MODE = BUBT (=1)

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MODE = BUBT (1)

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 temperature
     In1 = Temperature in K
     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 = Pressure of saturated liquid in kPa
     Out2 = Density of saturated liquid in kmol/m3
     Out3 = Pressure of saturated liquid in kPa (same as Out2)
     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:
BUBT=1      "mode for bubble point calculation at a given temperature"
T=350 [K]    "temperature"
mf=0.3          "mole fraction"
CALL EES_REFPROP('R32+R134a',BUBT, T, mf: PL, DL, PX, DV, y_32, y_134a)

{Solution:
BUBT=1
DL=10.08 [kmol/m^3]
DV=1.976 [kmol/m^3]
mf=0.3
PL=3260 [kPa]
PX=3260 [kPa]
T=350 [K]
y_134a=0.6164
y_32=0.3836
}

Example 2:
$UnitSystem SI C Pa mass
$ConvertEESREFPROPUnits
BUBT=1
T=50 [C]
Call ees_refprop('R134a',BUBT,T: PL,D_liq,PV,D_vap)

{Solution:
BUBT=1
D_liq=1102 [kg/m^3]
D_vap=66.27 [kg/m^3]
PL=1.318E+06 [Pa]
PV=1.318E+06 [Pa]
T=50 [C]
}

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