When friends and colleagues ask me what the CHEMCAD technical support group does, the best answer I have is: "We help chemical engineers address their challenges." This runs the gamut from simple to hard problems, and might include pushing for changes in CHEMCAD itself. One challenge we resolved was how to model some very non-ideal LLE systems in CHEMCAD.

The binary system of 1-propoxy 2-propanol and water has unusual behavior. There is both an upper and a lower critical solution temperature to the liquid-liquid region. Modeling this type of system in CHEMCAD proved to be quite a challenge.

What do we mean by upper and lower critical solution temperatures? As you increase temperature, you can form a second liquid phase. Keep increasing temperature, and the two liquid phases will coalesce back into a single liquid phase. A phase diagram for this behavior shows a closed ovoid.

If you wanted to model this, you would start by asking the following questions:

- Can CHEMCAD model liquid-liquid separation?

- Can CHEMCAD model this unusual liquid-liquid behavior?

- How do we (as users and engineers) inspect and adjust the simulator's model results for this problem?

You can use CHEMCAD to model a heterogeneous azeotrope—that is, a system where two liquid phases separate from each other. You can plot binary LLE diagrams, or the ternary 'binodal plot' that many of us remember from college.

For this simulation, we chose the NRTL K-value model. The NRTL model enables you to calculate γi from binary interaction parameters (BIPs). You can use γi to solve yi P = γi xi pisat. Normally this is used to calculate vapor-liquid equilibrium (Ki=yi/xi), but an optional modification to NRTL enables it to model liquid-liquid equilibrium. It's important to note that using NRTL with LLE will predict a second liquid phase only if the BIPs (from the CHEMCAD database or your work) will result in LLE.

It’s always wise to check what a K-value model is calculating, because sometimes you might need to adjust the settings for the model you’re using. One set of BIPs doesn't necessarily cover all conditions; the mathematical models aren't powerful enough to handle "all phenomena" with a single set of parameters.

In this case, using the Plot > Binary LLE and Plot > TPXY commands in CHEMCAD showed that the NRTL model did not match experimental data for the liquid-liquid separation.

To address this, we tried to quickly regress new BIPs from the literature data (Thermophysical > Regress BIPs). Regressing the LLE data did give us marginally better results, but we could not match the 'closed circle' seen in the experimental data for this unusual system.

Next, we decided to calculate the activity coefficient of each data point, and then regress a multi-parameter BIP from the activity coefficients. The results are shown below:

CHEMCAD now fits the experimental data quite well! We are now able to show the effects of having both an upper and a lower critical solution temperature. Using a sensitivity study and a flash unit makes it possible to move into (and back out of) the LLE region on a flowsheet.

## Tuesday, October 13, 2009

Subscribe to:
Post Comments (Atom)

David,

ReplyDeleteI briefly searched the site for your contact information, but was unsuccessful. So I'm hoping this tactic of posting a comment will reach you.

My name is David Disciascio; I am a new chemical engineer for Westinghouse Electric. I have recently encountered a slightly similar problem with CHEMCAD: I have found that the know data for the solubility of MIBK in water and vice versa does not match previous known experimental data by a co-worker. I have tried to solve this problem by regress the BIPs with the experimental data, although to no success. I am using the NRTL K value model in thermodynamic settings; with vapor/liquid/liquid/solid global phase setting selected. The new CHEMCAD results are closer, but still off by a factor of three! (closest) Do you have any suggestions to fixing the problem?

-Dave D

Dpd18

ReplyDeleteWelcome in! For questions like this, it's best to contact technical support at 1800CHEMCAD (press option 2), or via email at support @ chemstations.com

When you're doing the regression, be sure to checkmark the option which is labeled something like "use three phase algorithm for TPXY regression."

When you are shown the initial bip estimates (B12, B21, Alpha, A12, A21) you will notice that we only give initial bounds and values for B12,B21, and alpha. You could give initial values and bounds of -100 to 100 for the other two bips to let CHEMCAD try a 5 parameter regression.

If you're still having trouble...I would encourage you to contact technical support, and we will help you sort it out.

Can we do Sulfolane extraction of Aromates with CHEMCAD?

ReplyDeleteSulfolane extraction of Aromatics can surely be Simulated in Chemcad. You will need to regress some of BIPs. Just few data points are good enough for the missing pairs...

ReplyDeletehi, I want to ask one thing.. When I use pump on chemcad I see it give me negative value, do you know why?

ReplyDeletecan we increase the number of inputs to any unit operation in chemcad? (for eg. can we give two feed streams to a single cyclone seperator)?????....if so, how to do it???

ReplyDelete