The treatment of a multicomponent reversible reaction network is extremely complicated because the large number of rate constants must be precisely determined and the calculation based on these rate constants is tedious. In order to reduce the degrees of freedom of the process, the authors propose a method in which we regard the reactor and the separator as a whole. Based on this approach, a N-component reversible reaction system can be treated as a two-component system. This method leads to a simple and accessible way of determining the apparent rate experimentally. For first-order reactions, an explicit, simplified expression has been derived for both lumped and distributed parameter reaction systems.

A three-dimensional mathematical model, based on differential balances of mass and momentum, has been developed to describe the two-phase flow of gas and liquid through the dropping zone of the blast furnace. Agreement between observed and calculated valuesverifies the validity of this model. On the basis of this model, various parameters for the surrounding of the dry zone of Blast Furnace Cl-BF of the Capital Iron and Steel Company have been computed, from which a diagram for demarcation of fluidization of coke and flooding of slag has been proposed.

In order to find out the better types of inserts in tubes for augmentation of heat transfer of gases in the lower Reynolds number range, flow visualization by means of hydrogen bubble technique and comparative tests of the friction drag and heat transfer of air in vertical tubes with uniform wall temperature were made. Six types of inserts were studied in the region of Reynolds numbers from 500 to 10,000. The f-Re and Nu-Re correlations of various inserts under the test condition were obtained. The heat transfer augmentation performance of these types of inserts was evaluated. On this basis, friction drag and heat transfer characteristics of the helical ribbon were investigated experimentally. The friction drag and heat transfer correlations of this kind of insert with e/d from 0.067 to 0.234 and S/e from 3.89 to 13.25 were obtained. Combining the results of the flow visualization with the performance of heat transfer augmentation, it was suggested that the spiral flow consumes less energy than the boundary layer separation to produce the same heat transfer augmentation in the laminar or transitional range.

The study of gas-liquid contact regimes on Hy-contact valve tray shows that for ordinary operation conditions the dispersion structures are. in spray, mixed froth and froth regimes respectively. The mixed froth regime occurs most commonly within the normal vapor-liquid load range. Spray is likely to be promoted by a high vapor load, low liquid rate and low weir height. The distribution of spray-froth in the mixed froth regime is different at different places of the tray and varies with the liquid loads. The interrelationship between the regimes, liquid entrainment ratios and clear liquid height is obtained and two inversion points are defined. The mechanism and the physical model of the contact regimes are discussed and tentative correlations of the phase inversion points composed of dimensionless groups are proposed.

The exergy losses and thermodynamic efficiency of MSF plant with brine recirculation are discussed by means of temperature difference functions proposed by the author. In a MSF plant, the irreversible losses are found mainly in irreversible heat-transfer and flash evaporation processes. However, the basic variables are the temperature drop from stage to stage, and the temperature differences between flashed vapor and cooling water. In this paper, the flash temperature difference function, the heat transfer TD function, and the total TD function are suggested. The proposed TD functions of MSF plant provide a convenient tool toanalyse the irreversible behavior and evaluate the thermodynamic efficiency of this system, because without such improvement the calculation of the thermodynamic efficiency of a MSF plant according to the classical formula will be not only inconvenient but also insignificant. As a result of present analysis, the reasonable parameters based on the energy consumption are easily chosen. The above-mentioned principles are confirmed by typical commercial plants and a pilot plant in Tianjin.

The sequential method is first time used for the kinetic study of oxidation of sulfur dioxide on vanadium catalyst. Data have been taken under simulating industrial conditions. With preliminary experimental data, the parameters of candidate models are estimated by nonlinear leastsquare regression. The discriminations among the eleven rival models are based upon sixteen experimental data with proposed criteria. After only one designed sequential procedure, the adequate model is found. Finally, with minimum volume design criterion, sequential procedure is also used for precise estimation of parameters. The following non-first-order hyperbolic intrinsic kinetic equation is suggested:

The isobaric vapor-liquid equilibrium data at 760mm Hg of two ternary systems, ethyl acetate-benzene-toluene and carbon tetrachloride-ethyl acetate-benzene, are determined by a modified Colburn equilibrium still. The composition of ethyl acetate-benzene-toluene ternary system is determined from two properties, refractive index (nD20) and normal boiling point, while the composition of carbon tetrachloride-ethyl acetate-benzene ternary system is determined from refractive index (nD20) and density (d425). The experimental equilibrium data of two ternary systems are correlated by the equation obtained from copolymerization in the field of polymer chemistry with characteristic constants merely related with the corresponding pure components. The results of both two ternary systems are fairly satisfactory.

The effects of liquid and gas velocities, average diameter and density of solid particles and column diameter on liquid mixing in three-phase fluidized bed were determined. On the basis of the data obtained, the following correlation for Pe; was obtained:

High active catalyst system for polymerization of butadiene may be obtained by combining MoCl4OR and proper aluminum alkyl. The conversion of 80% of butadiene can be achieved with 5×10-5 mole of MoCl4OC8H17 per 1 mole of butadiene at 70℃ in hydrogenated gasoline. The polydispersity of the polymer in the range of 1.5-2.0 is carried out with the temperature of polymerization at 30-70℃. For the purpose of regulating molecular weight and chain structure of the polymer allyl halides (allyl iodide) is satisfactory. With the increase of amount of allyl iodide, the molecular weight of the polymer decreases, the content of 1,2-units increases and the regularity of chain structure of the polymer rises. Some of the physical properties of the polymer are as follows: the content of 1,2-unit, 88-97%, limiting viscosity number 1.8-6.2(30℃, toluene), glass temperature, -27--10℃, tensile yield strength, 6.5-8.5 (kg/cm2), ultimate tensile strength, 12-25 (kg/cm2) and elongation at break, 1700-2900%.

The polymer-solvent interaction parameter μ for poly (cis-1, 4-butadiene) was determined by stress-strain measurements of swollen gum and black vulcanizates. It is found that μ is a function of vr, μ = μ0+ βvr. The μ0 valuethus obtained is consistent with those determined by osmometry and light-scattering. The effective network chain densities of vulcanizates with different degree of curing were calculated by Flory-Rehner equation. The influence of effective network chain density for poly (cis-1, 4-butadiene) on vulca-nizate properties, such as tensile stress at 300% elongation, tensile strength, tear strength, ultimate elongation and so on were studied.