1. As I showed in message #8: the UOP-K factor of Pakistani crude 44 oAPI is about 12.0
For liquid products see my message #2
2. Stricktly speaking, yes, but that will be small compared to exchanger duties. Moreover there will be heat loss through the insulation of the column, exchangers, piping, so if you really want to drive yourself crazy you should also include that....
Serious: don't overdue accuracy, or you will waste too much time (that you don't have anymore) with details.
3. The overhead vapor from the column going to the condensor is not only hydrocarbon vapor but also includes steam. The hydrocarbon vapors will have a UOP-K of about 13 because it is mainly Light Naphtha. For the steam part use steam data.
However: Note that absolute value of enthalpy has no meaning, only enthalpy difference has. So I don't see how you can do a proper heat balance over the columns only. Frankly I don't see the point of that either.
And how are you going to handle the partly vaporized crude entering the column? You don't know how much vapor and how much liquid is present there.
Earlier I thought you were doing a heat balance over the whole CDU, but now .....
Edited by PingPong, 07 February 2014 - 02:15 PM.