The optimum conditions for the baffle plate insertion have been determined as follows:
(1) The optimum distance of baffle plates from the center line of a cylindrical vessel is equal to half the paddle length.
(2) The optimum Submersion length of baffle plates is also equal to half the paddle length.
(3) The optimum baffle width is equal to 10% of the vessel diameter.
(4) The optimum paddle' length, on the baffled conditions mentioned above, is equal to 40% of the vessel diameter.

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The Optimum construtions for gas-liquid agitation vessel have been determined as follows:
(1) The optimum submersion length of baffle plates is equal to half the liquid depth. Therefore, it is erroneous to use the baffle plates extending to the bottom of vessel as usually be found in Penicillin broth tanks.
(2) The optimum sparger loop diameter is equal to 80% of the paddle length.
(3) The optimum baffle plate width is equal to 18% or 12.5% of the tank diameter respectively, according to the number of baffle plates is 2 or 4.
(4) There is a certain minimum agitator speed needed, to absorbe gases effectively.
(5) Several types of agitators were compared each other.

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The stirrer speeds at which the contents of agitation vessels of various sizes come to similar states of mixing, are proportional to -2/3 power of the vessel diameters.
Moreover, in these corresponding speeds, the extraction velocities of solutes between two immiscible liquids and also the dissolution velocities of solid particles are equal in all ranges of stirrer speeds.
In the geometrically similar systems, powers absorbed per unit volume of agitated liquids are proportional to N³D².
From these results, it can be concluded that the agitation intensities can be measured by the power per unit volume of liquids, say H.P./m³.

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Experiments were conducted to compare the two different type reactors-the one is an usual agitated batch reactor and the other a continuous flow reactor. The flow reactor used is named "Blast Tube Reactor" composed of one long pipe only. Into this pipe, liquid and high speed gas stream are introduced resulting highly atomized phase.
In such conditons, mass transfer and contact area between liquid and gas are surplizingly increased.
As the standard of comparison of reactor performances, mass-transfe rate of a definite material from one liquid phase to the other was measured.
In the 1st. report, using the apparatus of Fig. 1-1, phenol transfer rate from water phase to benzene was measured varying shapes, positions and r.p.m. of agitator under a definite ratio of liquid volume. (H₂O:C₆H₆=6:4)
Measured capacity coefficients are shown in Fig. 3-7.
In the 2nd. report, using the apparatus of Fig. 2-1, phenole or acetic-acid transfer rate from benzene phase to water was measured.
The flow-pattern of blast tube reactor are shown in Fig. 2-2.
Data obtained are summalized in Tab. 1. Fig. 2-5 is the reproduction of typical results obtained in the Ist. report and Fig. 2-4 is those of this report. Comparison of both figures shows that much improvement in capacity coefficients are obtained for the blast tube reactor.

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In two foregoing parts, methods are indicated for determining the equilibrium relation indirectly, where a trial and error method is necessary to calculate the slope of the middle straight portion of XY curve. Relatively simple as it may be, the trial and error method is unadvisable. In this paper, a correlation is found between α₁/α₀ and n, where
α₁: ordinate of the upper XY straight line
α₀: ordinate of the lower XY straight line
and n: slope of the middle XY straight line, respectively,
and its application is informed by several examples. Effects of pressure on the equilibrium relation and the method of calculation are also discussed briefly.

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In the previous paper (this journal, 14, 270 (1950)) the author suggested a simple slide rule based on the general temperature relation of vapor pressure of liquids obtained. In the present, several slide rules are proposed for prediction of such relations as viscosity and surface tension of liquids vs temperature, viscosity and thermal conductivity of gases vs temperature, and critical temperature and critical pressure from normal boiling point. This slide rule can be constructed when the correlation between a physical constant, y, and a related variable, x, is expressed by a general equation, f₂(y)=f₁(x)+C, in which f₁ and f₂ are functions of dependent variables, x and y, respectively, and C is a constant depending on substances. If a pair of corresponding values (x₀, y₀) are given, C is eliminated, and any other correspondings of x and y are obtained. That is, if an only one point is available for a physical constant of a substance, all other values for that substance are obtainable at a glance with an accuracy satisfactory for engineering purposes.

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It is shown that a general method to caluculate the optimum temperature distribution in the catalyst zone which gives the maximum yield for the case in which a definite quantity of catalyst of a certain activity is used at a definite pressure can be given for any catalytic reaction when the accurate rate equation, the rate constants and the equillibrium constant of that reaction are known at every temperature. As an example, for the ammonia synthesis the actual optimum temperature distribution curve is calculated using the "Temkin-Emmett" rate-equation.

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