Exxonmobil Chemical Patents Inc.

Exxon Chemical Patents, Inc.

Exxonmobil Research and Engineering Company

Exxon Chemical Patents Inc (ecpi)

James Richardson Lattner

Keith Holroyd Kuechler

Christopher Lynn Becker

Teng Xu

Kun Wang

Nicolas P Coute

Jihad Mohammed Dakka

Stephen Neil Vaughn

Jeffrey Scott Smith

John Scott Buchanan

Gabor Kiss

Francisco Manuel Benitez

Steven E Silverberg

Hari Nair

Tan-Jen Chen

Luc R M Martens

Charles Morris Smith

Cor F Van Egmond

Frank Hershkowitz

Larry Lee Iaccino

James Harding Beech, Jr

Hsiang-Ning Sun

Robert H Blanpied

Michael W Weber

Patrick Brant

Shun Chong Fung

Kenneth Ray Clem

John Di-Yi Ou

Michael Peter Nicoletti

Richard Edwards Walter

Federico Barrai

Robert Patrick Reynolds, Jr

John W Chu

Paul F Keusenkothen

Stephen Zushma

Jane C Cheng

Edmund John Mozeleski

Mark Paul Hagemeister

John F Walzer, Jr

Lorenzo C DeCaul

Helge Jaensch

Machteld Maria Mertens

Guang Cao

Peter Loezos

Richard B Hall

Jason D Davis

Jeffrey Lawrence Brinen

Marcel J G Janssen

John Slocum Coleman

Anastasios I Skoulidas

David Ritchie Lumgair

Stephen Todd Cohn

Michael A Risch

Lu Han

Hong Cheng

Mohsen N Harandi

Stephen Harold Brown

James C Vartuli

Abhimanyu Onkar Patil

Wenyih Frank Lai

Sabato Miseo

Gary David Mohr

Doron Levin

Terry Eugene Helton

David B Spicer

Jon E Stanat

Stephen M Davis

Laughlin G McCullough

Jay L Reimers

Shifang Luke Luo

Ajit Bhaskar Dandekar

David T Ferrughelli

Robert D Denton

Jeevan Sahib Abichandani

Yun-Feng Chang

Marcel Johannes Janssen

Timothy Lee Hilbert

Michel Molinier

Moses Minta

Christine A Costello

Alan Anthony Galuska

Chunshe J Cao

Robert Scott Smith

Timothy Daniel Shaffer

Michael B Carroll

Timothy D Shaffer

Fred David Ehrman

Keith K Aldous

Himanshu Gupta

Steven Paul Rucker

Brian Michael Weiss

Mayank Shekhar

Thomas Herman Colle

Timothy Paul Bender

J Scott Buchanan

Frank Cheng-Yu Wang

Eric D Nelson

Robert P Reynolds

Javier Guzman

Raymond A Cook

Processes and systems for quenching an effluent. In certain embodiments, the process can include contacting a pyrolysis effluent and a first quench medium to produce a first quenched effluent. A bottoms stream that can include tar and an overhead stream that can include ethylene and propylene can be obtained from the first quenched effluent. The first quench medium can include a first portion of the bottoms stream that can include a first portion of the tar. In certain embodiments, the process can also include hydroprocessing a second portion of the bottoms stream that can include a second portion of the tar to produce a hydroprocessed product. A hydroprocessed bottoms stream can be obtained from the hydroprocessed product. In certain embodiments, the process can also include contacting at least a portion of the hydroprocessed bottoms stream and the first portion of the bottoms stream to produce the first quench medium.

Processes and systems for quenching pyrolysis effluents

In an embodiment, a method for decreasing reactor fouling in a steam cracking process is provided. The method includes steam cracking a hydrocarbon feed to obtain a quench oil composition comprising a concentration of donatable hydrogen of 0.5 wt. % or more based on a total weight percent of the quench oil composition; exposing a steam cracker effluent flowing from a pyrolysis furnace to the quench oil composition to form a mixture; and fractionating the mixture in a separation apparatus to obtain a steam cracker tar. In another embodiment, a hydrocarbon mixture is provided. The hydrocarbon mixture includes a mid-cut composition.

Steam cracking processes and the use of solvents streams produced by solvent-assisted tar conversion processes

Processes for upgrading a hydrocarbon. In some embodiments, the process can include contacting a hydrocarbon-containing feed with a first catalyst that can include a Group 8-10 element disposed on a support within a first conversion zone to effect dehydrogenation, dehydroaromatization, and/or dehydrocyclization of a portion of the feed to produce first conversion zone effluent that includes one or more upgraded hydrocarbons, molecular hydrogen, and unconverted feed. The process can also include contacting the first conversion zone effluent with a second catalyst that can include a Group 8-10 element disposed on a support within a second conversion zone to effect dehydrogenation, dehydroaromatization, and/or dehydrocyclization of at least a portion of the unconverted feed to produce a second conversion zone effluent that includes an additional quantity of upgraded hydrocarbon(s) and molecular hydrogen. A temperature of the second conversion zone effluent can be greater than a temperature of the first conversion zone effluent.

Processes and systems for upgrading alkanes and alkyl aromatic hydrocarbons

A hydrocarbon conversion process comprises pyrolysing at a temperature &#x2265;700&#xb0; C. a feedstock comprising hydrocarbon to produce a pyrolysis effluent comprising at least one Cto Colefin and Caliphatic and aromatic hydrocarbons. The pyrolysis effluent is contacted with an oleaginous quench stream to reduce the temperature of the pyrolysis effluent to &#x2264;400&#xb0; C. At least first and second streams are separated from the cooled effluent. The first stream comprises at least one Cto Colefin, and the second stream comprises a quench oil having an average boiling point at atmospheric pressure of at least 120&#xb0; C. At least a portion of the second stream is catalytically hydroprocessed to produce a hydroprocessed stream, which is combined with at least a portion of any remainder of the second stream to form the quench stream.

Hydrocarbon pyrolysis processes

A process for endothermic dehydrogenation including contacting a catalyst material in a moving bed reactor having at least one reaction zone, the moving bed reactor comprising a heat exchanger containing a heating medium, wherein the catalyst material and the heating medium do not contact one another, and wherein at least 50% of the delta enthalpy of the at least one reaction zone is provided by the heat exchanger; and contacting a feedstock comprising hydrocarbons with the catalyst material in the at least one reaction zone of the moving bed reactor under reaction conditions to convert at least a portion of the hydrocarbons to a first effluent comprising a product comprising alkenes, alkynes, cyclic hydrocarbons, and/or aromatics.

Processes and systems for the conversion of hydrocarbons

Processes are described for isomerizing one or more C-Calpha olefins to produce an isomerization mixture comprising one or more C-Cinternal olefins comprising contacting an olefinic feed comprising the one or more C-Calpha olefins with a catalyst under isomerization conditions, wherein the catalyst comprises a microporous crystalline aluminosilicate having an MWW framework. The resulting isomerization mixture typically exhibits a low pour point with maintained biodegradability properties as compared to the olefinic feed, and is particularly useful in drilling fluid and paper sizing compositions.

Processes for isomerizing alpha olefins

Processes and systems for upgrading a hydrocarbon feed. The process can include feeding a hydrocarbon feed, catalyst particles, and molecular hydrogen (H) into a separation zone. The hydrocarbon feed and Hcan be contacted in the presence of the catalyst particles under hydrotreating conditions in the separation zone that can include contacting under a total pressure of less than 3,500 kilopascals-gauge. The Hcan be fed into the separation zone at a rate of no greater than 270 cubic meters of Hper cubic meter of the hydrocarbon feed, where the volume of Hand hydrocarbon feed are based on a temperature of 25 C and a pressure of 101 kilopascals-absolute. A vapor phase hydrocarbon stream and a liquid phase hydrocarbon stream can be obtained from the separation zone. At least a portion of the vapor phase hydrocarbon stream can be fed into a pyrolysis reaction zone to produce a pyrolysis effluent.

Process and system for upgrading a hydrocarbon feed

A process including contacting one or more monomers, at least one catalyst system, and at least two condensing agents under polymerizable conditions to produce a polyolefin polymer is provided where the vapor pressure of the condensing agents is &#xb1;4 bara of the optimum vapor pressure given by the formula: optimum vapor pressure=614&#x2212;716*D+2.338*P+3.603*ln(MI), where the optimum vapor pressure has units (bara), D is the polyolefin polymer density with units (g/cc), P is the polymerization condition pressure with units (barg), and MI is the polyolefin polymer melt index with units (g/10 min). The invention also relates to a process where at least three condensing agents are used.

Polymerization process

The invention relates to approach temperatures and approach temperature ranges that are beneficial in operating a pyrolysis reactor, to pyrolysis reactors exhibiting a beneficial approach temperature, to processes for carrying out hydrocarbon pyrolysis in a pyrolysis reactor having a beneficial approach temperature. The pyrolysis reactor can be, e.g., a reverse-flow pyrolysis reactor, such as a regenerative reverse-flow pyrolysis reactor.

Pyrolysis reactor approach temperature

Disclosed herein are processes for producing neopentane. The processes generally relate to demethylating isooctane to produce neopentane. The isooctane may be provided by the alkylation of isobutane with butylenes.

Production of neopentane

Methods of transforming a hydrocarbon feedstream into an aromatization product in a multi-stage reverse flow reactor (RFR) apparatus are disclosed. The methods include at least two reaction stages in series, at least one being a pyrolysis stage and at least another being a catalytic aromatization stage. Using a highly saturated hydrocarbon feedstream the pyrolysis stage focuses on desaturation, while the catalytic aromatization stage focuses on aromatization. The catalytic aromatization stage contains a aromatization catalyst that can include substantially no magnesium, scandium, yttrium, titanium, zirconium, hafnium, vanadium, niobium, tantalum, chromium, molybdenum, tungsten, manganese, rhenium, iron, ruthenium, cobalt, rhodium, nickel, palladium, platinum, copper, silver, gold, gallium, indium, tin, lanthanides, or actinides, or, in some cases, substantially no added active metals at all. The aromatization product can contain at least 35 mol % aromatic hydrocarbons, based on a total amount of hydrogen and hydrocarbons in the aromatized hydrocarbon product.

Reactor apparatus for non-oxidative hydrocarbon conversion to aromatics, methods of using same, and products made using same

This disclosure relates to naphthalene-1,8-dicarboxylate ester compounds, lubricating oil base stocks comprising naphthalene-1,8-dicarboxylate ester compounds, lubricating oil compositions comprising such base stocks, and method of making such base stocks. The lubricating oil base stocks comprising naphthalene-1,8-dicarboxylate ester compounds exhibit desirable lubricating properties such as polarity.

Naphthalene-1,8-dicarboxylate ester compounds and lubricating oil base stocks and processes for making same

The invention relates to hydrocarbon pyrolysis, to equipment and materials useful for hydrocarbon pyrolysis, to processes for carrying out hydrocarbon pyrolysis, and to the use of hydrocarbon pyrolysis for, e.g., hydrocarbon upgrading.

Hydrocarbon pyrolysis

Disclosed herein are processes for producing neopentane. The processes generally relate to demethylating diisobutylene to produce neopentane. The diisobutylene may be provided by the dimerization of isobutylene.

Processes for producing neopentane are disclosed herein. Processes comprise demethylating a C-Calkane within a shell and tube reactor to produce a demethylation product including at least 10 wt % neopentane based on the weight of the demethylation product.

Processes to make neopentane using shell and tube reactors

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LaPorte, TX, United States of America

James Richardson Lattner