Density saturated liquid

Defibaugh, D.R., Morrison, G. (1996) Compressed liquid densities, saturated liquid densities, and vapor pressures of 1,1-difluoroet-hane. J. Chem. Eng. Data 41, 376-381. 

Density saturated liquid at normal boiling pressure (1) Density saturated vapor at normal boiling pressure (1) Triple point pressure [ ]... 

Equations for vapor pressure, liquid volume, saturated liquid density, liquid viscosity, heat capacity, and saturated Hquid surface tension are described in Refs. 13, 15, and 16. 

Example 20 Estimate the Density of Saturated Liquid Propane... 

From Mercury—Density and Thermal Expansion at Atmospheric Pressure and Temperatures from 0 to. 350 C, Tables of Standard Handbook Data, Standartov, Moscow, 1978. The density values obtainable from those cited for the specific volume of the saturated liquid in the Thermodynamic Properties subsection show minor differences. No attempt was made to adjust either set. 

The modified Rackett equation, density = (P /fiT.,)/ZRA was used. See Spencer, C. F., and R. P Danner, Improved Equation for Prediction of Saturated Liquid Density, y. Chem. Eng. Data 17, 236... 

The regression constants A, B, and D are determined from the nonlinear regression of available data, while C is usually taken as the critical temperature. The hquid density decreases approximately linearly from the triple point to the normal boiling point and then nonhnearly to the critical density (the reciprocal of the critical volume). A few compounds such as water cannot be fit with this equation over the entire range of temperature. Liquid density data to be regressed should be at atmospheric pressure up to the normal boihng point, above which saturated liquid data should be used. Constants for 1500 compounds are given in the DIPPR compilation. 

An analytical method for the prediction of compressed liquid densities was proposed by Thomson et al. " The method requires the saturated liquid density at the temperature of interest, the critical temperature, the critical pressure, an acentric factor (preferably the one optimized for vapor pressure data), and the vapor pressure at the temperature of interest. All properties not known experimentally maybe estimated. Errors range from about 1 percent for hydrocarbons to 2 percent for nonhydrocarbons. 

TABLE 2-396 The Modified Rockett Equation Input Parameters for Calculating Pure Saturated Liquid Densities... 

Figures 26-63 and 26-64 illustrate the significant differences between subcooled and saturated-liquid discharge rates. Discharge rate decreases with increasing pipe length in both cases, but the drop in discharge rate is much more pronounced with saturated liquids. This is because the flashed vapor effectively chokes the flow and decreases the two-phase density.

Critical pressure (psia) Saturated liquid density 499 673.0 533.1 640 473 598 525... 

In this table the parameters are defined as follows Bo is the boiling number, d i is the hydraulic diameter, / is the friction factor, h is the local heat transfer coefficient, k is the thermal conductivity, Nu is the Nusselt number, Pr is the Prandtl number, q is the heat flux, v is the specific volume, X is the Martinelli parameter, Xvt is the Martinelli parameter for laminar liquid-turbulent vapor flow, Xw is the Martinelli parameter for laminar liquid-laminar vapor flow, Xq is thermodynamic equilibrium quality, z is the streamwise coordinate, fi is the viscosity, p is the density, <7 is the surface tension the subscripts are L for saturated fluid, LG for property difference between saturated vapor and saturated liquid, G for saturated vapor, sp for singlephase, and tp for two-phase. 

The density of a material is a function of temperature and pressure but its value at some standard condition (for example, 293.15 K or 298.15 K at either atmospheric pressure or at the vapor pressure of the compound) often is used to characterize a compound and to ascertain its purity. Accurate density measurements as a function of temperature are important for custody transfer of materials when the volume of the material transferred at a specific temperature is known but contracts specify the mass of material transferred. Engineering applications utilize the density of a substance widely, frequently for the efficient design and safe operation of chemical plants and equipment. The density and the vapor pressure are the most often-quoted properties of a substance, and the properties most often required for prediction of other properties of the substance. In this volume, we do not report the density of gases, but rather the densities of solids as a function of temperature at atmospheric pressure and the densities of liquids either at atmospheric pressure or along the saturation line up to the critical temperature. 

For the CHF condition for two-phase crossflow on the shell side of horizontal tube bundles, few investigations have been conducted. Katto et al. (1987) reported CHF data on a uniformly heated cylinder in a crossflow of saturated liquid over a wide range of vapor-to-liquid density ratios. Recently, Dykas and Jensen (1992) and Leroux and Jensen (1992) obtained the CHF condition on individual tubes in a 5 X 27 bundle with known mass flux and quality. At qualities greater than zero, they found that the CHF data are a complex function of mass flux, local quality, pressure level, and bundle geometry. 

Katto, Y., S. Yokoya, S. Miake, and M. Taniguchi, 1987, CHF on a Uniformly Heated Cylinder in a Crossflow of Saturated Liquid over a Very Wide Range of Vapor-to-Liquid Density Ratio, Int. J. Heat Mass Transfer 30.1971-1977. (5)... 

Kay, W.B. Vapor pressures and saturated liquid and vapor densities of cyclopentane, methylcyclopentane, ethylcyclopentane and methylcyclohexane, J. Am. Chem. Soc., 69(6) 1273-1277, 1947. 

Antonow s rule is tlius only exact when the two mutually saturated liquids possess the same density. The observed values of cti2 should in general be slightly less than those determined from — In the case of oleic acid floating on water Devaux obtained a lens thickness of OT cm. Since p — 0 90 the interfacial surface tension should be O M dyne less than the value obtained with the aid of Antonow s rule. 

Peneloux et al. [35] have introduced a clever method of improving the saturated liquid molar volume predictions of a cubic equation of state, by translating the calculated volumes without efffecting the prediction of phase equilibrium. The volume-translation parameter is chosen to give the correct saturated liquid volume at some temperature, usually at a reduced temperature Tr = T/Tc = 0.7, which is near the normal boiling point. It is possible to improve the liquid density predictions further by making the translation parameter temperature dependent. 

Now we will examine the methods of estimating the density of a reservoir liquid at reservoir conditions. First, we will consider liquids at their bubble points or liquids in contact with gas in either case, we will call these saturated liquids. The first step in the calculation procedure is to determine the density of the liquid at standard condition. The next step is to adjust this density to reser >oir conditions. 

Cross section calculated from the molecular weight and density of liquid. The ratio of the partial pressure introduced (P) to the saturated vapor pressure (Pa). Adsorption amount on Cs2.2 divided by that on Cs2.5. J 1,3,5-Trimethylbenzene. e 1,3,5-Triisopropylbenzene. 

The equations given predict vapor behavior to high degrees of accuracy but tend to give poor results near and within the liquid region. The compressibility factor can be used to accurately determine gas volumes when used in conjunction with a vitial expansion or an equation such as equation 53 (77). However, the prediction of saturated liquid volume and density requires another technique. A correlation was found in 1958 between the critical compressibility factor and reduced density, based on inert gases. From this correlation an equation for normal and polar substances was developed (78) ... 

Maezawa, Y., Sato, H., Watanabe, K. (1990) Saturated liquid densities of HCFC 123 and HFC 134a. J. Chem. Eng. Data 35,225-228. Maezawa, Y., Sato, H., Watanabe, K. (1991a) Liquid densities and vapor pressures of l-chloro-l,l-difluoroethane (HCFC 142b). J. Chem. Eng. Data 36, 148-150. 

Determination of pure component parameters. In order to use the EOS to model real substances one needs to obtain pure component below its critical point, a technique suggested by Joffe et al. (18) was used. This involves the matching of chemical potentials of each component in the liquid and the vapour phases at the vapour pressure of the substance. Also, the actual and predicted saturated liquid densities were matched. The set of equations so obtained was solved by the use of a standard Newton s method to yield the pure component parameters. Values of exl and v for ethanol and water at several temperatures are shown in Table 1. In this calculation vH and z were set to 9.75 x 10"6 m3 mole"1 and 10, respectively (1 ). The capability of the lattice EOS to fit pure component VLE was found to be quite insensitive to variations in z (6[Pg.90]

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