Chevron Phillips Chemical Company LP

Phillips Petroleum Company

Chevron Philips Chemical Company, LP

Other

Lawrence Pump Inc.

Flowserve Management Company

Hottovy, John D.

Kufeld, Scott, E.

John D Hottovy

Scott E Kufeld

David H Burns

Donald W Verser

Dale A Zellers

Robert R McElvain

John H Tait

Ralph W Romig

James E Hein

Richard Peacock

Anurag Gupta

Robert K Franklin, Iii

Joel A Mutchler

Bruce E Kreischer

Carl W Fenderson

Gregory G Hendrickson

Penny A Zellers, Legal Representative

Max P McDaniel

Ai-Fu Chang

Harvey D Hensley

David J Przelomski

Teddy H Cymbaluk

Ethelwoldo P Perez

Ai-fu Chang

John D Stewart

Donald Paul Russell

Frederick C Lawrence

Elizabeth Ann Benham

Ted H Cymbaluk

Thanh Tri Nguyen

Thomas H Smith

Matthew G Thorn

William S Stewart

Catherine M Gill

Jerry T Lanier

Robert Bohmer

Bryan M Garner

Nelson T Black

David A Lockman

John O Lawmaster

Matthew T Haberly

Paresh C Mody

Michael C Carter

Clay K Thurman

Qing R Yang

Michael D Jensen

M Bruce Welch

Eric D Schwerdtfeger

Syriac J Palackal

Albert P Masino

Gary L Glass

Nathan E Stacy

Melvin B Welch

Carleton E Stouffer

Benjamin Milton Shaw

Larry L Nash

John E Blaesi

George R Rajaendran

Larry W Ezell

Thomas A Reid

Ragavan Vaidyanathan

Barry W Lowe

James S Fangmeier

Susannah Lane

Richard A Hernandez

Elliott W Johnson

William L Valerioti

Robert K Franklin

Gregory G Hendrikson

Randy L Hagenson

Ragayan Vaidyanathan

George K Rajaendran

Timothy Roetman

Robert R Mcelvain

Benjamin M Shaw

Teddy Cymbaluk

Donal W Verser

Robert Franklin

Donald Paul Russel

A process is described that includes flowing a carrier fluid through a transfer line, feeding polymer pellets into the transfer line at a feed location, measuring a first pressure value of the carrier fluid at a location in the transfer line upstream of the feed location, measuring a second pressure value of the carrier fluid and polymer pellets at a downstream location in the transfer line which is downstream of the feed location, and determining a mass flow rate of the polymer pellets flowing in the transfer line based on a differential pressure between the first pressure value and the second pressure value.

Measurement of product pellets flow rate

A process comprises polymerizing an olefin monomer in a loop reactor in the presence of a catalyst and a diluent, and producing a slurry comprising solid particulate olefin polymer and diluent. The Biot number is maintained at or below about 3.0 within the loop reactor during the polymerizing process. The slurry in the loop reactor forms a slurry film having a film coefficient along an inner surface of the reactor wall, and the film coefficient is less than about 500 BTU&#xb7;hr&#xb7;ft&#xb7;&#xb0; F..

Heat transfer in a polymerization reactor

The present embodiments provide a system and method for separation within a polymer production process. Specifically, a flashline heater configured according to present embodiments may provide more time than is required for complete vaporization of liquid hydrocarbons that are not entrained within a polymer fluff produced within a polymerization reactor. Such extra time may allow for liquid hydrocarbons that are entrained within the polymer fluff to be vaporized.

Flashline heater system and method

Olefin polymerization processes are described herein. The processes generally include circulating a slurry including an olefin monomer selected from C-Colefin monomers, a liquid diluent selected from C-Calkanes, catalyst and polyolefin particles under polymerization conditions within a loop reactor. In one or more specific embodiments, in operation, the process has a cavitation number of from 6 to 60 and the polymerization conditions include a polymerization temperature of from 38&#xb0; C. to 121&#xb0; C. and a polymerization pressure of from 27 bar to 50 bar. In other embodiments, the process has a Euler Number (Eu) of at least 5.

Flow in a slurry loop reactor

Embodiments of the present application provide a method for manufacturing a polyolefin and a system for implementing the method. The method comprises combining a catalyst with a diluent mixture containing a diluent and an olefin monomer in a polymerization reactor. The diluent may comprise propane, butane, or isobutane, or a combination thereof. The polymerization reactor is operated at a pressure above a critical pressure of the diluent, but below the critical temperature of the diluent.

Compressible liquid diluent in polyolefin polymerization

In an embodiment, a polymerization process comprises circulating, with a pump, a reaction mixture slurry in a polymerization loop reactor during a polymerization process, detecting a pressure change in the reaction mixture slurry downstream of the pump, generating, by a pressure controller, a takeoff valve actuation signal for a takeoff valve based on the pressure change, generating, by the pressure controller, a correction to the takeoff valve actuation signal, generating, by the pressure controller, a time delay for the correction, applying the correction to the takeoff valve actuation signal to generate a corrected takeoff valve actuation signal, providing the corrected takeoff valve actuation signal to the takeoff valve after the time delay, and adjusting a position of the takeoff valve in response to providing the corrected takeoff valve actuation signal. The reactor pressure is based on the takeoff valve position.

Pressure control to reduce pump power fluctuations

A process for making a low density polymer in a polymerization reactor system, the process comprising polymerizing an olefin monomer, and optionally an olefin comonomer, in the presence of a diluent in a polymerization reactor to make a polymerization product slurry consisting of a liquid phase and a solid phase, wherein the solid phase comprises an olefin polymer having a density of between about 0.905 g/cmto about 0.945 g/cm; and discharging the polymerization product slurry from the polymerization reactor through a continuous take-off valve to make a mixture further comprising a vapor phase. The mixture comprises a pressure less than a bubble point pressure of a component in the polymerization product slurry.

Polymerization product pressures in olefin polymerization

A process for component separation in a polymer production system, comprising separating a polymerization product stream into a gas stream and a polymer stream, wherein the gas stream comprises ethane and unreacted ethylene, distilling the gas stream into a light hydrocarbon stream, wherein the light hydrocarbon stream comprises ethane and unreacted ethylene, contacting the light hydrocarbon stream with an absorption solvent system, wherein at least a portion of the unreacted ethylene from the light hydrocarbon stream is absorbed by the absorption solvent system, and recovering a waste gas stream from the absorption solvent system, wherein the waste gas stream comprises ethane, hydrogen, or combinations thereof.

Component separations in polymerization

Techniques are provided for seal flush systems. A system may include a reactor circulation pump configured to circulate a slurry through a polymerization reactor. The slurry may include an olefin monomer, a catalyst, and a diluent. The system may also include a catalyst-inhibiting additive system configured to supply a catalyst-inhibiting additive to a seal of the reactor circulation pump and a seal flush system configured to generate a seal flush mixture and supply the seal flush mixture to the seal of the reactor circulation pump.

System and method for seal flush

A reactor system including an enclosed pressure relief system and/or a control system. The enclosed pressure relief system including a slurry separation system communicatively coupled with a pressure relief valve coupled to a loop reactor such that activation of the pressure relief valve results in discharge of a slurry from the loop reactor to the slurry separation system, wherein the slurry separation system is capable of separating solid and liquid components from gas components of the slurry and transmitting the gas components to a flare via a flare header.

System and method for closed relief of a polyolefin loop reactor system

A manufacturing system for producing polyolefin includes a polymerization reactor, a flash chamber, and a purge column. In certain embodiments, the purge column may receive a solids stream directly from the flash chamber. Further, the purge column may function as a feed tank for an extruder within an extrusion/loadout system. According to certain embodiments, the manufacturing system may be configured to consume less than 445 kilowatt-hours of energy per metric ton of polyolefin produced based on consumption of electricity, steam, and fuel gas.

Energy efficient polyolefin process

Growing community of inventors

Kingwood, TX, United States of America

John D Hottovy