalyst, preferably a noble metal containing zeolite beta catalyst which contains boron as a framework component of the zeolite to give a low alpha value, typically below 10. The hydroisomerization is carried out at with a 650&deg; F.&plus; conversion in the range of 10 to 40 weight percent of the feed. A final dewaxing step to target pour point may be used with relatively low loss, typically no more than 15 weight percent, during this dewaxing. The final products typically have VI values in excess of 125 and usually in the range of 130 to and are characterized by exceptional stability.

This invention discloses a process for producing a high Viscosity Index lubricant having a VI of at least 125 from a waxy hydrocarbon feed having a wax content of at least 40 wt %. The process comprises catalytically dewaxing waxy paraffins present in the feed by isomerization in the presence of hydrogen and in the presence of a low acidity large pore zeolite isomerization catalyst. This catalyst has a ratio of SiO.sub.2 /Al.sub.2 O.sub.3, as synthesized, of at least 50:1, and an alpha value of not greater than 20, wherein the catalyst is prepared in the absence of boron. The catalyst further comprises a noble metal hydrogenation component. The feed may be hydrocracked prior to dewaxing with the large pore zeolite. The feed may be solvent dewaxed prior to isomerization. The effluent of the isomerization step may also be further dewaxed by either solvent or catalytic means in order to achieve target pour point.

Wax hydroisomerization process employing a boron-free catalyst

Growing community of inventors

Moorestown, NJ, United States of America

Thomas F Degnan