In order to obtain the process design data of platforming plant, the pilot plant studies have been made in a multiple adiabatic reactor system containing three or four reactors in series. The pilot unit has a charge capacity oF200-350 kilograms of naphtha per day. The charge stock was 85-125℃ cut of straight run Yumen gasolines for toluene production. A heat balance method based on compositions of charge stoch and platforming products was developed to evaluate the temperature drop in each reactor. The results indicated that each reactor reached adiabatic conditions. The three reactor system operation gave 25% toluene yield (weight basis on feed), corresponding to 82% of the maximum possible from conversion of naphthenes in the charge. Li.quid yield of the platformate was 92% (weight basis). Byproduct hydrogen had a purity of 95% by volume.

Rate equations obtained with a number of industrial vanadium catalysts for the oxidation of sulfur dioxide showed the complicacy of the kinetics of the reaction. .Although the theoretical rate equation for this catalytic process remains uncertain, among emperical equations the following is prefer for design purposes:

The fraction of the internal surface available for industrial vanadium catalysts in the oxidation of sulfur dioxide is rather small and becomes even smaller at higher conversions. Data from both laboratory experiments and industrial practice supported this view. The new fact on the surface available in the catalyst indicates that hollow-catalyst can be used in any part of the industrial converter and gives much higher efficiency.

Methods are devised for calculating the change of inner temperature gradient in rubber goods during vulcanization whether the temperatures of conducting medium at the both two sides are same or not. During the vulcanization of complex rubber goods such as automobile tyres, the change of inner temperature gradient has been ever calculated by foreign rubber technologists. But for vulcanization of tyres on increasing temperature at steps i.e. the outside heating is changeable with time, such method of calculation is, up to present, not succeeded. We find that the results calculated by applying the heat-conducting equation for rubber, sheets with introduction of our concept of synthesized "equivalent" numbers for complex rubber goods and that measured directly are very approximate. 3 Charts are provided in order to simplyfy the calculation. Methods of calculation of vulcanizing effect and devising of vulcanizing conditions are suggested.

The single horizontal tube evaporator we used for investigation, being described in a preceeding paper[1], was modified with a vacuum system in order to operate the boiling experiments under diminished pressures. Binary liquid mixtures employed are:- (1) Water-ethanol; (2) Benzene-toluene. Range of experiments:- (1) Heat load, 4 = 4,000 40,000 kcal/m2:hr:(C) (2) Operating pressure, p = 200 760 mm. Hg. (3) Compositions of binary liquid mixtures. A) Benzene % in benzene-toluene system:- 0%, 12%, 25%, 50%, 75%, 88%, 100%, B) Ethanol % in vvater-ethanol system:- 5%, 25%, 60%, 91.8%. The boiling beat transfer coefficients of water under various pressures were examined as preliminary experiments, the results may be correlated as follows:- a=4.0 p0.2 q0.69 For pure benzene, we obtained the following-empirical formula,- and for pure toluene,- The heat transfer coefficients of boiling mixtures of different compositions, and under different pressures were correlated with dimensionless groups suggested by ; we propose that his original equation, can be used for binary liquid mixtures in the following modified form,- with error less than ±10%. We also correlated our experimental results with C. C.equation,- for binary liquid mixtures, we propose the following modified form, with error around (+)10%.

A single tube evaporator was designed for investigating heat transter coefficients of liquid metals .t either horizontal or vertical position. The heating element, the evaporating vessel and the :ondenser were made of stainless steel. The liquid metals employed were mercury, and amalgams containing various amounts of magne-ium and sodium. The boiling heat transfer coefficients were determined under pressures from 1~11 tmospheres (abs.), heat load from 5000~47000 kcal/m2:hr, and boiling temperatures from 356~ 24℃. For mercury, we obtained the following relation,- Similar results were obtained for amalgams. Experiments were carried out under N2 atmospheres.