Wilson correlation
ln(Kval) = ln(Pci/p)+5.373*(1+Aci)*(1-Tci/t)
can produce decent results with (light) hydrocarbons,
however your mixture may include water or other non-hydrocarbon fluids and a EOS (there are many available in process simulators and thermodynamic libraries) can produce much...
thanks all,
apetri, if possible I would stay with base version which probably includes more than I need (except for inhibitors)
PaoloPemi, thanks for advice, I'll test the method.
georgeverghese, I wish to evaluate a few polar compounds (alcohols and glycols which work as inhibitors by...
In some cases I need to calculate hydrate formation temperature ( or hydrate formation pressure ) for natural gas mixtures + inhibitors as methanol , glycol etc.
I have the base version of Prode Properties 1.2C4 which includes two models (PRX-NRTL-HV + PRX-CPA-NRTL-HV) for hydrates,
Prode...
HazGas,
if you imagine a single molecule (no interactions with other molecules) expanding from initial to final conditions the path is isentropic,
a problem, simulating a real behaviour, is that each molecule interact with each other and the final result is difficult to estimate,
simulators...
are you comparing isentropic vs. polytropic ?
"http://en.wikipedia.org/wiki/Gas_compressor"
consider the equations for ideal gases,
for real gases things are a bit more complex.
tables with Kvalues were common in old days,
my copy of API TDB includes a large collection,
you may find some data on GPSA chapter 25 "Equilibrium Ration (K) data"
Another possibility is to calculate kvalues yourself with a EOS,
details are shown on textbooks as The Properties of Gases adn...
in Matlab and Mathcad for Steam properties such as dH/dP , dH/dT , dS/dP , dS/dT , dV/dP , dV/dT ....
I utilize IAPWS95 model and a process library (Prode Properties),
IAPWS95 is the most accurate but it is complex to code,
you may find more easy IAPWS97 or use an external code as I do.
dcasto,
out of curiosity, how have you calculated those values ?
for pure ethane,
single polytropic stage with polytropic eff. 75%
tin 15 C pin 20 Bar.a
pout 120 bar.a
I get a tout of about 149 C
(about 50 C less)
indeed it seems a strange result,
perhaps in these cases it would be preferable a step by step solution as suggested by apetri,
at least you will be able to evidence the problem (if any),
unfortunately a (black box) unit allows only a limited access and control.
I would recommend to evaluate the list in this page
http://en.wikipedia.org/wiki/List_of_chemical_process_simulators
there are many good tools available with both a graphical interface and not, I would presume you are a chemeng, the best you can do is to download free/trial copies and make...
if the dew point is far from minimum operating temperature (say 3-4 times the max error) perhaps you may persuade the client to accept a correction with results from regular laboratory analysis, the same if there are really very small amounts of heavy components, differently better to budget a...
everything mentioned in sales contract is significant, if not perhaps GPSA manual (or equivalents) may provide some hints.
The point is that specifications parameters may include compositions, contaminants, water content etc. in addition to dew point, as example we have a maximum content for...
if your gas contains a significant amount of octane, nonane, or decane you must consider all these heavy components when calculating dew points, differently you get uncorrect values, the characterization works only when all these components (with a significant amount) are included...
