rotw, thanks for the contribute,
I think your objection is correct,
if one knows (a priori knowledge about the process) that all liquid water forms a separate phase probably the results are not too different,
however I see that some models predict some miscibility for heavy hydrocarbons or...
Paolo,
thanks, I understand the point, with complex models such as GERG 2008 it is not possible to generate "virtual" values for water fugacity at low temperatures (below freezing point), while the alpha function in Peng Robinson allows such extrapolations,
that makes sense and probably the...
thanks apetri,
many streams in my projects have hydrocarbons, CO2, N2 and water,
I fear that solving water separately (as pure fluid) I will lose many information about multiphase equilibria.
I am comparing phase diagrams generated by different models (Peng-Robinson, Soave, Lee Kesler Ploecker, GERG 2008 etc.) for mixtures with hydrocarbons + water,
I would like to use GERG 2008 as reference but it seems that this model doesn't work with light hydrocarbons + water fractions > 0.01...
I have water solubility measurements in vapor for methane-water, ethane-water, propane-water etc. for each measurement I know
Temperature Pressure Water content in vapor phase (Y)
282 K 10 Bar.a 0.0012
I wish to calculate the BIPs for different models (such as Peng Robinson, Soave...
thanks all for help
PaoloPemi,
I'll review Prode Properties and the methodology applied (not aware of that).
David,
it's a preliminary design, as you may know there are several kind of pumps/compressors allowing gas+liquid, at following stages we will define all the details
poli60,
I can...
In a gas pipeline project I have several wet gas compressors (80-90% gas)
for these compressors preliminary spec. give a 85% polytropic efficiency,
which is the standard procedure to model these compressors ?
I can model as adiabatic (assuming 85% efficiency) but I would prefer a more accurate...
