Abstract: In an aspect, a method for reducing the molecular weight of a polyester, comprises mixing a composition comprising a polyester oligomer and a polyester in a molten state to form a modified polyester; wherein the mixing occurs at a temperature of 230 to 330° C.; wherein the polyester oligomer is present in an amount of 0.1 to 50 weight percent based on 5 the total weight of the composition; wherein the polyester comprises a C2-12 alkyl phthalate polyester having a weight average molecular weight, Mwi, of 15,000 to 100,000 g/mol determined using gel permeation chromatography based on polystyrene standards; and wherein the modified polyester has a weight average molecular weight, Mwf, of at least 5% less than the weight average molecular weight of the polyester.

Abstract: A method of separating phenol can include: separating a first portion of acetone from a product stream in an evaporator unit, wherein the first portion of the acetone includes recycle acetone and bypass acetone; recycling the recycle acetone; withdrawing a bottom fraction from the evaporator unit; neutralizing the bottom fraction to form a distillation feed stream that is directed to a distillation column; separating the distillation feed stream into a bottom stream and an overhead stream, the bottom stream including a crude phenol fraction; passing the overhead stream through a condenser to produce a distillate as a crude acetone fraction, and wherein reflux ratio of the distillation column is less than or equal to 0.40, with the reflux ratio a ratio of a weight of a reflux to distillate weight; and directing the bypass acetone around the distillation column.

Abstract: Systems and methods for recovering phenol have been disclosed. The methods of recovering phenol includes concurrently processing, in a phenol recovery unit, a crude phenol stream from a phenol production unit, and a bisphenol-A purge stream from a bisphenol-A production unit to produce a first product stream comprising 60 to 95 wt. % phenol. The phenol recovery unit comprises a crude phenol distillation column and a bisphenol-A-phenol distillation column. The processing includes distilling a bottom stream from the crude phenol distillation column in the bisphenol-A-phenol distillation column.

Abstract: 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.

Abstract: 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.

Abstract: 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.

Abstract: 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 (1) to obtain the elastomer agglomerate composition; wherein the valve assembly (1) comprises the valve (2) and a seat (3) that are arranged opposite each other to provide a flow channel for the slurry to be homogenized with an emulsifying channel section (5) 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.

Abstract: 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° C. to 15° 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° C. lower than the first temperature; and forming the sulfonated phenol at the second temperature.

Abstract: 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 (1) to obtain the elastomer agglomerate composition; wherein the valve assembly (1) comprises the valve (2) and a seat (3) that are arranged opposite each other to provide a flow channel for the slurry to be homogenized with an emulsifying channel section (5) 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.

Abstract: The invention relates to a process for the production of an elastomer agglomerate composition, comprising the steps of: (a) providing a slurry comprising elastomeric particles in water, wherein the slurry has a temperature of 40 to 80° C., wherein the elastomeric particles are selected from the group consisting of polybutadiene particles, poly(styrene butadiene) particles comprising at least 50 wt % of units derived from butadiene, poly(acrylonitrile butadiene) particles and polybutylacrylate particles and combinations thereof, and wherein the slurry is substantially free of chemical agglomerants, preferably the amount of the chemical agglomerants being less than 0.01 wt % with respect to the total of the solids content in the slurry and any chemical agglomerants; and (b) forcing the slurry through an aperture to obtain the elastomer agglomerate composition.

Abstract: 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.

Abstract: 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.

Abstract: 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.

Abstract: 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.

Abstract: 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.

Abstract: 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° C. to 15° 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° C. lower than the first temperature; and forming the sulfonated phenol at the second temperature.

Abstract: 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.

Abstract: 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° C. to 15° 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° C. lower than the first temperature; and forming the sulfonated phenol at the second temperature.

Abstract: 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.

Abstract: 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.