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Still no answers... I can't use other software because the company I work for doesn't have them. Yes one company makes both but they have a different setup, as I mentioned before. Yes, the same EOS gives different results using the same assays, temperatures and pressures.

To compare the differences, I invite you to try identical hydrocarbon flashes with both programs. I've done it and the difference is significant. Next! Can I get any decent tips here?

It seems like the only advantage that Aspen Plus offers over Hysys is the ability to handle some (trace) solids...which is a negligible feature as far as I'm concerned. I heard that Hysys is better than Aspen Plus because Hysys does not truncate the binary coefficients. Therefore Hysys is much...

after a control valve where there is gas or liquid flashing to gas, you typically swage up to the required line size. having the RO on the bigger line size puts backpressure on the smaller line size-keeping the flow from going sonic in the smaller line size.

what's the difference between aspen one and hysys for hydrocarbon seperation simulations? i heard something about differences in binary coefficients. why is hysys and pro 2 the benchmark for refineries and why is aspen one not?

Suncor's engineers are top shelf. The reason for a minimum flow recirc is to keep the pump from damage when the discharge flow falls below the minimum flow specified by the pump vendor. The minimum flow is not only crucial for turndown conditions, but it's also good for the standby pump when...

no no, the CV is a few meters away from the vessel but not far. I figure the vortex breaker is needed for the valve for the same reasons as a pump, to keep the entrained vapours out.

I was involved in the startup of LPG storage vessels and we nitrogen purged the system before startup. Be sure to specify the nitrogen supply temperature for purging to the supplier. It arrives in liquid form. Ambient is good enough. The operator who will be purging the vessel should be wearing...

For vessels or tanks that have an outlet on the side, near the bottom tangent, isn't there still a possibility of vortexing when the liquid level is low-even if the liquid leaves from the side? Wouldn't a vortex breaker be good for an application where there isn't a pump, but a control valve on...

what is the velocity in the suction pipe? Does the suction pipe have at least 5 diameters of straight run (bigger line size) to the pump and a reducer right at the pump suction nozzle?

I agree that vortexing may be the culprit. Does the vessel have a vortex breaker at the pump nozzle?

I have used KORF on my last project and I really liked using it. However, for this thread the subject is flow regime, rather than pressure drop. The slug tool and flow regime maps are contradicting eachother. Right now I'm in the midst of a voting method where I look at the slug tool result...

After some extensive research and keeping in mind the correlations available in Hysis pipe segment calcs, it's clear that the best correlation to use for horizontal pipe is Gregory, Aziz and Mandhame. For horizontal pipe or angled pipe, Beggs and Brill is good too. For vertical pipe, Orkiszewski...

I'm using Hysis version 2006.5 and it appears that there's some contradictory calculations regarding slug flow. Using the slug calculation/prediction tool, it shows stable two phase flow. Great news! However, double checking with the flow regime map using beggs/brill or Aziz (horizontal pipe)...

I'm running hysis and I need a license for OLGA. I've been told that Beggs/Brill is good enough for two phase HC. I doubt it.

what's a good flow correlation for 2 phase? beggs/brill?

Maybe an internal ring manifold for the feed to the tank would help to keep the bottom agitated. If not, then a mechanical agitator-nothing wrong with that. The inlet and outlet should be 90 or 180 degrees from eachother. I wouldn't bother with settling time calcs. I'd just recommend the...

Normally I design gas lines for a velocity <30 m/s.

Amen. I even try to explain this to folks who have 20-30 years of experience and they look at me like a deer on the highway. This one revamp had the main process fluid going into two heat exchangers in series as two phase in and out and then a trim steam heater. I placed a backpressure control...

So why the hell do so many engineers design heat exchangers for 2 phase flow when it could easily be avoided and you end up with a smaller HX and better heat transfer?