Viscosity saturated liquid

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. 

Values extracted and in some cases rounded off from ttose cited in RaLinovict (ed.), Theimophysical Propeities of Neon, Ai gon, Kiypton and Xenon, Standards Press, Moscow, 1976. Ttis source contains values for tte compressed state for pressures up to 1000 bar, etc. t = triple point. Above tbe sobd line tbe condensed phase is solid below it, it is liquid. Tbe notation 5.646. signifies 5.646 X 10 . At 83.8 K, tbe viscosity of tbe saturated liquid is 2.93 X 10 Pa-s = 0.000293 Ns/ui . Tbis book was published in English translation by Hemisphere, New York, 1988 (604 pp.). 

Extensive tables of the viscosity and thermal conductivity of air and of water or steam for various pressures and temperatures are given with the thermodynamic-property tables. The thermal conductivity and the viscosity for the saturated-liquid state are also tabulated for many fluids along with the thermodynamic-property tables earlier in this section. 

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. 

A distillation operation separating a low-viscosity hydrocarbon mixture requires three shell-and-tube heat exchangers. The liquid feed is to be preheated to saturated liquid by heat recovery from another low-viscosity hydrocarbon stream. The reboiler is to be a vertical thermosyphon using steam heating. 

Note that the viscosity of the saturated liquid is equal to the viscosity of the saturated vapor at the critical point. The isobars above the saturation line give the viscosity of liquid ethane, and the isobars below the saturation line give the viscosity of ethane gas. 

Fig. 15. Viscosity of liquid water under saturation conditions as a function of 1 IT (plot of data given in97))...

Cp = isobaric specific heat c = isochoric specific heat e = specific internal energy h = enthalpy k = thermal conductivity p = pressure s = specific entropy t = temperature T = absolute temperature u = specific internal energy 4 = viscosity V = specific volume / = subscript denoting saturated liquid g = subscript denoting saturated vapor... 

The uncertainties in density are 0.05% in the saturated liquid density between 290 and 320 K, 0.2% in the liquid phase at temperatures to 400 K (with somewhat higher uncertainties above 100 MPa, up to 0.5%), 1% in the liquid phase up to 500 MPa, and 2% at higher temperatures as well as in the vapor phase. Vapor pressures have an uncertainty of 0.2%, and the uncertainties in liquid heat capacities and liquid sound speeds are 1%. The uncertainty in heat capacities may be higher at pressures above 10 MPa. The estimated uncertainty in viscosity is 1% along the saturated liquid line, 2% in compressed liquid to 200 MPa, 5% in vapor and supercritical regions. Uncertainty in thermal conductivity is 3%, except in the supercritical region and dilute gas which have an uncertainty of 5%. 

Typical uncertainties are 0.05% for density, 0.02% for vapor pressure, 0.5% to 1% for heat capacity, 0.05% for vapor speed of sound, and 1% for liquid speed of sound, except in the critical region. The uncertainty in viscosity is 1.5% along the saturated-liquid line, 3% in the liquid phase, 0.5% in the dilute gas, 3% to 5% in the vapor phase, and 5% in the supercritical region, rising to 8% at pressures above 40 MPa. Below 200 K, the uncertainty is 8%. The uncertainty in thermal conductivity is 5%. 

Sastri SRS, Rao KK (2000) A new method for predicting saturated liquid viscosity at temperatures above the normal boiling point. Fluid Phase Equilib 175 311-323... 

Figure 148. Liquid requirements for obtaining saturations S, defined by the power consumption curve as a function of the amount of PVP (binder) added to the formulation (also influence of viscosity on liquid requirement, see text) ...

The second method is quite harsh but similar to RESS process as they both involve use of SFCO as a solvent rather than an anti-solvent. This process involves dissolving the SF in molten solute and the resulting supercritical solution fed via an orifice into a chamber to allow rapid expansion under ambient conditions [17], The dissolved gas decreases the viscosity of the molten compound and so the gas saturated liquid phase is expanded to generate particles from materials that are not necessarily soluble in SF. The presence of the CO allows the material to melt at temperature significantly lower than the normal melting or glass transition temperature. 

There are many potential models that have been proposed in the Hterature. Among the popular ones that are currently enjoying widespread applications are the Lennard-Jones (LJ 12-6) equation and the Buckingham Exp-6 equation. The parameters of these equations are usually obtained by matching the theory (i.e., DFT) or simulation results (e.g., MC simulations) against various experimental properties, e.g., second virial coefficient, viscosity, vapor pressure, saturated liquid density, or surface tension, at the temperature at which the adsorption is carried out. 

The viscosity of a saturated liquid as a function of temperature can be expressed by,... 

Argon matrix reactions of alkali-metal atoms with F2 have been studied, using laser Raman and i.r. spectroscopy. The F—F stretching motion in the F2 ion occurs at ca. 460 cm compared with 892 cm" for the neutral molecule the latter band is very close to that for the gaseous molecule, and this fact clearly shows that intermolecular fluorine bonding is very feeble. Absolute measurements of the coefficient of shear viscosity of compressed liquid F2 at 90—300 K and for pressures up to 20 MPa and of saturated liquid F2 at 70—144 K have been reported. ... 

The solubility of gases in liquids is increased and that of solids is usually decreased by raising the pressure. Therefore, the solid solute of a saturated solution may precipitate during the generation of pressure and is no longer accessible for the reaction. The viscosity of liquid increases approximately twice every kilobar. This effect is particularly important for reactions containing diffusion-controlled steps. Finally, the compressibility of liquids is usually small compared to that of... 

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