The viscosity data of 61 gaseous substances under normal pressure are critically assessed. The data collected were published either for the fifty of the substances in the years from 1967 to 1979 or for the others from 1960 to 1966. The mathematical expressions used in the literature for correlating viscosity data of gaseous substances with temperature are reviewed, systematized and selected to correlate the data assessed. The coefficients of the selected correlations are determined by the method of least squares with a digital computer. The values of viscosity calculated by these correlations are then compared with the experimental measurements. For the four-coefficient correlations,(I)and In,the overall per cent deviations are 0.160 and 0.157 respectively. Equation(I) is recommended for simplicity of calculation. The two-coefficient correlations, and have nearly the same accuracy of estimating viscosity values. Equation (IV) is simple for use and equation (III) can correlate data of wider temperature range with an overall per cent deviation of 0.460.

Based on the modified surface film renewal model, a mathematical model for the liquid phase mass transfer accompanied by a 1st-order irreversible chemical reaction is derived, i. e. A discussion of the "Chemical Method" used for the determination of inter-facial area is presented. In applying this model, k1=2 is being taken as the condition for the absorption process approaching to steady state, the concept for the time of reaction penetrating through is proposed. If the depth where the relative solute concentration be degraded to 0.01 is taken as the thickness of the reaction zone ,an expression for calculating is derived. Moreover, a process for calculating the interfacial area and the frequencies of surface renewal by this model is also suggested. Based on the procedure proposed, some data taken from the literature are treated, and the results are compared with that from the Danckwerts model.

In this paper, an empirical method based on two atom-parameter equations is developed. The initial heats of chemisorption for H2 and O2 on transition d-metals are successfully evaluated. Furthermore, the energy of activation of surface chemisorption of oxygen with transition d-metals surfaces are empirically calculated using a bond energy bond order (BEBO) approach. The agreement of the calculated results with the experimental data is satisfactory. The metals are then calssified approximately into three groups, A,B and C,in which the chemisorption properties are different from each other.

A cup-jet absorber is one of the high velocity co-current equipment of mass transfer. Research on this equipment in related literatures was only restricted to the operation conditions below the liquid-gas ratio m = 8 1/m3, while works on the liquid-gas ratio m=101/m3 have not been found yet in the periodicals. The present paper is dealing with the study of the foll wing two subjects:(1) Observation of the flow patterns in a cup-jet absorber;(2)Approach to the correlated method of the pressure drop and the mass transfer data of the cup-jet absorber under the high liquid-gas ratio. The experiments were undertaken on air-ammonia-water system under the conditions of liquid-gas ratio m= 4to30 l/m3 and gas velocity WG=10to50m/s at the bootom of the cup. We arrived at the following conclusions: (1) The operation regions of a cup-jet absorber were divided into three differant flow patterns. The first state is known as a pulsation state, the second as a homogeneous and continuous state, and the third as an extreme turblent state. ( 2 ) We have presented the following empirical equations for a cup-jet absorber. In a dry column, if Re≤3.1×104, the pressure drop data for a cup-jet absorber are correlated La=8.95×10-1Re0.95 and if Re>3.14×104, La=1.168×10-1Re where La is the Lagranian number, and Re is the Reynolds number. In a wetted-cup column with the dimensionless group 0.06 and when , the flow state is of the second pattern, when , that is the third state, where the gas velocity at the bottom of the cup, m/s; the gas density, kg/m3; the gas viscosity, kg.s/m2; d0 -the diameter at the bottom of the cup, m. Besides, we have also found that the mass transfer data can be correlated by the following empirical equation; where, the overall gas mass transfer coefficient for a cup-jet in kg- mols/h.m3(unit molar concentration difference); NOG-the number of overall gas transfer units for a cup-jet.

Following the selection of internals for a 109mm diameter fluidized bed, four kinds of internals were evaluated for a 360mm diameter fluidized bed on the basis of the oxidation of o-xylene to phthalic anhydride. The yield of phthalic anhydride was chosen as the test index. The results obtained were essentially the same as those for the previous smaller bed, i.e.,the lower baffles were the best, the perforated plate slightly inferior, and the vertical tubes the least ideal. But, when vertical tubes were used in combination with horizontal plates, equivalent effects were noted with plate-type baffles having smaller spacings. Regression equations showed that fluidized beds equipped with vertical tubes were less sensitive to temperature and gas velocity, implying that the flow patterns were not the same as those for horizontal internals.

The residence time distribution for reactors with circulating systems is analysed. Equations for calculation of this residence time distribution are derived. By means of the computer, the data of the residence time distribution at various cycle ratio have been obtained. At some conditions the simplified methods for calculation of the residence time distribution for reactors with circulating systems are suggested.

The Lee-Kesler equation has been extended to gas mixtures containing hydrogen when the modified Kays rule proposed in this paper is used to determine pseudocritical constants of the mixtures. The modified Kays, rule is with A =1.15, where y find 6 are the shape factors. By using, the modified Kays rule, the Lee-Kesler equation is applied to calculate the compressibility factors of three systems, which are nitrogen-hydrogen, hydrogen-methane-nitrogen, hydrogen-nitrogen-carbon dioxide - carbon monoxide-methane, all containing hydrogen, over a wide range of pressure and temperature. Computation of the compressibility factors are carried out in the following procedure; 1. for hydrogen, 0o = 1.45, (t>o = 2. calculation of and (from equations 6 and 7 , 3 . Calculation of QT and

A procedure for qualitative and quantitative analysis of organic sulfur compounds in natural gas has been established. Chromatographic methods and selective chemical reactions have been used to determine the boiling points and structures of the sulfur compounds. Relative retentions of 12 S-compounds on 4 different liquid phases were given. Experiments on 4 compounds containing different S-group indicate that within certain concentration range, the responses of FPD as expressed by h1/2.w is independent of the nature of the S-group. Thus, a single calibration curve can be used to determine all S-compounds. Comparing with other methods, satisfactory results of qualitative and quantitative analysis of three representative natural gases in Sichuan gas fields have been obtained.

The angle factor for radiation to a tube bank is an important quantity in the industrial furnace design. In the past years, the graphical representation was frequently used. In this paper, the formulas calculating the angle factors for radiation to a bank of oval tubes are derived. These formulas are usable for the industrial furnace design. The primary results are as follows. Single bank of oval tubes:The local angle factor at any given point A(Fig. 2) is: Single-Side radiation, Double-Side radiation, where ≤PAE and≤EAG can be calculated from Eq. ( 9 ), (10), (8) and (5) respectively. Double bank of oval tubes:The local angle factor at any given point (Fig. 3,Fig. 5)is:Single-side radiation (the bank which is far away from the radiation side). Double-Side radiation, FA,D(Kt ,K2,K3,B) =FAKi ,K2,B) + FA(K, ,K2,K3, - 6) where /^GAE, /_PmAE and^/PN2AE can be calculated from Eq. (33), (32),(28),(27),(26),(25),(24) and(21) respectively. Some calculated results of the angle factor for radiation to a single bank of oval tubes are given in table 1 as an illustration example.