Dear Art Montemayor,
Happy easter. I have followed your instruction about the steps and also about getting the kerns book. I do have the book and i have read it. I have gone through example in the book as you have recommended. The section you recommended was for single vapour. So i went through the mixed vapour section rather than single vapour as i have mixed gases going into the condenser. The examples in the book did mention about iterating to derive the bubble point and dew point in order to get the weighted change in temperature, which until then i cannot calculate my Heat duty and follow the condenser design through. Another issue is the fact that i cannot find Antoine coefficient for the gases and temperature am dealing with. I have tried perry's and all its mentioning is about hydrocarbon's. I am confused on how to get the vapour pressure of each gas in the mixture, vapour pressure of each pure component (gas), mole fraction of the liquid as that cannot be calculated without the vapour pressures. Most of the books i read had a data for K-value for each component which is in graphical form. All text books including kern only had for hydrocarbons which is different from mine.
I am also not sure of the method am using for this design which is the one you recommended. Most books including Kern talked about examples of vapour coming from a distillation column which is very common in the oil industries but in my own case its a Nuclear plant where waste gases are coming from 2 furnaces. I have attached the excel sheet of what i have done but am stuck as i cannot calculate the vapour pressures and K values.
The double pipe condenser is very near to the end of the ventilation system on the
plant. The only thing between the outlet of the condenser and the
ventilation fan will be a HEPA filter. The fan will typically pull a vacuum
of about 35mbar and a HEPA filter will have a dP of about 25mbar. So the exit on the condenser will be at -10mbar g. Given the remaining 10mbar
will have to drive the whole ventilation system right back to the
dissolver, so therefore, I would not have a dP > 5mbar across the vapour side.
Please have a look at the labelled spread sheet 1. The sheet 2 were the values for K, Fz and etc i derived before correcting the mass balance (at the bottom of sheet 2, titled Furnace condenser). As soon as the mass balance was corrected i could not derive the vapour pressures and X values.