Chevron Phillips Chemical Company LP

Phillips Petroleum Company

Other

Chevron Philips Chemical Company, LP

Bruce E Kreischer

Ronald D Knudsen

Brooke L Small

Eduardo J Baralt

Orson L Sydora

John D Hottovy

Steven M Bischof

Scott E Kufeld

Ronald G Abbott

Warren M Ewert

Steven D Bridges

James L Hillier

Max P McDaniel

Eric J Netemeyer

Qing R Yang

Eric D Schwerdtfeger

Joel A Mutchler

Uriah J Kilgore

Albert P Masino

Richard M Buck

William B Beaulieu

Kenneth D Hope

Kent E Mitchell

Jared T Fern

Jeffrey W Freeman

Mark E Lashier

Glyndal D Cowan

Kendall M Hurst

Ralph W Romig

Lyle R Kallenbach

Gregory G Hendrickson

Richard L Anderson

Catherine M Gill

John D Stewart

Harvey D Hensley

Steve Hutchison

William M Woodard

Ralph V Franklin

Ron D Knudsen

Paul J DesLauriers

Chung Ching Tso

Donald W Verser

Rebecca A Gonzales

James E Hein

Jamie N Sutherland

Ryan W Snell

Jeffery C Gee

Scott G Morrison

Vivek Rohatgi

Joseph S Shveima

Donald A Stern

Rickey D Badley

Matthew F Milner

Willie J Isom

William J Fisher

Varadee Vittur

Leonard E Powell

Michael A Rhodes

Maruti Bhandarker

Bruce H Marantis

R Kim Perry

Steven Hutchinson

Qing Yang

Max P Mcdaniel

The present disclosure relates to the integration of systems and methods associated with steam cracking, oligomerization reactions, hydrogenation reactions, and aromatization reactions for the production of benzene via the hydrogenation of oligomers produced from ethylene. In some aspects, the disclosed systems and methods utilize one or more of an oligomerization process, a hydrotreating process, and an aromatization process for producing a benzene comprising effluent. In further aspects, the systems and methods disclosed herein utilize one or more selective oligomerization catalyst systems.

Flexible benzene production via selective-higher-olefin oligomerization of ethylene

Disclosed herein are processes and reaction systems for controlling a temperature of an oligomerization reaction zone using a heat exchange system.

Heat exchange configurations for oligomerization of olefins

Methods for determining ethylene concentration in an ethylene oligomerization reactor using an ultrasonic flow meter are described, and these methods are integrated into ethylene oligomerization processes and related oligomerization reactor systems.

Methods for operating ethylene oligomerization reactor systems with an integrated ultrasonic flow meter

Disclosed herein are oligomerization processes in which ethylene and a catalyst system are first combined for a suitable residence time in an activation vessel, prior to introduction into a reaction zone to oligomerize ethylene to form a desired oligomer product, such as 1-hexene and/or 1-octene. Related oligomerization reaction systems that include the activation vessel also are disclosed. In these oligomerization processes and reaction systems, the catalyst system can be fully activated as it leaves the activation vessel and enters the reaction zone, thus providing greater catalyst utilization and less catalyst waste.

Oligomerization catalyst system activation and related ethylene oligomerization processes and reaction systems

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 into 5 in, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr)(gal) to 6.0 (lb)(hr)(gal).

Ethylene oligomerization/trimerization/tetramerization reactor

Methods for recycling ethylene from a reaction zone effluent stream from an oligomerization reaction zone, in which the reaction zone effluent stream contains an oligomer product effluent having at least 20 mass % octene(s), include a step of separating the reaction zone effluent stream into a first stream containing ethylene and less than 5 mass % Colefins, a second stream containing butene(s) and less than 10 mass % Colefins, a third stream containing at least 96 mass % hexene(s), and a fourth stream containing at least 96 mass % octene(s). The ethylene-rich first stream is recycled into the oligomerization reaction zone, while the recycle of 1-butene and other butenes is reduced significantly.

Methods for recycling ethylene in an ethylene oligomerization reactor system

A process comprising a) contacting (i) ethylene, (ii) a catalyst system comprising 1) a heteroatomic ligand iron salt complex, or a heteroatomic ligand and an iron salt, (iii) hydrogen, and (iv) optionally an organic reaction medium; and b) forming an oligomer product wherein 1) the oligomer product has a Schulz-Flory K value from 0.4 to 0.8 and 2) the oligomer product comprises (a) less than 1 wt. % of polymer, (b) less than 1 wt. % compounds having greater than 70 carbon atoms, (c) less than 1 wt. % compounds having a weight average molecular weight of greater than 1000 g/mol, or (d) any combination thereof wherein the weight percentage is based on the total weight of the oligomer product.

Ethylene oligomerization processes

A process comprises introducing an olefin monomer and a catalyst system or catalyst system components into a reaction mixture within a reaction system. The reaction system comprises: a total reaction mixture volume, and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area. The process also comprises oligomerizing the olefin monomer within the reaction mixture, determining one or more reaction system operating parameters during the oligomerizing, controlling the one or more reaction system operating parameters during the oligomerizing, maintaining a ratio of the total heat exchanged surface area to a total reaction mixture volume within the reaction system in a range from 0.75 into 5 in, maintaining an oligomer product discharge rate from the reaction system between 1.0 (lb)(hr)(gal) and 6.0 (lb)(hr)(gal), and discharging a reaction system effluent comprising the oligomer product from the reaction system.

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Kingwood, TX, United States of America

Bruce E Kreischer