Abstract: A filter cake of crude isophthalic acid is dispersed as a slurry in acetic acid, and thereafter heated to a temperature bringing about the dissolving of the isophthalic acid. Such hot solution is subjected to very rapid evaporative crystallization in a single crystallization zone maintained at a pressure at which volatilization of the acetic acid occurs and at a temperature within the range of 180.degree.-250.degree. F., the heat input being controlled to promote such very rapid volatilization that more than half of the solvent quickly is volatilized. Moreover, more than half of the isophthalic acid content of the effluent is in the solids suspended in the slurry of such effluent. Because the volatilization is so rapid, only a relatively short residence time in the single crystallization zone is required for obtaining an effluent suitable for transfer to a separation zone. Isophthalic acid crystals are separated from the mother liquor in such separation zone.

Abstract: A liquid mixture of normal butane and isobutane is catalytically oxidized at 15-45% conversion of the isobutane per pass at conditions favoring selective oxidation of the isobutane with minimized oxidation of the normal butane, thereby eliminating the need for superfractionation for ultrapurification of the isobutane prior to the oxidation step. Conditions include 260.degree.-340.degree. F., 200-1000 psig, 1-10 hour residence time, 1-500 ppm of catalyst selected from distributable (e.g. soluble) forms of chromium, cobalt, nickel, manganese, molybdenum, and mixtures thereof.

Abstract: Isobutane is injected into a liquid mixture concurrently with the injection of an oxygen-containing gas. Molybdenum catalyst is present. The oxidation is selective for the formation of tertiary butyl alcohol (TBA) so that the proportions of tertiary butyl hydroperoxide (TBHP), acetone, methanol, carbon dioxide or other less desirable products are relatively low. The tertiary butyl hydroperoxide produced by the reaction and/or the di-tertiary butyl peroxide in the reaction mixture remain in the reaction mixture while continuously distilling a product stream rich in tertiary butyl alcohol and those components boiling below TBA. After appropriate processing, such product stream is utilized as a blending component for gasoline.

Abstract: Isobutane is oxidized in a pressurized reactor in the presence of a solubilized molybdenum catalyst to produce a mixture of tertiary butyl alcohol, tertiary butyl hydroperoxide, methanol, acetone, and other oxygen containing compounds. Unreacted isobutane is recycled. Streams of normally gaseous components, comprising carbon dioxide and carbon monoxide are withdrawn from the effluent streams. A liquid stream withdrawn from the reactor, after being debutanized, is subjected to a thermal decomposition zone under several atmospheres pressure at about 280.degree. F. for from 2 to about 8 hours to reduce the concentration of tertiary butyl hydroperoxide.The liquid derived from the decomposition zone is distilled to provide a distillate stream comprising predominantly tertiary butyl alcohol and a minor proportion of methanol. Said distillate stream is heat treated to destroy residual TBHP and then transferred to a gasoline blending zone in which it is added to hydrocarbons.

Abstract: Hazards are dealt with by appropriate placement of high heat capacity flame arrestor packings at suitable zones in the flow of the process streams comprising vapors of flammable mixture containing water and more than 10 mol % tertiary butyl hydroperoxide (conveniently designated as TBHP). Stainless steel mesh or other corrosion resistant high heat capacity packing is inserted in the lower portion of the first distillation zone, from which all components more volatile than dilute aqueous TBHP are removed. Suitable packing is also inserted into the upper portion of the second distillation zone, whereby a flammable mixture containing more than 10 mol % TBHP, is distilled without allowing a large plenum filled with flammable vapor. The vapor line between the top of such distillation zone and a condensation zone features a plurality of flame arrestors (e.g.

Abstract: The entry portions of the tubes of a Worrell-type emergency cooler are modified so that the peak temperature of said modified tube is maintained at less than about 650.degree. F., thereby allowing carbon steel to be employed for heat transfer tubes. Such entry portions feature tubular members (conveniently called ferrules) having controlled thermal conductivity significantly greater than conventional insulators, but significantly less than conventional thermal conductors.

Abstract: Isobutane is oxidized to provide a debutanized oxidate comprising tertiary butyl alcohol, acetone, water and other byproducts including high boiling products. Water is removed by extractive distillation using a combination of water and xylene as the extractant. The molar amount of recycled water is greater than the amount of water to be removed from the oxidate. By thus recirculating water through the decantation zone the acetone is satisfactorily coextracted from the butyl alcohol in such a manner that a stream of acetone and a stream of water, as well as the desired dry stream of tertiary butyl alcohol can be withdrawn. If the water is not recycled, the acetone will concentrate in the upper section of the distillation zone and reduce the volatility of water, thereby inhibiting the water removal from the tertiary butyl alcohol.

Abstract: A flame arrestor is provided which can be connected with closely adjacent upstream and downstream portions of a pipeline. The gas flows through an array of narrow tubes immersed in the lower half of a normally liquid heat transfer fluid, thus normally maintaining the gas composition at ambient temperature. Even if a flame front enters either connector of the flame arrestor, the cooling effectively quenches the flame before the flame front can advance through the liquid-cooled narrow tubes to the other connector of the flame arrestor. The array of tubes is arranged as a return loop so that each tube can maintain structural integrity while expanding and contracting during rapid changes of temperature. Moreover, such return loop permits the connectors to be more readily attached to the upstream and downstream adjacent portions of the pipeline.

Abstract: A flame arrestor directs the gas stream to flow through an array of narrow tubes immersed in a normally liquid heat transfer fluid. The gas composition flowing through the flame arrestor is normally maintained at the ambient temperature of such liquid. Even if a flame front enters either connection for the flame arrestor, the cooling effectively quenches the flame before the flame front can advance through the liquid-cooled narrow tubes to the other connector of the flame arrestor, because such a large amount of liquid must be evaporated before the flame arrestor can be heated above the boiling point of the liquid. At both the inlet and outlet zones, where there is a transition between the relatively large cross-sectional area of the array of tubes and the smaller pipes for connecting to the pipeline, a hollow, liquid-cooled member serves as an internal baffle for such transition zone.

Abstract: In a system in which compressed ethylene is scheduled to flow through pipes, and in which there is danger of decomposition of ethylene and danger of the spreading of a reaction boundary of the exothermic decomposition reaction, a method and means are provided for quenching the advancement of the decomposition. Ethylene is directed from large diameter pipes into an array of spaced apart small diameter tubes which are not overheated when subjected to the combination of head and tail boundaries of the advancing plug of decomposition products. Such overheating of the tubes by the leading and trailing flames can be prevented by cooling the exterior of the tubes with a fluid normally maintained at about ambient temperature, thereby cooling the compressed ethylene sufficiently to quench the decomposition reaction. The cooling fluid is desirably an aqueous system adapted to be converted to steam under severe conditions.

Abstract: The severity of oxidation conditions in each of two stages is regulated so that the concentration of metatoluic acid in the liquid does not exceed 2 weight per cent in the first stage and does not exceed 0.4 weight per cent in the second stage. Total impurities and intermediate aromatic oxidation products are thus sufficiently low that the particles of isophthalic acid which grow in the slurry of reaction mixture in acetic acid do not contain an excessive amount of impurities. The flow rates of feed, interstage slurry, and product slurry as expressed in mols of aromatic components per hour are approximately equalized and regulated as a part of the monitoring to assure compliance with such oxidation severity standards, both stages being in the 100.degree.-130.degree.C. range.

Abstract: Butadiene is prepared by directing a C.sub.4 hydrocarbon stream through seven parallel adiabatic beds. The dehydrogenation period and the regeneration period are each about 9 1/5 minutes with evacuation and purge taking about 2 3/5 minutes of the 21 minute cycle. The temperature of the regeneration gas is individually adjusted in response to the summation of deviation of targeted conversion from average conversion and reactor deviation from average conversion amongst all reactors. Moreover, such adjustment minimizes deviations of each reactor from average conversion during the previous 21 minute cycle.The dehydrogenation effluent is mixed and sent through a common quenching zone. The quenched product stream's density varies in response to the extent of conversion, permitting measurement of conversion for each three minutes. Average conversion for each cycle is measured by averaging the conversions for such seven time periods. The density data are directed to a digital computer.