An azeotropic cleaning solvent composition has from about 96 to about 98 weight percent 1,1,1,3,3,3-hexafluoro-2-methoxypropane (“HFMOP”) and from about 2 to about 4 weight percent acetone, for example, about 97 weight percent HFMOP and about 3 weight percent acetone. Another composition of the invention has a weight ratio of HFMOP to acetone of about 24 to about 99, for example, about 24 to 49. Conventional additives such as surfactants, lubricants and co-solvents may be present in an amount not to exceed about 10 weight percent of the composition. A method of the invention comprises contacting an article of manufacture with the solvent composition in order to clean the article of manufacture and then removing the solvent composition from the article of manufacture.

This present disclosure relates to processes and apparatuses for use of a single dividing wall distillation column for phenol fractionation. More specifically, the present disclosure relates to processes and apparatuses for phenol fractionation by combining crude acetone column and cumene-AMS column into a single dividing wall distillation column. The proper allocation of steam or water injection, chemical treatment reactor and internal liquid phase separator, the positioning of the side draw enables high yield of acetone and phenol.

This present disclosure relates to processes and apparatuses for use of a single dividing wall distillation column for phenol fractionation. More specifically, the present disclosure relates to processes and apparatuses for phenol fractionation by combining crude acetone column and cumene-AMS column into a single dividing wall distillation column. The proper allocation of steam or water injection, chemical treatment reactor and internal liquid phase separator, the positioning of the side draw enables high yield of acetone and phenol.

A process for the treatment of waste water, spent air, and hydrocarbon containing liquid and gaseous streams in the cumene/phenol complex is described. Various effluent streams are combined in appropriate collection vessels, including a spent air knockout drum, a hydrocarbon buffer vessel, a fuel gas knockout drum, a phenolic water vessel, and a non-phenolic water vessel. Streams from these vessels are sent to a thermal oxidation system.

A process for the treatment of waste water, spent air, and hydrocarbon containing liquid and gaseous streams in the cumene/phenol complex is described. Various effluent streams are combined in appropriate collection vessels, including a spent air knockout drum, a hydrocarbon buffer vessel, a fuel gas knockout drum, a phenolic water vessel, and a non-phenolic water vessel. Streams from these vessels are sent to a thermal oxidation system.

In an embodiment, a method of recovering acetone comprises separating a bisphenol A stream into a bisphenol A product stream and an extraction stream comprising unreacted acetone; recovering the unreacted acetone in a recovery section of the bisphenol A production facility and forming a bisphenol A plant acetone recovery stream comprising methanol and a recovered acetone; introducing the bisphenol A plant acetone recovery stream to a phenol purification plant; and purifying the bisphenol A plant acetone recovery stream in the phenol purification plant to form an acetone product stream. The acetone product stream can comprise a reduced amount of methanol as compared to the bisphenol A plant acetone recovery stream.

In an embodiment, a method of recovering acetone comprises separating a bisphenol A stream into a bisphenol A product stream and an extraction stream comprising unreacted acetone; recovering the unreacted acetone in a recovery section of the bisphenol A production facility and forming a bisphenol A plant acetone recovery stream comprising methanol and a recovered acetone; introducing the bisphenol A plant acetone recovery stream to a phenol purification plant; and purifying the bisphenol A plant acetone recovery stream in the phenol purification plant to form an acetone product stream. The acetone product stream can comprise a reduced amount of methanol as compared to the bisphenol A plant acetone recovery stream.

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.

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.

A method of producing phenol and acetone can comprise: alkylating benzene with a C.sub.2-6 alkyl source in the presence of a zeolite catalyst to produce a C.sub.8-12 alkylbenzene; oxidizing the C.sub.8-12 alkylbenzene in the presence of an oxygen containing gas to produce a C.sub.8-12 alkylbenzene hydroperoxide; cleaving decomposing the C.sub.8-12 alkylbenzene hydroperoxide in the presence of an acid catalyst to produce phenol, a C.sub.3-6 ketone, and undesirable side products such as, but not limited to acetaldehyde, DMBA, acetophenel one, AMS, AMS dimers, unidentified heavies, or a combination comprising at least one of the foregoing; and monitoring a concentration of the C.sub.8-12 alkylbenzene hydroperoxide in a process stream of a reactor in real time at a temperature and a pressure of the process stream; and in real time, controlling a parameter of the reactor and/or the cleaving decomposing in response to the concentration of the C.sub.8-12 alkylbenzene hydroperoxide.