In the development of high-temperature and low-temperature chemical industries, design problems on nonadiabatic heat exchange equipments be-come gradually important. Differential equations of heat balances and transfer rates are given for cases with or without phase change of each fluid. These equations are solved under three different conditions includ-ing variation of overall transfer coefficients through both (tube and shell) walls. Conditions deviated from adiabatic operation have been discussed in case III. These methods are finally illustrated with a practical example and compared with results from adiabatic assumption, showing the import-ance of nonadiabatic consideration.

In literature, assumptions of negligible holdup or constant molal holdup are usually adopted for the batch rectification calculations. It is, however, that in actual cases the number of moles of holdup will vary from plate to plate and from time to time as composition does; therefore, the error introduced when using the constant molal holdup assumption will be con-siderable to a large amount of mixtures. In the present paper the assump-tion of constant volume holdup is proposed and therefrom equations are derived for the following processes. At the end of the "prerun" period, the amount and composition of Liquid in the still, we and Xwe, may be calculated by solving the following equations: where "h" denotes the volume of liquid holdup for each plate and "H" the corresponding number of moles, "a" and "b" are defined by equation (1) and may be considered as constants, "W0" is the moles of liquid origin-ally charged and "N" is the total number of plates of the column. For constant distillate composition processes, where "D" denotes moles of distillate and Y" is the yield fraction. By introducing the concepts of fictitious straight equilibrium line and fictitious straight operating line, the following equations are obtained: where "m" and "p" are the slopes of fictitious equilibrium line and operat-ing line respectively. From equations (6) and (9) "p" and "mD" can be solved, substitute "p" into equations (7) and (8) "mn" and "xn" are obtain-ed, then from values of "xn" and equations (4) and (5) D, W, and Y are determined. For intermittent processes with each withdrawal at steady state of the column, where V= volume of withdrawal, subscripts "q" and "q - 1" denote q-th and (q-1)-th round of steady state in the column respectively. Combine equations (10) and (11) with equation (3), successive values of "WE" and "XWe" can be obtained. The yield fraction after the s-th round of withdrawal is where For non-ideal systems, unless the equilibrium curve can be represented by y = Ax + Bx2 + Cx3, the same procedure outlined above can be followed but with instead of equations (8) and (9).

Although shale oil contains much high melting point paraffin wax, un-saturated hydrocarbons and other unstable compounds, it can produce a little that can be used for preparing transformer oil. We can separate this by distillation and dewaxing, and then by washing with acid and alkali, finally by teating with acitive green shale or clay. Thus, we can obtain a product with flash point above 140℃., and pour point below -20℃. and enough chemical stability required for transformer oil without adding any freezing-point-lowering agent and antioxydant. Furthermore, the lower viscosity of shale oil is much profitable to the cooling effect of transformer oil. In accordance with the following flow sheet, we can prepare a trans-former oil from shale oil with similar properties as those manufactured in the U.S S.R., U.S.A. and Japan. tapping adjustment of Flashing point & pouring point settling filtration product of transformer oil

This article deals with the research on the rod tint and color instensity of immedial indone effected by the temperature and quantity of sulfur used in the process. The method employed in this experiment can be briefly described as follows: (1) Finding out the most appropriate temperature by using a determin-ing quantity of sulfur; (2) Finding out the most exact quantity of sulfur by the temperature found; and (3) Finding out again the most desirable temperature by the known quantity of sulfur. With these repeated findings an immedial indone with a strong red tint and deep color intensity is obtained. It is found that the quantity of sulfur used is 1.5 times of that of indophenol at a temperature of 115?116℃., if the quantity of sodium sulfide used is 3 times of that of indophenol (±8%).

The aim of the present work is to find a suitable solidifier for the manufacture of solid alcohol. Two series of experiments were made. In the first series, the solidifiers were prepared. from wood oil, lard, or resin with aqueous solution of sodium hydroxide. In the second series, the solidifiers were made from stearic acid and solid sodium hpdroxide in various proportions. These experiments showed that the best solid alcohol is composed of I part stearic acid, 0.15 part solid sedium hydroxide and 20 parts 95 o/0 ethyl alcohol. The melting point, alcohol content and combus-tion residue of this solid alcohol are 61.5℃., 94.61% and 5.4% respectively

The calculated values of refractive index and the density of paraffins, naphthenes and petroleum fractions are two factors of considerable impor-tance in hydrocarbon analysis. Though some methods have been proposed for the calculation, they are too complicated to be made useful in routine usage for hydrocarbon analysis of petroleum fractions. The authors proposed a simple, rapid and accurate method. On the basis of available data, the refractive index and density calculated by the authors method have, on the average, deviations of 0.0018 and 0.0048 grams per ml. respectively for pure saturated hydrocarbons, and of 0.0012 and 0.0018 grame per ml. for saturated petroleum fractions. Accuracy, simplicity and rapidity aro its chief advantages.