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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