A new two-parameter cubic equation of state for predicting phase behavior of pure compounds and mixtures

The Patel–Teja and the Peng–Robinson EoSs performance when Soave alpha function is replaced by an exponential function

“…(24) have been proposed and used for some authors to determine parameters in their respective equations of state [1,58,59]. The weight factors w 1 and w 2 are fixed according to the equation of state.…”

“…The parameters which have to be estimated for the PT EoS are those that belong to the alpha function and the empiric critical compressibility factor. The weight factors employed are those chosen by Dashtizadeh et al [58].…”

Comparison of the prediction power of 23 generalized equations of state: Part II — Parametric evaluation

“…The studied EOSs in the first part [1] were the RKS (RedlichKwong-Soave) [5], RKTCC (Redlich-Kwong-Twu-CoonCunningham) [15], RKNB (Redlich-Kwong-Nasrifar-Bolland) [16], HK (Harmens-Knapp) [17], PR (Peng-Robinson) [18,19], PRTCC (Peng-Robinson-Twu-Coon-Cunningham) [20], PRGGPR (Peng-Robinson-Gasem-Gao-Pan-Robinson) [9], KM (KubicMartin) [21], NB (Nasrifar-Bolland) [22], NM (NasrifarMoshfeghian) [23], MNM (modified NM) [24], TB (Trebble-Bishnoi) [25], TBS (Salim-Trebble-Bishnoi) [26], PT (Patel-Teja) [27], PTV (Patel-Teja-Valderrama) [28], KS (Kumar-Starling) [29], MKS (Chu-Zuo-Guo) [30], Jiuxun [31], MMM (Mohsennia-Modarres-Mansoori) [32], DPTG (Dashtizadeh-Pazouki-Taghikhani-Ghotbi) [33], LKP (Lee-Kesler-Plöcker et al) [34], BWRSH (Benedict-WebRubin-Starling-Han) [35] and BWRSHN (Benedict-WebRubin-Starling-Han-Nishumi) [36,37]. Details of the aforementioned equations (functional form and parameters) have been summarized in the first part [1] under six more general forms of TB, Martin, KS, Jiuxun, cubic hard-core and truncated Virial which encompass the others.…”

Toward artificial intelligence-based modeling of vapor liquid equilibria of carbon dioxide and refrigerant binary systems

“…7 The cubic, non-cubic and hard-sphere equations of state (EoS) can be applied for estimating the VLE data and thermophysical properties. [8][9][10] Although these semi empirical equations were derived based on reliable physical principles and often show acceptable preciseness for predicting the phase behaviour of pure and mixtures, they have rare application in the process design software, because of their complex terms and many adjustable parameters that are required in mixing rules. [11][12][13] Adjustment of these parameters through iterative method is tedious, and moreover there exists no guaranty for finding the best set of parameters.…”