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Phase Equilibria , Model Selection In Prode
#1
Posted 03 May 2018 - 02:56 PM
#2
Posted 03 May 2018 - 03:51 PM
for water-hydrocarbons phase equilibria the main differences (between Peng Robinson, PR and Peng Robinson Extended, PRX in Prode Properties) are due to the different alpha functions,
I think it is possible, within certain limits, reduce the differences including a temperature dependence in BIPs
but i do not see many advantages,
Peng Robinson (and Soave Redlich Kwong) are good for non-polar fluids,
for polar fluids there are alternatives (the Peng Robinson Extended in Prode Properties is an example)
#3
Posted 07 May 2018 - 08:54 AM
thanks Paolo,
I know that PRX has different alpha function,
I have a client which does these calc.s with Kabadi-Danner (which is not available in my Base version),
these streams include hydrocarbons, N2, CO2, H2S, water (up to 8 % mole fract.), methanol etc.
which model do you suggest ?
#4
Posted 07 May 2018 - 11:34 AM
Kabadi & Danner model (based on SRK) includes a composition dependence for water-hydrocarbons
aij = a1ij + a2ij * zw
a1ij = zi*zj*aij a2ij = zi*zw*awij
in Prode the awij's are icalculated only for water-hydrocarbons pairs (I believe the same in other simulators),
if you have other polar fluids (methanol etc.) better to use a extended EOS as PRX with complex mixing rules as Huron Vidal, in Prode Properties it is the PRX-NRTL (P-HV) model
in general I prefer PRX with complex mixing rules,
if BIPs are not present in Prode database, do use the data regression procedure...
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