Although the β-distribution function has been applied to determining the composition distribution function, the proposed method is described with the purpose of distillation calculation for the complex mixture. The experiment is carried out for the petroleum naphtha fraction, however, the functional characteristics are determined by the experiment of simple distillation, S. D., and examined with the equilibrium flash vaporization, E. F. V. In order to calculate S. D. and E. F. V. curves, the physical properties of hydrocarbons such as molecular weight and vapor pressure are correlated with the normal boiling point.

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Using mainly Amberlite LA-II (secondary amine) as the liquid anion exchanger, ion exchange equilibria for Cl^-⇔N0₃^-, Cl^-⇔CH₃COO^- and Cl^-⇔SO₄^2- systems, respectively, were measured.
The results indicated that equilibrium relationship could be expressed by the mass action law. However, in Cl^-⇔CH₃COO^- system, the free amine concentration from amine salts of acetic acid type and the distribution equilibrium of acetic acid, and also, in Cl^-⇔SO₄^2- system, the dissociation of an electrolyte in aqueous phase had to be considered. Further, it was found that the exchange equilibrium was a little influenced by temperat Are but not influenced by non-counter ion and in Cl^-⇔NO₃^- system, by kinds of dilution solvent, too.

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The problem of heat transfer with conduction in thewall of flat plate bounding a fluid in laminar flow isconsidered. The analysis is developed to determinethe effect of the conduction in the wall on heattransfer with laminar boundary layer flow.
It is confirmed that the factors determining theimportance of the conduction in the wall are Reynoldsnumber, the thickness and the length of the wall, andthe ratio on the conductivity of the wall to that ofthe fluid.
Experiments on the flat plate are done, and experimentalresults are in good agreement with the analyticalresults.

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Theoretical and experimental studies have beenperformed of the pressure-swing adsorption comprisingfour steps to remove components of low concentrations from gas mixtures. Following conclusionswere obtained:
1) As for linear isotherm systems, effluent concentrationsand variations of concentration fronts in theadsorption, pressure reducing and purge steps can beestimated theoretically.
2) In the pressure reducing step, an analytical solutionderived under an assumption of the equilibriumdesorption shows good agreements with experimentalvalues.
Moreover, the theory and the experimental resultswere applied to the removal of radioactive Kryptonin waste gases from the reprocessing of spent reactorfuels, methods of the process calculation were providedand a specific example of the calculation was descrived.

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The stream function of gas is drived to clarify the behavior of gas around bubbles in an incipient fluidized bed. These functions are utilized to estimate both the gas flow pattern and the amount of gas transferred across a bubble surface during its formation.
It was found that during the formation of bubble the amount of gas exchange between the bubble and the surrounding dense phase may be considerably larger than that during the rise of bubble.

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This paper is concerned with the pressure drops where the solid concentration is controlled during the transportation of solid particles. The demand of change in the concentration is to have a certain concentrat on of solid at the end of the transport line, because it sometimes occurs that the condition at the end of line does not fit for that of transportation due to blocking, pulsation and another reasons. To satisfy both of conditions of the concentration for the transportation and at the end of line an equipment to control the concentration by means that sucks or injects transport air from the slit located on the tube wall is devised.The pressure drops along the transport line is measured for various flow conditions using relatively small particles of 60-200μ. Basing on the particle motion, nondimentional forms are derived and experimental data in various flow conditions are shown as a same tendency for suction and injection of transport air respectively. The photographic measurement of mean particle velocities is made by a stroboscopic method using a rotating shutter and it is ascertained that the derived nondimensional forms are applicable for this kind of problems.

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Although a higher purity of CO₂ gas brings about a lower cost of the urea process, the separation cost of CO₂ gas from NH₃ synthesis becomes higher. So there will be the optimum pressure of intermediate stage separation.
In this paper this economics is analyzed from point of view of utility and investment. The calculations were carried out as follows:
At first the flash equilibria at two stages were calculated at various intermediate pressure, and then the increase in cost was estimated for both CO₂ separation system and urea process. The calculated results showed that the optimum pressure was between 8 and 10 atm. At a lower pressure than 8 atm, the total cost is controlled by the increase in CO₂ separation cost because of very large amount of recycle gas and water. On the contrary, at a higher pressure than 10 atm, it is controlled by the increas in eurea production cost because of increase in amount of unconverted NH3 and CO₂.

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