Sabic Global Technologies B.v.

General Electric Company

Sabic Innovative Plastics IP B.v.

Other

Sabic Innovation Plastics IP B.v.

Mark Erik Nelson

Andrey Vladimirovich Zinenkov

Arkady Samuilovich Dykman

Ahmed Abouelfetouh Youssef

Victor Vladimirovich Pinson

Andrey Yurievich Sokolov

Ilya Yurievich Krupenko

Valery Yurievich Aristovich

Dmitrij Nikolayevich Zhukov

Gary Charles Davis

Husnu Alp Alidedeoglu

Arkady Samuilovich Dyckman

Paulus Johannes Maria Eijsbouts

Joseph John Caringi

Prashant Kumar

Viktor Vladimirovich Pinson

Robert Joseph Nick

Karl Aaron Baro

Osit Karroonnirun

Drew Elliot Williams

Ilja Nikolayevich Grebenshchikov

Willem Lodewyk Sederel

Ilya Nikolaevich Grebenshchikov

Daniel Joseph Brunelle

Paul Dean Sybert

Niles R Rosenquist

Eugene Pauling Boden

Theodorus L Hoeks

Peter David Phelps

Ravi Rajamani

David Paul Mobley

James Louis DeRudder

Larry I Flowers

Vern Lowry

Dejin Li

Matthew Robert Pixton

Zhaohui Su

Dane Ferraris

Parfait Jean Likibi

Donald E Owens, Iii

Vijay Kumar Millikarjun Hanagandi

James Patrick Williams

Victor Vladimiovich Pinson

Valentina Amerik

Erik Hendrick Capelle

Alexey Leonidovich Moskvin

Lubov Borisovna Drozdova

Victor Vladimrovich Pinson

Zinenkov Andrey Vladimirovich

Dykman Arkady Samuilovich

Grebenshchikov Ilja Nikolayevich

Pinson Victor Vladimirovich

Louis Derudder James

Richard Rosenquist Niles

A method for oxidizing a hydrocarbon includes feeding an oxidant to a top portion of a reactor; reacting the hydrocarbon with the oxidant in the reactor to obtain a reaction product stream, the reaction product stream exiting a reactor outlet at a bottom portion of the reactor; and recycling a portion of the reaction product stream to the top portion of the reactor; and introducing the oxidant into an oxidation liquid comprising the portion of the reaction product stream recycled to the top portion of the reactor to form a reaction media stream entering a reactor inlet at the top portion of the reactor. A pressure of the reactor outlet exceeds a pressure of the reactor inlet by at least 5%. The reaction media stream moves vertically downwards in the reactor.

Method and system for oxidizing cumene and hydrocarbons

A sampling system for an optical cell containing a process fluid comprises a first bi-directional pump in fluid communication with a sampling path and a second bi-directional pump in fluid communication with the first bi-directional pump and a storage vessel. The first bi-directional pump is configured to withdraw a first sample of the process fluid and to cause the first sample to flow towards the first bi-directional pump. The second bi-directional pump is configured to withdraw a second sample from the storage vessel and to cause the second sample to move toward and mix with the first sample. A first rate of withdraw of the first sample is greater than a second rate of movement of the second sample toward the first sample, and the difference between the first rate and the second rate correspond to a pre-determined ratio of the first sample mixed with the second sample.

Optical analysis and sampling systems

In an embodiment, a method of recovering phenol comprises heating a preheater inlet stream in a preheater to form a splitter inlet stream; separating the splitter inlet stream into a splitter top outlet stream and a splitter bottom outlet stream in a splitter column; separating the splitter bottom outlet stream into a crude top outlet stream and a crude bottom outlet stream in a crude phenol column; hydro-extracting the crude top outlet stream in a hydro-extractor column to form an extractor primary outlet stream; recovering a product phenol outlet stream from the extractor primary outlet stream in a finishing column; combining a bisphenol A plant phenol recovery stream from a bisphenol A reaction from a bisphenol A phenol purification system with the preheater inlet stream, the splitter inlet stream, the splitter bottom outlet stream, the crude top outlet stream, or a combination comprising at least one of the foregoing.

Method of recovering phenol from a BPA production plant and the plant for recovering the same

The invention relates to a process for the production of an elastomer agglomerate composition, comprising: forcing a slurry through an aperture in a valve assembly () to obtain the elastomer agglomerate composition; wherein the valve assembly () comprises the valve () and a seat () that are arranged opposite each other to provide a flow channel for the slurry to be homogenized with an emulsifying channel section () that is provided with the aperture; wherein the emulsifying flow channel section is arranged at an angle (a) with respect to an axial center line of the valve in a cross sectional view of the valve assembly; and wherein the slurry comprises elastomeric particles in water.

Process for production of elastomer agglomerate composition, elastomer agglomerate composition and its use

A method for the manufacture of a sulfonated phenol for use as a cumene hydroperoxide decomposition catalyst can comprise: combining phenol and a sulfonating agent at a first temperature that is 1&#xb0; C. to 15&#xb0; C. higher than a melting temperature of the phenol, to form a reaction mixture at the first temperature; reducing the first temperature of the reaction mixture to a second temperature that is 10 to 40&#xb0; C. lower than the first temperature; and forming the sulfonated phenol at the second temperature.

Optimization of O-sulfonated phenol production for cumene hydroperoxide cleavage

In an embodiment, an optical system comprises an optical cell having an interior fluid chamber defined by an interior surface of a housing, a process inlet disposed in the housing and in fluid communication with the interior fluid chamber, and a process outlet disposed in the housing and in fluid communication with the interior fluid chamber, wherein the process inlet and process outlet facilitate the flow of a fluid through the interior fluid chamber. A sampling outlet can be disposed in the housing and in fluid communication with the interior fluid chamber. A first bi-directional pump can be in fluid communication with the sampling outlet and a first storage vessel and can be configured to withdraw a first sample of the fluid via the sampling outlet and to cause the first sample to flow into the first storage vessel.

In an embodiment, a method of recovering phenol from a bisphenol A production facility comprises reacting phenol and acetone to produce a bisphenol A stream; separating the bisphenol A stream into a product bisphenol A stream and a purge stream; separating the purge stream into a primary top outlet stream and a primary bottom outlet stream; adding an acid catalyst to the primary bottom outlet stream to form a cracker inlet stream; separating the cracker inlet stream into a cracker top outlet stream and a cracker bottom outlet stream; separating the cracker top outlet stream and the cracker bottom outlet stream into a secondary top outlet stream and a secondary bottom outlet stream; forming a bisphenol A plant phenol recovery stream; combining the bisphenol A plant phenol recovery stream with a stream of a phenol purification plant.

A process for preparing polybutylene terephthalate (PBT) which includes step of melting solid PBT oligomer having an IV of between 0.13 and 0.17 dL/g and a CEG of between 90 and 180 mmol/kg; and further step of the PBT oligomer polycondensation; wherein the polycondensation process is carried out continuously using a melt tank for melting oligomers, one or more reactors for post-condensation processing, and one or more finishing reactors to increase molecular weight. The resulting PBT has an intrinsic viscosity (IV) of between 0.5 and 1.3 dl/g and a carboxylic end group (CEG) concentration of between 1 and 75 mmol/kg.

Continuous process for making polybutylene terephthalate

In an embodiment, a method of recovering an unreacted phenol from a bisphenol A production facility comprises reacting an initial phenol and an initial acetone in the presence of a catalyst to produce a bisphenol A stream comprising the unreacted phenol of the initial phenol and a bisphenol A, separating a purge stream comprising the unreacted phenol, and wherein the unreacted phenol is present in the purge stream in an amount of 60 to 90 wt %, based on the total weight of the purge stream; adding the purge stream to a phenol purification section of a phenol production facility; and forming a purified phenol outlet stream in the phenol purification section, wherein the purified phenol outlet stream comprises a total phenol concentration of greater than or equal to 99.5 wt % based on the total weight of the purified phenol outlet stream.

Method of recovering phenol from a BPA production facility and the facility for recovering the same

A process for making oligomers of polybutylene terephthalate (PBT) with desirable intrinsic viscosity and carboxylic end group concentrations includes combining 1.4-butane diol (BDO). terephthalic acid and a catalyst to from a mixture and heating the mixture until the clearing point is reached based on visual inspection. The PBT oligomers are used in a continuous process for making polybutylene terephthalate (PBT) resin.

Process for making polybutylene terephthalate oligomers

Systems and methods for the production of phenol and acetone from cumene oxidation products. One method includes reacting cumene and an oxidizing agent to produce a cumene oxidation product including cumene hydroperoxide and dimethyl benzyl alcohol, converting at least a portion of the dimethyl benzyl alcohol to cumene hydroperoxide by reacting the at least a portion of the dimethyl benzyl alcohol with hydrogen peroxide in both an organic phase and an aqueous to produce a converted cumene oxidation product, and cleaving the converted cumene oxidation product to produce an output product including one or more of phenol, acetone, and alpha-methylstyrene.

Controlled conversion of dimethyl benzyl alcohol to cumene hydroperoxide formed during the cumene oxidation process

Disclosed herein are a method and systems for cumene hydroperoxide cleavage with an improved configuration for online instrumentation. The systems comprise a first fluid loop comprising one or more reactors and a fluid pump and a second fluid loop in fluid communication with the first fluid loop. This second fluid loop comprises an instrument configured to measure a characteristic of a fluid flowing through the second loop, wherein an input of the second fluid loop is disposed downstream of said fluid pump and an output of the second fluid loop is disposed upstream of said fluid pump. The method comprises causing fluid to flow within a first stage comprising one or more reactors and a fluid pump, wherein the first stage is configured to decompose a cumene hydroperoxide in the presence of a catalyst mixture to form a dicumyl peroxide mixture. The method also comprises causing at least a portion of the fluid to flow through a instrumentation line in open fluid communication with the first stage. This instrumentation line comprises an instrument configured to measure a characteristic of the fluid flowing through the instrumentation line and an input of the instrument line is disposed downstream of said fluid pump.

System and process for cumene hydroperoxide cleavage with improved online instrumentation configuration

The disclosure concerns methods comprising forming a phenol and acetone mixture from decomposition of a cumene hydroperoxide or a phenol, acetone, and AMS from the decomposition of a mixture containing dicumyl peroxide in a system comprising one or more reactors where at least a portion of an inner surface of the one or more reactors has a polymer coating and wherein the coating inhibits build-up of a fouling precipitate on the coated inner surface of the one or more reactors as compared to such build-up in the absence of the coating.

Coating to inhibit fouling of reactors for cumene hydroperoxide cleavage

An apparatus for oxidation of a C-Calkylbenzene reactant to a C-Calkylbenzene hydroperoxide product, the re-actor can comprise: a flow reactor comprising a reactant inlet, an oxidate product outlet, wherein the reactor is configured to provide a liquid flow from the reactant inlet to the product outlet, a gas inlet configured to introduce an oxygen-containing gas into the reactor, and an inlet sparger configured to flow gas bubbles comprising the oxygen-containing gas within the liquid flow, and wherein: the inlet sparger is configured to flow the gas bubbles having a diameter of 1.0 mm to 5.0 mm over a gas bubble residence time from 1 to 200 seconds, and/or the inlet sparger configured to flow the gas bubbles such that greater than or equal to 80% of the gas bubbles do not coalesce into larger bubbles over a gas bubble residence time of 1 to 200 seconds.

Alkylbenzene hydroperoxide production using dispersed bubbles of oxygen containing gas

Growing community of inventors

Mt. Vernon, IN, United States of America

Mark Erik Nelson