Abstract: A desalting method for extracting salt from phenol production waste of a phenol process, comprising the steps of: (a) receiving said phenol production waste from the phenol process; (b) providing a parting agent operable to separate, on contact, an organic material into an organic phase and an aqueous phase; (c) providing an extractant operable, on contact, to absorb salt into an aqueous phase, wherein said extractant comprises an aqueous NaHSO4 solution; (d) performing at least one sequential extraction step, in at least one corresponding sequential extraction system, on said phenol production waste, to extract salt therefrom.

Abstract: A two-step method of crude phenol treatment from impurities, wherein a first step comprises oxidizing hydroxyacetone and aldehydes impurities, in phenol medium by air oxygen with the use of a heterogeneous catalyst which contains transition metals, and a second step comprises treating the unoxidized impurities with the use of a heterogeneous acidic catalyst. The separation of treatment by-products compounds produced during said phenol treatment may then be carried out by a conventional fractionation, distillation, or equivalent method, to produce highly purified product phenol.

Abstract: Disclosed is a method for the production of product acetone of higher oxidation stability where the product acetone is produced by a multi-step rectification process in the presence of alkali catalyst. The embodiments of the method of present invention utilize a two-column and a one-column scheme of product acetone rectification from an acetone stream. In a two-column embodiment of the present invention, acetone is taken off in a vapor phase as a side-draw in a first column and directed to a partial condenser wherein it is separated into liquid and vapor phases with a simultaneous feed of aqueous sodium hydroxide solution to the first column above the feed tray.

Abstract: A new phenol and acetone production process reduces the amount of necessary stages for obtaining phenol and acetone, results in higher yield of desired products and requires less complex equipment implementation and less energy than current processes of a similar type.

Abstract: Purification of cumene hydroperoxide cleavage products from hydroxyacetone and carbonyl compounds is accomplished via extraction of hydroxyacetone and carbonyl compounds from cleavage products with a circulating water-salt solution in an extractor during an extraction stage and subsequent conversion of hydroxyacetone and other carbonyl compounds into deep condensation products in a HAC reactor operating as a plug-flow reactor or mixing reactor or as their combination. The conversion/condensation process is conducted in the water-salt solution by treating the hydroxyacetone and carbonyl compounds with alkaline agents. Various homogenous and/or heterogeneous alkaline catalysts may be used. Optionally multiple sequential extraction stages may be connected to the HAC reactor for improved performance.

Abstract: Disclosed is a process for the cleavage of technical cumene hydroperoxide (CHP) into phenol, acetone and .alpha.-methylstyrene. In a first stage, the CHP cleavage process is conducted in such a way to maintain the heat generation rate and the heat removal rate balanced in each of the CHP cleavage reactors. The cleavage of the CHP is conducted under substantially isothermal conditions at a temperature in the range of 47-50.degree. C. In the second stage of the process dicumylperoxide (DCP) and dimethylbenzene alcohol (DMBA) cleavage is carried out in a multi-section plug-flow reactor under non-isothermal conditions at a controlled temperature increase. The temperature is controlled with the use of thermocouples installed in each section of the reactor. The obtained temperature profile is compared with the temperature profile required by the kinetic model based on .DELTA.T in each section of the reactor.