4 replies to this topic

[B-2 Spirit]

Hello All,

I am working on a refinery expansion study.
I have the TBP curves of the crude feed.
How can I estimate the yield of various fractions such as LPG, Nahptha, kerosene, diesel and residue using TBP data?

I also have the plant data (i.e. ASTM D 86 curves ) of the produced cuts.
Can I validate the results my simulation (Base case - current operation) by using this data?


regards,
Alok

[ankur2061]

Alok,

There is an excellent description related to various cuts from atmospheric and vacuum distillation units based on the TBP curves of the crude in the following book:

Chapter 3 - The atmospheric and vacuum crude distillation units

"Handbook of Petroleum Processing" by David S.J. "Stan" Jones & Peter R. Pujado

Another good reference that could help you, is the book

"Refining Processes Handbook" by Surinder Parkash

Hope this helps.

Regards,
Ankur.

[Qzymandias]

Pick a cut to measure

Define a range for it i.e. 315oF to 450oF for Kerosene

Find the % at which 450oF crosses your curve

Subtract from that the % at which 315oF crosses your curve

Presto: that is the % of the crude you can expect to yield as that fraction.


Ozy

Edited by Qzymandias, 02 December 2011 - 08:44 AM.

[kkala]

Another source that can be useful is "Petroleum Refinery Engineering" by W. L. Nelson, 4rth edition, McGraw-Hill (1958). Chapter 4, Evaluation of Oil Stocks seems to be on the subject; yields of commercial products also depend on the specific processing applied by the refinery. Other Chapters may also be of interest. English units are used (rather a disadvantage today), contrary to most technical books from India.
My experience on simulators is quite limited and out of fractional distillation, so "experienced" guidance would be welcomed. Following was ear-caught.
1. You have to replace inlet crude by a representative mixture of pseudo components, real components (e.g. C3H8, etc) can be included.
2. TBP curve can be useful for (1), I do not know whether it is adequate (http://www.cheresour...0646-petroleum/). Simulator manual can clarify and give specific help.
3. ASTM D86 is non fractionating distillation curve, so it is not anticipated to be of help (Nelson, ibid, Distillation curves).
4. Simulation of whole operating refinery seems to be quite laborious as a task, e.g. over here a preheating train was once simulated, or even smaller areas. Awareness of plant operating conditions are also needed. Simplified simulation of a unit could be useful in giving insight, experience, verifying partial results, etc.

Edited by kkala, 02 December 2011 - 09:45 AM.

[B-2 Spirit]

Many thanks to all memebers who replied to my querry, the book by Pujada is really really helpful and so were your inputs.

thanks and regards,
Alok