Abstract: A method is disclosed in which a first gas is contacted with a solid at an elevated reaction temperature to produce a gaseous product, the solid being deactivated during said contact and exothermically reactivated by a second gas and again contacted with the first gas, the improvement includes the steps of:(a) providing a quantity of the solids in relatively equal amounts to at least these fixed bed reactors;(b) sequentially operating each fixed bed reactor according to the cycle comprising: (1) preheating introducing the first gas into a first end of the reactor and withdrawing gaseous product from a second end of the reactor; (2) preheating the first gas to reaction temperature by introducing the first gas into the fixed bed of solids at a plurality of points along the length of the reactor and withdrawing the preheated gas from the second end of the reactor; and (3) reactivating the deactivated solids by introducing the second gas into the fixed bed of solids at a plurality of points along the length of th

Abstract: A method is disclosed in which a first gas is contacted with a solid at an elevated reaction temperature to produce a gaseous product, the solid being deactivated during said contact and further, being exothermically reactivated by a second gas, the improvement which comprises providing the solids in at least three reactor zones and sequantically operating each reactor according to the cycle: reaction/reactant preheat/solids reativation. Preferaly the reactors are operated concurrently such that, at any time, at least one reactor is producing product and at least one reactor is preheating reactant to reaction temperature.

Abstract: An apparatus is disclosed in which a first gas is contacted with a solid at an elevated reaction temperature to produce a gaseous product, the solid being deactivated during said contact and exothermically reactivated by a second gas and again contacted with the first gas, the improvement includes the steps of:(a) providing a quantity of the solids in relatively equal amounts to at least these fixed bed reactors;(b) sequentially operating each fixed bed reactor according to the cycle comprising: (1) preheating introducing the first gas into a first end of the reactor and withdrawing gaseous product from a second end of the reactor; (2) preheating the first gas to reaction temperature by introducing the first gas into the fixed bed of solids at a plurality of points along the length of the reactor and withdrawing the preheated gas from the second end of the reactor; and (3) reactivating the deactivated solids by introducing the second gas into the fixed bed of solids at a plurality of points along the length o

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: 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: The concentration of tertiary butyl alcohol in the isobutane feed to a reactor for the preparation of tertiary butyl hydroperoxide is controlled to be within the range from about 10% to about 30% whereby the conversion and selectivity and reaction rates provide advantageous results.