Patent GB-1138420-A (GB)
Title: Hydrocarbon oxidation process
Inventor: RUSSELL JOSEPH L
IPC: B01J19/24
Filed: 1967-07-31
Abstract: 1,138,420. Oxidation of hydrocarbons. HALCON INTERNATIONAL Inc. 31 July, 1967 [4 Aug., 1966], No. 53024/67. Heading C2C. The invention relates to an improvement in a process for the oxidation of a hydrocarbon in the liquid phase with molecular oxygen in the presence of a boron adjuvant wherein a vapour mixture containing the hydrocarbon and oxidation products of the hydrocarbon having the same hydrocarbon structures as the hydrocarbon, water and inerts, is continuously removed during the oxidation, which comprises the recovering from the vapour mixture a fraction which is enriched in the oxidation products. Preferably the vapour mixture which is continuously removed from the oxidation zone by means of line 7 is contacted with liquid, relatively cold, hydrocarbon in absorption-distillation zone 8 and there is recovered via line 9 a fraction which is enriched in hydrocarbon oxidation products which have the same carbon structure as the hydrocarbon. In a preferred embodiment the feed hydrocarbon preferably cyclohexane together with the boron adjuvant is introduced into the first reactor 111 in a series of four reactors, and is oxidized in each reactor the reaction mixture from each reactor 111 in turn passing to the next by a mixture of oxygen with nitrogen via line 119, and passes into distillation zone 121 wherein separation of the mixture takes place. Liquid cooled hydrocarbon is introduced via line 122 and in the bottom few trays scrubs out entrained solid boric acid or borate esters which might be carried over in the gases from the oxidation zone and which eventually would interfere with vaporizer operation. A liquid stream containing the scrub boron materials is returned via lines 123 and 112 back to the oxidation system. The vapours are contacted with cooled liquid hydrocarbon introduced through line 124 and a fractional distillation occurs. At a lower point in the distillation zone a stream which is enriched in the oxidation products, i.e. alcohol, ketone, hydroperoxide, and the like is withdrawn by means of line 125. At a point above this withdrawal, a stream of substantially pure hydrocarbon is withdrawn through line 126 and is returned to the oxidation system, preferably after first being preferred vaporized (not shown) to a point necessary to provide heating in the oxidation zones. Although this stream is shown as returning by means of lines 126 and 112 to the first oxidation zone, in actual practice the stream is distributed to all of the oxidation zone and the amount is sufficient to provide the heat necessary in each zone to sustain the reaction. The vapour mixture passing overhead from zone 121 travels via line 127 to condensation zone 128 wherein the condensible components are condensed and the cooled mixture passes via line 129 to separation zone 130 wherein a liquid vapour separation takes place. The vapours which mainly comprise inerts pass through line 131, a portion being purged while preferably a portion is used to dilute air and form the oxidizing gas feed. Condensed liquid passes from zone 130 via line 132 to decantation zone 133 and separates into a lower aqueous phase and an upper organic phase, the former being discarded and the latter passing via line 124 into zone 121 to provide liquid hydrocarbon for the fractional distillation step. The solution of oxidation products in hydrocarbon passes via line 125 to hydrogenation zone 135, hydrogen being introduced via line 136 and the mixture is subjected to a controlled hydrogenation reaction preferably in a liquid phase, whereby both hydroperoxide and ketone are converted to the corresponding alcohol. The effluent from this zone comprises essentially a solution of alcohol oxidation product in the hydrocarbon after separation of hydrocarbon is recovered via line 137. The hydrogenation effluent may be recycled back to the oxidation system, and preferably to the reactor 111 or, alternatively, it may be fractionally distilled to recover the alcohol product and to separate hydrocarbon for recycle. It is advantageous to recycle the hydrogenation effluent back to the oxidation system as shown via lines 137 and 112 as the presence of the alcohol tends to enhance the oxidation reaction and the alcohol is not subject to significant further degradation upon passage through the oxidation passage through the oxidation zones. As a less desirable alternative to the above, the stream passes from distillation zone 121 via line 125 and is returned directly to the oxidation system, e.g. by the dotted line 138 to oxidation zone 116. The oxidation mixture from the last oxidation zone 118 is removed via line 139 and passed to hydrolysis zone 140, water being added via line 141 and the borate esters contained in the reaction mixture are hydrolysed to boric acid plus alcohol in zone 140. The hydrolysis mixture passes via line 142 to decantation zone 143 wherein a lower aqueous boric acid phase is separated via line 144 and an organic oxidation product solution in hydrocarbon is separated via line 145. Preferably the aqueous boric acid phase is treated to recover orthoboric acid which after dehydration are desirably recycled to the oxidation. The product-hydrocarbon mixture is worked up in accordance with known procedures to recover the ketone-alcohol product oil. The oxidation of cyclohexane is described with reference to the flow sheet.