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if you do not know the components in the mixture robably the best solution is to heat the bottle and measure the resulting pressure, as already suggested by LittleInch, if you know (or can guess) the composition, the approach suggested by APetri can help to estimate the final pressure, assuming...

while I prefer Olga / Leda models for these simulations, I would suggest the specialized textbooks for a detailed analysis of the different aspects which can influence the results, for a short introduction and discussion see for example, https://www.spe.org/dl/docs/2014/Trick.pdf but it's a...

RVAmeche, I prefer PRODE for these calc's but you can use another simulator as well, however, as library, Prode offers several advantages when working with Excel or similar applications (while a simulator is more suitable for solving complex plants).

rotw, I agree with you, I compared GERG 2008 and several EOS models with polytropic compression test cases provided by R.A.Huntington in 1985 (and 2017) papers, for CO2 Pin 75.85 Bara Tin 310 K Pout 413.7 Bara Tout 460 K Huntington 3 points model (included in Prode Properties) gives these...

yes, when required one should adopt GERG 2008 or other complex models.

I did some tests with the steady state column in Prode Properties to compare EOS models such as Peng-Robinson, Soave etc. (the Extended PRX-SRKX versions in Prode) with GERG 2008 model which should be more accurate on both vapor-liquid and enthalpy, for several separations (HC) I observe that...

Ok

actually I load BIPs for CPA from VLE database in Prode, however, calculated liquid-liquid fractions are different from our reference while vapor-liquid is Ok, what can I do for calculating the correct vapor-liquid and liquid-liquid fractions ?

does Prode Properties require the same BIPs for vapor-liquid and liquid-liquid phase equilibria with CPA Cubic Plus Association ?

thanks gaswell, the values calculated with MEG are close to GPA report but I have not experience including salts, ok, CPA electrolyte looks more suitable than Pitzer for this application.

we inject glycol as hydrate inhibitor in a natural gas stream which contains water + some salts (mainly Nacl), glycol dosage has been estimated averaging depression temperatures of MEG & salts (GPA), I have now Prode software, do you have expericence with CPA electrolyte or Pitzer models ? Can...

thanks, I suppose I should do that (i.e. choose the conservative approach) altough costs are a important factor for final decision.

problem : PSV sizing for two phase (vapor+liquid) flow for HC mixtures comment : I observe quite large differences 20/25% and more with different methods as HEM (API Omega) HEM (rigorous) HNE and HNE-DS, not sure which is the most accurate, In some cases HNE and HNE-DS return reduced areas...

thanks both for the comments! Latexman, yes compared with HEM the HNE-DS seems less conservative, supposing for example that vapor fraction is not constant the orifice may be undersized... to me this method seems much more critical with reference to process condition. PaoloPemi, yes I am aware...

I am evaluating the impact of HNE (ISO 4126) model over HEM (API Omega) for liquid and two-phase (vapor+liquid) flows, as I understand the HNE model predicts critical flows in excess of 200% and more over HEM model and that can signicantly reduce the size of orifices under certain conditions...