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                                                        CHEMICAL ENGINEERING
                           Chao Seader equation (C S)
                           The Chao Seader equation gives accurate predictions for light hydrocarbons and
                           hydrogen, but is limited to temperatures below 530 K; Chao and Seader (1961).
                           Grayson Stread equation (G S)
                           Grayson and Stread (1963) extended the Chao Seader equation for use with hydrogen
                           rich mixtures, and for high pressure and high temperature systems. It can be used up to
                           200 bar and 4700 K.

                           Peng Robinson equation (P R)
                           The Peng Robinson equation is related to the Redlich Kwong Soave equation of state
                           and was developed to overcome the instability in the Redlich Kwong Soave equation
                           near the critical point; Peng and Robinson (1970).

                           Brown K  10  equation (B K10)

                           Brown, see Cajander et al. (1960), developed a method which relates the equilibrium
                           constant K to four parameters: component, pressure, temperature, and the convergence
                           pressure. The convergence pressure is the pressure at which all K values tend to 1. The
                           Brown K 10 equation is limited to low pressure and its use is generally restricted to vacuum
                           systems.

                           8.16.4. Correlations for liquid phase activity coefficients
                           The liquid phase activity coefficient,   i , is a function of pressure, temperature and liquid
                           composition. At conditions remote from the critical conditions it is virtually independent
                           of pressure and, in the range of temperature normally encountered in distillation, can be
                           taken as independent of temperature.
                             Several equations have been developed to represent the dependence of activity coeffi-
                           cients on liquid composition. Only those of most use in the design of separation processes
                           will be given. For a detailed discussion of the equations for activity coefficients and their
                           relative merits the reader is referred to the book by Reid et al. (1987), Walas (1984) and
                           Null (1970).

                           Wilson equation
                           The equation developed by Wilson (1964) is convenient to use in process design:
                                                           n

                                                                        n 
                                                                              x i A ik
                                                          
            
            
                                           ln   k D 1.0   ln   x j A kj                          8.38
                                                                           n
                                                                           
        
                                                          jD1          iD1    x j A ij    
                                                                            jD1
                           where   k D activity coefficient for component k,
                             A ij ,A ji D Wilson coefficients (A values) for the binary pair i, j,
                                  n D number of components.
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