Studies were made on the kinetics of CuO reacting with gaseous mixtures of SO2, O2 and N2 of different compositions at temperatures ranging from 200 to 700℃. At low temperatures the reaction product is basic copper sulfate. Copper Sulfate is found at high temperatures and only after a large amount of basic sulfate has been formed. After about 30% of the original CuO has been converted into copper sulfate, a hard non-permeable copper sulfate layer is produced around the sample. Further reaction is controlled by gaseous diffusion through this reaction product layer. The amount of basic sulfate and normal sulfate produced has been found to increase linearly with reaction time before the formation of the non-permeable layer. The rate of formation of basic sulfate in the low temperature range and normal sulfate in the high temperature range can be represented by the following equation. where Rav. is the time-average reaction rate in weight percent per unit time; psO2 and pO2 are the partial pressures of S02 and O2 respectively;k1 k2 and k3 are constants. A reaction mechanism has been postulated. The reaction rate is considered to be controlled by the formation of sulfate ion on the solid surface between the adsorbed SO2 on the oxygen ion and another oxygen ion. In the absence of O2 in the gas phase, Cu3O is also formed as a reaction product. As Cu2O is a p-type semiconductor, the reaction rate is increased under this condition. The reaction follows a different mechanism with SO3 in the gaseous mixture, to which the present conclusion does not apply.

On the basis of previous work in hydrofining crude benzole with pure hydrogen, further study was made of the utilization of low concentration hydrogen as a raw treating gas. Successful precaution was employed to overcome coking trouble by means of pretreatment of the crude benzole and raw gas, effect of which was discussed. The influence of process variables on Br. No. and S reduction in the product oil was then investigated; the differences in reactivity of crude benzole from several sources were also observed. A set of compromised operating conditions for hydrofining crude benzole from a certain plant to obtain a product of Br. No.<0.5 and S<0.01% was suggested. The result was verified in a larger equipment with 200ml. catalyst volume. The activity of the catalyst could be maintained through the 200-hr, run. Material balance was obtained with a liquid yield of 98.7%. The product oil of Br. No.0.3 and S 0.002% after fraction nation gave benzene of synthetic grade with a 99.1% recovery. Additional experiments showed that the type 402 catalyst retained its good activity after regeneration and prolonged heat treatment at elevated temperature. Development work with pure hydrogen was carried out in a pilot plant of 9-liter catalyst volume. Under a pressure of 20 kg/cm2, 380℃, L. H. S. V. 2.0, a product of Br. No. 0.4, S 0.01% was obtained, with a liquid yield of 98.2%. Benzene, fractionated out, was of synthetic grade. The activity of the catalyst, prepared with industrial grade carrier and on an enlarged scale, remained unchanged during this 150 hr. run, and its good regeneration ability and thermal stability were also confirmed. Further demonstration plant work was recommanded to collect design data and to gain additional operating experience.

The total rate of mass transfer for the case of non-equilibrium at the liquid liquid interface for a non-ideal laminar jet was derived as follows. The interfacial mass transfer coefficient ks was then calculated from the experimental . The laminar jet was used for studying the interfacial diffusional resistance of the liquid-liquid systems. It was measured that the isobutanol-water system at nominal contact time of 0.065 to 0.342 seconds and temperature of 25℃ had interfacial resistance of 1.4 hours/meter and the ethyl acetatewater system at nominal contact time of 0.066 to 0.262 seconds and three temperatures had interfacial resistances as follows. Temperature, ℃ 20 25 30 Interfacial resistance, hours/meter 2.4 1.6 1.2 The cyclohexanol-water system at nominal contact time of 0.081 to 0.404 seconds and temperature of 25℃ had interfacial resistance of 6.3 hours/meter. From the experimental results, the interfacial resistance is closely related to the temperature, and increases with a decrease in temperature. For ethyl acetate-water system, tap water or aqueous solutions with small amount of surface-active agents such as Nekal BX or sodium hexadecanyl sulfonate was also used as jet liquid to study the interfacial resistance of mass transfer. It was found that these all Had no effect on the rate of mass transfer.