The range of application of the equation of state proposed by Martin and Hou for gases was extended into liquid region. The improvement was achieved by retaining the constant, B4, in the original equation, namely and imposing the condition, , on the equation. The constant, B4, was then evaluated for a given compound. The calculated values of the saturated liquid molar volumes for carbon dioxide, normal butane, argon, methane and nitrogen, were compared with the data reported, in the reduced temperature range from about 0.65 to 1.0. The average deviation was less than 5% in each case, without loss of accuracy in gaseous region. Furthermore, no additional data were required for evaluation of the constants of the improved equation.

Experimental study of flow pattern and liquid velocity distribution by the tracer technique in a two-meter diameter single pass sieve half-tray using air-water system reveals that there exist highly non-ideal flowing behavior. Typical residence-time distribution curves covering the whole tray deck are presented, from which four flow regions can be observed, a main channelling region of non-uniform flow, a sideway region of accompanied subsidiary flow, a small region of backward flow and a complete mixing region next to the inlet weir. The tray models available in the present literature seem incapable to simulate all these complicated hydrodynamic phenomena in a large tray. An eddy diffusion model with consideration of non-uniform liquid velocity field has been developed from the basic partial differential equation of mass transfer by introducing a velocity distribution function j. Since the experimental liquid velocity profile follows approximately the exponential rule, function j can be taken in similar form with two experimentally determined constants which are dependent on the flowing condition. The non-linear partial differential equation is solved by the method of finite element. For this purpose, the equation should be transformed into elliptic form by mullipying an integrating factor (B) which is equal to exp[PejZ] where Pe is Peclet number and Z is dimensionless flow length. A computer program is designed according to this method to predict numerically the concentration profiles in the whole tray deck as well as the Murphree tray efficiencies under various operating conditions. Typical computed results are presented and discussed.

A laser technique was developed for the purpose of investigating the movement of particles in a two-dimensional gas-fluidized bed. With the aid of this technique three typical modes of these particles movements influenced by the bubble were observed. A wake renewal length was measured. It was discovered that, fw, the ratio of wake volume to bubble volume, should be considered not as a constant throughout the bed but as a function of the bubble volume. Under the same superficial gas velocity through the bed, the intensity of particle circulation was different at different heights and heigher levels more intensified circulations were, observed.

The design of tumbler (precessional) centrifuge is based on the theory of precessional separation. It is a type of automatically,continuouslly operating filter-centrifuge. This article contains two aspects: I . According to the structure feature of the horizontal precessional centrifuge, the horizontal type makes the movement of the drum more complicated than verticle type. But we did our design on the basis of the mechanical model of "the stability conditions of rotation of a rigid body about a fixed point" and so obtained the stable conditions and parameters of the drum. Theoretical analysis proved that dynamic charactaristic of precessional centrifuge is similar to that of the centrifuge, which is rotating about one single fixed axis with almost the same size of the drum. The structure characteristics will be analysed and has been proved as follows: 1) The productive capacity of precessional centrifuge with low separationfactor is similar to that of the other type of the centrifuge which needs a much high separation factor. 2) The energy distribution ratio K between solid and hollow shaft of the drum can be obtained as formula wherefl-angle between the rotating and revolutionary axis(solid and hollow shaft). I . In accordance with the mechanical model ofthe stability condition of the rigid body rotating about a fixed point",an important formula for steady work of drum has been obtaind and condition Jxi, &2-the rotating and revolutionary anglar velocities of the drum, Jx, Jy, J*-the moments of inertia of the drum with respect to the three principle axes X, Y, Z through the fixed point

Under the conditions similar to industrial ammonia synthesis, the intrinsic kinetics of Series "A" Catalysts (A110, A106) made in China for ammonia synthesis has been investigated. After the experiment data have been correlated by corrective expression of simple Temkin-Pyzhev equation, it is found that this equation is also valid for intrinsic kinetics of Series "A" Catalysts in ammonia synthesis. With the aid of computation of optimum program, we find that it is most desirable to take the value of 0.5 for a in Temkin-Pyzhev equation. The apparent energy of activation has been found to be between 40,000-45,000 kcal/kg-mol. This agrees to the results found by the previous workers. A suitable kinetics equation and kinetics parameters for application to engineering are suggested. By comparative study of kinetic data, the author have verified that the performance of catalyst A110 is better than A106 and those foreign-made commercial catalysts of same type, especially in the lower temperature range.

The kinetics of methane steam catalytic reforming reaction over Z 102 nickel catalyst had been investigated in internal recycle gradientless reactor at atmospheric pressure. Experimental conditions were as follows:reaction temperature range 500-700℃, H2O/CH4=2.5-4.5 (molar ratio), methane space velocities 2000-10000ml/h.g-cat. According to the analysis of experimental results the authors have considered that carbon monoxide and carbon dioxide are formed together in these reaction process, i. e, catalytic steam reforming of methane may be represented by parallel reaction model. The rate equations of carbon monoxide and carbon dioxide formation were obtained respectively. The dependencies of reaction rate constants k1 and k2 on temperature can be fitted in with Arrhenius equation. Some investigators considered that water gas shift reaction equilibrium was very rapidly attained in the catallytic steam reforming of methane process under usual operating conditions. Our calculations of experimental data shows that this opinion is incorrect.

A mixed kinetic model with a computer program has been proposed for the processing of the hydrodesulphrisation and hydrodenitrogenation experimental data, which can not be treated by first order or pseudo-second order kinetics. A brief review of the authors pseudo-second order kinetic model is also presented. In the pseudo-second order kinetic model a hyperbolic function of type is used to describe the experimental conversion level - reciprocoal of LHSV curves. By defining the extreme value of conversion level Ym under certain operating conditions and catalyst as Lim Y=1/b, it is possible to trans- form the above function to the following pseudo-second order kinetic equation: where and the following model equation is obtained: The predicted values of % conversion are in good agreement with the experimental values. In the case when b<1, the model fails to describe the behaviour of conver-sion curves kinetically, so a mixed kinetic model is developed by assuming both the first and second order reactions can take place on the catalyst simultaneously. Thus the following kinectic equation is obtained: The rate constants K1 and K2 can be found on a computer by preassuming a series of K2/K1 ratio and K1 values and then minimizing the sum of squares of the difference between experimental and predicted values of Y. Generally the mixed kinetic model can be used for a broad range of kinetic data in hydroprocessing. However, in the case of b>l,the pseudo-second order kinetic model seems to be preferred.

The rheological behavior of slurry of coarse polypropylene particles can not be determined by means of ordinary viscometers due to its kinematic unstability and "the wall effect" occurred in the measurement of viscosity. After ascertaining the slurry of polypropylene to be Bingham liquid by using Brabender viscometer the workers determined the plastic viscosity and yield value from the correlation between agitation power number and Reynolds number of Bingham liquid in the chemical vessel with ribbon agitator. As a result, the basic data of heat transfer, mixing and agitation in the liquid bulk polymerization of propylene were provided.

The design of a liquid membrane system for the liquid surfactant membrane seperation and concentration of K+ for use in practice is presented. First, a suitable method of design is selected, the form of the apparatus used in this method being changed in a proper way. Then, the facilitated and the active transports of K+ are investigated. We predict:(1)the presence of NaCl in KCl will cause an increase in the flow of K+;(2) this Cl- present may be one source of energy necessary for the active transport of K+;(3)the flow of K+ will be further increased if the Cl- present is replaced by Br- or I-. The experimental results are consistent with the predictions. Finally, a concrete design is suggested.

Based on classical regression analysis, experiments were carried out under certain constraints on test conditions. Using stepwise regression method, the equation for calculating the circulating water quantity of coil-type waste heat boiler has been obtained. Experimental data were compared with results calculated by the said equation.