Binary Data Source 1 Binary Triple 3 Binary Noisy Binary Data Channel Majority Decision on 3 Binary Digits Destination [Pg.191]

Unfortunately, good binary data are often not available, and no model, including the modified UNIQUAC equation, is entirely adequate. Therefore, we require a calculation method which allows utilization of some ternary data in the parameter estimation such that the ternary system is well represented. A method toward that end is described in the next section. [Pg.66]

RETURNS ERG=0 UNLESS BINARY DATA ARE MISSING FOR THE SYSTEM, IN WHICH [Pg.311]

LOADS ouPE COMPONENT AND BINARY DATA FOP USE IN THF VARIOUS CORRELATIONS FOR LIQUID AND VAPOP PHASE NONIDEALITIES, THEN DOCUMENTS THE INPUT DATA. [Pg.232]

SET ERR RETURN FOR MISSING BINARY DATA 199 IFI IABS(ER).EQ.1 ) ERR=1 RETURN [Pg.329]

B. Ternary Phase Diagram from Binary Data. 196 [Pg.139]

For systems of type II, if the mutual binary solubility (LLE) data are known for the two partially miscible pairs, and if reasonable vapor-liquid equilibrium (VLE) data are known for the miscible pair, it is relatively simple to predict the ternary equilibria. For systems of type I, which has a plait point, reliable calculations are much more difficult. However, sometimes useful quantitative predictions can be obtained for type I systems with binary data alone provided that [Pg.63]

VAPOR COMPOSITIONS Z. ENTH RETURNS ERE=0 UNLESS BINARY DATA ARE [Pg.296]

A generalisation of the similarity formulae for binary data can be derived, based on the work of Tversky [Tversky 1977 Bradshaw 1997]. This takes the form [Pg.693]

Error flag, integer variable normally zero ERG = 1 indicates binary data are missing. [Pg.310]

To illustrate, predictions were first made for a ternary system of type II, using binary data only. Figure 14 compares calculated and experimental phase behavior for the system 2,2,4-trimethylpentane-furfural-cyclohexane. UNIQUAC parameters are given in Table 4. As expected for a type II system, agreement is good. [Pg.64]

Many well-known models can predict ternary LLE for type-II systems, using parameters estimated from binary data alone. Unfortunately, similar predictions for type-I LLE systems are not nearly as good. In most cases, representation of type-I systems requires that some ternary information be used in determining optimum binary parameter. [Pg.79]

Table 12.3 Formulae for various commonly used ways to compute the similarity or distance between molecules. For the binary data a is defined to be the number of bits on in molecule A, b is the number of bits on in molecule B and c is the number of bits that are on in both A and B. Table based on [Willett et al. 1998], |

Figure 4-14. Predicted liquid-liquid equilibria for a typical type-II system shows good agreement with experimental data, using parameters estimated from binary data alone. |

Type A. Component 1 is only partially miscible with components 2 through m, but components 2 through m are completely miscible with each other. Binary data only are required for this type of system [Pg.73]

Appendix C-7 gives interaction parameters for noncondensable components with condensable components. (These are also included in Appendix C-5). Binary data sources are given. [Pg.144]

Figure 16 shows observed and calculated VLE and LLE for the system benzene-water-ethanol. In this unusually fortunate case, predictions based on the binary data alone (dashed line) are in good agreement with the experimental ternary data. Several factors contribute to this good agreement VLE data for the mis- [Pg.69]

The accuracy of our calculations is strongly dependent on the accuracy of the experimental data used to obtain the necessary parameters. While we cannot make any general quantitative statement about the accuracy of our calculations for multicomponent vapor-liquid equilibria, our experience leads us to believe that the calculated results for ternary or quarternary mixtures have an accuracy only slightly less than that of the binary data upon which the calculations are based. For multicomponent liquid-liquid equilibria, the accuracy of prediction is dependent not only upon the accuracy of the binary data, but also on the method used to obtain binary parameters. While there are always exceptions, in typical cases the technique used for binary-data reduction is of some, but not major, importance for vapor-liquid equilibria. However, for liquid-liquid equilibria, the method of data reduction plays a crucial role, as discussed in Chapters 4 and 6. [Pg.5]

Two further examples of type I ternary systems are shown in Figure 19 which presents calculated and observed selectivities. For successful extraction, selectivity is often a more important index than the distribution coefficient. Calculations are shown for the case where binary data alone are used and where binary data are used together with a single ternary tie line. It is evident that calculated selectivities are substantially improved by including limited ternary tie-line data in data reduction. [Pg.71]

The equation of Krichevsky and Ilinskaya can readily be extended to high-pressure solutions of a gas in a mixed solvent, as shown by O Connell (01) and discussed briefly by Orentlicher (03). This extension makes it possible to predict the behavior of simple multicomponent systems using binary data only. [Pg.170]

In Equation (24), a is the estimated standard deviation for each of the measured variables, i.e. pressure, temperature, and liquid-phase and vapor-phase compositions. The values assigned to a determine the relative weighting between the tieline data and the vapor-liquid equilibrium data this weighting determines how well the ternary system is represented. This weighting depends first, on the estimated accuracy of the ternary data, relative to that of the binary vapor-liquid data and second, on how remote the temperature of the binary data is from that of the ternary data and finally, on how important in a design the liquid-liquid equilibria are relative to the vapor-liquid equilibria. Typical values which we use in data reduction are Op = 1 mm Hg, = 0.05°C, = 0.001, and = 0.003 [Pg.68]

See also in sourсe #XX -- [ Pg.18 , Pg.79 , Pg.88 , Pg.120 , Pg.181 , Pg.187 ]

See also in sourсe #XX -- [ Pg.373 , Pg.399 ]

See also in sourсe #XX -- [ Pg.373 , Pg.399 ]

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