5,767,322. From treater IV through line 3, the oxidizer feed comprising cumene and other products of oxidation enters reactor A in the lower portion. Lines having the same numbers as in FIG. 2. III decanter which removes the aqueous phase containing carbonates and salts from the organic product stream, IV secondary settler (treater) which prepares the feed for reactor A, V condenser which condenses the offgases from the reactors A, B, C & D and recovers cumene and water, VI settler which separates the aqueous and organic phases for recycle to the treater IV, Since the wet oxidation process is well-known to the skilled artisan, the prior art process of FIG. Oxidizer feed comprising cumene is fed through 3 to the lower part of the first reactor (A). 3,187,055 as useful. In FIG. The organic layer is recycled directly to treater IV through line 23 along with the aqueous layer from decanter III through line 10. 2, curve X is based on data points from water-emulsion cumene oxidation with Na2 CO3 and curve Y is based on data points from water-emulsion cumene oxidation with NaHCO3. NaHCO3 formed in the reactors of the second stage is removed from the lower part of the reactors along with water stream, separated from oxidation products in the settler III and is treated in line 10 with ammonia in an equimole ratio or in mole ratio 2:1 to the sodium bicarbonate formed in these reactors. Phosphoric acid is often favored over aluminium halides. The process description of Turton et al. It was… A part of the treated aqueous sodium carbonate solution through 8 from reactors A and B is removed from the process through treater IV and sent through 9 to biotreatment and another part flows through decanter III and 10 as recycle to treater IV and then to reactors A, B, C and D. A stream of off gas from the reactors is added through 11 into condenser V to condense cumene and water entrained with air. Spent aqueous carbonate is removed from recycle loop 18 of treater IV through line 9. In line 10 the ammonia rapidly forms NaNH4 CO3 which further enhances neutralization of organic acids in the aqueous layer of treater IV. 2 is unexpected as NaHCO3 is a salt of a strong base and a weak acid, has a pH value>7 (.about.8.6), and thus should not favor the reaction of acidic CHP cleavage to phenol and acetone. In FIG. Condensate recycles to treater IV through line 7. To monitor the completeness of neutralization of this mixture after mixing with NH3 (stream 33), the pH is maintained within the range 8-10. The wet organic layer containing CHP, cumene and impurities cascades from reactor A through line 14 to B, then from B through line 15 to C and then from C through line 16 to D. The wet organic layer then leaves D through line 17 to go to decanter III. 3,187,055 as useful. In line 7 the ammonia immediately and efficiently neutralizes the organic acids in the condensate from the off gases from reactors A, B, C and D. By forming water-soluble ammonium salts of these organic acids in the organic stream, these unwanted impurities are readily removed for disposal in the spent carbonate layer of treater IV through line 9 after passing through reactors A and B (Stage I). 3. The temperature ranges in the reactors given in the examples and the number of reactors do not limit the scope of this invention. Compressors, pumps and other minor equipment items are omitted. To be certain there is a clear understanding of FIGS. A helium sparge has been found to keep the diluted tetrabutylammonium hydroxide free of air and atmospheric CO2. FIG. The results obtained are demonstrated by examples 2-3. These measurements are made by ion exclusion chromatography. The substantially equivalent mol % selectivity shown in FIG. OK. Streitwieser, A; Heathcock, C.H. These measurements are made by ion exclusion chromatography. Accordingly, the description of the drawing will first identify the key pieces of equipment shown as follows: A, B, C and D reactors or oxidizers which oxidize cumene to cumene hydroperoxide. The sodium carbonate in the recycle water-salt stream of the prior art process is typically converted to 80-100% sodium bicarbonate by neutralization of organic acids (Table 1). As far as chemistry and technology are concerned, the prior art process of water-emulsion cumene oxidation is characterized by the following parameters: 1. 3 is a process flow diagram of the wet oxidation (water-emulsion cumene oxidation) process of the present invention to make cumene hydroperoxide.