TEORIADEECUACIONESDEESTADO_3411

THERMODYNAMICS

JOURNAL REVIEW

Equations of State for the Calculationof Fluid-Phase Equilibria

Ya Song Wei and Richard J. SadusComputer Simulation and Physical Applications Group, School of Information Technology,

Swinburne University of Technology, Hawthorn, Victoria 3122, Australia

Progress in de®eloping equations of state for the calculation of fluid-phase equilibriais re®iewed. There are many alternati®e equations of state capable of calculating thephase equilibria of a di®erse range of fluids. A wide range of equations of state fromcubic equations for simple molecules to theoretically-based equations for molecularchains is considered. An o®er®iew is also gi®en of work on mixing rules that are used toapply equations of state to mixtures. Historically, the de®elopment of equations of statehas been largely empirical. Howe®er, equations of state are being formulated increas-ingly with the benefit of greater theoretical insights. It is now quite common to usemolecular simulation data to test the theoretical basis of equations of state. Many ofthese theoretically-based equations are capable of pro®iding reliable calculations, partic-ularly for large molecules.

IntroductionEquations of state play an important role in chemical engi-

neering design, and they have assumed an expanding role inthe study of the phase equilibria of fluids and fluid mixtures.Originally, equations of state were used mainly for pure com-ponents. When first applied to mixtures, they were used only

Žfor mixtures of nonpolar Soave, 1972; Peng and Robinson,. Ž1976 and slightly polar compounds Huron et al., 1978; Asse-

.lineau et al., 1978; Graboski and Daubert, 1978 . Subse-quently, equations of state have developed rapidly for thecalculation of phase equilibria in nonpolar and polar mix-tures. There are many advantages in using equations of statefor phase equilibria calculations. Equations of state can beused typically over wide ranges of temperature and pressure,and they can be applied to mixtures of diverse components,ranging from the light gases to heavy liquids. They can beused to calculate vapor-liquid, liquid-liquid, and supercriticalfluid-phase equilibria without any conceptual difficulties.The calculation of phase equilibria has been discussed exten-

Žsively elsewhere Sadus, 1992a, 1994; Sandler, 1994; Dohrn,.1994; Raal and Muhlbauer, 1998 and earlier reviews of vari-¨

Žous aspects of equations of state are also available Martin,

Correspondence concerning this article should be addressed to R. J. Sadus.

1979; Gubbins, 1983; Tsonopoulos and Heidman, 1985; Hanet al., 1988; Anderko, 1990; Sandler, 1994; Economou and

.Donohue, 1996 .The van der Waals equation of state was the first equation

to predict vapor-liquid coexistence. Later, the Redlich-KwongŽ .equation of state Redlich and Kwong, 1949 improved the

accuracy of the van der Waals equation by introducing tem-Ž .perature-dependence for the attractive term. Soave 1972

Ž .and Peng and Robinson 1976 proposed additional modifica-tions to more accurately predict the vapor pressure, liquid

Ž .density, and equilibria ratios. Carnahan and Starling 1969 ,Ž . Ž .Guggenheim 1965 , and Boublik 1981 modified the repul-

sive term of the van der Waals equation of state to obtainaccurate expressions for hard body repulsion. Other workersŽChen and Kreglewski, 1977; Christoforakos and Franck,

.1986; Heilig and Franck, 1989 modified both the attractiveand repulsive terms of the van der Waals equation of state.

In addition to modeling small molecules, considerable em-phasis has been placed recently on modeling chain-like

Ž .molecules. Based on the theories of Prigogine 1957 andŽ . ŽFlory 1965 , other workers Beret and Prausnitz, 1975;

.Donohue and Prausnitz, 1978 developed a perturbed hard-Ž .chain theory PHCT equation of state for chain molecules.

January 2000 Vol. 46, No. 1AIChE Journal 169

To overcome the mathematical complexity of the PHCTŽ .equation of state, Kim et al. 1986 developed a simplified

Ž .version SPHCT by replacing the complex attractive part ofa PHCT by a simpler expression. To take into account theincrease in attractions due to dipolar and quadrupolar forces,

Ž .Vimalchand and Donohue 1985 obtained fairly accuratemultipolar mixture calculations by using the perturbed

Ž .anisotropic chain theory PACT . Ikonomou and DonohueŽ .1986 extended PACT to obtain an equation of state whichtakes into account the existence of hydrogen bonding, namely,

Ž .the associated perturbed anisotropic chain theory APACTequation of state.

Advances in statistical mechanics and an increase of com-puter power have allowed the development of equations ofstate based on molecular principles that are accurate for real

Žfluids and mixtures. Using Wertheim’s theory Wertheim,. Ž . Ž .1984a,b , Chapman et al. 1990 and Huang and Radosz 1990

Ž .developed the statistical associating fluid theory SAFTwhich is accurate for pure fluids and mixtures containing as-sociating fluids. Recently, various modified versions, such as

ŽLJ-SAFT Banaszak et al., 1994; Kraska and Gubbins,. Ž .1996a,b and VR-SAFT Gil-Villegas et al., 1997 have been

developed. A common feature of many newly developedequations of state is the increasing use of insights gained from

Ž .molecular simulation Sadus, 1999a to improve the accuracyof the underlying model.

Our aim is to present a wide-ranging overview of recentprogress in the development of equations of state encompass-ing both simple empirical models and theoretically-basedequations. Many useful equations of state can be constructedby combining different models of repulsive and attractive in-termolecular interactions. The theoretical backbone of thecontribution from intermolecular repulsion is the concept ofhard-sphere repulsion, whereas attractive interactions aremodeled commonly using empirical or semi-empirical ap-proach. Polymers and large chain-like molecules can betreated successfully by using a hard-sphere chain model andthis aspect is discussed. Equations of state for associatingmolecules are examined in detail and comparisons betweendifferent equations of state are considered. Commonly, equa-tions of state are developed initially for pure substances. Mix-ing rules are required to extend equations of state to mix-tures, and this topic is also addressed.

Equations of State for Simple MoleculesThe van der Waals equation of state, proposed in 1873

Ž .Rowlinson, 1988 , was the first equation capable of repre-senting vapor-liquid coexistence

V aZs y 1Ž .

V y b RTV

Ž .where Z is the compressibility factor Zs pVrRT , T is tem-perature, V is volume, p is the pressure, and R is the molaruniversal gas constant. The parameter a is a measure of theattractive forces between the molecules, and the parameter b

Žis the covolume occupied by the molecules if the moleculesare represented by hard-spheres of diameter s , then bs

3 .2p Ns r3 . The a and b parameters can be obtained from

Table 1. Modifications to the Attractive Term ofvan der Waals Equation

attŽ .Equation Attractive Term yZa

Ž . Ž .Redlich-Kwong RK 1949 1.5Ž .RT VqbŽ .a T

Ž . Ž .Soave SRK 1972Ž .RT VqbŽ .a T V

Ž . Ž .Peng-Robinson PR 1976w Ž . Ž .xRT V Vqb qb Vyb

Ž .a TŽ .Fuller 1976

Ž .RT VqcbŽ .a T V

Ž .Heyen 1980 2w Ž Ž . . Ž . xRT V q b T qc Vyb T cŽ .Sandler, 1994Ž .a T V

Ž .Schmidt-Wenzel 1980 2 2Ž .RT V qubVqwbŽ .a T V

Ž .Harmens-Knapp 1980 2 2w Ž . xRT V qVcby cy1 bŽ .a T V

Ž .Kubic 1982 2Ž .RT VqcŽ .a T V

Ž . Ž .Patel-Teja PT 1982w Ž . Ž .xRT V Vqb qc Vyb

Ž .a T VŽ .Adachi et al. 1983

wŽ .Ž .xRT Vyb Vqb2 3

Ž .a T VŽ . Ž .Stryjek-Vera SV 1986a 2 2wŽ .xRT V q2bVyb

Ž .a T VŽ .Yu and Lu 1987

w Ž . Ž .xRT V Vqc qb 3VqcŽ .a T V

Ž . Ž .Trebble and Bishnoi TB 1987 2 2w Ž . Ž .xRT V q bqc Vy bcqdŽ .a T V

Ž .Schwartzentruber and Renon 1989wŽ .Ž .xRT Vqc Vq2cqb

the critical properties of the fluid. The van der Waals equa-Ž .tion can be regarded as a ‘‘hard-sphere repulsive q

attractive’’ term equation of state composed from the contri-bution of repulsive and attractive intermolecular interactions,respectively. It gives a qualitative description of the vapor and

Žliquid phases and phase transitions Van Konynenburg and.Scott, 1980 , but it is rarely sufficiently accurate for critical

properties and phase equilibria calculations. A simple exam-ple is that for all fluids, the critical compressibility factor pre-dicted by Eq. 1 is 0.375, whereas the real value for differenthydrocarbons varies from 0.24 to 0.29. The van der Waalsequation has been superseded by a large number of other,more accurate equations of state. Many of these equationscan be categorized in terms of modifications to the basic vander Waals model.

Modification of the attracti©e termMany modifications of the attractive term have been pro-

posed. Some of these are summarized in Table 1.Ž .Benedict et al. 1940 suggested a multiparameter equation

Ž .of state, known as the Benedict-Webb-Rubin BWR equa-

January 2000 Vol. 46, No. 1 AIChE Journal170

tion

B RT y A yC rT 2 bRT y a a a0 0 0Zs1q q q2 5ž /ž /RTV RTV RTV

c g gq 1q exp y 2Ž .3 2 2 2ž / ž / ž /RT V V V

where A , B , C , a, b, c, a , g are eight adjustable parame-0 0 0ters. The BWR equation could treat supercritical compo-nents and was able to work in the critical area. However, theBWR equation suffers from three major disadvantages. First,the parameters for each compound must be determined sep-arately by the reduction of plentiful, accurate pressure-

Ž .volume-temperature PVT and vapor-liquid-equilibriumŽ .VLE data. Secondly, the large number of adjustable param-eters makes it difficult to extend to mixtures. Thirdly, its ana-lytical complexity results in a relatively long computing time.Today, because of advances in computing capabilities, thelatter disadvantage has lost much of its significance but theother disadvantages remain.

Perhaps, the most important model for the modification ofthe van der Waals equation of state is the Redlich-Kwong

Ž .equation Redlich and Kwong, 1949 . It retains the originalvan der Waals hard-sphere term with the addition of a tem-perature-dependent attractive term

V aZs y 3Ž .1.5V y b RT V q bŽ .

For pure substances, the equation parameters a and b areusually expressed as

as0.4278 R2T 2.5rpc c 4Ž .5bs0.0867RT rpc c

Ž .Carnahan and Starling 1972 used the Redlich-Kwong equa-tion of state to calculate the gas-phase enthalpies for avariety of substances, many of which are polar andror notspherically symmetric. Their results showed that theRedlich-Kwong equation is a significant improvement over

Ž .the van der Waals equation. Abbott 1979 also concludedthat the Redlich-Kwong equation performed relatively well

Žfor the simple fluids Ar, Kr, and Xe for which the acentric.factor is equal to zero , but it did not perform well for com-

plex fluids with nonzero acentric factors.The Redlich-Kwong equation of state can be used for mix-

tures by applying mixing rules to the equation of state param-Ž .eters. Joffe and Zudkevitch 1966 showed that a substantial

improvement in the representation of fugacity of gas mix-tures could be obtained by treating interaction parameters asempirical parameters. Calculations of the critical propertiesof binary mixtures indicated that, for most binary mixtures,the accuracy of the predicted critical properties could be im-proved substantially by adjusting the value of the interactionparameter in the mixing rule for the a term. Spear et al.Ž .1969 also demonstrated that the Redlich-Kwong equationof state could be used to calculate the vapor-liquid critical

Ž .properties of binary mixtures. Chueh and Prausnitz 1967a,b

showed that the Redlich-Kwong equation can be adapted topredict both vapor and liquid properties. Several other work-

Ž .ers Deiters and Schneider, 1976; Baker and Luks, 1980 ap-plied the Redlich-Kwong equation to the critical propertiesand the high-pressure phase equilibria of binary mixtures.

Ž .For ternary mixtures, Spear et al. 1971 gave seven examplesof systems for which the vapor-liquid critical properties ofhydrocarbon mixtures could be calculated by using theRedlich-Kwong equation of state. The results showed that theaccuracy of the Redlich-Kwong equation of state calculationsfor ternary systems was only slightly less than that for theconstituent binaries.

The success of the Redlich-Kwong equation has been theimpetus for many further empirical improvements. SoaveŽ . 1.51972 suggested replacing the term arT with a more gen-

Ž .eral temperature-dependent term a T , that is

V a TŽ .Zs y 5Ž .

V y b RT V q bŽ .

where

20.5 ¶2 c2R T Ta T s0.4274 1q m 1yŽ . c cž /½ 5ž /p T • 6Ž .2ms0.480q1.57v y0.176v

cRTbs0.08664 ßcp

and v is the acentric factor. To test the accuracy of Soave-Ž .Redlich-Kwong SRK equation, the vapor pressures of a

number of hydrocarbons and several binary systems were cal-Ž .culated and compared with experimental data Soave, 1972 .

In contrast to the original Redlich-Kwong equation, Soave’smodification fitted the experimental curve well and was ableto predict the phase behavior of mixtures in the critical re-

Ž .gion. Elliott and Daubert 1985 reported accurate correla-tions of vapor-liquid equilibria with the Soave equation for95 binary systems containing hydrocarbon, hydrogen, nitro-gen, hydrogen sulfide, carbon monoxide, and carbon dioxide.

Ž .Elliott and Daubert 1987 also showed that the Soave equa-tion improved the accuracy of the calculated critical proper-

Ž .ties of these mixtures. Accurate results Han et al., 1988 werealso obtained for calculations of the vapor-liquid equilibriumof symmetric mixtures and methane-containing mixtures.

Ž . Ž .In 1976, Peng and Robinson 1976 redefined a T as

20.5 ¶2 c2R T Ta T s0.45724 1q k 1yŽ . c cž /½ 5ž /p T • 7Ž .2ks0.37464q1.5422 v y0.26922v

cRTbs0.07780 ßcp

Recognizing that the critical compressibility factor of theŽ .Redlich-Kwong equation Z s0.333 is overestimated, theyc

also proposed a different volume dependence


V a T VŽ .Zs y 8Ž .w xV y b RT V V q b q b V y bŽ . Ž .

Ž .The Peng-Robinson PR equation of state slightly improvesthe prediction of liquid volumes and predicts a critical com-

Ž .pressibility factor of Z s0.307. Peng and Robinson 1976cgave examples of the use of their equation for predicting thevapor pressure and volumetric behavior of single-componentsystems, and the phase behavior and volumetric behavior ofthe binary, ternary, and multicomponent system and con-cluded that Eq. 8 can be used to accurately predict the vaporpressures of pure substances and equilibrium ratios of mix-tures. The Peng-Robinson equation performed as well as orbetter than the Soave-Redlich-Kwong equation. Han et al.Ž .1988 reported that the Peng-Robinson equation was supe-rior for predicting vapor-liquid equilibrium in hydrogen andnitrogen containing mixtures.

The Peng-Robinson and Soave-Redlich-Kwong equationsare used widely in industry. The advantages of these equa-tions are that they can accurately and easily represent therelation among temperature, pressure, and phase composi-tions in binary and multicomponent systems. They only re-quire the critical properties and acentric factor for the gener-alized parameters. Little computer time is required and goodphase equilibrium correlations can be obtained. However, thesuccess of these modifications is restricted to the estimationof vapor pressure. The calculated saturated liquid volumesare not improved and are invariably higher than experimen-tal measurements.

Ž .Fuller 1976 proposed a three parameter equation of statewhich has the form

V a TŽ .Zs y 9Ž .

V y b RT V qcbŽ .

The c parameter in Eq. 9 is defined in terms of the ratio ofŽ .the covolume to the volume b s brV

1 1 3 3c b s y y 10Ž . Ž .(ž /b b 4 2

The other equation of state parameters are calculated from

RT ¶cbsV bŽ .b pc

1y b 2qcb y 1qcbŽ .Ž . Ž .V b s bŽ .b 22qcb 1y bŽ .Ž .

2V b R T a TŽ . Ž .a ca T sŽ . •p 11c Ž .

21qcb V bŽ . Ž .bV b sŽ .a 2

b 1y b 2qcbŽ . Ž .1r2 1r2a T s1q q b 1yTŽ . Ž . Ž .r

1r4q b s br0.26 mŽ . Ž . ß2ms0.480q1.5740v y0.176v

The compressibility factor at the critical point is

1y bc 2qc b y 1qc bŽ .Ž . Ž .c c c cZ b s 12Ž . Ž .c 22qc b 1y bŽ .Ž .c c c

Fuller’s modification contains two useful features. First, theequation of state leads to a variable critical compressibilityfactor, and secondly, a new universal temperature function isincorporated in the equation making both the a and b pa-rameters functions of temperature. Fuller’s equation can bereduced to the Soave-Redlich-Kwong and van der Waalsequations. If b s 0.259921, then we have c s1, V sc a0.4274802, V s 0.0866404, Z s 0.333, and the Soave-b cRedlich-Kwong equation is obtained. If b has a value ofc1r3, then cs0, V s0.421875, V s0.125, Z s0.375, anda b cthe van der Waals equation is obtained.

Ž .Fuller 1976 reported that Eq. 9 could be used to corre-late saturated liquid volumes to a root-mean-square devia-tion of less than 5%. In the majority of cases it also improvedthe vapor-pressure deviations of the original Soave-Redlich-Kwong equation. The results of calculations indicated thatthis equation is capable of describing even polar moleculeswith reasonable accuracy.

In common with Fuller’s equation, Table 1 shows that afeature of many of the empirical improvements is the addi-tion of adjustable parameters. A disadvantage of three ormore parameter equations of state is that the additional pa-rameters must be obtained from additional pure component

Ž .data. They almost invariably require one or more additionalmixing rules when the equation is extended to mixtures. ThePeng-Robinson and Soave-Redlich-Kwong equations fulfillthe requirements of both simplicity and accuracy since theyrequire little input information, except for the critical proper-ties and acentric factor for the generalized parameters a andb. Consequently, although many equations of state have beendeveloped, the Peng-Robinson and Soave-Redlich-Kwongequations are widely used in industry, and often yield a more

Ž .accurate representation Palenchar et al., 1986 than otheralternatives. The application of cubic equations of state tothe calculation of vapor-liquid equilibria has been discussed

Ž .recently by Orbey and Sandler 1998 .

Modification of the repulsi©e termThe other way to modify the van der Waals equation is to

examine the repulsive term of a hard-sphere fluid. Many ac-curate representations have been developed for the repulsiveinteractions of hard spheres and incorporated into an equa-tion of state. Some alternative hard-sphere terms are summa-rized in Table 2. Perhaps the most widely used alternative tothe van der Waals hard-sphere term is the equation proposed

Ž .by Carnahan and Starling 1969 who obtained an expressionfor the compressibility factor of hard-sphere fluids that com-

Ž . Žpares very well Figure 1 with molecular-dynamics data Al-.der and Wainwright, 1960 . The form of the Carnahan-Star-

ling equation is

1qhqh 2 yh 3h sZ s 13Ž .31yhŽ .


Table 2. Modifications to the Repulsive Term of thevan der Waals Equation

h sŽ .Equation Repulsive Term Z21qhqh

Ž .Reiss et al. 1959 3Ž .1yh

21qhqhŽ .Thiele 1963 3Ž .1yh

1Ž .Guggenheim 1965 4Ž .1yh

2 31qhqh yhŽ .Carnahan-Starling 1969 3Ž .1yh

Ž .RT V q bŽ .Scott et al. 1971

Ž .V V y b2 2 2 3Ž . Ž .1q 3a y2 hq 3a y3a q1 h y a h

Ž .Boublik 1981 3Ž .1yh

where hs br4V is the packing fraction defined in terms ofŽ .the molecular covolume b .

To improve the accuracy of the van der Waals equation,Ž .Carnahan and Starling 1972 substituted Eq. 13 for the tra-

Ž .ditional term Vr V y b in Eq. 1, resulting in the followingŽ .equation of state CSvdW

1qhqh 2 yh 3 aZs y 14Ž .3 RTV1yhŽ .

Both a and b can be obtained by using critical properties

Figure 1. Hard-sphere compressibility factors from dif-ferent equations of state with molecular simu-lation data.

Ž .^, Alder and Wainwright 1960 ; `, Barker and Hender-Ž .son 1971 for hard spheres.

Ž 2 c2 c c c. Ž .as0.4963R T rp , bs0.18727RT rp . Sadus 1993 hasdemonstrated that Eq. 14 can be used to predict the Type IIIequilibria of nonpolar mixtures with considerable accuracy.

Ž .The Guggenheim equation Guggenheim, 1965 is a simplealternative to the Carnahan-Starling equation. It also incor-porates an improved hard-sphere repulsion term in conjunc-tion with the simple van der Waals description of attractiveinteractions

1 aZs y 15Ž .4 RTV1yhŽ .

Ž c c. ŽThe covolume b s 0.18284RT rp and attractive a s2 c2 c.0.49002 R T rp equation of state parameters are related

to the critical properties.The Guggenheim equation of state has been used to pre-

dict the critical properties of a diverse range of binary mix-Žtures Hicks and Young, 1976; Hurle et al., 1977a,b; Hicks et

al., 1977, 1978; Semmens et al., 1980; Sadus and Young,1985a,b; Waterson and Young, 1978; Toczylkin and Young,1977, 1980a,b,c; Sadus, 1992a, 1994; Wei and Sadus, 1994a,

.1999 . Despite the diversity of the systems studied, good re-sults were reported consistently for the vapor-liquid criticallocus. The critical liquid-liquid equilibria of Type II mixtureswas also represented adequately. In contrast, calculations in-volving Type III equilibria are typically only semiquantitativeŽ .Christou et al., 1986 because of the added difficulty of pre-dicting the transition between vapor-liquid and liquid-liquidbehavior. The Guggenheim equation has also proved valu-able in calculating both the vapor-liquid critical propertiesŽ .Sadus and Young, 1988 and general critical transitions of

Ž .ternary mixtures Sadus, 1992a; Wei and Sadus, 1994b . Goodresults have also been reported for the vapor-liquid and liq-uid-liquid equilibria of binary mixtures containing either he-

Ž . Ž .lium Wei and Sadus, 1996 or water Wei et al., 1996 as onecomponent.

Ž .Boublik 1981 generalized the Carnahan-Starling hard-sphere term for molecules of arbitrary geometry via the intro-

Ž .duction for a nonsphericity parameter a . Svejda and KohlerŽ .1983 employed the Boublik expression in conjunction with

Ž . Ž .Kihara’s 1963 concept of a hard convex body HCB to ob-Ž .tain a generalized van der Waals equation of state HCBvdW

1q 3a y2 hq 3a 2 y3a q1 h 2 y a 2h 3 aŽ . Ž .Zs y 16Ž .3 RTV1yhŽ .

Ž . Ž .Sadus et al. 1988 and Christou et al. 1991 have used Eq.16 for the calculation of the vapor-liquid critical properties ofbinary mixtures containing nonspherical molecules. The re-sults obtained were slightly better than could be obtainedfrom similar calculations using the Guggenheim equation of

Ž .state. Sadus 1993 proposed an alternative procedure for ob-taining the equation of state parameters. Equation 16 in con-junction with this modified procedure can be used to predictType III critical equilibria of nonpolar binary mixtures with agood degree of accuracy.

Ž .Sadus 1994 compared the compressibility factors pre-dicted by the van der Waals, Guggenheim and Carnahan-Starling hard-sphere contributions with molecular simulation

Ždata Alder and Wainwright, 1960; Barker and Henderson,


. Ž .1971 for a one-component hard-sphere fluid Figure 1 . Thecomparison demonstrates that the Guggenheim and Carna-han-Starling hard-sphere terms are of similar accuracy at lowto moderately high densities. It is at these densities that mostfluid-fluid transitions occur.

The failure of the van der Waals hard-sphere term at mod-erate to high densities has important consequences for theprediction of phase equilibria at high pressure. For example,

Ž .it has been demonstrated Sadus, 1992a that equations ofstate such as the Redlich-Kwong and Peng-Robinson equa-tions do not describe correctly the liquid-liquid critical behav-ior of mixtures that can be classified as exhibiting Type IIIbehavior in the classification scheme of van Konynenburg and

Ž .Scott 1980 . In contrast, equations of state with more accu-rate hard-sphere terms, such as the Carnahan-Starling orGuggenheim terms, can be often used to reproduce quantita-

Žtively the features of Type III behavior Sadus, 1992a, 1993;.Wei et al., 1996 .

Combining modification of both attracti©e and repulsi©eterms

Other equations of state have been formed by modifyingboth attractive and repulsive terms, or by combining an accu-rate hard-sphere model with an empirical temperature de-pendent attractive contribution.

Ž .Carnahan and Starling 1972 combined the Redlich-KwongŽ .attractive term with their repulsive term CSRK

1qhqh 2 yh 3 aZs y 17Ž .3 1.5RT V q bŽ .1yhŽ .

Their results demonstrated that this combination improvedthe prediction of hydrocarbon densities and supercritical

Ž .phase equilibria. De Santis et al. 1976 also tested Eq. 17and concluded that it yielded good results for the case ofpure components spanning ideal gases to saturated liquids.When applied to mixtures for predicting vapor-liquid equilib-ria, good accuracy in wide ranges of temperature and pres-sure can be obtained.

Ž .Chen and Kreglewski 1977 demonstrated that a good rep-resentation of the phase behavior of simple fluids could beobtained using an equation of state formed by substitutingthe a term in Eq. 17 with the power series fit of simulation

Ž .data reported by Alder et al. 1972 for square-well fluids.The functional form of this equation dubbed ‘BACK’ is

2 3 i j1qhqh yh u hZs y jD 18Ž .Ý Ý i j3 kT t1yhŽ . i j

where D are universal constants which have been fitted toi jaccurate pressure-volume-temperature, internal energy, andsecond virial coefficient data for argon by Chen and Kre-

Ž .glewski 1977 , and urk is the temperature-dependent dis-persion energy of interaction between molecules and t s0.7405. Historically, the complicated nature of the attractiveterm has precluded it from routine phase equilibria calcula-tions. However, as discussed below, the BACK equation hasbeen the inspiration for further development.

Ž .Christoforakos and Franck 1986 proposed an equationŽ . Ž .CF of state which used the Carnahan-Starling 1969 ex-pression for the repulsive term and a square-well intermolec-ular potential for attractive intermolecular interactions.

3 2 2 3V qV b qVb y b 4b e3Zs y l y1 exp y1Ž .3 ž /V RTV y bŽ .

19Ž .

Ž c .3rmwhere b s b T rT , m is typically assigned a value of 10,and V denotes molar volume. The other equation of stateparameters can be derived from the critical properties

bs0.04682 RT crpc ¶•e 20Ž .c 3sT ln 1q2.65025r l y1Ž .ßR

The e parameter reflects the depth of the square-well inter-molecular potential, and l is the relative width of the well.This equation was applied successfully to the high tempera-ture and high-pressure phase behavior of some binary aque-

Ž .ous mixtures Christoforakos and Franck, 1986 .Ž .Heilig and Franck 1989, 1990 modified the Christo-

forakos-Franck equation of state. They used a temperature-Ž .dependent Carnahan-Starling 1969 representation of repul-

sive forces between hard spheres and an alternative square-well representation for attractive forces. The functional form

Ž .of the Heilig-Franck HF equation of state is

V 3q b V 2 q b 2V y b 3 BZs q 21Ž .3 V q CrBŽ .V y bŽ .

The B and C terms in Eq. 21 represent the contributionsfrom the second and third virial coefficients, respectively, ofa hard-sphere fluid interacting via a square-well potential.This potential is characterized by three parameters reflecting

Ž .intermolecular separation s , intermolecular attractionŽ . Ž .erRT , and the relative width of the well l . The following

Ž .universal values Mather et al., 1993 were obtained by solv-ing the critical conditions of a one-component fluid, ls

3 c Ž1.26684, N s rV s0.24912 where N denotes Avogadro’sA A. cconstant and erRT s1.51147. Accurate calculations of the

Žcritical properties of both binary and ternary mixtures Heilig.and Franck, 1989, 1990 have been reported. Shmonov et al.

Ž .1993 used Eq. 21 to predict high-pressure phase equilibriafor the waterqmethane mixture and reported that theHeilig-Franck equation of state was likely to be more accu-rate than other ‘‘hard-sphereqattractive term’’ equations ofstate for the calculation of phase equilibria involving a polarmolecule.

Ž .Deiters 1981 reported a further example of an equationof state, based on the Carnahan-Starling hard-sphere termplus an improved attractive term. A feature of Deiters’ equa-tion of state is that the Carnahan-Starling term is adjusted tomore accurately reflect the repulsion of real fluids and theattractive term is obtained from an approximate formulationof square-well fluid interactions. The equation works well at


low pressures, but the critical properties at high pressures areŽ .not predicted accurately Mainwaring et al., 1988 .

Ž .Shah et al. 1994 developed an equation of state by defin-Ž hs.ing empirical relationships for the repulsive Z and the

Ž att.attractive Z contribution to the compressibility factor

V a k V ¶1h sZ s q 2V y k aŽ . V y k aŽ .0 0

2aV q k acV0attZ syV V q e V y k a RTŽ .Ž .0 • 22Ž .T

a s0.165V exp y0.03125 lnc½ ž /Tc

32T

y0.0054 ln½ 5ž / 5T ßc

In Eq. 22, a represents the molar hard-sphere volume of thefluid, k s1.2864, k s2.8225, and e is a constant, and a and0 1c are temperature-dependent parameters. A new, quarticequation of state equation is formed by combining the aboverelationships

V a k V aV q k ac1 0Zs q y2V y k a RT V q e V y k aŽ .Ž . Ž .V y k aŽ .0 00

23Ž .

Equation 23 only needs three properties of a fluid, namely,the critical temperature, the critical volume, and acentricfactor to reproduce pressure-volume-temperature and ther-modynamic properties accurately. Although it is a quarticequation and yields four roots, one root is always negativeand, hence, physically meaningless; therefore, it behaves like

Ž .a cubic equation. Shah et al. 1994 compared their quarticŽ . Ž .equation with the Peng-Robinson 1976 and Kubic 1982

equations of state and concluded that it was more accuratethan either the Peng-Robinson or the Kubic equation of state.

Ž .Lin et al. 1996 extended the generalized quartic equationŽ .of state Eq. 23 to polar fluids. When applied to polar fluids,

the equation requires four characteristic properties of thepure component, namely: critical temperature, critical vol-ume, acentric factor, and dipole moment. They calculatedthermodynamic properties of 30 polar compounds, and alsocompared with experimental literature values and the Peng-Robinson equation for seven polar compounds. Their resultsshowed that various thermodynamic properties predictedfrom the generalized quartic equation of state were in satis-factory agreement with the experimental data over a widerange of states and for a variety of thermodynamic proper-ties. The generalized quartic equation of state improves theaccuracy of calculations of enthalpy, second virial coeffi-cients, and the pressure-volume-temperature properties.

In Figure 1, we compare the compressibility factor pre-Ž . Ždicted by the Shah et al. 1994 hard-sphere term k s1.2864,0

.k s2.8225, and ys arV with molecular simulation data1Ž .Alder and Wainwright, 1960; Barker and Henderson, 1971

for one-component hard-sphere fluid. Figure 1 shows that theaccuracy of hard-sphere term of Shah et al. equation is closeto the accuracy of the Carnahan-Starling hard-sphere term.

Equations of State for Chain MoleculesPerturbed hard chain theory

Ž .Prigogine 1957 introduced a theory to explain the proper-ties of chain molecules which is based on the premise thatsome rotational and vibrational motions depend on densityand hence affect the equation of state and other configura-

Ž .tional properties. Based on Prigogine’s ideas, Flory 1965proposed a simple theory for polymer behavior. Flory’s workis similar to Prigogine’s theory except the expressions used toaccount for intermolecular interactions are taken from free-volume concepts instead of lattice theory. Limitations of bothPrigogine’s and Flory’s theories are that they can only be usedat high densities and are limited to calculations of liquid-phase properties. They give qualitatively incorrect results atlow densities, because they do not approach the ideal gas lawat zero density.

Based on perturbed hard-sphere theory for small moleculesŽ .valid at all densities and Prigogine’s theory for chain

Ž .molecules valid only at liquid-like densities , Beret andŽ .Prausnitz 1975 developed the perturbed hard-chain theory

Ž .PHCT equation of state for fluids containing very largemolecules, as well as simple molecules. The PHCT equationof state is valid for both gas- and liquid-phase properties. ThePHCT equation differs from Prigogine’s and Flory’s equa-

Žtions in two important aspects Vimalchand and Donohue,.1989 . First, to increase the applicability of the PHCT equa-

tion to a wider range of density and temperature, more accu-rate expressions in the PHCT equation are used for therepulsive and attractive partition functions. Secondly, thePHCT equation corrects the major deficiency in the theoriesof Prigogine and Flory by meeting the ideal gas limit at lowdensities.

The PHCT equation of state is derived from the followingŽ .partition function Q

N NN VV yff NQs exp q 24Ž . Ž .r , ®3 N ž /ž /V 2kTN !L

where q is the contribution of rotational and vibrationalr, ®motion of a molecule, N is the number of molecules, L is thethermal de Broglie wavelength and f is the mean potential.The V term is the free-volume, which is defined as the vol-fume available to the center of mass of one molecule as itmoves around the system holding the positions of all othermolecules fixed. The value of V can be calculated from thef

Ž .Carnahan and Starling 1972 expression for hard-spheres

tr® 3tr®y4Ž .Ž .˜ ˜V sV exp 25Ž .f 21ytr®Ž .˜

0 Ž 0where ® is a reduced volume defined as ®sVrnr® where ®˜ ˜is the close-packed volume per mole and r is the number of

.segments per molecule .


In general, the PHCT equation can be written as

aZs Z hard chain y 26Ž . Ž .

RTV

When Eq. 25 is used to determine the hard chain compress-ibility factor, and a is calculated from Alder’s polynomial

Ž .relationship Alder et al., 1972 for square-well molecular dy-namics data, the functional form of the PHCT equation ofstate is

24 tr® y2 tr®Ž . Ž .˜ ˜Zs1qc 31ytr®Ž .˜

4 Me q mA 1nm0q r® 27Ž . Ž .Ý Ý my1ž / ny1ž / ž /˜kTV ®̃ Tns1 ms1

where c is 1r3 the number of external degrees of freedom,e q is characteristic energy per molecule, and k is Boltzmann’sconstant. The A terms are dimensionless constants and arenmindependent of the nature of the molecules, and n, m arethe index for the exponent in a Taylor series in a reciprocalreduced volume. In effect, the PHCT equation of state ex-

Ž .tends the BACK equation of state Eq. 18 for chainmolecules.

w 0 Ž . xThe adjustable parameters r® , e qrk and c of the PHCTequation of state can be obtained from pressure-volume-tem-perature data for gases and liquids and from vapor-pressure

Ž .data. Beret and Prausnitz 1975 gave values for these param-eters for 22 pure fluids and compared theory with experimentfor several fluids. The results indicated that the PHCT equa-tion was applicable to a wide variety of fluids, from hydrogento eicosane to polyethylene. However, they also reported thatthe PHCT equation was not good in the critical region incommon with other analytical equations of state.

In re-deriving the PHCT equation to allow calculation ofŽ .mixture properties, Donohue and Prausnitz 1978 slightly

modified the perturbed hard-chain theory to yield better purecomponent results and, more importantly, extended thePHCT equation to multicomponent mixtures. The partitionfunction was given by

NN cV V yf®Qs exp 28Ž .3N ž /V 2ckTN !L

Equation 28 accounts for the effect of rotational and vibra-tional degrees of freedom on both the repulsive and attrac-tive forces. The pure component and binary parameters canbe obtained by fitting experimental data. Donohue and

Ž .Prausnitz 1978 reported that the PHCT equation of statecan represent the properties of most mixtures commonly en-countered in petroleum refining and natural-gas processingeven when the components differ greatly in size, shape, orpotential energy.

ŽSubsequently, many workers Kaul et al., 1980; Liu and.Prausnitz, 1979a,b, 1980; Ohzone et al., 1984 have applied

the PHCT equation to predict thermodynamic properties ofnumerous and varied types of systems of industrial interest.

Ž .Kaul et al. 1980 predicted Henry’s constants using the PHCT

equation with low values of the binary interaction parameter,and they extended the PHCT equation to predict the secondvirial coefficient of both pure fluids and mixtures. Liu and

Ž .Prausnitz 1979a showed that the PHCT equation can beused to accurately predict the solubilities of gases in liquidpolymers, where the light component is supercritical, whereasthe usual approach using excess functions is not useful intreating such supercritical gas-polymer systems. Liu and

Ž .Prausnitz 1979b, 1980 also applied the PHCT equation forŽphase equilibrium calculations in polymeric systems poly-

.mer-solvent, polymer-polymer, polymer-polymer-solvent ,taking into account the molecular weight distribution of poly-

Ž .meric molecules. Ohzone et al. 1984 correlated the purecomponent parameters reported by Donohue and PrausnitzŽ . Ž .1978 and Kaul et al. 1980 with the group volumes of BondiŽ . Ž .1968 . Chien et al. 1983 proposed a useful chain-of-rota-

Ž .tors COR equation in the spirit of the BACK and PHCTequations.

The PHCT equation is successful in calculating the proper-ties of fluids, but a practical limitation is its mathematicalcomplexity, as a result of the use of the Carnahan-Starlingfree-volume term and the Alder power series. Consequently,calculations, especially for mixtures, are time consuming. In-spired by the proven ability of the PHCT equation in calcu-lating the properties, modifications of the theory have beenproposed with the aim of simplifying the equation of state.

Simplified perturbed hard chain theoryŽ .Kim et al. 1986 developed a simplified version of PHCT

equation by replacing the attractive term of the PHCT equa-tion with a theoretical, but simple, expression based on the

Ž .local composition model of Lee et al. 1985 ; the equation isŽ .called the simplified perturbed hard chain theory SPHCT

V UYrepZs1qc Z y Z 29Ž .m Už /V qV Y

where c is 1r3 the number of external degrees of freedomper molecule, Z is the maximum coordination number,mV U represents the closed-packed molar volume given by

3 'Ž .N ss r 2 , where N is Avogadro’s number, s is the num-A Aber of segments per molecule, and s is the hard-core diame-ter of a segment. The remaining terms are calculated from

2 ¶4hy2hrepZ s 31yhŽ .

UT • 30Ž .Y sexp y1ž /2TUhst V rV ßUT se qrck

For pure substances, the SPHCT equation of state can bewritten as

4hy2h 2 Z cV UYmZs1qc y 31Ž .U3 V qV Y1yhŽ .


Ž UThe SPHCT equation of state has three parameters c, T ,U.and V and these parameters can be evaluated by fitting

simultaneously both vapor pressure and liquid density data.Ž .Kim et al. 1986 obtained these three parameters for several

Ž .n-alkanes and multipolar fluids, and van Pelt et al. 1992 andŽ .Plackov et al. 1995 reported values for more than one hun-

dred fluids.To extend the SPHCT equation to mixtures, Kim et al.

Ž .1986 proposed the following set of mixing and combiningrules

3 ¶s si iiU U² :V s x V s xÝ Ýi i i '2i

² :c s x cÝ i ii

e q •i j iU U 32Ž .² :c® Y s x x c ® exp y1Ý i j i i j ž /2c kTiij

s qsii j js si j 2

ße s e e'i j ii j j

Ž² :.The terms in angular brackets ??? represent mixtureproperties. For mixtures, the SPHCT equation of state be-comes

2 ² U :4hy2h Z cV Ym² :Zs1q c y 33Ž .U3 ² : ² :V q cV Y r c1yhŽ .

The SPHCT equation of state retains the advantages of thePHCT equation, and it also can be used to predict the prop-erties, at all densities, of fluids covering the range from argonand methane to polymer molecules. The SPHCT equationpredicts pure-component molar volumes and vapor pressures

Žalmost as accurately as the original PHCT equation Beret.and Prausnitz, 1975 . It can also predict mixture properties

with reasonable accuracy using only pure-component proper-ties. This simpler equation has been used in a number ofapplications, including for mixtures of molecules which differ

Ž . Ž .greatly in size Peters et al., 1988 . Van Pelt et al. 1991, 1992applied this simplified version to binary critical equilibria.

Ž .Ponce-Ramirez et al. 1991 reported that the SPHCT equa-tion of state was capable of providing adequate phase equi-librium predictions in binary carbon dioxide-hydrocarbonsystems over a range of temperature of interest to the oil

Ž .industry. Plackov et al. 1995 showed that the SPHCT equa-tion of state can be used to improve the quality of predictedvapor pressures of ‘‘chain-like’’ molecules over the entire

Ž .range of vapor-liquid coexistence. Van Pelt et al. 1991 usedthe SPHCT equation to calculate phase diagrams for binarymixtures and to classify these phase diagrams in accordance

Ž .with the system of van Konynenburg and Scott 1980 .

Hard-sphere chain equations of stateThe concept of a ‘‘hard-sphere chain’’ is the backbone of

many systematic attempts to improve equations of state for

Ž .real fluids. Wertheim 1987 proposed a thermodynamic per-Ž .turbation theory TPT which accommodates hard-chain

molecules. As described below, TPT is the basis of manyequations of state. The TPT concept has been extended to

Ž .include dimer properties Ghonasgi and Chapman, 1994 andŽ .application to star-like molecules Phan et al., 1993 and hard

Ž .disks Zhou and Hall, 1995 have been reported. Work onŽTPT models continues to be an active research area Stell et

.al., 1999a,b .Ž .Chapman et al. 1988 generalized Wertheim’s TPT model

to obtain the following equation of state for the compressibil-ity factor of a hard-chain of m segments

ln g hs sŽ .hc hsZ s mZ y my1 1qh 34Ž . Ž .ž /h

hsŽ .where g s is the hard-sphere site-site correlation functionat contact, s is the hard-sphere diameter, hsp mrs 3r6 isthe packing fraction, and r is the number density. The com-pressibility factor of hard sphere can be accurately deter-

Ž .mined from the Carnahan-Starling equation Eq. 13 . For theCarnahan-Starling equation, the site-site correlation functionis

2yhhsg s s 35Ž . Ž .32 1yhŽ .

Dimer properties have also been incorporated successfullyŽ .into the generalized Flory-type GF-D equations of state

ŽHonnell and Hall, 1989; Yethiraj and Hall, 1991; Gulati and.Hall, 1998 .

Ž .Ghonasgi and Chapman 1994 modified TPT for thehard-sphere chain by incorporating structural information forthe diatomic fluid. The compressibility factor of a hard chaincan be determined from the hard-sphere compressibility fac-tor and the site-site correlation function at contact of both

Ž hs. Ž hd.hard spheres g and hard dimers g

m ln g hs sŽ .hsZs mZ y 1qhž /2 h

m ln g hs sŽ .y y1 1qh 36Ž .ž / ž /2 h

Ž .Chiew 1991 obtained the site-site correlation results for harddimers

1q2hhdg s s 37Ž . Ž .22 1yhŽ .

The addition of dimer properties into the hard-sphere chainequation of state is also a feature of the Generalized Flory-

Ž . Ž .Dimer GF-D equation of state Honnell and Hall, 1989 .Ž .Chang and Sandler 1994 proposed two variants of a ther-

Ž .modynamic perturbation-dimer TPT-D equation. The TPT-D1 equation can be expressed as


1qhqh 2 yh 3 m h 5y2hŽ .Zs m y 1q3 ž /ž / 2 1yh 2yhŽ .Ž .1yhŽ .

m 2h 2qhŽ .y y1 1q 38Ž .ž / ž /2 1yh 1q2hŽ .Ž .

whereas the TPT-D2 can be represented as

1qhqh 2 yh 3 m h 5y2hŽ .Zs m y 1q3 ž /ž / 2 1yh 2yhŽ .Ž .1yhŽ .

m h 3.498y0.24hy0.414h 2Ž .y y1 1q 39Ž .ž / ž /2 1yh 2yh 0.534q0.414hŽ .Ž .Ž .

Ž . Ž .Using the TPT-D approach Eq. 36 , Sadus 1995 pro-posed that, in general

g hds g hs ahqc 40Ž . Ž .

where a and c are the constants for a straight line and thevalues can be obtained by fitting the molecular simulationdata for g hs and g hd. Equation 40 can be used in conjunctionwith Eq. 36 to obtain a new equation of state, called the sim-

Žplified Thermodynamic Perturbation Theory-Dimer STPT-.D equation of state. The general form of the STPT-D equa-

tion of state for pure hard-sphere chains is

ln g hs a 2y m hŽ .hsZs1q m Z y1 q 1y m h q 41Ž . Ž . Ž .

h 2 ahqcŽ .

Ž .Sadus 1995 applied the STPT-D equation to the predictionof both the compressibility factor of 4-, 8-, 16-, 51- and 201-mer hard-chains and the second virial coefficients of up to128-mer chains. Comparison with molecular simulation dataindicated that the STPT-D equation generally predicts boththe compressibility factor and the second virial coefficient

Žmore accurately than other equations of state Chiew equa-.tion, GF-D, TPT-D1, TPT-D2 .

By using some elements of the one-fluid theory, SadusŽ .1996 extended the STPT-D equation to hard-sphere chainmixtures without requiring additional equation of state pa-rameters. The compressibility factor predicted by the STPT-Dequation of state was compared with molecular simulationdata for several hard-sphere chain mixtures containing com-ponents with either identical or dissimilar hard-sphere seg-ments. Good agreement with simulation data was obtainedwhen the ratio of hard-sphere segment diameters for thecomponent chains is less than 2. The accuracy of the STPT-Dequation compared favorably with the results obtained forother hard-sphere chain equations of state. Recently, a sim-

Žplification of the STPT-D equation has been proposed Sadus,.1999b . The word-sphere chain approach has also been ex-Ž .tended Sadus, 2000 to include HCB chains.

Perturbed anisotropic chain theoryBy including the effects of anisotropic multipolar forces ex-

plicitly into the PHCT equation of state, Vimalchand et al.

Ž .Vimalchand and Donohue, 1985; Vimalchand et al., 1986Ž .developed the perturbed anisotropic chain theory PACT

which is applicable to simple as well as large polymericmolecules with or without anisotropic interactions. The PACTequation of state accounts for the effects of differences inmolecular size, shape, and intermolecular forces includinganisotropic dipolar and quadrupolar forces. In terms of thecompressibility factor, the PACT equation of state can berepresented as

Zs1q Z repq Z isoq Zani 42Ž .

The 1q Z rep term is evaluated in an identical way to the cor-Ž .responding of the PHCT equation of state see Eq. 27 .

By extending the perturbation expansion of Barker andŽ .Henderson 1967 for spherical molecules to chainlike

molecules, the attractive Lennard-Jones isotropic interac-tions are calculated as

2L J L JA A2 2iso L J L J L JZ s Z q Z y2Z 1y 43Ž .1 2 1 L J L Jž / ž /A A1 1

where A is the Helmholtz function, LJ stands for Lennard-Jones, and iso denotes isotropic interactions. The contribu-tions to Eq. 43 are evaluated from

LJ ¶A c A1 1ms Ý mÑkT ®̃T m

LJA c C C C2 1m 2 m 3ms q qÝ m mq1 mq22ÑkT 2® ® 2®˜ ˜ ˜T m

c mA1mL JZ s Ý1 m˜ ®̃T m • 44Ž .c mC mq1 C mq2 CŽ . Ž .1m 2 m 3mL JZ s q qÝ2 m mq1 mq22˜ 2® ® 2®˜ ˜ ˜T m

T ckTT̃ s sUT e q

'® ® 2®s s˜ U 3 ß® N rsA

with the constants A sy8.538, A sy5.276, A s3.73,11 12 13A sy7.54, A s23.307, and A sy11.2, C sy3.938,14 15 16 11C sy3.193, C sy4.93, C s10.03, C s11.703, C s12 13 14 21 22y3.092, C s4.01, C sy20.025, C sy37.02, C s26.9323 24 31 32and C s26.673.33

The anisotropic multipolar interactions are calculated us-Ž .ing the perturbation expansion of Gubbins and Twu 1978

assuming the molecules to be effectively linear

2ani aniA A3 3ani ani ani aniZ s Z q Z y2Z 1y 45Ž .2 3 2 ani aniž / ž /A A2 2

where the superscript ani denotes the anisotropic interac-


tions and

ani Ž10. ¶A cJ2sy12.44

2NkT T̃ ®̃Q

ani Ž15.A cJ cK3s2.611 q77.716

3 3 2NkT ˜ ˜T ® T ®˜ ˜Q Q

Ž10. Ž10.cJ ln JaniZ sy12.44 1q r̃2 2 r˜ ˜T ®̃Q

Ž15. Ž15.cJ ln JaniZ s2.611 1q r̃3 3 r˜ ˜T ®̃ •Q 46Ž .

cK ln Kq77.716 2q r̃

3 2 r˜ ˜T ®̃Q

'® ® 2®s s˜ U 3® N rsA

T ckTT̃ s sQ UT e qQ Q

5r3 2N QA se sQ ß' a2 s

where a is the surface area of a segment, s is the soft-coresdiameter of a segment and the quadrupole moment, Q is re-lated to the quadrupolar interaction energy per segment, Q2

s2 Ž U.5r3sQ rr ® . In Eq. 46, the J terms are the integrals given

Ž .by Gubbins and Twu 1978 .The PACT equation is valid for large and small molecules,

for nonpolar and polar molecules, and at all fluid densities.Ž .The calculations of Vimalchand et al. 1986 show that the

explicit inclusion of multipolar forces allows the properties ofhighly nonideal mixtures to be predicted with reasonable ac-curacy without the use of a binary interaction parameter.However, for pure fluids, the predictive behavior of the PACTequation of state is similar to other comparable equations ofstate.

Equations of State for Associating FluidsAssociated perturbed anisotropic chain theory

Ž .Ikonomou and Donohue 1986 incorporated the infiniteequilibrium model and monomer-dimer model into the PACTequation to derive the associated perturbed anisotropic chain

Ž .theory APACT equation of state. The APACT equation ofstate accounts for isotropic repulsive and attractive interac-tions, anisotropic interactions due to the dipole andquadrupole moments of the molecules and hydrogen bond-ing, and is capable of predicting thermodynamic properties ofpure associating components as well as mixtures of more than

Ž .one associating component Ikonomou and Donohue, 1988 .The APACT equation of state is written in terms of the com-pressibility factor, as a sum of the contributions from theseparticular interactions

Zs1q Z repq Zatt q Zassoc 47Ž .

The Zassoc term for one and two bonding sites per moleculeis evaluated from the material balance and expressions for

assoc Žthe chemical equilibria. The Z is given by Ikonomou and.Donohue, 1986; Economou and Donohue, 1991, 1992

nTassocZ s y1 48Ž .n0

where n is the true number of moles, and n is the numberT 0of moles that would exist in the absence of association. Therepulsive and the attractive terms in the APACT equationare association independent because of the assumptions madeabout the variation of the parameters of the associatingspecies with the extent of association. The Z rep and Zattr are

Ž .given by Vimalchand et al. 1985, 1986 and Economou et al.Ž .1995

2 ¶4hy2hrepZ sc 3 • 491yh Ž .Ž . ßattr L J L J ani aniZ s Z q Z q ??? q Z q Z q ???1 2 2 3

Ž .Economou and Donohue 1992 extended the APACTequation of state to compounds with three associating sitesper molecule. The three-site APACT equation of state wasdeveloped to allow calculation of vapor-liquid equilibria andliquid-liquid equilibria of systems of water and hydrocarbons.

Ž .Economou and Donohue 1992 tested the accuracy of thethree-site APACT equation over a large range of tempera-tures and pressures for aqueous mixtures with polar and non-polar hydrocarbons. They concluded that the three-siteAPACT equation was accurate in predicting phase equilibriaof different types for aqueous mixtures of nonpolar hydrocar-bons with no adjustable parameters. For aqueous mixtureswith polar hydrocarbons, the three-site APACT equation re-quires a binary interaction parameter for the accurate esti-

Žmation of the phase equilibria. The comparison Economou.and Donohue, 1992 of the two-site and three-site APACT

equations of state was also investigated for the prediction ofthe thermodynamic properties of pure water from the triplepoint to the critical point. For most of the systems examined,the three-site APACT equation was in better agreement withthe experimental data than the two-site APACT equation.

Ž .Smits et al. 1994 applied the APACT equation to the su-percritical region of pure water and showed that, over a largepressure and temperature range that included the near-criti-cal region, the agreement between calculations and experi-mental data was good. They also reported that, although thedifference between the APACT two-site and the APACTthree-site model appeared to be small, the accuracy of thethree-site APACT equation of state for volumetric propertieswas higher than that of the two-site model. Economou and

Ž .Peters 1995 demonstrated that the APACT equation can beapplied to correlate the vapor pressure and the saturated liq-uid and saturated vapor densities of pure hydrogen fluoridefrom the triple point up to the critical point with good accu-

Ž .racy. Economou et al. 1995 applied the APACT equation towater-salt phase equilibria and showed that the APACT


equation accounted explicitly for the strong dipole-dipole in-teractions between water and salt molecules. Other theoreti-cally based models of association are discussed elsewhereŽ .Stell and Zhou, 1992; Zhou and Stell, 1992 .

Statistical associating fluid theoryŽ .By extending Wertheim’s 1984a,b, 1986a,b,c, 1987 theory,

Ž .Chapman et al. 1988, 1990 proposed a general statisticalŽ .associating fluid theory SAFT approach. Huang and Ra-

Ž .dosz 1990 developed the SAFT equation of state. The SAFTequation of state accounts for hard-sphere repulsive forces,

Ždispersion forces, chain formation for nonspherical.molecules and association, and it is presented as a sum of

four Helmholtz function terms

A Aideal Aseg Achain Aassoc

s q q q 50Ž .NkT NkT NkT NkT NkT

where A and Aideal are the total Helmholtz function and theideal gas Helmholtz function at the same temperature anddensity.

The term Aseg represents segment-segment interactionsand can be calculated from

Aseg Aseg0

s m 51Ž .NkT NkT

seg Žwhere m is the number of segments per chain, and A per0.mole of segments is the residual Helmholtz function of the

nonassociated spherical segments. It has two contributions:the hard-sphere and dispersion

Aseg Ahs Adisp0 0 0

s q 52Ž .NkT NkT NkT

The hard-sphere term can be calculated as proposed by Car-Ž .nahan and Starling 1969

Ahs 4hy3h 20

s 53Ž .2NkT 1yhŽ .

Ž .For the dispersion term, Huang and Radosz 1990 used aŽ .power series that was initially fitted by Alder et al. 1972 to

molecular dynamics data for a square-well fluids

disp i jA u h0s D 54Ž .Ý Ý i jNkT kT ti j

where D are universal constants which have been fitted toi jaccurate pressure-volume-temperature, internal energy, andsecond viral coefficient data for argon by Chen and Kre-

Ž .glewski 1977 , and urk is the temperature-dependent dis-persion energy of interaction between segments.

The term Achain is due to the presence of covalent chain-forming bonds among the segments and can be determined

from

Achain 1yhr2s 1y m ln 55Ž . Ž .3NkT 1yhŽ .

The term Aassoc is the Helmholtz function change due to as-sociation and for pure components it can be calculated from

assocA X 1as ln X y q M 56Ž .Ý aNkT 2 2a

where M is the number of association sites on each molecule,X is the mole fraction of molecules that are not bonded ata

site a , and the summation is over all associating sites on themolecule.

Ž .Huang and Radosz 1990 also gave the SAFT equation interms of the compressibility factor

Zs1q Zhsq Zdispq Zchain q Zassoc 57Ž .

where

2 ¶4hy2hhsZ s m 31yhŽ .

i ju hdispZ s m jDÝÝ i j kT ti j • 58Ž .

25r2 hyhŽ .chainZ s 1y mŽ . w x1yh 1y 1r2 hŽ . Ž .

A1 1 XassocZ s r yÝ A ß2 rXA

Ž .Chapman et al. 1990 reported that the agreement withmolecular simulation data was good at all the stages of modeldevelopment for associating spheres, mixtures of associatingspheres, and nonassociating chains up to ms8. Huang and

Ž .Radosz 1990, 1991 applied their SAFT equation to corre-late vapor-liquid equilibria of over 100 real fluids, and theyalso demonstrated that the SAFT equation was applicable tosmall, large, polydisperse, and associating molecules over the

Ž .whole density range. Huang and Radosz 1991 tested 60Ž .phase equilibrium data sets for asymmetric smallqlarge and

associating binary systems. They concluded that the mixingrules for the hard sphere, chain, and associating terms werenot required when using rigorous statistical mechanical ex-pressions. Only the dispersion term required mixing rules, andonly one binary temperature-independent parameter was re-quired to represent the experimental data. Yu and ChenŽ .1994 also used the SAFT equation to examine the liquid-liquid phase equilibria for 41 binary mixtures and 8 ternarymixtures using many of the parameters of Huang and RadoszŽ . Ž .1990, 1991 . Economou and Tsonopoulos 1997 appliedAPACT and SAFT equations of state to predict the phaseequilibrium of waterrhydrocarbon mixtures.


Simplified statistical associating fluid theoryŽ .Fu and Sandler 1995 developed a simplified statistical as-

Ž .sociating fluid theory SSAFT equation by modifying the dis-persion term of the equation. The SSAFT equation is of the

Ž hs.same form as Eq. 57. It retains the original hard-sphere Z ,Ž chain. Ž assoc. Ž .chain Z , and association Z terms see Eq. 58 but

the contribution of dispersion interactions is given by

V UYdispZ sy mZ 59Ž .M Už /V qV Ys

ŽEquation 59 is the attraction term for a square-well fluid Lee.et al., 1985 and was used in the SPHCT equation of state.

For pure components, the parameters of the SSAFT equa-tion of state were obtained by fitting vapor pressure and liq-

Ž .uid density data and the results Fu and Sandler, 1995showed that the SSAFT equation was generally similar to, orslightly more accurate than, the original SAFT equation.When the SSAFT equation applied to both self-associatingand cross-associating binary mixtures, only one binary ad-

Žjustable parameter was needed. The comparison Fu and.Sandler, 1995 with the original SAFT equation for binary

mixtures demonstrated that the simplified SAFT equation ofstate usually led to better correlated results than the originalSAFT equation, and was simpler and easier to use.

( )Hard-sphere statistical associating fluid theory HS-SAFTThe HS-SAFT equation of state is a simplified version of

the SAFT equation of state, which treats molecules as chainsof hard-sphere segments with van der Waals interactions. In

Ž .the HS-SAFT Chapman et al., 1988 equation, the Helmholtzfunction A is separated into different contributions as

A Aideal Ahs Am f Achain Assoc

s q q q q 60Ž .NkT NkT NkT NkT NkT NkT

hs Ž .where A is the contribution from hard spheres HS to theHelmholtz function and Am f are the contributions from

Ž .long-range meanfield mf dispersion forces to the Helmholtzfunction. The sum of Ahs and Am f is called Amono

Amono Ahs Am f

s q 61Ž .NkT NkT NkT

that is, the monomer-monomer contribution to the Helmholtzfunction which refers to the term Aseg in the original SAFT

Ž .equation Chapman et al., 1990; Huang and Radosz, 1990 .Ž . Ž .Galindo et al. 1996, 1997 and Garcia-Lisbona et al. 1998

Ž .used the expression of Boublik 1970 for the hard-spherecontribution

hs 3 3A 6 z 3z z zs 1 2 2s yz ln 1yz q qŽ .0 32 2ž /NkT pr 1yzz Ž . z 1yzŽ .33 3 3

62Ž .

where r s NrV is the total number density of the mixture.

The reduced densities z for a binary mixture are defined asl

npr prl l lz s x m s s x m s q x m s 63Ž .Ž .Ýl i i i 1 1 1 2 2 26 6is1

z is the overall packing fraction of the mixture, m is the3 inumber, and s is the diameter of spherical segments of chainii.

The contribution due to the dispersive attractive interac-tions is given at the mean-field level in terms of the van derWaals one-fluid theory. For binary mixtures

Am f r2 2 2 2sy a x m q2a x x m m q a x m 64Ž .Ž .11 1 1 12 1 2 1 2 22 2 2NkT kT

where a represents the integrated strength of segment-seg-ment mean-field attraction, and m is the number of spheri-2cal segments of chain 2.

Ž .By using the HS-SAFT equation, Galindo et al. 1996, 1997performed the phase equilibria predictions with good agree-ment with experimental results for binary mixtures of water

Ž .q n-alkanes Galindo et al., 1996 and waterqhydro fluorideŽ . Ž .Galindo et al., 1997 . Garcia-Lisbona et al. 1998 used HS-SAFT to describe the phase equilibria of aqueous solutionsof alkyl polyoxyethylene mixtures and reported that the HS-SAFT equation was able to describe the phase behavior ofthese systems. The results showed the reasonable agreementbetween the theoretical prediction and experimental results.

( )Lennard-Jones statistical associating fluid theory LJ-SAFTŽ .Banaszak et al. 1994 incorporated Lennard-Jones interac-

tions in the context of thermodynamic perturbation theory toformulate an equation of state for Lennard-Jones chains.They demonstrated the feasibility of the LJ-SAFT formula-tion, however, comparison of the calculated compressibilityfactor for 8-mer, 16-mer, and 32-mer chains did not matchsimulation data.

Ž .Later, Kraska and Gubbins 1996a,b also developed anequation of state for Lennard-Jones chains by modifying theSAFT equation of state in two major ways. First, a Lennard-Jones equation of state was used for the segment contribu-tion; secondly, a term was added that accounts for thedipole-dipole interaction in substances like the 1-alkanols andwater. In terms of the Helmholtz function the general expres-sion for the LJ-SAFT equation of state is

A Aideal Aseg Achain Aassoc Adipole

s q q q q 65Ž .NkT NkT NkT NkT NkT NkT

where Adipole is a term for the effect of long-range dipolarinteraction. For the hard-sphere term

Ahs 5 h 34y33hq4h 2Ž .s ln 1yh q 66Ž . Ž .2NkT 3 6 1yhŽ .

For the Lennard-Jones segment term, Kraska and GubbinsŽ . Ž .1996a,b used the Kolafa and Nezbeda 1994 equation whichcovers a larger range of temperature and density and is more


reliable outside the region of fit. It can be expressed as

Aseg mU2 U jh s ir2s A qexp ygr rTD B q C T rŽ . Ý Ž .2, h BH i jž /NkT NkT ij

67Ž .

where

0 ¶ir2D B s C TÝ2, h BH i

isy7Ur s mbrVm •p 68Ž .U 3hs r sBH6

1ir2s s D T q D ln TÝBH i ln ß

isy2

where C and D , C and D are numerical constants andi i i j lnadjustable parameters, hBH stands for hybrid Barker-Henderson, and details were given by Kolafa and NezbedaŽ .1994 .

For the dipole-dipole term, the resulting Helmholtz func-tion is

Adipole A 12s 69Ž .ž /NkT T 1y A rAŽ .3 2

where

U U4 ¶2p r mŽ6.A sy J2 U3 T

U2 U 6332p 14p r m333A s K(3 222U 2135 5 T •T Tk 70Ž .BUT s s˜ eT

U 3'm smr e msUr s rb ß3bs N sL

The coefficients J Ž6. and K 333 are integrals over two-body222and three-body correlation function for the Lennard-Jones

Ž .fluid and have been calculated by Twu and Gubbins 1978a,b .Ž .Kraska and Gubbins 1996a,b applied the LJ-SAFT equa-

tion of state to pure fluids and binary mixtures. The resultsfor pure fluids showed substantially better agreement withexperiment than the original SAFT equation for the phasediagram the n-alkanes, 1-alkanols, and water. The LJ-SAFT

Ž .equation of state was also found Kraska and Gubbins, 1996bto be more accurate in describing binary mixtures of n-alkanern-alkane, 1-alkanolrn-alkane, and waterrn-alkane

Ž .than the original SAFT equation. Recently, Chen et al. 1998reported an alternative LJ-SAFT equation. They reportedthat the vapor pressures calculated from their equation canbe fitted to experiment more accurately than the originalSAFT equation.

( )Square-well statistical associating fluid theory SW-SAFTThe thermodynamic perturbation formalism was extended

Ž .by Banaszak et al. 1993 to obtain an equation for chains ofŽ .square-well statistical associating fluid theory SW-SAFT

molecules

ln g sws s , hŽ .swc swsZ s mZ q 1y m 1qh 71Ž . Ž .ref ž /h

where g sws is the site-site correlation function at contact ofsquare-well spheres, and Z sws is the compressibility factor ofrefsquare-well spheres which can be calculated from Barker-

Ž .Henderson perturbation theory. Tavares et al. 1995 alsoproposed equation of states for square-well chains using theSAFT approach. In addition to properties of monomer seg-ments, they included dimer properties in the spirit of the

Ž .TPT-D1 equation Eq. 38 . The concepts have been extendedŽto hetero-segmented molecules Adidharma and Radosz,

.1998 . Recently, six different SW-SAFT models have beenŽ .reviewed Adidharma and Radosz, 1999 . According to the

Ž .comparison reported by Adidharma and Radosz 1999 , theaddition of dimer structure does not improve the usefulnessof SW-SAFT equations for representing real fluids signifi-cantly. Originally, the validity of SW-SAFT equations werelimited to a square well with a width of 1.5s . This limitation

Žhas been addressed by subsequent work Chang and Sandler,.1994; Gil-Villegas et al., 1997 .

By providing an additional parameter which characterizedthe range of the attractive part of the monomer-monomer

Ž .potential, Gil-Villegas et al. 1997 proposed a general ver-sion of SAFT for chain molecules formed from hard-core

Ž .monomers with an arbitrary potential of variable range VR .As discussed above, the general form of the SAFT equationof state can be written as

A Aideal Amono Achain Aassoc

s q q q 72Ž .NkT NkT NkT NkT NkT

Ž .In VR-SAFT Gil-Villegas et al., 1997 , the ideal Helmholtzfunction Aideal and the contribution to the Helmholtz func-tion due to interaction association Aassoc are the same as inEq. 50. The contribution due to the monomer segments Amono

is given by

Amono Am Ahs2s m s m q b A q b A 73Ž .1 2ž /NkT NkT NkT

where Am is the Helmholtz function per monomer, m is thenumber of monomers per chain, b s1rkT , and A and A1 2are the first two perturbation terms associated with the at-tractive well.

The contribution to the Helmholtz function due to the for-mation of a chain of m monomers Achain is

AchainMsy 1y m ln y s 74Ž . Ž . Ž .

NkT

MŽ .where y s is the monomer-monomer background correla-tion function evaluated at hard-core contact.


Ž .Gil-Villegas et al. 1997 gave the analytical expressions ofthe A and A for square-well fluids ranges 1.1F lF1.81 2

Asws A®dWg hs 1: h 75Ž .Ž .1 1 eff

1 Asw1sw h sA s eK h 76Ž .2 2 h

where e and l are the depth and the range parameter of theattractive well, respectively, and

®dW 3 ¶A sy4he l y1Ž .1

1yh r2effh s •g 1; h sŽ . 77Ž .eff 31yhŽ .eff ß2 3h sc hqc h qc heff 1 2 3

The coefficients c were given by the matrixn

c 2.25855 y1.50349 0.249434 11

c y0.669270 1.40049 y0.827739 ls22� 0 � 0 � 0c 10.1576 y15.0427 5.30827 l3

78Ž .

Ž . hsIn the second-order term Eq. 76 , K is the isothermalcompressibility of the hard-sphere fluid and was given by

41yhŽ .hsK s 79Ž .21q4hq4h

The analytical expressions of the A and A for Sutherland1 2fluids and Yukawa fluids over variable range were also given

Ž .by Gil-Villegas et al. 1997 .The VR-SAFT equation broadens the scope of the original

Ž .SAFT equation Huang and Radosz, 1990 and improves thechain contribution and the mean-field van der Waals descrip-tion for the dispersion forces of the HS-SAFT treatment.

Ž .Gil-Villegas et al. 1997 demonstrated the adequacy of theVR-SAFT equation in describing the phase equilibria of chainmolecules such as the n-alkanes and n-perfluoroalkanes.

Ž .Davies et al. 1998 showed the VR-SAFT provided a simpleand compact equation of state for Lennard-Jones chains, andit is valid for ranges of density and temperature of practical

Ž .interest. McCabe et al. 1998 used the VR-SAFT equationto predict the high-pressure fluid-phase equilibrium of binarymixtures of n-alkanes and obtained good agreement with ex-

Ž .periment. Galindo et al. 1998 provided a detailed analysiso f th e V R -S A F T a p p ro a c h fo r m ix tu re s o ffluids with nonconformal intermolecular potentials, that is,which have attractive interactions of variable range. They ex-amined the adequacy of the monomer contribution to theHelmholtz function by comparing with computer simulationdata. The results showed that the VR-SAFT equation of staterepresented well the vapor-liquid and liquid-liquid phaseequilibria of mixtures containing square-well molecules.

Ž .Tavares et al. 1997 reported a completely analytical equa-tion of state for square-well chains. Their equation is valid

Ž .for a range of well widths 1F lF2 , and it leads to goodpredictions of the compressibility factor of 4-mer, 8-mer, and16-mer square-well chains. A completely analytical equationis desirable for phase equilibria calculations, but it comes atthe cost of a considerable increase in mathematical complex-ity.

Cubic plus association equation of stateŽ .Kontogeorgis et al. 1996 presented an equation of state

suitable for describing associating fluids. The equation com-Žbines the simplicity of a cubic equation of state the Soave-

.Redlich-Kwong and the theoretical background of theperturbation theory employed for the association part. The

Ž .resulting equation, called cubic plus association CPA equa-tion of state, was given by

V a 1 1 XaZs y q r y 80Ž .Ý ž /V y b RT V y b X 2 rŽ . aa

where the physical term is that of the Soave-Redlich-Kwongequation of state and the associating term is taken from SAFT

Ž .equation Huang and Radosz, 1990 . Kontogeorgis et al.Ž .1996 applied this new equation of state to pure componentsand obtained good correlations of both vapor pressures andsaturated liquid volumes for primary-alcohols, phenol, tert-butyl alcohol, triethylene glycol, and water.

Ž .Voutsas et al. 1997 applied the CPA equation of state toliquid-liquid equilibrium calculations in alcoholqhydro-carbon mixtures. They used the conventional van der Waalsone-fluid mixing rules for the attractive parameter a and theco-volume parameter b. Satisfactory results were obtained inall cases using only a single temperature-independent binaryinteraction parameter. They also compared the performanceof CPA equation of state with that of the SRK and SAFTequations of state and concluded that the CPA equation pro-vided an improvement over the SRK equation and performedsimilar to the SAFT equation of state.

Heteronuclear chainsThe preceeding equations of state can only be applied to

homogeneous chains, that is, chains composed of identicalsegments. Instead, many real chain-like fluids are heteroge-neous being composed of different alternating segments.Furthermore, we are often interested in studying mixtures ofdifferent types of chains. Several equations of state have beenproposed relatively recently that tackle the problem of het-eronuclear chains.

Ž .Amos and Jackson 1992 used a bonded hard-sphere ap-proach to devise an equation of state for the compressibilityfactor of hard spheres of different size. The compressibilityfactor for a fluid mixture of heteronuclear hard chainmolecules is

rhsZs Z y1 x m q1Ž . Ý i i

is1

m y1 hsr i ln g s j, jq1Ž .j, jq1y x h 81Ž .Ý Ýi ž /his1 js1


where x is the mole fraction of chains of component i, m isi ithe number of segments in a chain of component i, s is thejdiameter of segment j on a chain of component i, and sj, jq1

Ž .s s qs r2 is the bond length between adjacent seg-j jq1Ž .ments. Amos and Jackson 1992 reported good agreement

between simulation data and the compressibility factor pre-dicted by Eq. 81 for mixtures containing diatomic and tri-

Ž .atomic entities. Malakhov and Brun 1992 also generalizedthermodynamic perturbation theory in a similar way to for-mulate an equation of state for heteronuclear chains.

Ž .Song et al. 1994a developed a perturbed hard-sphereŽ .chain PHSC equation of state that can be applied to het-

erogeneous mixtures. In general terms, the PHSC equationof state for m-component mixtures containing r segments can

Ž .be represented as Song et al., 1994b

m2prZs1q x x r r s g sŽ .Ý i j i j i j i j i j3 ij

m mry x r y1 g s y1 y x x r r a 82Ž . Ž .Ž .Ý Ýi i i j i j i j i j i jkTi ij

This equation has been used successfully to predict the liq-Žuid-liquid equilibria for binary polymer solutions Song et al.,

. Ž .1994b . Comparison Sadus, 1995 of the hard-sphere contri-butions of Eq. 82 with molecular simulation data indicatesthat this part of the equation is less accurate than otherhard-sphere chain alternatives. However, an advantage of Eq.82 is that it can be applied easily to mixtures of heteroge-neous chains by simply using a different value of r for thedifferent chains. An equation for heteronuclear chains has

Ž .also been reported Hu et al., 1996 using a cavity-correlationfunction approach.

Ž .Banaszak et al. 1996 extended the SAFT equation of stateto apply to copolymers. The copolymer-SAFT equation in-cludes contributions from chain heterogeneity and mi-

Ž .crostructure. Banaszak et al. 1996 demonstrated that thecopolymer-SAFT equation of state reproduces the qualitative

Ž .cloud point behavior of propaneqpoly ethylene-co-butene .Ž .More recently, Han et al. 1998 reported that the copoly-

mer-SAFT equation of state can be used to correlate the softchain branching effect on the cloud point pressures ofcopolymers of ethylene with propylene, butene, hexene, andoctene in propane. The copolymer-SAFT equation can alsobe used to predict phase transitions in hydrocarbonqchain

Ž .solutions Pan and Radosz, 1998 and solid-liquid equilibriaŽ .Pan and Radosz, 1999 .

Ž .Shukla and Chapman 1997 extended the SAFT equationof state for fluid mixtures consisting of heteronuclear hardchain molecules, and they formulated expressions for thecompressibility factor of pure block, alternate, and randomcopolymer systems. For the relatively simple case of pure al-ternate copolymers consisting of m -mers of type a and m -a bmers of type b, the compressibility factor is

ln g hs sŽ .ab abhsZs Z y1 mq1y my1 h 83Ž . Ž . Ž .h

where ms m q m and m s m .a b a b

Ž .Recently, Blas and Vega 1998 applied their modified ver-Ž .sion of the SAFT equation of state Blas and Vega, 1997 to

predict thermodynamic properties, as well as liquid-vaporequilibria, of binary and ternary mixtures of hydrocarbons.

Ž .Adidharma and Radosz 1998 have introduced hetero-bonding into the SW-SAFT equation of state. The resultingequation can provide reasonable predictions of the phase be-havior of mixtures of large homo- and heterosegmented

Ž . Ž .molecules. Kalyuzhnyi et al. 1988 and Lin et al. 1988 havealso used the concept of heteronuclear chains to model poly-mers.

Comparing Equations of StateInterrelationships between different equations of state

It is evident from the preceding descriptions that there is asubstantial inter-relationship between various different equa-tions of state. It is very rare for an equation of state to bedeveloped entirely from scratch. Typically, new equations ofstate are proposed as modifications of existing ones, or suc-cessful components of one or more equations of state arereused to form a new equation. This component reuse iscommon to both empirical and theoretical equations of state.

Invariably, equations of state are formed by combining sep-arate contributions from repulsive and attractive interactions.If we consider the repulsion term as forming the underlyingbasis of the equation of state, the interrelationships betweenvarious equations of state can be summarized conveniently byan equation of state tree, as illustrated in Figure 2. In Figure2, the tree grows from our knowledge of intermolecular inter-actions. The main branches of the tree represent differentways of representing intermolecular repulsion. We can iden-tify branches representing the van der Waals, Carnahan-Star-ling, HCB, PHCT, and TPT terms. The addition of a differ-ent attraction term to these branches results in a differentequation of state capable of predicting phase equilibria. Fig-ure 2 illustrates the dichotomy between empirical and theo-retical equations of state. The empirical equations of statestem almost exclusively from the van der Waals repulsivebranch. In contrast, theoretical equations of state are formedfrom different branches that represent alternative ways of ac-counting for the repulsion of nonspherical bodies. These dif-ferent repulsion branches converge to a common point, whichrepresents the limiting case of hard-sphere repulsion as de-scribed by the Carnahan-Starling equation.

The tree diagram illustrates the importance of the Red-lich-Kwong equation as the precursor for the development ofempirical attraction terms. In contrast, the PHCT and SAFTequations of state are the precursors of many theoretical at-traction terms.

Comparison with experimentExperimental data provides the ultimate test of the accu-

racy of an equation of state. However, there are several fac-tors that make it difficult to make absolute quantitative judg-ments about the relative merits of competing equations ofstate from a comparison with experimental data. The distinc-tion must also be made between correlation and genuineprediction. Nevertheless, we can make some useful generalcomments about the accuracy of different categories of equa-tions of state. However, before doing so, it is instructive to


Figure 2. Equation-of-state tree showing the interrelationship between various equations of state.

identify some of the reasons why an absolute quantitativejudgment is difficult:Ž . Ž1 The very large number of equations of state Sandler,.1994 is an obvious factor that makes the assessment of dif-

ferent equations of state difficult. In this context, it should benoted that the problem is compounded by the practice ofequation of state developers testing their equation of stateagainst experimental data, but not offering an identical com-parison with other equations of state. Nonetheless, the closeinter-relationship between the different equations of state al-lows some scope for a category by category evaluation.Ž .2 The accuracy of equations of state is often dependent

on highly optimized equation of state parameters. Theseequations of state parameters are typically tuned to a particu-lar region of interest and breakdown outside this region. Forexample, an equation of state tuned for atmospheric pres-sures is unlikely to predict high-pressure phenomena with

Ž .equal accuracy Sadus, 1992a .Ž .3 Comparison of the effectiveness of the equation of state

for mixtures is hampered by the additional uncertainties in-troduced by different mixture prescriptions, combining rulesand unlike interaction parameters. These topics are dis-cussed in detail in the section discussing mixing rules.Ž .4 Users of equations of states often adopt a favorite

equation of state with which they become expert in using.This can result in considerable inertia to change that hinders

the evaluation of alternatives, particularly if the alternativesare more complicated.

Partly because of the above factors, there are relatively fewŽreports in the literature Spear et al., 1971; Soave, 1972; Car-

nahan and Starling, 1972; Beret and Prausnitz, 1975; Pengand Robinson, 1976; Abbott, 1979; Martin, 1979; Elliott andDaubert, 1985; Kim et al., 1986; Han et al., 1988; Mainwaringet al., 1988; Sadus, 1992; Plackov et al., 1995; Plohl et al.,

.1998 comparing the predictive properties of two or moreequations of state over the same range of physical conditionsand experimental data.

Equations of state are used frequently to correlate experi-mental data rather than to provide genuine predictions. It iswell known that the van der Waals equation cannot be usedto correlate accurately the vapor-liquid coexistence of purefluids. In contrast, the addition of further adjustable parame-ters and temperature dependence to the attractive term usedin the Redlich-Kwong, Soave-Redlich-Kwong and Peng-Robinson equations of state result in accurate correlationsŽ .Abbott, 1979; Han et al., 1988 of the vapor pressure. How-ever, a large improvement in the prediction of vapor pres-

Ž .sures can be obtained Plackov et al., 1995 by using eitherthe Guggenheim or Carnahan-Starling van der WaalsŽ .CSvdW equations of state. The predictions of the Guggen-heim and CSvdW equations cannot compete with the accu-racy obtained from empirical correlations with cubic equa-


tions of state. However, their improved accuracy alonedemonstrates clearly that the success of the cubic equationsof state is due largely to the ability of the empirical improve-ments to compensate for the inadequacy of the van der Waalsrepulsion term.

Theoretical equations of state can also be used to correlateŽ .experimental data. For example, van Pelt et al. 1992 corre-

lated the SPHCT equation of state with experimental datafor the vapor-liquid coexistence of polyatomic molecules andn-alkanes. The results indicate that the SPHCT provided bet-ter correlations than cubic equations of state. This is a com-mon finding for other multiparameter theoretical equationsof state. However, the benefit of using a theoretical equationfor correlation is moot because they are considerably morecomplicated than cubic equations. The true value in using atheoretical equation is their improved ability to predict phaseequilibria rather than merely correlate data.

At low pressures, either empirical or theoretical equationsof state can be used to at least qualitatively predict phaseequilibria. In this region, the highly optimized parameters ofempirical parameters generally enable empirical equations toprovide superior accuracy than otherwise can be obtainedfrom theoretical equations of state. However, empirical equa-tions will almost invariably fail to predict the high-pressure

Ž .phase behavior of multicomponent mixtures Sadus, 1992a .Ž .For example, the results obtained Sadus, 1992a, 1994 for

the high-pressure equilibria of binary mixtures predicted byeither the Redlich-Kwong and Peng-Robinson equations ofstate are not even qualitatively reliable. This failure can beattributed unequivocally to the breakdown of the van der

Ž .Waals repulsion term Figure 1 at the moderate to high den-sities encountered at high pressures. In contrast, theoreticalequations using either the Carnahan-Starling or Guggenheimmodel of repulsion can be used to obtain quantitatively accu-rate predictions at high pressures. A curious exception to thisrule is the high-pressure phase behavior of the heliumqwaterbinary mixture which can be represented accuratelyŽ .Sretenskaja et al., 1995 by the simple van der Waals equa-tion of state.

Another weakness of empirical equations of state, which isalso related to the inadequacy of the van der Waals repulsionterm, is that they cannot be used to calculate full range ofphase equilibria of mixtures. Van Konynenburg and ScottŽ .1980 classified the phase behavior of binary mixtures intofive main types based on different critical behavior. The van

Table 3. Average Absolute Deviation of the CalculatedCompressibility Factor of m-Hard-Sphere Chains

Compared with Molecular Simulation Data

Ž .AAD %U U U UU Um GF-D TPT-D1 TPT-D2 Virial-PROSA STPT-D

4 1.72 1.04 0.76 0.858 3.58 1.88 1.78 1.28

16 6.64 2.63 3.74 1.6732 10.44 4.27 5.75 1.0851 5.37 2.72 3.26 6.25 3.97

201 9.35 5.89 6.51 8.98 3.92

U Ž .From Sadus 1995 .UU Ž .From Stell et al. 1999b .

der Waals, and other empirical equations, can be used to atleast qualitatively predict these five types. However, since thework of van Konynenburg and Scott, many more phase typeshave been documented experimentally including a sixth type

Ž .of behavior Schneider, 1978 associated commonly withaqueous mixtures involving liquid-liquid immiscibility at highpressures. This so-called Type VI behavior can be predicted

Ž .by the SPHCT equation of state Van Pelt et al., 1991 . Morerecently, the existence of Type VI behavior has been pre-

Ž .dicted using the CSvdW Yelash and Kraska, 1998 andŽ .Guggenheim Wang et al., 2000 equations of state. In con-

trast, Type VI behavior cannot be calculated by using an em-pirical equation of state.

Historically, both the empirical and theoretical ‘‘hard-sphereqattractive term’’ have been applied successfully be-yond the natural range of validity of the hard-sphere concept.This success can be attributed in part to clever correlationrather than the capabilities of the equation of state. How-ever, it is evident that the quest to genuinely predict the phaseequilibria of large molecules will rely increasing on theoreti-cally-based models that account for the complexity of molec-ular interaction. Currently, either the SAFT or PHCT ap-proaches appear to be promising approaches towards this

Žgoal. Some improvements have been reported recently Chiew.et al., 1999; Kiselev and Ely, 1999; Feng and Wang, 1999 .

Comparison with molecular simulation dataŽ .Molecular simulation Sadus, 1999 is playing an increas-

ingly valuable role in validating the accuracy of the underly-ing theoretical basis of equations of state. Molecular simula-tion provides exact data to test the accuracy of theory. Forexample, an equation of state for the compressibility factor ofLennard-Jones atoms must reproduce the compressibility fac-tors for Lennard-Jones atoms obtained from molecular simu-lation. Discrepancies between theory and simulation can beattributed unambiguously to the failure of theory to repre-sent adequately the underlying model. In contrast, directcomparison of a theoretical model with experiment does notprovide useful information regarding the validity of the the-ory, because experimental data does not represent the ideal-ized behavior of the theoretical model. However, comparisonof the results of a simulation-verified model with experimentdoes indicate the strength or weakness of theory to representexperiment adequately.

Probably, the best known example of the role of molecularsimulation is the testing of hard-sphere repulsion terms

Ž .against simulation data for hard spheres Figure 1 . The re-sult of this comparison indicates that the Carnahan-Starlingand Guggenheim terms are accurate theoretical models,whereas the van der Waals term fails at moderate to highdensities.

More recently, molecular simulation data have proved use-ful in determining the accuracy of theoretical models forhard-sphere chains. A comparison with simulation data forthe compressibility factor predicted by several hard-spherechain equations of state is summarized in Table 3. Generally,the data in Table 3 indicate that the STPT-D equation isconsiderably more accurate than the GF-D, TPT-D1, TPT-D2, and PROSA equations. The comparison of theory withsimulation does not guarantee that using any of these equa-


tions will result in an accurate description of real chainmolecules. However, using a simulation-verified model doesmean that any discrepancies of theory with experiment arenot merely due to the failure of theory to represent ade-quately the underlying model. Instead, the discrepancies canbe attributed unambiguously to the limitations of theory perse to model real molecules.

Mixing RulesThe great utility of equations of state is for phase equilib-

ria calculations involving mixtures. The assumption inherentin such a calculation is that the same equation of state usedfor pure fluids can be used for mixtures if we have a satisfac-tory way to obtain the mixture parameters. This is achievedcommonly by using mixing rules and combining rules, whichrelated the properties of the pure components to that of themixture. The discussion will be limited to the extension of aand b parameters. These two parameters have a real physicalsignificance and are common to many realistic equations ofstate.

The simplest possible mixing rule is a linear average of theequation of state parameters

as x a 84Ž .Ý i ii

bs x b 85Ž .Ý i ii

Ž .Equation 85 is sometimes employed Han et al., 1988 be-cause of its simplicity, but Eq. 84 is rarely used because itdoes not account for the important role of unlike interactionin binary fluids. Consequently, employing both Eqs. 84 and85 would lead to the poor agreement of theory with experi-ment.

The ©an der Waals mixing rulesThe most widely used mixing rules are the van der Waals

one-fluid prescriptions

as x x a 86Ž .Ý Ý i j i ji j

bs x x b 87Ž .Ý Ý i j i ji j

where a and b are the constants of the equation for pureii iiŽ .component i, and cross parameters a and b i/ j arei j i j

determined by an appropriate combining rule with or withoutbinary parameters.

Equations 86 and 87 are based on the implicit assumptionthat the radial distribution function of the componentmolecules are identical, and they both explicitly contain acontribution from interactions between dissimilar molecules.

Ž .A comparison Harismiadis et al., 1991 with computer simu-lation has concluded that the van der Waals mixing rules arereliable for mixtures exhibiting up to an eight-fold differencein the size of the component molecules. The performance ofthe van der Waals mixing rules has also been tested thor-

Ž .oughly for several equations of state by Han et al. 1988 .Ž .They used the van der Waals mixing rule Eq. 86 to obtainŽ .parameter a and the linear mixing rule Eq. 85 to obtain

parameter b. Their results showed that most of equations ofstate with the van der Waals mixing rules were capable ofrepresenting vapor-liquid equilibria with only one binary ad-justable parameter for obtaining a .i j

Equations 86 and 87 are also adequate for calculating thephase behavior of mixtures of nonpolar and slightly polar

Ž .compounds Peng and Robinson, 1976; Han et al., 1988 .Ž . ŽVoros and Tassios 1993 compared six mixing rules the one-

and two parameters van der Waals mixing rules; the pres-sure- and density-dependent mixing rules; two based on ex-

.cess Gibbs energy models: MHV2 and Wong-Sandler andconcluded that the van der Waals mixing rules give the bestresults for nonpolar systems. For the systems that containedstrongly polar substances such as alcohols, water and ace-tone, the van der Waals mixing rule did not yield reasonable

Ž .vapor-liquid equilibrium results. Anderko 1990 gave someexamples of the failure of the van der Waals mixing rules forstrongly nonideal mixtures.

Impro©ed ©an der Waals mixing rulesŽMany workers Adachi and Sugie, 1986; Panagiotopoulos

and Reid, 1986; Stryjec and Vera, 1986a,b; Schwartzentruber.et al., 1987; Sandoval et al., 1989 have proposed modifica-

tions for the van der Waals prescriptions. A common ap-proach is to include composition-dependent binary interac-tion parameters to the a parameter in the van der Waalsmixing rule and leave the b parameter rule unchanged. Someof examples are summarized in Table 4.

Table 4. Composition-Dependent Mixing Rules

Reference a Term in Eq. 86i j1r2Ž . Ž . w Ž .xAdachi and Sugie 1986 a a 1y l q m x y xii j j i j i j i j1r2Ž . Ž . w Ž . xPanagiotopoulos and Reid 1986 a a 1y k q k y k xii j j i j i j ji i

1r2Ž . Ž . Ž .Stryjek and Vera 1986b a a 1y x k y x kii j j i i j j jiŽ .Margules-type

k ki j ji1r2Ž . Ž .Stryjek and Vera 1986b a a 1yi i j j x k q x ki i j j jiŽ .Van Laar-typem x y m xi j i ji j1r2Ž . Ž . Ž .Schwartzentruber et al. 1987 a a 1y k y l x q xii j j i j i j i jm x q m xi j i ji j

k s k ; l sy l ; m s1y m ; k s l s0ji i j ji i j ji i j 11 11

1r2Ž . Ž . w Ž . Ž .Ž .xSandoval et al. 1989 a a 1y k x q k x y0.5 k q k 1y x y xii j j i j i ji j i j ji i j


Ž .Adachi and Sugie 1986 kept the functional form of thevan der Waals mixing rule, left the b parameter unchanged,and added an additional composition dependence and pa-rameters to the a parameter in the van der Waals one-fluidmixing rules

as x x a 88Ž .Ý Ý i j i j

1r2a s a a 1y l y m x y x 89Ž . Ž . Ž .i j ii j j i j i j i j

Ž .Adachi and Sugie 1986 showed that their mixing rule can beapplied to the binary and ternary systems containing stronglypolar substances.

Ž . ŽSadus 1989 used conformal solution theory Sadus, 1992a,.1994 to derive an alternative to the conventional procedure

for obtaining parameter a of equation of state. Instead ofproposing an average of the pure component parameter data,the a parameter for the mixture is calculated directly. Conse-quently, a is a function of composition only via the conformal

Ž .parameters f , h and the contribution from the combinato-rial entropy of mixing. The a parameter is obtained by takingthe positive root of the following quadratic equation

2 2Y X Y X X X2 6a u y2 f rf q f rf q2h rhy2 f hrfhq hrhŽ . Ž .Y Y2 � 4q aRTV f u y h rhy f rfB

2Y X X X3q2f u h rhq f hrfhy hrhŽ .� 4A

2Y X6q2u y h rhq hrh q1rx 1y xŽ . Ž .� 42 2 2X X2y RTV f f rf y hrhŽ . Ž . Ž .� 4A

2Y X Y2qf u h rhy hrh y1rx 1y x yf f h rhu s0Ž . Ž .� 4B A B

90Ž .

where superscripts X and Y denote successive differentiation ofthe conformal parameters, and u and f are characteristic ofthe equation of state. The main advantage of Eq. 90 is thatthe a parameter can be calculated directly from the criticalproperties of pure components without using combining rules

Ž .for the contribution of unlike interactions. Sadus 1992a,bhas applied the above equation to the calculation of the va-por-liquid critical properties of a wide range of binary mix-tures. The agreement was generally very good in view of thefact that no adjustable parameters were used to arbitrarilyoptimize the agreement between theory and experiment.

Mixing rules from excess Gibbs energy modelsŽ .Huron and Vidal 1979 suggested a method for deriving

mixing rules for equations of state from excess Gibbs energymodels. Their method relies on three assumptions. First, theexcess Gibbs energy calculated from an equation of state atinfinite pressure equals an excess Gibbs energy calculatedfrom a liquid-phase activity coefficient model. Secondly, thecovolume parameter b equals the volume V at infinite pres-sure. Third, the excess volume is zero. By using the Soave-

Ž .Redlich-Kwong equation Eq. 5 and applying the common

Ž .linear mixing rule Eq. 85 for the volume parameter b, theresulting expression for parameter a is

En a gii às b x y 91Ž .Ý i b ln 2iiis1

where g E is the value of the excess Gibbs energy at infinite`

Žpressure and can be calculated from Renon and Prausnitz,.1968

n

x G CÝ j ji jinjs1Eg s x 92Ž .Ý n` i

is1 x GÝ� 0k kik s1

with

C s g y g ¶ji ji ii

•C 93Ž .jiG s b exp y a ßji j již /RT

where g and g are the interaction energies between unlikeji iiŽ . Ž .g and like g molecules; a is a nonrandomness param-ji ii jieter. The Huron-Vidal mixing rule for a is deduced by apply-ing Eq. 91

n

x G CÝ j ji jin a 1 js1iias b x y 94Ž .Ý ni b ln 2iiis1 x GÝ k ki

k s1

with a , C and C as the three adjustable parameters. Whenji i j jia s0, the Huron-Vidal mixing rule reduces to the van derji

Ž .Waals mixing rule. Huron and Vidal 1979 showed that theirmixing rule yields good results for nonideal mixtures. SoaveŽ .1984 found that the Huron-Vidal mixing rule representedan improvement over the classical quadratic mixing rules andmade it possible to correlate vapor-liquid equilibria for highlynonideal systems with good accuracy. The Huron-Vidal mix-ing rule has also been applied to a variety of polar and asym-

Žmetric systems Adachi and Sugie, 1985; Gupte and Daubert,.1986; Heidemann and Rizvi, 1986 .

A weakness of the Huron-Vidal mixing rule is that theequation of state excess Gibbs energy at near atmosphericpressure differs from that at infinite pressure. Therefore, theHuron-Vidal mixing rule has difficulty in dealing with low-

Žpressure data. Several proposals Lermite and Vidal, 1992;.Soave et al., 1994 have been reported to overcome this diffi-

culty.Ž .Mollerup 1986 modified Eq. 94 by retaining that the ex-

cess volume is zero but evaluating the mixture parameter adirectly from the zero pressure excess free energy expression.The modified mixing rule has the form

Ea a f G RT bi i is x y q x ln f 95Ž .Ý Ýi i cž / ž / ž / ž /b b f f f bii i


where

b ¶if si ®i

b •f s 96Ž .®

® ®if s y1 y1c ž /ž / ßb bi

Ž .The mixing rule Eq. 95 depends on the liquid-phase volumeof the mixture and individual components, and is a less re-strictive assumption than the Huran-Vidal mixing rule.

Ž .This basic concept Mollerup, 1986 was implemented byŽ .Michelsen 1990 . Using a reference pressure of zero and the

Ž .Soave-Redlich-Kwong equation of state Eq. 5 , MichelsenŽ .Michelsen, 1990; Dahl and Michelsen, 1990 repeated thematching procedure of Huron and Vidal resulting in the fol-lowing mixing rule called the modified Huron-Vidal first or-

Ž .der MHV1

En n1 G ba s x a q q x ln 97Ž .Ý Ýi ii i ž /q RT b1 i iis1 is1

where

a s arbRT ¶n •bs x bÝ 98Ž .i ii

is1 ßa s a rb RTii ii ii

with the recommended value of q sy0.593. In addition,1Ž .Dahl and Michelsen 1990 derived an alternative mixing rule

referred to as the modified Huron-Vidal second-orderŽ .MHV2

n n E nG b2 2q a y x a q q a y x a s q x lnÝ Ý Ý1 i i i 2 i i i iž / ž / ž /RT biiis1 is1 is1

99Ž .

with suggested values of q sy0.478 and q sy0.0047.1 2Ž .Dahl and Michelsen 1990 investigated the ability of

MHV2 to predict high-pressure vapor-liquid equilibriumwhen used in combination with the parameter table of modi-

Ž .fied UNIFAC Larsen et al., 1987 . They concluded that sat-isfactory results were obtained for the mixtures investigated.

Ž .Dahl et al. 1991 demonstrated that MHV2 was also able tocorrelate and predict vapor-liquid equilibria of gas-solvent bi-nary systems and to predict vapor-liquid equilibria for multi-component mixtures using the new parameters for gas-solventinteractions together with the modified UNIFAC parameter

Ž .table of Larsen et al. 1987 .Generally, the use of the infinite pressure or zero pressure

standard states for mixing in the equation of state will lead toinconsistencies with the statistical mechanical result that thesecond virial coefficient must be a quadratic function of com-

Ž .position. Wong and Sandler 1992 used the Helmholtz func-

tion to develop mixing rules to satisfy the second virial condi-tion. For the mixture parameters of an equation of state, aand b are

Ea Ai às b x q 100Ž .Ý i b Ci

ax x byÝÝ i j ž /RT i j

bs 101Ž .EA a` i1q y xÝ i ž /RT b RTi

where C is a constant dependent on the equation of state' 'Ž Ž .selected for example, C is equal to 1r 2 ln 2 y1 for the

. EPeng-Robinson equation of state and A is the excess`

Helmholtz function at infinite pressure, and

1y k aa aŽ .i j jiby s b y q b y 102Ž .i jž / ž / ž /RT 2 RT RTi j

where k is a binary interaction parameter.i jŽ . ŽWong and Sandler 1992 tested the mixing rules Eq. 100

.and Eq. 101 , and concluded that they were reasonably accu-rate in describing both simple and complex phase behavior ofbinary and ternary systems for the diverse systems they con-

Ž .sidered. Wong et al. 1992 demonstrated that the Wong-San-dler mixing rules can be used for highly nonideal mixtures.The mixing rules can be applied at temperatures and pres-sures that greatly exceed the experimental data used to ob-

Ž .tain the parameters. Huang and Sandler 1993 compared theWong-Sandler and MHV2 mixing rules for nine binary andtwo ternary systems. They showed that either the MHV2 orWong-Sandler mixing rules can be used to make reasonablehigh-pressure vapor-liquid equilibrium predictions from low-pressure data. They used the Peng-Robinson and Soave-Re-dlich-Kwong equations of state and found that the errors inthe predicted pressure with the Wong-Sandler mixing rulewere, on the average, about half or less of those obtained

Ž .when using the MHV2 mixing rule. Orbey and Sandler 1994used the Wong-Sandler mixing rule to correlate the vapor-liquid equilibria of various polymerqsolvent and solventqlong chain hydrocarbon mixtures. They concluded that theWong-Sandler mixing rule can correlate the solvent partialpressure in concentrated polymer solutions with high accu-racy over a range of temperatures and pressures with temper-ature-independent parameters.

To go smoothly from activity coefficient-like behavior tothe classical van der Waals one fluid mixing rule, Orbey and

Ž .Sandler 1995 slightly reformulated the Wong-Sandler mix-ing rules by rewriting the cross second virial term given inEq. 102 as

a a 1y kŽ .'b q ba i j i jŽ .i jby s y 103Ž .ž /RT 2 RTi j

while retaining the basic equations, Eq. 100 and Eq. 101. Or-Ž .bey and Sandler 1995 tested five binary systems and one

ternary mixture and showed that this new mixing rule wascapable of both correlating and predicting the vapor-liquid


equilibrium of various complex binary mixtures accuratelyover wide ranges of temperature and pressure and that it canbe useful for accurate predictions of multicomponent vapor-liquid equilibria.

Ž .Castier and Sandler 1997a,b performed critical point cal-culations in binary systems utilizing cubic equations of statecombined with the Wong-Sandler mixing rules. To investigatethe influence of the mixing rules on the shape of the calcu-lated critical phase diagrams, the van der Waals equation ofstate was combined with the Wong-Sandler mixing rulesŽ .Castier and Sandler, 1997a . The results showed that manydifferent types of critical phase diagrams can be obtainedfrom this combination. When the Wong-Sandler mixing rules

Ž .are combined with the Stryjek and Vera 1986a version ofŽ . Žthe Peng-Robinson 1976 equation of state Castier and San-

.dler, 1997b , it was able to predict quantitatively the criticalbehavior of some highly nonideal systems involving com-pounds such as water, acetone, and alkanols. For some highlyasymmetric and nonideal mixtures, such as waterq n-dodecane, only qualitatively correct critical behavior could bepredicted.

ŽSeveral other mixing rules have been proposed Heide-mann and Kokal, 1990; Soave, 1992; Holderbaum andGmehling, 1991; Boukouvalas et al., 1994; Tochigi, 1995;

.Novenario et al., 1996; Twu and Coon, 1996; Twu et al., 1998based on excess free energy expressions. Comparison andevaluation for various mixing rules can be found in the works

Ž . Ž .of Knudsen et al. 1996 , Voros and Tassios 1993 , MichelsenŽ . Ž .and Heidemann 1996 , Wang et al. 1996 , Abdel-Ghani and

Ž . Ž .Heidemann 1996 , Orbey and Sandler 1996 , HeidemannŽ . Ž .1996 , and Twu et al. 1998 .

Combining rulesAs noted above, any mixing rule will invariably contain a

contribution from interactions between unlike molecules. InŽ .other words, the cross terms a and b i/ j must be evalu-i j i j

ated. They can be determined by an appropriate combiningrule. The contribution from unlike interaction to the inter-

Ž .molecular parameters representing energy e and hard-Ž .sphere diameter s can be obtained from

¶e sj e e'i j i j ii j j • 104Ž .s qsŽ .ii j js sz ßi j i j 2

Ž .In Eq. 104, the j also commonly defined as 1y k andi j i jŽ .z also commonly defined as 1y l terms are adjustablei j i j

parameters which are used to optimize agreement betweentheory and experiment. The z term does not significantlyi jimprove the analysis of high-pressure equilibria, and it can be

Ž .usually omitted z s1 . The j term is required, because iti j i jcan be interpreted as reflecting the strength of unlike inter-action except the simple mixtures of molecules of similar size.This interpretation is supported by the fact that values of j i jobtained from the analysis of the critical properties of manybinary mixtures consistently decline with increasing size dif-ference between the component molecules as detailed else-

Ž .where Sadus, 1992a, 1994 .

In terms of the equation of state parameters, the equiva-lent combining rules to Eq. 104 are

a a ¶ii j ja sj bi j i j i j( b bii j j • 105Ž .

31r3 1r3b q bŽ .ii j jb sz ßi j i j 8

Žwhere the rule for b is referred to as the Lorentz rule Hicksi j.and Young, 1975; Sadus, 1992a . More commonly, the equa-

tion of state parameters are obtained from

¶a sj a a'i j i j ii j j

• 106Ž .b q bŽ .ii j jb sz ßi j i j 2

where the combining rule for a is referred to as the van deri jWaals combining rule. At this point, it should be noted thatthere is a common misconception in the literature that Eq.106 and not Eq. 105 is the equivalent of Eq. 104. This error isunderstandable in view of the functional similarity of Eqs.106 and 104. However, it should also be observed that the aand b parameters have dimensions of energy=volume andvolume, respectively, compared with a dimension of energyfor e and a dimension of distance for s . Another combiningrule for b is the geometric mean rule proposed by Goodi j

Ž .and Hope 1970

b sz b b 107Ž .'i j i j ii j j

Ž . ŽSadus 1993 compared the accuracy of the Lorentz Eq.. Ž . Ž .105 , arithmetic Eq. 106 , and geometric Eq. 107 rules for

b when used in the prediction of Type III phenomena. Fori jmolecules of similar size, all three combining rules give al-most identical results, but the discrepancy increases substan-tially for mixtures of molecules of very dissimilar size. SadusŽ .1993 proposed an alternative combining rule by taking a 2:1geometric average of the Lorentz and arithmetic rules with-out the z parameter, that is,i j

2 1r31r3 1r3 1r3b s 1r4 2 b q b b q b 108� 4Ž . Ž .Ž .Ž .i j ii j j ii j j

Ž . Ž .Sadus 1993 reported that the new combining rule Eq. 108is generally more accurate that either the Lorentz, arith-metic, or geometric combining rules.

ConclusionsConsiderable progress has been achieved in the develop-

ment of equations of state. Many highly successful empiricalequations of state have been proposed that can be used tocalculate the phase behavior of simple fluids. However, amore sophisticated approach is required for complicatedmolecules. To meet the challenge posed by large and compli-cated molecules, equations of state are being developed in-creasingly with an improved theoretical basis. These new


equations are playing an expanding role in the accurate cal-culation of fluid-phase equilibria. Equation of state develop-ment has been aided greatly by new insights into the natureof intermolecular interaction and molecular simulation data.In particular, molecular simulation is likely to have an ongo-ing and crucial role in the improvement of the accuracy ofequations of state. A continuing challenge is to improve theprediction of the phase behavior of mixtures. The main im-pediment to the prediction of mixture phenomena is our un-derstanding of interactions between dissimilar molecules. Thisis also an area that is likely to benefit from the input ofmolecular simulation data.

AcknowledgmentsY.S.W. thanks the Australian government for an Australian Post-

graduate Award.

NotationBWRsBenedict-Webb-RubinCPAscubic plus association

CFsChristoforakos-FranckGF-Dsgeneralized Flory-dimerHCBshard convex body

HCBvdWshard convex body van der WaalsHFsHeilig-Franck

HS-SAFTshard sphere statistical associating fluid theoryLJ-SAFTsLennard-Jones statistical associating fluid theory

MHV1smodified Huron-Vidal first orderMHV2smodified Huron-Vidal second order

PROSAsproduct-reactant Ornstein-Zernike approachRKsRedlich-Kwong

SRKsSoave-Redlich-KwongSSAFTssimplified statistical Associating fluid theory

SW-TPT-Ds square-well thermodynamic perturbation theory-di-mer

TBsTrebble and BishnoiTPT-D1s thermodynamic perturbation theory-dimer 1TPT-D2s thermodynamic perturbation theory-dimer 2

TPT1s first-order thermodynamic perturbation theoryTPT2ssecond-order thermodynamic perturbation theory

VR-SAFTs variable range statistical associating fluid theory

Bssecond virial coefficientcsequation of state parameter

Cs third virial coefficientD suniversal constants in BACK equationi j

esequation of state constantfsconformal parameter, free energygsconformal parameter; interaction energy between

moleculesŽ .g s ssite-site correlation function at contact

GsGibbs functionhsconformal parameterksequation of state constant

msnumber of monomers; equation of state parameterpsreduced pressure˜qsnumber of external segments per molecule; equation

of state parameterTUs characteristic temperature in the SPHCT equation of

stateT̃sreduced temperatureus intermolecular potential termYsparameter of SPHCT equation of statezstemperature-dependence constantasnonsphericity parameterbsequation of state parameter, 1rkTesenergy of interaction; attractive depth of square-wellzs interaction parameter; reduced densitylsequation of state parameter, width of square-wellmschemical potential

jsunlike interaction parameterps3.14159tsnumerical constantvsacentric factor; orientation of moleculeSssummation

Subscripts and superscripts0sdenotes component; reference system1sdenotes component; first-order term of perturbation

theory2sdenotes component; second-order term of perturba-

tion theoryUs configurational property; perfect gas contribution

assocsassociationattsattractive

BHsBarker-Hendersoncscritical property

chainschain termdipolesdipole-dipole term

dispsdispersionD suniversal constantsi jhcshard chain

hcbshard convex bodyhBHshybrid Barker-Henderson

hdshard-dimeris ith componentjs jth component

LJsLennard-Jonesmsmixture

mfsmean fieldmonosmonomer-monomer term

psperturbationrsrotational motion of a molecule; number of segment

per moleculereps repulsiveressresidualswssquare well

®svibrational motion of a molecule

Literature CitedAbdel-Ghani, R. M., and R. A. Heidemann, ‘‘Comparison of DG

Excess Mixing Rules for Multi-Phase Equilibria in Some TernaryŽ .Systems,’’ Fluid Phase Equilib., 116, 495 1996 .

Abbott, M. M., ‘‘Cubic Equation of State: An Interpretive Review,’’Equations of State in Engineering and Research, Adv. in ChemistrySer., 182, K. C. Chao and R. L. Robinson eds., American Chemical

Ž .Society, Washington, DC, p. 47 1979 .Adachi, Y., B. C. Lu, and H. Sugie, ‘‘Three-Parameter Equations of

Ž .State,’’ Fluid Phase Equilib., 13, 133 1983 .Adachi, Y., and H. Sugie, ‘‘Effects of Mixing Rules on Phase Equi-

Ž .librium Calculations,’’ Fluid Phase Equilib., 24, 353 1985 .Adachi, Y., and H. Sugie, ‘‘A New Mixing Rule-Modified Conven-

Ž .tional Mixing Rule,’’ Fluid Phase Equilib., 28, 103 1986 .Adidharma, H., and M. Radosz, ‘‘A Prototype of an Engineering

Equation of State for Hetero-Segmented Polymers,’’ Ind. Eng.Ž .Chem. Res., 37, 4453 1998 .

Adidharma, H., and M. Radosz, ‘‘A Study of Square-Well SAFT Ap-Ž .proximations,’’ Fluid Phase Equilib., 161, 1 1999 .

Alder, B. J., and T. E. Wainwright, ‘‘Molecular Dynamics: II. Be-haviour of a Small Number of Elastic Spheres,’’ J. Chem. Phys., 33,

Ž .1439 1960 .Alder, B. J., D. A. Young, and M. A. Mark, ‘‘Studies in Molecular

Dynamics: X. Corrections to the Augmented van der Waals The-Ž .ory for Square-Well Fluid,’’ J. Chem. Phys., 56, 3013 1972 .Ž .Amos, M. D., and G. Jackson, ‘‘Bonded Hard-Sphere BHS Theory

for the Equation of State of Fused Hard-Sphere PolyatomicŽ .Molecules and Their Mixtures,’’ J. Chem. Phys., 96, 4604 1992 .

Anderko, A., ‘‘Equation-of-State Methods for the Modelling of PhaseŽ .Equilibria,’’ Fluid Phase Equilib., 61, 145 1990 .

Asselineau, L., G. Bogdanic, and J. Vidal, ‘‘Calculation of Thermo-dynamic Properties and Vapour-Liquid Equilibria of Refrigerants,’’

Ž .Chem. Eng. Sci., 33, 1269 1978 .


Baker, L. E., and K. D. Luks, ‘‘Critical Point and Saturation Pres-sure Calculations for Multipoint Systems,’’ Soc. Pet. Eng. J., 20, 15Ž .1980 .

Barker, J. A., and D. Henderson, ‘‘Perturbation Theory and Equa-tion of State for Fluids. II: A Successful Theory of Liquids,’’ J.

Ž .Chem. Phys., 47, 4714 1967 .Barker, J. A., and D. Henderson, ‘‘Monte Carlo Values for the Ra-

dial Distribution Function of a System of Fluid Hard Spheres,’’Ž .Mol. Phys., 21, 187 1971 .

Barker, J. A., and D. Henderson, ‘‘Theories of Liquids,’’ Ann. Re®.Ž .Phys. Chem., 23, 439 1972 .

Banaszak, M., Y. C. Chiew, and M. Radosz, ‘‘Thermodynamic Per-turbation Theory of Polymerization: Sticky Chains and Square-Well

Ž .Chains,’’ Phys. Re®. E., 48, 3760 1993 .Banaszak, M., Y. C. Chiew, R. O’Lenick, and M. Radosz, ‘‘Thermo-

dynamic Perturbation Theory: Lennard-Jones Chains,’’ J. Chem.Ž .Phys., 100, 3803 1994 .

Banaszak, M., C. K. Chen, and M. Radosz, ‘‘Copolymer SAFT Equa-tion of State. Thermodynamic Perturbation Theory Extended to

Ž .Heterobonded Chains,’’ Macromol., 29, 6481 1996 .Benedict, M., G. R. Webb, and L. C. Rubin, ‘‘An Empirical Equa-

tion for Thermodynamic Properties of Light Hydrocarbons andTheir Mixtures. I. Methane, Ethane, Propane and Butane,’’ J.

Ž .Chem. Phys., 8, 334 1940 .Beret, S., and J. M. Prausnitz, ‘‘Perturbed Hard-Chain Theory: An

Equation of State for Fluids Containing Small or Large Molecules,’’Ž .AIChE J., 26, 1123 1975 .

Blas, F. J., and L. F. Vega, ‘‘Thermodynamic Behaviour of Homonu-clear and Heteronuclear Lennard-Jones Chains with Association

Ž .Sites from Simulation and Theory,’’ Mol. Phys., 92, 135 1997 .Blas, F. J., and L. F. Vega, ‘‘Prediction of Binary and Ternary Dia-

Ž .grams Using the Statistical Associating Fluid Theory SAFTŽ .Equation of State,’’ Ind. Eng. Chem. Res., 37, 660 1998 .

Bondi, A., Physical Properties of Molecular Crystals, Liquids, andŽ .Glasses, Wiley, New York 1968 .

Boublik, T., ‘‘Hard-Sphere Equation of State,’’ J. Chem. Phys., 53,Ž .471 1970 .

Boublik, T., ‘‘Statistical Thermodynamics of Nonspherical MoleculeŽ .Fluids,’’ Ber. Bunsenges. Phys. Chem., 85, 1038 1981 .

Boukouvalas, C., N. Spiliotis, P. Coutsikow, and N. Tzouvaras, ‘‘Pre-diction of Vapour-Liquid Equilibrium with the LCVM Model. ALinear Combination of the Huron-Vidal and Michelsen MixingRules Coupled with the Original UNIFAC and the t-mPR Equa-

Ž .tion of State,’’ Fluid Phase Equilib., 92, 75 1994 .Carnahan, N. F., and K. E. Starling, ‘‘Equation of State for Nonat-

Ž .tracting Rigid Spheres,’’ J. Chem. Phys., 51, 635 1969 .Carnahan, N. F., and K. E. Starling, ‘‘Intermolecular Repulsions and

Ž .the Equation of State for Fluids,’’ AIChE J., 18, 1184 1972 .Castier, M., and S. I. Sandler, ‘‘Critical Points with the Wong-San-

dler Mixing Rule. I. Calculations with the van der Waals EquationŽ .of State,’’ Chem. Eng. Sci., 52, 3393 1997a .

Castier, M., and S. I. Sandler, ‘‘Critical Points with the Wong-San-dler Mixing Rule. II. Calculations with a Modified Peng-Robinson

Ž .Equation of State,’’ Chem. Eng. Sci., 52, 3579 1997b .Chang, J., and S. I. Sandler, ‘‘An Equation of State for the Hard-

Sphere Chain Fluid: Theory and Monte Carlo Simulation,’’ Chem.Ž .Eng. Sci., 49, 2777 1994 .

Chapman, W. G., G. Jackson, and K. E. Gubbins, ‘‘Phase Equilibriaof Associating Fluids: Chain Molecules with Multiple Bonding

Ž .Sites,’’ Mol. Phys., 65, 1057 1988 .Chapman, W. G., K. E. Gubbins, G. Jackson, and M. Radosz, ‘‘New

Reference Equation of State for Associating Liquids,’’ Ind. Eng.Ž .Chem. Res., 29, 1709 1990 .

Chen, C.-K., M. Banaszak, and M. Radosz, ‘‘Statistical AssociatingFluid Theory Equation of State with Lennard-Jones ReferenceApplied to Pure and Binary n-Alkane Systems,’’ J. Phys. Chem. B.,

Ž .102, 2427 1998 .Chen, S. S., and A. Kreglewski, ‘‘Applications of the Augmented van

der Waals Theory of Fluids: I. Pure Fluids,’’ Ber. Bunsen-Ges. Phys.Ž .Chem., 81, 1048 1977 .

Chien, C. H., R. A. Greenkorn, and K. C. Chao, ‘‘Chain-of-RotatorsŽ .Equation of State,’’ AIChE J., 29, 560 1983 .

Chiew, Y. C., ‘‘Percus-Yevick Integral-Equation Theory for Ather-mal Hard-Sphere Chains: I. Equations of State,’’ Mol. Phys., 70,

Ž .129 1990 .

Chiew, Y. C., ‘‘Percus-Yevick Integral Equation Theory for Ather-mal Hard-Sphere Chains: II. Average Intermolecular Correlation

Ž .Functions,’’ Mol. Phys., 73, 359 1991 .Chiew, Y. C., D. Chang, J. Lai, and G. H. Wu, ‘‘A Molecular-Based

Equation of State for Simple and Chainlike Fluids,’’ Ind. Eng.Ž .Chem. Res., 38, 4951 1999 .

Christoforakos, M., and E. U. Franck, ‘‘An Equation of State forBinary Fluid Mixtures to High Temperatures and High Pressures,’’

Ž .Ber. Bunsenges. Phys. Chem., 90, 780 1986 .Christou, G., T. Morrow, R. J. Sadus, and C. L. Young, ‘‘Phase Be-

haviour of FluorocarbonqHydrocarbon Mixtures: Interpretation ofType II and Type III Behaviour in Terms of a ‘‘Hard SphereqAttractive Term’’ Equation of State,’’ Fluid Phase Equilib., 25, 263Ž .1986 .

Christou, G., C. L. Young, and P. Svejda, ‘‘Gas-Liquid Critical Tem-peratures of Binary Mixtures of Polar CompoundsqHydrocarbonsor q Other Polar Compounds,’’ Ber. Bunsenges. Phys. Chem., 95,

Ž .510 1991 .Chueh, P. L., and J. M. Prausnitz, ‘‘Vapor-Liquid Equilibria at High

Pressures. Vapour-Phase Fugacity Coefficients in Nonpolar andŽ .Quantum-Gas Mixtures,’’ Ind. Eng. Chem. Fundam., 6, 492 1967a .

Chueh, P. L., and J. M. Prausnitz, ‘‘Vapour-Liquid Equilibria at HighPressures. Calculation of Partial Molar Volumes in Nonpolar Liq-

Ž .uid Mixtures,’’ AIChE J., 13, 1099 1967b .Dahl, S., and M. L. Michelsen, ‘‘High-Pressure Vapor-Liquid Equi-

librium with a UNIFAC-Based Equation of State,’’ AIChE J., 36,Ž .1829 1990 .

Dahl, S., A. Fredenslund, and P. Rasmussen, ‘‘The MHV2 Model: AUNIFAC-Based Equation of State Model for Prediction of GasSolubility and Vapour-Liquid Equilibria at Low and High Pres-

Ž .sures,’’ Ind. Eng. Chem. Res., 30, 1936 1991 .Davies, L. A., A. Gil-Villegas, and G. Jackson, ‘‘Describing the Prop-

erties of Chains of Segments Interacting via Soft-Core Potentialsof Variable Range with the SAFT-VR Approach,’’ Int. J. Thermo-

Ž .phys., 19, 675 1998 .Deiters, U., and G. M. Schneider, ‘‘Fluid Mixtures at High Pres-

sures. Computer Calculations of the Phase Equilibria and the Crit-ical Phenomena in Fluid Binary Mixtures from the Redlich-Kwong

Ž .Equation of State,’’ Ber. Bunsenges. Phys. Chem., 80, 1316 1976 .Deiters, U., ‘‘A New Semiempirical Equation of State for Fluids: I.

Ž .Derivation,’’ Chem. Eng. Sci., 36, 1147 1981 .De Santis, R., F. Gironi, and L. Marrelli, ‘‘Vapour-Liquid Equilib-

rium from a Hard-Sphere Equation of State,’’ Ind. Eng. Chem.Ž .Fundam., 15, 183 1976 .

Dohrn, R., Berechnung ®on Phasengleichgewichten, Vieweg, Braun-Ž .schweig 1994 .

Donohue, M. D., and J. M. Prausnitz, ‘‘Perturbed Hard Chain The-ory for Fluid Mixtures: Thermodynamic Properties for Mixtures in

Ž .Natural Gas and Petroleum Technology,’’ AIChE J., 24, 849 1978 .Economou, I. G., and M. D. Donohue, ‘‘Chemical, Quasi-Chemical

and Perturbation Theories for Associating Fluid,’’ AIChE J., 37,Ž .1875 1991 .

Economou, I. G., and M. D. Donohue, ‘‘Equation of State with Mul-tiple Associating Sites for Water and Water-Hydrocarbon Mix-

Ž .tures,’’ Ind. Eng. Chem. Res., 31, 2388 1992 .Economou, I. G., and M. D. Donohue, ‘‘Equations of State for Hy-

Ž .drogen Bonding Systems,’’ Fluid Phase Equilib., 116, 518 1996 .Economou, I. G., and C. J. Peters, ‘‘Phase Equilibria Prediction of

Hydrogen Fluoride Systems from an Associating Model,’’ Ind. Eng.Ž .Chem. Res., 34, 1868 1995 .

Economou, I. G., C. J. Peters, and J. de Swaan Arons, ‘‘Water-SaltPhase Equilibria at Elevated Temperatures and Pressures: ModelDevelopment and Mixture Predictions,’’ J. Phys. Chem., 99, 6182Ž .1995 .

Economou, I. G., and C. Tsonopoulos, ‘‘Associating Models andMixing Rules in Equation of State for WaterrHydrocarbon Mix-

Ž .tures,’’ Chem. Eng. Sci., 52, 511 1997 .Elliott, J. R., and T. E. Daubert, ‘‘Revised Procedures for Phase

Equilibrium Calculations with the Soave Equation of State,’’ Ind.Ž .Eng. Chem. Process Des. De®., 24, 743 1985 .

Elliott, J. R., and T. E. Daubert, ‘‘Evaluation of an Equation of StateMethod for Calculating the Critical Properties of Mixtures,’’ Ind.

Ž .Eng. Chem. Res., 26, 1686 1987 .Feng, W., and W. Wang, ‘‘A Perturbed Hard-Sphere-Chain Equa-

tion of State for Polymer Solutions and Blends Based on the


Square-Well Coordination Number Model,’’ Ind. Eng. Chem. Res.,Ž .38, 4966 1999 .

Flory, P. J., ‘‘Statistical Thermodynamics of Liquid Mixtures,’’ J.Ž .Amer. Chem. Soc., 87, 1833 1965 .

Fu, Y. H., and S. I. Sandler, ‘‘A Simplified SAFT Equation of Statefor Associating Compounds and Mixtures,’’ Ind. Eng. Chem. Res.,

Ž .34, 1897 1995 .Fuller, G. G., ‘‘A Modified Redlich-Kwong-Soave Equation of State

Capable of Representing the Liquid State,’’ Ind. Eng. Chem. Fun-Ž .dam., 15, 254 1976 .

Galindo, A., P. J. Whitehead, and G. Jackson, ‘‘Predicting the High-Pressure Phase Equilibria of Waterq n-Alkanes Using a Simpli-fied SAFT Theory with Transferable Intermolecular Interaction

Ž .Parameters,’’ J. Phys. Chem., 100, 6781 1996 .Galindo, A., P. J. Whitehead, G. Jackson, and A. B. Burgess, ‘‘Pre-

dicting the Phase Equilibria of Mixtures of Hydrogen Fluoride withŽ .Water, Difluoromethane HFC-32 , and 1, 1, 1, 2-Tetrafluoro-

Ž .ethane HFC-134a Using a Simplified SAFT Approach,’’ J. Phys.Ž .Chem., 101, 2082 1997 .

Galindo, A., L. A. Davies, A. Gil-Villegas, and G. Jackson, ‘‘TheThermodynamics of Mixtures and the Corresponding Mixing Rulesin the SAFT-VR Approach for Potentials of Variable Range,’’ Mol.

Ž .Phys., 93, 241 1998 .Garcia-Lisbona, M. N., A. Galindo, and G. Jackson, ‘‘Predicting the

High-Pressure Phase Equilibria of Binary Aqueous Solution of 1-Butanol, n-Butoxyethanol and n-Decylpentaoxyethylene EtherŽ . Ž .C E Using the SAFT-HS Approach,’’ Mol. Phys., 93, 57 1998 .10 5

Ghonasgi, D., and W. G. Chapman, ‘‘A New Equation of State forŽ .Hard Chain Molecules,’’ J. Chem. Phys., 100, 6633 1994 .

Gil-Villegas, A., A. Galindo, P. J. Whitehead, S. J. Mills, G. Jackson,and A. N. Burgess, ‘‘Statistical Associating Fluid Theory for ChainMolecules with Attractive Potentials of Variable Range,’’ J. Chem.

Ž .Phys., 106, 4168 1997 .Good, R. J., and C. J. Hope, ‘‘New Combining Rule for Intermolecu-

lar Distances in Intermolecular Potential Functions,’’ J. Chem.Ž .Phys., 53, 540 1970 .

Graboski, M. S., and T. E. Daubert, ‘‘A Modified Soave Equation ofState for Phase Equilibrium Calculations,’’ Ind. Eng. Chem. Pro-

Ž .cess. Des. De®., 17, 443 1978 .Gubbins, K. E., ‘‘Equations of State-New Theories,’’ Fluid Phase

Ž .Equilib., 13, 35 1983 .Gubbins, K. E., and C. H. Twu, ‘‘Thermodynamics of Polyatomic

Ž .Fluid Mixtures: I. Theory,’’ Chem. Eng. Sci., 33, 863 1978 .Guggenheim, E. A., ‘‘Variations on van der Waals’ Equation of State

Ž .for High Densities,’’ Mol. Phys., 9, 199 1965 .Gulati, H. S., and C. K. Hall, ‘‘Generalized Flory Equations of State

for Copolymers Modeled as Square-Well Chains,’’ J. Chem. Phys.,Ž .108, 7478 1998 .

Gupte, P. A., and T. E. Daubert, ‘‘Extension of UNIFAC to HighPressure VLE Using Vidal Mixing Rules,’’ Fluid Phase Equilib., 28,

Ž .155 1986 .Han, S. J., H. M. Lin, and K. C. Chao, ‘‘Vapour-Liquid Equilibrium

of Molecular Fluid Mixtures by Equation of State,’’ Chem. Eng.Ž .Sci., 43, 2327 1988 .

Han, S. J., D. J. Lohse, M. Radosz, and L. H. Sperling, ‘‘Short ChainBranching Effect on the Cloud-Point Pressures of EthyleneCopolymers in Subcritical and Supercritical Propane,’’ Macromol.,

Ž .31, 2533 1998 .Harismiadis, V. I., N. K. Koutras, D. P. Tassios, and A. Z. Pana-

giotopoulos, ‘‘Gibbs Ensemble Simulations of Binary Lennard-Jones Mixtures. How Good is Conformal Solutions Theory for

Ž .Phase Equilibrium Predictions,’’ Fluid Phase Equilib., 65, 1 1991 .Harmens, A., and H. Knapp, ‘‘Three Parameter Cubic Equation of

State for Normal Substances,’’ Ind. Eng. Chem. Fundam., 19, 291Ž .1980 .

Heidemann, R. A., ‘‘Excess Free Energy Mixing Rules for CubicŽ .Equations of State,’’ Fluid Phase Equilib., 116, 454 1996 .

Heidemann, R. A., and S. S. H. Rizvi, ‘‘Correlation of Ammonia-Water Equilibrium Data with Various Peng-Robinson Equation of

Ž .State,’’ Fluid Phase Equilib., 29, 439 1986 .Heidemann, R. A., and S. L. Kokal, ‘‘Combined Excess Free Energy

Ž .Models and Equations of State,’’ Fluid Phase Equilib., 56, 17 1990 .Heilig, M., and E. U. Franck, ‘‘Calculation of Thermodynamic Prop-

erties of Binary Fluid Mixtures to High Temperatures and HighŽ .Pressures,’’ Ber. Bunsenges. Phys. Chem., 93, 898 1989 .

Heilig, M., and E. U. Franck, ‘‘Phase Equilibria of MulticomponentFluid Systems to High Pressures and Temperatures,’’ Ber. Bunsen-

Ž .ges. Phys. Chem., 94, 27 1990 .Hicks, C. P., and C. L. Young, ‘‘The Gas-Liquid Critical Properties

Ž .of Binary Mixtures,’’ Chem. Re®., 75, 119 1975 .Hicks, C. P., and C. L. Young, ‘‘Critical Properties of Binary Mix-

Ž .tures,’’ J. Chem. Soc. Faraday Trans. I, 72, 122 1976 .Hicks, C. P., R. L. Hurle, and C. L. Young, ‘‘Theoretical Predictions

of Phase Behaviour at High Temperatures and Pressures for Non-Polar Mixture: 4. Comparison with Experimental Results for Car-bon Dioxideq n-Alkane,’’ J. Chem. Soc. Faraday Trans. II, 73, 1884Ž .1977 .

Hicks, C. P., R. L. Hurle, L. S. Toczylkin, and C. L. Young, ‘‘UpperCritical Solution Temperatures of HydrocarbonqFluorocarbon

Ž .Mixtures,’’ Aust. J. Chem., 31, 19 1978 .Holderbaum, T., and J. Gmehling, ‘‘PRSK: A Group Contribution

Equation of State Based on UNIFAC,’’ Fluid Phase Equilib., 70,Ž .251 1991 .

Honnell, K. G., and C. K. Hall, ‘‘A New Equation of State for Ather-Ž .mal Chains,’’ J. Chem. Phys., 90, 1841 1989 .

Hu, Y., H.-L. Liu, and J. M. Prausnitz, ‘‘Equation of State for FluidsŽ .Containing Chainlike Molecules,’’ J. Chem. Phys., 104, 396 1996 .

Huang, H., and S. I. Sandler, ‘‘Prediction of Vapour-Liquid Equilib-ria at High Pressure Using Activity Coefficient Parameters Ob-tained from Low Pressure Data: A Comparison of Two Equation

Ž .of State Mixing Rules,’’ Ind. Eng. Chem. Res., 32, 1498 1993 .Huang, S. H., and M. Radosz, ‘‘Equation of State for Small, Large,

Polydisperse, and Associating Molecules,’’ Ind. Eng. Chem. Res.,Ž .29, 2284 1990 .

Huang, S. H., and M. Radosz, ‘‘Equation of State for Small, Large,Polydisperse, and Associating Molecules. Extension to Fluid Mix-

Ž .tures,’’ Ind. Eng. Chem. Res., 30, 1994 1991 .Hurle, R. L., L. S. Toczylkin, and C. L. Young, ‘‘Theoretical Predic-

tions of Phase Behaviour at High Temperatures and Pressures forNon-Polar Mixture: 2. Gas-Gas Immiscibility,’’ J. Chem. Soc. Fara-

Ž .day Trans. II, 73, 613 1977a .Hurle, R. L., F. Jones, and C. L. Young, ‘‘Theoretical Predictions of

Phase Behaviour at High Temperatures and Pressures for Non-Polar Mixture: 3. Comparison with Upper Critical Solution Tem-peratures for PerfluoromethylcyclohexaneqHydrocarbons,’’ J.

Ž .Chem. Soc. Faraday Trans. II, 73, 618 1977b .Huron, M. J., D. N. Dufour, and J. Vidal, ‘‘Vapour-Liquid Equilib-

rium and Critical Locus Curve Calculations with Soave Equationfor Hydrocarbon Systems with Carbon Dioxide and Hydrogen Sul-

Ž .fide,’’ Fluid Phase Equilib., 1, 247 1978 .Huron, M. J., and J. Vidal, ‘‘New Mixing Rules in Simple Equation

of State for Representing Vapour-Liquid Equilibria of StronglyŽ .Nonideal Mixtures,’’ Fluid Phase Equilib., 3, 255 1979 .

Ikonomou, G. D., and M. D. Donohue, ‘‘Thermodynamics of Hydro-gen-Bonded Molecules: The Associated Perturbed Anisotropic

Ž .Chain Theory,’’ AIChE J., 32, 1716 1986 .Ikonomou, G. D., and M. D. Donohue, ‘‘Extension of the Associated

Perturbed Anisotropic Chain Theory to Mixtures with More thanŽ .One Associating Component,’’ Fluid Phase Equilib., 39, 129 1988 .

Joffe, J., and D. Zudkevitch, ‘‘Fugacity Coefficients in Gas MixturesContaining Light Hydrocarbons and Carbon Dioxide,’’ Ind. Eng.

Ž .Chem. Fundam., 5, 455 1966 .Kalyuzhnyi, Yu. V., C.-T. Lin, and G. Stell, ‘‘Primitive Models of

Chemical Association. IV. Polymer Percus-Yevick Ideal-Chain Ap-proximation for Heteronuclear Hard-Sphere Chain Fluids,’’ J.

Ž .Chem. Phys., 108, 6525 1998 .Kaul, B. K., M. D. Donohue, and J. M. Prausnitz, ‘‘Henry’s Con-

stants and Second Virial Coefficients from Perturbed Hard ChainŽ .Theory,’’ Fluid Phase Equilib., 4, 171 1980 .

Kihara, T., ‘‘Convex Molecules in Gaseous and Crystalline States,’’Ž .Ad®. in Chem. Phys., V, 147 1963 .

Kim, C. H., P. Vimalchand, M. D. Donohue, and S. I. Sandler, ‘‘Lo-cal Composition Model for Chainlike Molecules: A New Simpli-fied Version of the Perturbed Hard Chain Theory,’’ AIChE J., 32,

Ž .1726 1986 .Kiselev, S. B., and J. F. Ely, ‘‘Crossover SAFT Equation of State:


Application for Normal Alkanes,’’ Ind. Eng. Chem. Res., 38, 4993Ž .1999 .

Knudsen, K., E. H. Stenby, and A. Fredenslund, ‘‘A ComprehensiveComparison of Mixing Rules for Calculation of Phase Equilibria in

Ž .Complex Systems,’’ Fluid Phase Equilib., 82, 361 1996 .Kolafa, J., and I. Nezbeda, ‘‘The Lennard-Jones Fluid: An Accurate

Analytic and Theoretically Based Equation of State,’’ Fluid PhaseŽ .Equilib., 100, 1 1994 .

Kontogeorgis, G. M., E. C. Voutsas, I. V. Yakoumis, and D. P. Tas-sios, ‘‘An Equation of State for Associating Fluids,’’ Ind. Eng.

Ž .Chem. Res., 35, 4310 1996 .Kraska, T., and K. E. Gubbins, ‘‘Phase Equilibria Calculations with a

Modified SAFT Equation of State: 2. Binary Mixtures of n-Al-kanes, 1-Alkanols, and Water,’’ Ind. Eng. Chem. Res., 35, 4738Ž .1996a .

Kraska, T., and K. E. Gubbins, ‘‘Phase Equilibria Calculations with aModified SAFT Equation of State. 1. Pure Alkanes, Alkanols, and

Ž .Water,’’ Ind. Eng. Chem. Res., 35, 4727 1996b .Kubic, W. L., ‘‘A Modification of the Martin Equation of State for

Calculating Vapour-Liquid Equilibria,’’ Fluid Phase Equilib., 9, 79Ž .1982 .

Larsen, B. L., P. Rasmussen, and A. Fredenslund, ‘‘A ModifiedUNIFAC Group-Contribution Model for Prediction of PhaseEquilibria and Heats of Mixing,’’ Ind. Eng. Chem. Res., 26, 2274Ž .1987 .

Lee, K. H., M. Lombardo, and S. I. Sandler, ‘‘The Generalized vander Waals Partition Function: II. Application to the Square-Well

Ž .Fluid,’’ Fluid Phase Equilib., 21, 177 1985 .Lermite, C., and J. Vidal, ‘‘A Group Contribution Equation of State

for Polar and Non-Polar Compounds,’’ Fluid Phase Equilib., 72, 111Ž .1992 .

Lin, C.-T., Yu. V. Kalyuzhnyi, and G. Stell, ‘‘Primitive Models ofChemical Association. III. Totally Flexible Sticky Two-Point Modelfor Multicomponent Heteronuclear Fixed-Chain-Length Polymer-

Ž .ization,’’ J. Chem. Phys., 108, 6513 1998 .Lin, Y. L., P. R. Bienkowski, V. M. Shah, and H. D. Cochran, ‘‘Ex-

tension of a Generalized Quartic Equation of State to Pure PolarŽ .Fluids,’’ AIChE J., 40, 152 1996 .

Liu, D. D., and J. M. Prausnitz, ‘‘Thermodynamics of Gas Solubili-Ž .ties in Molten Polymers,’’ J. Appl. Poly. Sci., 24, 725 1979a .

Liu, D. D., and J. M. Prausnitz, ‘‘Molecular Thermodynamics ofPolymer Compatibility: Effect of Contact Agility,’’ Macromol., 12,

Ž .454 1979b .Liu, D. D., and J. M. Prausnitz, ‘‘Calculation of Phase Equilibria for

Mixtures of Ethylene and Low-Density Polyethylene at High Pres-Ž .sures,’’ Ind. Eng. Chem. Process Des. De®., 19, 205 1980 .

Malakhov, A. O., and E. B. Brun, ‘‘Multicomponent Hard-SphereHeterochain Fluid: Equations of State in a Continuum Space,’’

Ž .Macromol., 25, 6262 1992 .Mainwaring, D. E., R. J. Sadus, and C. L. Young, ‘‘Deiters’ Equation

Ž .of State and Critical Phenomena,’’ Chem. Eng. Sci., 43, 459 1988 .Martin, J. J., ‘‘Cubic Equations of State}Which?,’’ Ind. Eng. Chem.

Ž .Fundam., 18, 81 1979 .Mather, A. E., R. J. Sadus, and E. U. Franck, ‘‘Phase Equilibria inŽ .WaterqKrypton at Pressures from 31 MPa to 273 MPa and

Ž .Temperatures from 610 K to 660 K and in WaterqNeon from 45MPa to 255 MPa and from 660 K to 700 K,’’ J. Chem. Thermodyn.,

Ž .25, 771 1993 .McCabe, C., A. Galindo, L. A. Davies, A. Gil-Villegas, and G. Jack-

son, ‘‘Predicting the High-Pressure Phase Equilibria of BinaryMixtures of n-Alkanes using the SAFT-VR Approach,’’ Int. J.

Ž .Thermophys., 19, 1511 1998 .Michelsen, M. L., ‘‘A Modified Huron-Vidal Mixing Rule for Cubic

Ž .Equation of State,’’ Fluid Phase Equilib., 60, 213 1990 .Michelsen, M. L., and R. A. Heidemann, ‘‘Some Properties of Equa-

tion of State Mixing Rules Derived from Excess Gibbs Energy Ex-Ž .pressions,’’ Ind. Eng. Chem. Res., 35, 278 1996 .

Mollerup, J., ‘‘A Note on the Derivation of Mixing Rules from Ex-Ž .cess Gibbs Energy Models,’’ Fluid Phase Equilib., 25, 323 1986 .

Morris, W. O., P. Vimalchand, and M. D. Donohue, ‘‘The Per-turbed-Soft-Chain Theory: An Equation of State Based on the

Ž .Lennard-Jones Potential,’’ Fluid Phase Equilib., 32, 103 1987 .Novenario, C. R., J. M. Caruthers, and K. C. Chao, ‘‘A Mixing Rule

to Incorporate Solution Model into Equation of State,’’ Ind. Eng.Ž .Chem. Res., 35, 269 1996 .

Ohzone, M., Y. Iwai, and Y. Arai, ‘‘Correlation of Solubilities ofHydrocarbon Gases and Vapors in Molten Polymers Using Per-

Ž .turbed-Hard-Chain Theory,’’ J. Chem. Eng. Japan, 17, 550 1984 .Orbey, N., and S. I. Sandler, ‘‘Vapor-Liquid Equilibrium of Polymer

Solutions Using a Cubic Equation of State,’’ AIChE J., 40, 1203Ž .1994 .

Orbey, N., and S. I. Sandler, ‘‘Reformulation of Wong-Sandler Mix-Ž .ing Rule for Cubic Equations of State,’’ AIChE J., 41, 683 1995 .

Orbey, N., and S. I. Sandler, ‘‘Analysis of Excess Free Energy BasedŽ .Equations of State Models,’’ AIChE J., 42, 2327 1996 .

Orbey, H., and S. I. Sandler, Modeling Vapor-Liquid Equilibria, Cam-Ž .bridge University Press, Cambridge 1998 .

Palenchar, R. M., D. D. Erickson, and T. W. Leland, ‘‘Prediction ofBinary Critical Loci by Cubic Equations of State,’’ Equation ofState }Theories and Applications, ACS Symp. Ser., K. C. Chao and

Ž .R. L. Robinson, Jr., eds., 300, 132 1986 .Panagiotopoulos, A. Z., and R. C. Reid, ‘‘New Mixing Rule for Cu-

bic Equation of State for Highly Polar, Asymmetric Systems,’’Equation of State }Theories and Applications, K. C. Chao and R. L.

Ž .Robinson, Jr., eds., ACS Symp. Ser., 300, 571 1986 .Pan, C., and M. Radosz, ‘‘Copolymer SAFT Modeling of Phase Be-

havior in Hydrocarbon-Chain Solutions: Alkane Oligomers,Ž .Polyethylene, Poly ethylene-co-olefin-1 , Polystyrene, and

Ž . Ž .Poly ethylene-co-styrene ,’’ Ind. Eng. Chem. Res., 37, 3169 1998 .Pan, C., and M. Radosz, ‘‘SAFT Modeling of Solid-Liquid Equilibria

in Naphthalene, Normal-Alkane and Polyethylene Solutions,’’ FluidŽ .Phase Equilib., 155, 4453 1999 .

Patel, N. C., and A. S. Teja, ‘‘A New Cubic Equation of State forŽ .Fluids and Fluid Mixtures,’’ Chem. Eng. Sci., 37, 463 1982 .

Peng, D. Y., and D. B. Robinson, ‘‘A New Two-Constant EquationŽ .of State,’’ Ind. Eng. Chem. Fundam., 15, 59 1976 .

Peters, C. J., J. de Swaan Arons, J. M. H. Levelt Sengers, and J. S.Gallagher, ‘‘Global Phase Behaviour of Mixtures of Short and Long

Ž .n-Alkanes,’’ AIChE J., 34, 834 1988 .Phan, S., E. Kierlik, M. L. Rosinberg, H. Yu, and G. Stell, ‘‘Equa-

tions of State for Hard Chain Molecules,’’ J. Chem. Phys., 99, 5326Ž .1993 .

Plackov, D., D. E. Mainwaring, and R. J. Sadus, ‘‘Prediction ofOne-Component Vapor-Liquid Equilibria from the Triple Point tothe Critical Point Using a Simplified Perturbed Hard-Chain The-

Ž .ory Equation of State,’’ Fluid Phase Equilib., 109, 171 1995 .Plohl, O., T. Giese, R. Dohru, and G. Brunner, ‘‘A Comparison of 12

Equations of State with Respect to Gas-Extraction Processes: Re-production of Pure-Component Properties When Enforcing theCorrect Critical Temperature and Pressure,’’ Ind. Eng. Chem. Res.,

Ž .37, 2957 1998 .Ponce-Ramirez, L., C. Lira-Galeana, and C. Tapia-Medina, ‘‘Appli-

cation of the SPHCT Model to the Prediction of Phase EquilibriaŽ .in CO -Hydrocarbon Systems,’’ Fluid Phase Equilib., 70, 1 1991 .2

Prigogine, I., The Molecular Theory of Solutions, North-Holland, Ams-Ž .terdam 1957 .

Raal, J. D., and A. L. Muhlbauer, Phase Equilibria: Measurement and¨Ž .Computation, Taylor and Francis, London 1998 .

Redlich, O., and J. N. S. Kwong, ‘‘On the Thermodynamics of Solu-tions. V: An Equation of State. Fugacities of Gaseous Solutions,’’

Ž .Chem. Re®., 44, 233 1949 .Reed, T. M., and K. H. Gubbins, Applied Statistical Mechanics, Mc-

Ž .Graw-Hill, New York 1973 .Reiss, N. R., H. L. Frisch, and J. L. L. Lebowitz, ‘‘Statistical Me-

Ž .chanics of Rigid Spheres,’’ J. Chem. Phys., 31, 369 1959 .Renon, H., and J. M. Prausnitz, ‘‘Local Composition in Thermody-

namic Excess Functions for Liquid Mixtures,’’ AIChE J., 14, 135Ž .1968 .

Rowlinson, J. S., J. D. ®an der Waals: On the Continuity of the GaseousŽ .and Liquid States, Elsevier, Amsterdam 1988 .

Sadus, R. J., and C. L. Young, ‘‘Phase Behaviour of Carbon DioxideŽ .and Hydrocarbon Mixtures,’’ Aust. J. Chem., 38, 1739 1985a .

Sadus, R. J., and C. L. Young, ‘‘Phase Behaviour of Binary n-Al-kanenitrile and n-Alkanes and Nitromethane and Alkane Mix-

Ž .tures,’’ Fluid Phase Equilib., 22, 225 1985b .Sadus, R. J., and C. L. Young, ‘‘The Critical Properties of Ternary


Mixtures: Siloxane and Perfluoromethylcyclohexane and SiloxaneŽ .Mixtures,’’ Chem. Eng. Sci., 43, 883 1988 .

Sadus, R. J., C. L. Young, and P. Svejda, ‘‘Application of Hard Con-vex Body and Hard Sphere Equations of State to the Critical Prop-

Ž .erties of Binary Mixtures,’’ Fluid Phase Equilib., 39, 89 1988 .Sadus, R. J., ‘‘Attractive Forces in Binary Mixtures: A Priori Predic-

tion of the Gas-Liquid Critical Properties of Binary Mixtures,’’ J.Ž .Phys. Chem., 93, 3787 1989 .

Sadus, R. J., High Pressure Phase Beha®iour of Multicomponent FluidŽ .Mixtures, Elsevier, Amsterdam 1992a .

Sadus, R. J., ‘‘Predicting the Gas-Liquid Critical Properties of BinaryMixtures: An Alternative to Conventional Mixing Rules,’’ Ber.

Ž .Bunsenges. Phys. Chem., 96, 1454 1992b .Sadus, R. J., ‘‘Influence of Combining Rules and Molecular Shape

on the High Pressure Phase Equilibria of Binary Fluid Mixtures,’’Ž .J. Phys. Chem., 97, 1985 1993 .

Sadus, R. J., ‘‘Calculating Critical Transitions of Fluid Mixtures:Ž .Theory vs. Experiment,’’ AIChE J., 40, 1376 1994 .

Sadus, R. J., ‘‘Equations of State for Hard-Sphere Chains,’’ J. Phys.Ž .Chem., 99, 12363 1995 .

Sadus, R. J., ‘‘A Simplified Thermodynamic PerturbationTheory}Dimer Equation of State for Mixtures of Hard-Sphere

Ž .Chains,’’ Macromol., 29, 7212 1996 .Sadus, R. J., Molecular Simulation of Fluids: Theory, Algorithms and

Ž .Object-Orientation, Elsevier, Amsterdam 1999a .Sadus, R. J., ‘‘Simple Equation of State for Hard-Sphere Chains,’’

Ž .AIChE J., 45, 2454 1999b .Sadus, R. J., ‘‘An Equation of State for Hard Convex Body Chains,’’

Ž .Mol. Phys. 2000 .Sandler, S. I., ed., Models for Thermodynamic and Phase Equilibria

Ž .Calculations, Marcel Dekker, New York 1994 .Sandoval, R., G. Wilczek-Vera, and J. H. Vera, ‘‘Prediction of

Ternary Vapour-Liquid Equilibria with the PRSV Equation ofŽ .State,’’ Fluid Phase Equilib., 52, 119 1989 .

Schmidt, G., and H. Wenzel, ‘‘A Modified van der Waals EquationŽ .of State,’’ Chem. Eng. Sci., 35, 1503 1980 .

Schneider, G. M., Chemical Thermodynamics 2. A Specialist PeriodicalReport, M. L. McGlashan, ed., The Chemical Society, LondonŽ .1978 .

Schwartzentruber, J., F. Galivel-Solastiouk, and H. Renon, ‘‘Repre-sentation of the Vapor-Liquid Equilibrium of the Ternary SystemCarbon Dioxide-Propane-Methanol and Its Binaries with a CubicEquation of State: A New Mixing Rule,’’ Fluid Phase Equilib., 38,

Ž .217 1987 .Schwartzentruber, J., and H. Renon, ‘‘Development of a New Cubic

Equation of State for Phase Equilibrium Calculations,’’ Fluid PhaseŽ .Equilib., 52, 127 1989 .

Scott, R. L., Physical Chemistry, An Ad®anced Treatise, Vol. 8A: LiquidState, H. Eyring, D. Henderson, and W. Jost, eds., Academic Press,

Ž .New York 1971 .Semmens, J., S. D. Waterson, and C. L. Young, ‘‘Upper Critical So-

lution Temperatures of Perfluoro-n-HexaneqAlkane, Sulfur Hex-afluorideqSiloxane and PerfluoropropaneqSiloxane Mixtures,’’

Ž .Aust. J. Chem., 33, 1987 1980 .Shah, V. M., P. R. Bienkowski, and H. D. Cochran, ‘‘Generalized

Quartic Equation of State for Pure Nonpolar Fluids,’’ AIChE J.,Ž .40, 152 1994 .

Shah, V. M., Y. L. Lin, P. R. Bienkowski, and H. D. Cochran, ‘‘AGeneralized Quartic Equation of State,’’ Fluid Phase Equilib., 116,

Ž .87 1996 .Shmonov, V. M., R. J. Sadus, and E. U. Franck, ‘‘High Pressure and

Supercritical Phase Equilibria PVT-Data of the Binary WaterqMethane Mixture to 723 K and 200 MPa,’’ J. Phys. Chem., 97, 9054Ž .1993 .

Shukla, K. P., and W. G. Chapman, ‘‘SAFT Equation of State forFluid Mixtures of Hard Chain Copolymers,’’ Mol. Phys., 91, 1075Ž .1997 .

Smits, P. J., I. G. Economou, C. J. Peters, and J. de Swaan Arons,‘‘Equation of State Description of Thermodynamic Properties ofNear-Critical and Supercritical Water,’’ J. Phys. Chem., 98, 12080Ž .1994 .

Soave, G., ‘‘Equilibrium Constants from a Modified Redlich-KwongŽ .Equation of State,’’ Chem. Eng. Sci., 27, 1197 1972 .

Soave, G., ‘‘Improvement of the van der Waals Equation of State,’’Ž .Chem. Eng. Sci., 39, 357 1984 .

Ž .Soave, G., ‘‘A New Expression of q a for the Modified Huron-VidalŽ .Method,’’ Fluid Phase Equilib., 72, 325 1992 .

Soave, G., A. Bertucco, and L. Vecchiato, ‘‘Equation of State GroupContributions from Infinite-Dilution Activity Coefficients,’’ Ind.

Ž .Eng. Chem. Res., 33, 975 1994 .Song, Y., S. M. Lambert, and J. M. Prausnitz, ‘‘A Perturbed Hard-

Sphere-Chain Equation of State for Normal Fluids and Polymers,’’Ž .Ind. Eng. Chem. Res., 33, 1047 1994a .

Song, Y., S. M. Lambert, and J. M. Prausnitz, ‘‘Liquid-Liquid PhaseDiagrams for Binary Polymer Solutions from a Perturbed Hard-Sphere-Chain Equation of State,’’ Chem. Eng. Sci., 49, 2765Ž .1994b .

Spear, R. R., R. L. Robinson, Jr., and K. C. Chao, ‘‘Critical States ofMixtures and Equations of State,’’ Ind. Eng. Chem. Fundam., 8, 2Ž .1969 .

Spear, R. R., R. L. Robinson, Jr., and K. C. Chao, ‘‘Critical States ofTernary Mixtures and Equations of State,’’ Ind. Eng. Chem. Fun-

Ž .dam., 10, 588 1971 .Sretenskaja, N. G., R. J. Sadus, and E. U. Franck, ‘‘High-Pressure

Phase Equilibria and Critical Curve of the WaterqHelium SystemŽ .to 200 MPa and 723 K,’’ J. Phys. Chem., 99, 4273 1995 .

Stell, G., and Y. Zhou, ‘‘Microscopic Modeling of Association,’’ FluidŽ .Phase Equilib., 79, 1 1992 .

Stell, G., C.-T. Lin, and Yu. V. Kalyuzhnyi, ‘‘Equations of State ofFreely Jointed Hard-Sphere Chain Fluids: Theory,’’ J. Chem. Phys.,

Ž .110, 5444 1999a .Stell, G., C.-T. Lin, and Yu. V. Kalyuzhnyi, ‘‘Equations of State of

Freely Jointed Hard-Sphere Chain Fluids: Numerical Results,’’ J.Ž .Chem. Phys., 110, 5458 1999b .

Stryjek, R., and J. H. Vera, ‘‘PRSV: An Improved Peng-RobinsonEquation of State for Pure Compounds and Mixtures,’’ Can. J.

Ž .Chem. Eng., 64, 323 1986a .Stryjek, R., and J. H. Vera, ‘‘PRSV: An Improved Peng-Robinson

Equation of State with New Mixing Rules for Strongly Non IdealŽ .Mixtures,’’ Can. J. of Chem. Eng., 64, 334 1986b .

Svejda, P. and F. Kohler, ‘‘A Generalized van der Waals Equation ofState: I. Treatment of Molecular Shape in Terms of the Boublik

Ž .Nezbeda Equation,’’ Ber. Bunsenges. Phys. Chem., 87, 672 1983 .Tavares, F. W., J. Chang, and S. I. Sandler, ‘‘Equation of State for

the Square-Well Chain Fluid Based on the Dimer Version ofŽ .Wertheim’s Perturbation Theory,’’ Mol. Phys., 86, 1451 1995 .

Tavares, F. W., J. Chang, and S. I. Sandler, ‘‘A Completely AnalyticEquation of State for the Square-Well Chain Fluid of Variable

Ž .Width,’’ Fluid Phase Equilib., 140, 129 1997 .Thiele, E., ‘‘Equation of State for Hard Spheres,’’ J. Chem. Phys., 39,

Ž .474 1963 .Tochigi, K., ‘‘Prediction of High-Pressure Vapour-Liquid Equilibria

Ž .Using ASOG,’’ Fluid Phase Equilib., 104, 253 1995 .Toczylkin, L. S., and C. L. Young, ‘‘Comparison of the Values of

Interaction Parameter from Upper Critical Solution Temperaturesof AcetoneqAlkanes with Values Obtained from Gas-Liquid Crit-

Ž .ical Temperatures,’’ Aust. J. Chem., 30, 767 1977 .Toczylkin, L. S., and C. L. Young, ‘‘Gas-Liquid Critical Tempera-

tures of Mixtures Containing Electron Donors. Part 1. Ether Mix-Ž .tures,’’ J. Chem. Thermodyn., 12, 355 1980a .

Toczylkin, L. S., and C. L. Young, ‘‘Gas-Liquid Critical Tempera-tures of Mixtures Containing Electron Donors. Part 2. Amine Mix-

Ž .tures,’’ J. Chem. Thermodyn., 12, 365 1980b .Toczylkin, L. S., and C. L. Young, ‘‘Upper Critical Solution Temper-

atures of HydrocarbonqFluorocarbon Mixtures: Mixtures withŽ .Specific Interactions,’’ Aust. J. Chem., 33, 465 1980c .

Trebble, M. A., and P. R. Bishnoi, ‘‘Extension of the Trebble-Bishnoi Equation of State to Fluid Mixtures,’’ Fluid Phase Equilib.,

Ž .40, 1 1987 .Tsonopoulos, C., and J. L. Heidman, ‘‘From Redlich-Kwong to the

Ž .Present,’’ Fluid Phase Equilib., 24, 1 1985 .Twu, C. H., and J. E. Coon, ‘‘CEOSrAE Mixing Rules Constrained

by vdW Mixing Rule and Second Virial Coefficient,’’ AIChE J., 42,Ž .3212 1996 .

Twu, C. H., J. E. Coon, and D. Bluck, ‘‘A Zero-Pressure CubicEquation of State Mixing Rule for Predicting High Pressure Phase


Equilibria Using Infinite Dilution Activity Coefficients at LowŽ .Temperature,’’ Fluid Phase Equilib., 150–151, 181 1998 .

Twu, C. H., and K. E. Gubbins, ‘‘Thermodynamics of PolyatomicŽ .Fluid Mixtures: I. Theory,’’ Chem. Eng. Sci., 34, 863 1978a .

Twu, C. H., and K. E. Gubbins, ‘‘Thermodynamics of PolyatomicFluid Mixtures: II. Polar, Quadrupolar and Octopolar Molecules,’’

Ž .Chem. Eng. Sci., 33, 879 1978b .Van Konynenburg, P. H., and R. L. Scott, ‘‘Critical Lines and Phase

Equilibria in Binary van der Waals Mixtures,’’ Philos. Trans. R.Ž .Soc. London, Ser. A, 298, 495 1980 .

Van Pelt, A., C. J. Peters, and J. de Swaan Arons, ‘‘Liquid-LiquidImmisicibility Loops Predicted with the Simplified-Perturbed-

Ž .Hard-Chain Theory,’’ J. Chem. Phys., 95, 7569 1991 .Van Pelt, A., C. J. Peters, and J. de Swaan Arons, ‘‘Application of

the Simplified-Perturbed-Hard-Chain Theory for Pure Compo-Ž .nents Near the Critical Point,’’ Fluid Phase Equilib., 74, 67 1992 .

Vilmalchand, P., and M. D. Donohue, ‘‘Thermodynamics ofQuadrupolar Molecules: The Perturbed-Anisotropic-Chain The-

Ž .ory,’’ Ind. Eng. Chem. Fundam., 24, 246 1985 .Vilmalchand, P., I. Celmins, and M. D. Donohue, ‘‘VLE Calcula-

tions for Mixtures Containing Multipolar Compounds Using theŽ .Perturbed Anisotropic Chain Theory,’’ AIChE J., 32, 1735 1986 .

Vilmalchand, P., and M. D. Donohue, ‘‘Comparison of Equations ofŽ .State for Chain Molecules,’’ J. Phys. Chem., 93, 4355 1989 .

Voros, N. G., and D. P. Tassios, ‘‘Vapour-Liquid Equilibria in Non-polarrWeakly Polar Systems with Different Types of Mixing Rules,’’

Ž .Fluid Phase Equilib., 91, 1 1993 .Voutsas, E. C., G. M. Kontogeorgis, I. V. Yakoumis, and D. P. Tas-

sios, ‘‘Correlation of Liquid-Liquid Equilibria for AlcoholrHydro-carbon Mixtures Using the CPA Equation of State,’’ Fluid Phase

Ž .Equilib., 132, 61 1997 .Wang, J.-L., G.-W. Wu, and R. J. Sadus, ‘‘Closed-Loop Liquid-Liquid

Equilibria and the Global Phase Behavior of Binary Mixtures,’’ inŽ .press 2000 .

Wang, W., Y. Qu, C. H. Twu, and J. E. Coon, ‘‘Comprehensive Com-parison and Evaluation of the Mixing Rules of WS, MHV2, and

Ž .Twu et al.,’’ Fluid Phase Equilib., 116, 488 1996 .Waterson, S. D., and C. L. Young, ‘‘Gas-Liquid Critical Tempera-

tures of Mixtures Containing an Organosilicon Compound,’’ Aust.Ž .J. Chem., 31, 957 1978 .

Wei, Y. S., and R. J. Sadus, ‘‘Calculation of the Critical High Pres-sure Liquid-Liquid Phase Equilibria of Binary Mixtures Contain-ing Ammonia: Unlike Interaction Parameters for the Heilig-Franck

Ž .Equation of State,’’ Fluid Phase Equilib., 101, 89 1994a .Wei, Y. S., and R. J. Sadus, ‘‘Critical Transitions of Ternary Mix-

tures: A Window on the Phase Behaviour of Multicomponent Flu-Ž .ids,’’ Int. J. Thermophys., 15, 1199 1994b .

Wei, Y. S., and R. J. Sadus, ‘‘Vapour-Liquid and Liquid-Liquid PhaseEquilibria of Binary Mixtures Containing Helium: Comparison of

Experiment with Predictions using Equations of State,’’ Fluid PhaseŽ .Equilib., 122, 1 1996 .

Wei, Y. S., R. J. Sadus, and E. U. Franck, ‘‘Binary Mixtures of Wa-terqFive Noble Gases: Comparison of Binodal and Critical Curves

Ž .at High Pressures,’’ Fluid Phase Equilib., 123, 1 1996 .Wei, Y. S., and R. J. Sadus, ‘‘Phase Behavior of Ternary Mixtures: A

Theoretical Investigation of the Critical Properties of Mixtures withŽ .Equal Size Components,’’ Phys. Chem. Chem. Phys., 1, 4399 1999 .

Wertheim, M. S., ‘‘Fluids with Highly Directional Attractive Forces:Ž .I. Statistical Thermodynamics,’’ J. Stat. Phys., 35, 19 1984a .

Wertheim, M. S., ‘‘Fluids with Highly Directional Attractive Forces:II. Thermodynamic Perturbation Theory and Integral Equations,’’

Ž .J. Stat. Phys., 35, 34 1984b .Wertheim, M. S., ‘‘Fluids with Highly Directional Attractive Forces:

Ž .III. Multiple Attraction Sites,’’ J. Stat. Phys., 42, 459 1986a .Wertheim, M. S., ‘‘Fluids with Highly Directional Attractive Forces:

Ž .IV. Equilibrium Polymerization,’’ J. Stat. Phys., 42, 477 1986b .Wertheim, M. S., ‘‘Fluids of Dimerizing Hard Spheres, and Fluid

Mixtures of Hard Spheres and Dispheres,’’ J. Chem. Phys., 85, 2929Ž .1986c .

Wertheim, M. S., ‘‘Thermodynamic Perturbation Theory of Polymer-Ž .ization,’’ J. Chem. Phys., 87, 7323 1987 .

Wong, S. S. H., and S. I. Sandler, ‘‘A Theoretically Correct MixingŽ .Rule for Cubic Equations of State,’’ AIChE J., 38, 671 1992 .

Wong, S. S. H., H. Orbey, and S. I. Sandler, ‘‘Equation of StateMixing Rule for Nonideal Mixtures Using Available Activity Coef-ficient Model Parameters and that Allows Extrapolation over LargeRanges of Temperature and Pressure,’’ Ind. Eng. Chem. Res., 31,

Ž .2033 1992 .Yelash, L. V., and T. Kraska, ‘‘Closed-Loops of Liquid-Liquid Im-

miscibility in Binary Mixtures of Equal Sized Molecules Predictedwith a Simple Theoretical Equation of State,’’ Ber. Bunsenges. Phys.

Ž .Chem., 102, 213 1998 .Yethiraj, A., and C. K. Hall, ‘‘Generalized Flory Equations of State

Ž .for Square-Well Chains,’’ J. Chem. Phys., 95, 8494 1991 .Yu, J. M., and B. C.-Y. Lu, ‘‘A Three-Parameter Cubic Equation of

State for Asymmetric Mixture Density Calculation,’’ Fluid PhaseŽ .Equilib., 34, 1 1987 .

Yu, M. L., and Y. P. Chen, ‘‘Correlation of Liquid-Liquid PhaseEquilibria Using the SAFT Equation of State,’’ Fluid Phase Equilib.,

Ž .94, 149 1994 .Zhou, Y., and C. K. Hall, ‘‘Thermodynamic Perturbation Theory for

Fused Hard-Sphere and Hard-Disk Chain Fluids,’’ J. Chem. Phys.,Ž .103, 2688 1995 .

Zhou, Y., and G. Stell, ‘‘Chemical Association in Simple Models ofMolecular and Ionic Fluids: III. The Cavity Function,’’ J. Chem.

Ž .Phys., 96, 1507 1992 .

Manuscript recei®ed Feb. 9, 1999, and re®ision recei®ed July 27, 1999.


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