MODE = BUBP (=3)

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MODE = BUBP (3)

Note: If the $ConvertEESREFPROPUnits directive is used in the EES program, inputs should be provided in the unit system defined in EES and outputs will be automatically converted to the unit system defined in EES. The units shown for inputs and outputs in the following description apply when the $CONVERTEESREFPROPUNITS directive is not used.

Description: Bubble point calculation for a given pressure
     In1 = Pressure in kPa
     In2 = mole fraction of first component in saturated liquid (skip for pure fluid)
     ...
     InN = mole fraction of next to last component
            Note: If the /mass flag is provided with the $CONVERTEESREFPROPUNITS directive, mass fractions should be provided instead of mole fractions.
     Out1 = Temperature of saturated liquid in K
     Out2 = Density of saturated liquid in kmol/m3
     Out3 = Temperature of saturated liquid in K (Same as Out1)
     Out4 = Density of saturated vapor in kmol/m3
     Out5..OutN = Mole fractions of each component in vapor at equilibrium with the liquid
               Note: Mass fractions (in place of mole fractions) are output if the /mass flag is provided with the $CONVERTEESREFPROPUNITS directive


Example 1:
BUBP=3
P=100 [kPa]
mf=0.3
Mixture$='R32+R134a'
Call ees_refprop(Mixture$, BUBP, P, mf: TL, DL, TX, DV, y_32, y_134a)

{Solution:
BUBP=3
DL=15.64 [kmol/m^3]
DV=0.05322 [kmol/m^3]
TL=235.3 [K]
TX=235.3 [K]
y_134a=0.4139
y_32=0.5861
}

Example 2:
$UnitSystem SI C Pa mass
$ConvertEESREFPROPUnits
BUBP=3
P=1E5 [Pa]
Call ees_refprop('R134a', BUBP, P : TL, D_liq,TV , D_vap)

{Solution:
BUBP=3
D_liq=1378 [kg/m^3]
D_vap=5.193 [kg/m^3]
P=100000 [Pa]
TL=-26.36 [C]
TX=-26.36 [C]
}

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