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Total pressure, vapor—liquid equilibrium data for the binary system 2-methyl-1,3-butadiene and 2-methylbutene-2 are reported at 310.93, 316.48 and 322.04 K. The experimental uncertainties in measured variables, expressed as standard deviations, are 0.0005 mole fraction, 0.01 K and 0.2% of measured pressure. The coefficients for a modified Wilson solution model are also reported. These coefficients were determined from the experimental data using a general non-linear least-squares technique which accounts for experimental uncertainties in independent and dependent variables. The standard deviations of prediction for temperature-independent coefficients are 0.17% for pressure, 0.001 K for temperature and 0.00001 for mole fraction.

Total pressure, vapor-liquid equilibrium data for the binary system composed of 2-methylbutene-1 and 2-methyl-1,3-butadiene are reported at 310.93, 316.48 and 322.03 K. The uncertainties in the measured variables, expressed as standard deviations, are 0.001 mole fraction, 0.02 K, and 0.1% of measured pressure. The coefficients for a modified form of the Wilson solution model are also reported. These coefficients were determined from the data using a general non-linear least squares technique which takes into account uncertainties in both the independent and dependent variables. The standard deviation of prediction, for temperature independent coefficients, is 0.24% for pressure, 0.0001 for mole fraction, and 0.02 K for temperature.

This article presents new, total pressure data for the isoprene—n-pentane binary system over the temperature range 300–330 K. The experimental design procedure of Howat and Swift was used as a guide for the selection of data points and for the analysis of the impact of random and potential systematic errors on the data. Regression analysis procedures used are those presented by Shanker et al. Quatitative data are presented which show the effect of mercury—hydrocarbon interaction on the measured vapor pressures of C5 hydrocarbons. The new data surpass the precision of any previously published literature data for this binary pair. The uncertainty in the measurements are 0.02 K, 0.08 kPa and 0.002 mole fraction. The predicted azeotrope composition is 0.743±0.003 mole fraction isoprene with no significant change with temperature.

A variational method has been used to study the entrance and exit effects in a falling cylinder viscometer for creeping and noncreeping flow. The computed result indicate solution convergence for NRe less than 100 and agree with experiment within ± 0.5% for NRe less than 25.

Viscosities, obtained with a falling-cylinder viscometer, are presented for liquid methane, ethane, and propane from their normal boiling points to their critical points and for n-butane from its normal boiling point to 100°C. The data of this study are compared with those of other investigators. The experimental viscosities of this study are correlated within ± 5% over the reduced-temperature range from 0.65 to 0.95 by means of a modified Smith-Brown correlation. The Grunberg-Nissan equation for estimating the critical viscosity was tested with the experimentally determined critical viscosities of this study and was found satisfactory.

The theory and calibration procedure for a cylindrical falling body viscometer is presented. Experimental viscosity data are given for liquid methane from −150°C. to the critical point and for liquid propane from −185° to +90°C. The maximum experimental error for methane data is ±8% and for propane data ±5%.

The viscosities and densities of methane-propane mixtures were determined at pressures to 5,000 lb./sq.in.abs. for 22.1 and 50.0 mole % methane over a temperature range from −120 to 37.78°C. and for 75.3 mole % methane over a temperature range from −150° to 37.78°C. Reproducibility of the viscosity data was ± 2%, and the agreement with literature values was, on the average, within ± 2%. The reproducibility of the density data was ± 0.8%, and the agreement with literature values was ± 1.2%.

A theoretical analysis was made for laminar fluid flow in the annulus of a falling cylinder viscometer. A viscometer calibration constant was defined from the results of this analysis. This constant was expressed in terms of only the physical dimensions of the viscometer. The volues lidity of the theory was demonstrated by the agreement between predicted and experimental values of the viscometer constant. Methods of representing calibration data were compared. Temperature and pressure effects on the viscometer constants were related to the mechanical properties of the viscometer materials. The results of this investigation showed that the practical design of falling cyclinder viscometers is possible.

Total pressure and PVT data are reported on n-butane, butene-1, and butadiene-1,3 and their mixtures over the temperature range 100/sup 0/ to 150/sup 0/F and the pressure range 20 to 500 psia. The data have an estimated precision of 0.1%. The experimental data are correlated, and the vapor-liquid equilibrium behavior of the binary systems is computed by integration of the general coexistence equation by the method Manley and Swift. Wilson parameters for the binary systems are computed from the experimental data and used to predict the ternary system bubble-point pressures. The predicted pressures are compared with experimental results to test the validity of the predictions, and satisfactory agreement is achieved. No ternary azeotrope is observed over the range of conditions investigated. (19 refs.)

The viscosities of methane and propane were determined at pressures to 5,000 lb./sq. in. abs. over a temperature range from −170° to 0°C. and −100° to 0°C., respectively, and the densities of propane were measured at pressures to 5,000 lb./sq. in. abs. over the temperature range from −100° to 0°C. Reproducibility of the viscosity data was about ± 1.2% and for the most part agreement with literature values was within ± 2%. the estimated accuracy of the density measurement was ± 0.5%. The data reported were well correlated in terms of residual viscosity vs. density.