![]() However, the bubble point temperature is unknown and the other terms are complex functions of temperature, pressure, and composition for both vapor and liquid phases. ![]() The vapor and liquid phase fugacities must be equal at equilibrium. Such activity coefficient models include the Wilson, NRTL, or UNIQUAC options. This is done by multiplying the liquid mole fraction with the activity coefficient and a reference pure component fugacity (close to the vapor pressure only at low pressures). The Dalton Law approximation for the vapor phase partial pressures must be multiplied by the vapor phase fugacity coefficient obtained from such an equation of state.įor complex chemical mixtures, one must modify the ideal liquid phase fugacity (Raoult's Law). Examples are the Soave, Peng-Robinson, BWR, or Lee-Kesler equations of state. For high pressure hydrocarbon systems, an equation of state can be used for both phases. This is done using the appropriate thermodynamics to model the vapor and liquid phase fugacities. The only reliable way to compute the vapor pressure of a multicomponent mixture is to perform a bubble point calculation. I find none of the answers provided to date to be theoretically correct.
0 Comments
Leave a Reply. |
AuthorWrite something about yourself. No need to be fancy, just an overview. ArchivesCategories |