Abstract: Use of a specific combination of catalysts for the first and second steps of the process for the conversion of CHP to BPA provides high yields of BPA and low impurity yields, without a requirement for the intermediate purification steps. In the first step, CHP is cleaved in the presence of an acid treated clay such as acid treated Montmorillonite clay to produce phenol and acetone. In the second step, the phenol and acetone produced is reacted, preferably without intermediate purification, in the presence of a cation exchange resin catalyst that includes a cation exchange resin and a mercaptan or mercaptoalkanoic acid promoter to produce BPA.

Abstract: Use of a specific combination of catalysts for the first and second steps of the process for the conversion of CHP to BPA provides high yields of BPA and low impurity yields, without a requirement for the intermediate purification steps. In the first step, CHP is cleaved in the presence of a sulfated metal oxide catalyst such as sulfated Zirconia to produce phenol and acetone. In the second step, the phenol and acetone produced is reacted, preferably without intermediate purification, in the presence of a cation exchange resin catalyst that includes a cation exchange resin and a mercaptan or mercaptoalkanoic acid promoter to produce BPA.

Abstract: Use of a specific combination of catalysts for the first and second steps of the process for the conversion of CHP to BPA provides high yields of BPA and low impurity yields, without a requirement for the intermediate purification steps. In the first step, CHP is cleaved in the presence of an acid treated clay such as acid treated Montmorillonite clay to produce phenol and acetone. In the second step, the phenol and acetone produced is reacted, preferably without intermediate purification, in the presence of a cation exchange resin catalyst that includes a cation exchange resin and a mercaptan or mercaptoalkanoic acid promoter to produce BPA.

Abstract: Use of a specific combination of catalysts for the first and second steps of the process for the conversion of CHP to BPA provides high yields of BPA and ow impurity yields, without a requirement for the intermediate purification steps. In the first step, CHP is cleaved in the presence of a sulfated metal oxide catalyst such as sulfated Zirconia to produce phenol and acetone. In the second step, the phenol and acetone produced is reacted, preferably without intermediate purification, in the presence of a cation exchange resin catalyst that includes a cation exchange resin and a mercaptan or mercaptoalkanoic acid promoter to produce BPA.

Abstract: A process for separating sulfonic acid compounds from a phenolic solvent is provided by contacting the phenolic solvent with a hydrotalcite-type material (HTM). The process can be applied in the conventional industrial process for converting cumene to phenol to remove sulfonic acid compounds from the phenol product. A process and a facility for producing purified phenol by converting cumene to phenol are provided. In the conversion of cumene to phenol, the phenol often contains carbonyl-type impurities. The phenol and carbonyl-type impurities are reacted in the presence of a sulfonic acid cation exchange resin catalyst (IER) to produce a reaction product that may contain sulfonic acid compounds. The reaction product is contacted with an HTM to reduce the amount of sulfonic acid compounds which may be present and to produce a purified phenol-containing stream. The purified phenol-containing stream may be further purified using conventional separation techniques, such as distillation.

Abstract: A process for separating sulfonic acid compounds from a phenolic solvent is provided by contacting the phenolic solvent with a hydrotalcite-type material (HTM). The process can be applied in the conventional industrial process for converting cumene to phenol to remove sulfonic acid compounds from the phenol product. A process and a facility for producing purified phenol by converting cumene to phenol are provided. In the conversion of cumene to phenol, the phenol often contains carbonyl-type impurities. The phenol and carbonyl-type impurities are reacted in the presence of a sulfonic acid cation exchange resin catalyst (IER) to produce a reaction product that may contain sulfonic acid compounds. The reaction product is contacted with an HTM to reduce the amount of sulfonic acid compounds which may be present and to produce a purified phenol-containing stream. The purified phenol-containing stream may be further purified using conventional separation techniques, such as distillation.

Abstract: A process for converting carbonyl-type impurities contained in a phenolic solvent to high-boiling derivatives is provided by contacting the phenolic solvent with a hydrotalcite-type material (HTM). The phenol can be separated from the high-boiling derivatives using conventional separation techniques, such as distillation, so the invention also provides a process for separating carbonyl-type impurities, such as hydroxyacetone (HA), from a phenolic solvent. The process can be applied in the conventional industrial process for converting cumene to phenol to remove carbonyl-type impurities from the phenol product. A process and a facility for producing purified phenol by converting cumene to phenol are provided. In the conversion of cumene to phenol, the phenol often contains carbonyl-type impurities. The phenol and carbonyl-type impurities are reacted in the presence of an HTM to produce phenol and high-boiling derivatives.

Abstract: The present invention relates generally to a method for treating phenol tar, and, more particularly to a method for separating valuable products from phenol tar by treating the tar with steam.

Abstract: Greater efficiency in a water-alkaline emulsion cumene oxidation process using a cascade of reactors is obtained by splitting the reactor cascade into 2 stages with the first stage utilizing NH.sub.4 NaCO.sub.3 as the active carbonate in the stage containing less than 18% by weight cumene hydroperoxide and using Na.sub.2 CO.sub.3 as the active carbonate in the stage containing more than 18% by weight cumene hydroperoxide. By directly injecting ammonia into a recycle stream organic acids are efficiently neutralized. A counter current water wash of the second stage also increases process efficiency by scrubbing out unwanted impurities. Control of pH in the process improves efficiency and reduces impurity levels.

Abstract: Greater efficiency in a water-alkaline emulsion cumene oxidation process using a cascade of reactors is obtained by splitting the reactor cascade into 2 stages with the first stage utilizing NH.sub.4 NaCO.sub.3 as the active carbonate in the stage containing less than 18% by weight cumene hydroperoxide and using Na.sub.2 CO.sub.3 as the active carbonate in the stage containing more than 18% by weight cumene hydroperoxide. By directly injecting ammonia into a recycle stream organic acids are efficiently neutralized. A counter current water wash of the second stage also increases process efficiency by scrubbing out unwanted impurities. Control of pH in the process improves efficiency and reduces impurity levels.

Abstract: Valuable products are recovered from phenol tar by thermocracking under controlled conditions in the presence of polyphosphoric acid. Bisphenol A tars can be optionally cracked under these conditions mixed with the phenol tar and enhanced yields obtained.

Abstract: The present invention is an improved method for the recovery of phenol from a cleavage mass resulting from the sulfuric acid cleavage of cumene hydroperoxide comprising neutralizing the cleavage mass, forming an aqueous phase and an organic phase, separating the organic phase into an acetone-rich stream and a phenol-rich stream, removing phenol tars from the phenol-rich stream and cracking the phenol tars wherein the improvement comprises maintaining the pH of the cleavage mass during neutralization between 4.0 and about 4.9 whereby the sulfuric acid is converted to the bisulfate salt and substantially no free sulfuric acid remains in the cleavage mass and corrosion of process equipment is reduced.As a result of this improved process, a phenol tar waste stream containing less than about 4 parts per million by weight of chromium is obtained.

Abstract: This invention relates to processing of a mixture of tars produced in phenol manufacture and in bisphenol manufacture. The heating of a bottom liquid from a bisphenol-A process together with phenol tar from in a cumene-to-phenol process in a distillation column-type thermal cracking reactor at 290.degree.-360.degree. C. at a mass ratio of 1:(1-10) is employed. The process is carried out by feed entering into the middle of the column and valuable products removed as overhead.

Abstract: A process comprising the addition of a degradation inhibiting effective amount of an amine having a boiling point above that of the phenol used in the process to a composition comprising the said phenol and a bisphenol, the addition occurring prior to a procedure which subjects the bisphenol to substantial heat, said bisphenol produced from an acidic ion exchange resin catalyzed reaction of the said phenol and a ketone or aldehyde.

Abstract: A process comprising the addition of a degradation inhibiting effective amount of an amine having a boiling point above that of the phenol used in the process to a composition comprising the said phenol and a bisphenol, the addition occurring prior to a procedure which subjects the bisphenol to substantial heat, said bisphenol produced from an acidic ion exchange resin catalyzed reaction of the said phenol and a ketone or aldehyde.

Abstract: A process for improving the quality of phenol which comprises(a) introducing a liquid phenol composition comprising above about 95 weight percent phenol on a dry basis, organic acid contaminants, and organic ketone contaminants;(b) introducing water into the distillation tower, together with the phenol stream or in a separate stream;(c) heating the phenol composition and water to a temperature sufficiently high to vaporize the water;(d) allowing the organic acid contaminant to build to a concentration whereby sufficient acid is present to catalyze a reaction between an organic ketone contaminant and phenol, thereby forming a new compound(s) and;(e) removing the said formed compound(s) from the distillation tower by hydroextractive steam distillation.

Abstract: In accordance with the invention there is a process for reducing the water content of acetone prepared from cumene which includes the steps ofa. adding cleaving effective catalytic quantities of sulfuric acid to a mixture comprising cumene hydroperoxide and cumene, the cumene hydroperoxide making up about 81 to 83 weight percent of the said mixture, thereby producing a mixture comprising phenol, acetone, cumene and sulfuric acid;b. neutralizing the said sulfuric acid with an aqueous alkali hydroxide and separating the alkali metal sulfate from the mixture comprising phenol, acetone, water and cumene, the water being from about 40 to 60 weight percent of the total weight of water and cumene, the cumene being present in sufficient quantities to cause the formation of two liquid phases upon condensing the acetone fraction distillate;c. separating by distillation the acetone fraction from the phenol fraction, said acetone fraction containing acetone, water, aldehyde, and other organics including cumene;d.

Abstract: Benzene, toluene and ethylbenzene is removed from the heavy residues of a phenol distillation in a phenol and acetone from cumene process.

Abstract: Benzene is removed from the heavy residues of a phenol distillation in a phenol and acetone from cumene process.