hcostello

08-04-2013, 02:36 PM

recently I have been requested to verify a series of phase equilibria calc's in critical area for a mixture of 15 hydrocarbons + water, CO2, H2S

The mole fraction of water it's 0.01 and the water separates forming a second liquid phase.

The vapor-liquid-liquid phase envelope utility available in PRODE PROPERTIES allows to draw the whole phase diagram including the three phase line,

once the phase diagram has been generated it's possible to verify results from different flash operations available in PRODE PROPERTIES such as,

isothermal flash operations,

specified enthalpy and pressure or temperature

specified entropy and pressure or temperature

specified volume and pressure or temperature

the phase diagram, generated directly in Excel, includes the equilibrium points (t,p) on dew line, bubble line plus three phases lines plus cricondentherm, cricondenbar and critical points.

With these values one can solve a flash operation e verify if phase equilibria results are in accordance.

For this I have utilized Excel to create tables of values vs. several t, p starting from atmospheric pressure and up to cricondenbar.

PRODE PROPERTIES shows a reliable convergence also for points very close to critical (in my tests at distance of 0.05 K from critical point).

You may find additional information and download PRODE PROPERTIES in this thread

''

The mole fraction of water it's 0.01 and the water separates forming a second liquid phase.

The vapor-liquid-liquid phase envelope utility available in PRODE PROPERTIES allows to draw the whole phase diagram including the three phase line,

once the phase diagram has been generated it's possible to verify results from different flash operations available in PRODE PROPERTIES such as,

isothermal flash operations,

specified enthalpy and pressure or temperature

specified entropy and pressure or temperature

specified volume and pressure or temperature

the phase diagram, generated directly in Excel, includes the equilibrium points (t,p) on dew line, bubble line plus three phases lines plus cricondentherm, cricondenbar and critical points.

With these values one can solve a flash operation e verify if phase equilibria results are in accordance.

For this I have utilized Excel to create tables of values vs. several t, p starting from atmospheric pressure and up to cricondenbar.

PRODE PROPERTIES shows a reliable convergence also for points very close to critical (in my tests at distance of 0.05 K from critical point).

You may find additional information and download PRODE PROPERTIES in this thread

''