Hi Siddarth

Thanks for your interest in our software. I'm always pleased to hear from chemical engineers who want to contribute, because I think that the experience with flowsheet modelling (Aspen etc) really help you to understand what the ASCEND software is all about.

The easier part of this project in FPROPS would be to add support for new fluid types. I would particularly welcome support for incompressible fluids, which would allow us to merge code like models/johnpye/moltensalt.a4c and models/johnpye/liquidsodium.a4c with our FPROPS code, allowing us to unify a range of models that make use of these properties. This should be a fairly straightforward exercise.

Next, I would suggest adding support for Soave-Redlich-Kwong (SRK, http://en.wikipedia.org/wiki/Redlich%E2%80%93Kwong_equation_of_state) or another related and commonly-used cubic equation of state. We already have Peng-Robinson, but the implementation of these cubic EOSs will be made cleaner once we attempt to add another cubic EOS as that will help us to identify the common and distinct aspects the are required in the architecture. For example, solving the phase equilbrium of a pure species for fixed (p,h) is probably essentially the same code for all cubic EOSs, but currently we don't have the architecture for that, and it needs to be developed.

We are very keen to make progress on calculating phase equilibrium. My understanding is that a suitable approach is to implement the calculation of fugacity, and then to implement external relations that return the residual (difference) in fugacity between the different phases, for each component. Then the ASCEND solver (QRSlv etc) can be given the task of iterating to get the phase equilibrium. However, I am a mechanical engineer, and it would be great if you could seek some advice on this question. Krishnan Chittur (CCed) may be able to help in the first instance. Krishnan has previously supervised other student projects with FPROPS.

Another approach, perhaps easier to test and encapsulate, would be to implement the entire phase equilbrium in external C code (ie in FPROPS), and not to leave any of the iteration to ASCEND to perform. This is probably less efficient at the system simulation level, but conceptually may be easier to implement.

Hope this helps,

Cheers
JP

On 08/03/15 06:13, Siddharth Pandey wrote:
Hello everyone,

My name is Siddharth Pandey, and am currently pursuing a Bachelor of Engineering [Hons] in/Chemical Engineering/at the Birla Institute of Technology and Science [BITS-Pilani], India. I am interested in contributing to ASCEND under the GSOC 2015 program.

I have setup ASCEND on my system for developing purposes. Having gone through the overview and the developer's manual, I decided next to identify the tentative project upon which I could work. I've decided to work upon the FPROPS library, extending to both/'new fluid types'/ and '/ideal //mixture support'./ I understand that this project aims at providing various calculations for ideal, incompressible fluids. Before I begin work upon the above topic, I would appreciate help from the mentors on the following :

1. Theories required for implementing the ideal mixture support; and further considerations for property calculations of non-ideal mixtures. 2. New fluid types under FPROPS; their equations of state and their implementation as data structures using C.

I have completed multiple courses in advanced thermodynamics, mass transfer and fluid mechanics under my curriculum and thus think that this project would be appropriate for my skill sets. I would like to add that I've worked with both C and Python extensively before.

It would greatly help my efforts if I could be guided along the above stated topics and through further details of the project itself.

Regards,
Siddharth Pandey

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