Margules activity model

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The Margules activity model is a simple thermodynamic model for the excess Gibbs free energy of a liquid mixture introduced in 1895 by Max Margules.[1][2] After Lewis had introduced the concept of the activity coefficient, the model could be used to derive an expression for the activity coefficients of a compound i in a liquid, a measure for the deviation from ideal solubility, also known as Raoult's law.

In chemical engineering the Margules Gibbs free energy model for liquid mixtures is better known as the Margules activity or activity coefficient model. Although the model is old it has the characteristic feature to describe extrema in the activity coefficient, which modern models like NRTL and Wilson cannot.


Excess Gibbs free energy[edit]

Margules expressed the excess Gibbs free energy of a binary liquid mixture as a power series of the mole fractions xi:

In here the A, B are constants, which are derived from regressing experimental phase equilibria data. Frequently the B and higher order parameters are set to zero. The leading term assures that the excess Gibbs energy becomes zero at x1=0 and x1=1.

Activity coefficient[edit]

The activity coefficient of component i is found by differentiation of the excess Gibbs energy towards xi. This yields, when applied only to the first term and using the Gibbs–Duhem equation,:[3]

In here A12 and A21 are constants which are equal to the logarithm of the limiting activity coefficients: and respectively.

When , which implies molecules of same molecular size but different polarity, the equations reduce to the one-parameter Margules activity model:

In that case the activity coefficients cross at x1=0.5 and the limiting activity coefficients are equal. When A=0 the model reduces to the ideal solution, i.e. the activity of a compound is equal to its concentration (mole fraction).


Using simple algebraic manipulation, can be stated that increases or decreases monotonically within all range, if or with , respectively. When and , the activity coefficient curve of component 1 shows a maximum and compound 2 minimum at:

Same expression can be used when and , but in this situation the activity coefficient curve of component 1 shows a minimum and compound 2 a maximum. It is easily seen that when A12=0 and A21>0 that a maximum in the activity coefficient of compound 1 exists at x1=1/3. Obvious, the activity coefficient of compound 2 goes at this concentration through a minimum as a result of the Gibbs-Duhem rule.

The binary system Chloroform(1)-Methanol(2) is an example of a system that shows a maximum in the activity coefficient of Chloroform. The parameters for a description at 20 °C are A12=0.6298 and A21=1.9522. This gives a minimum in the activity of Chloroform at x1=0.17.

In general, for the case A=A12=A21, the larger parameter A, the more the binary systems deviates from Raoult's law; i.e. ideal solubility. When A>2 the system starts to demix in two liquids at 50/50 composition; i.e. plait point is at 50 mol%. Since:

For asymmetric binary systems, A12≠A21, the liquid-liquid separation always occurs for


Or equivalently:

The plait point is not located at 50 mol%. It depends on the ratio of the limiting activity coefficients.

Recommended values[edit]

An extensive range of recommended values for the Margules parameters can be found in the literature.[5][6] Selected values are provided in the table below.

System A12 A21
Acetone(1)-Chloroform(2)[6] -0.8404 -0.5610
Acetone(1)-Methanol(2)[6] 0.6184 0.5788
Acetone(1)-Water(2)[6] 2.0400 1.5461
Carbon tetrachloride(1)-Benzene (2)[6] 0.0948 0.0922
Chloroform(1)-Methanol(2)[6] 0.8320 1.7365
Ethanol(1)-Benzene(2)[6] 1.8362 1.4717

See also[edit]


  1. ^ Margules, Max (1895). "Über die Zusammensetzung der gesättigten Dämpfe von Misschungen". Sitzungsberichte der Kaiserliche Akadamie der Wissenschaften Wien Mathematisch-Naturwissenschaftliche Klasse II. 104: 1243–1278.
  2. ^ Gokcen, N.A. (1996). "Gibbs-Duhem-Margules Laws". Journal of Phase Equilibria. 17 (1): 50–51. doi:10.1007/BF02648369. 
  3. ^ Phase Equilibria in Chemical Engineering, Stanley M. Walas, (1985) p180 Butterworth Publ. ISBN 0-409-95162-5
  4. ^ Wisniak, Jaime (1983). "Liquid—liquid phase splitting—I analytical models for critical mixing and azeotropy". Chem Eng Sci. 38 (6): 969–978. doi:10.1016/0009-2509(83)80017-7. 
  5. ^ Gmehling, J.; Onken, U.; Arlt, W.; Grenzheuser, P.; Weidlich, U.; Kolbe, B.; Rarey, J. (1991–2014). Chemistry Data Series, Volume I: Vapor-Liquid Equilibrium Data Collection. Dechema. 
  6. ^ a b c d e f g Perry, Robert H.; Green, Don W. (1997). Perry's Chemical Engineers' Handbook (7th ed.). New York: McGraw-Hill. pp. 13:20. ISBN 0-07-115982-7.