1. Analysis of Flow Boiling
P M V Subbarao
Professor
Mechanical Engineering Department
Selection of Optimal Parameters for Healthy and Safe Furnace Walls…..

2. Plant Efficiency & Market Structural Change
1970’s Efficiency

3. Modern Measure of Performance

4. Efficiency improvements in coal-fired generation

5. Electricity generating costs in selected regions

6. Phases in Flow Boiling

7. Flow of steam-water mixture
Relatively cold water enters at the bottom of the riser tubes.
The temperature of the water is slightly below the saturation temperature : Sub-cooled liquid.
The lower most section is called as economizer.
This portion of the furnace will receive enough heat to evaporate the water in the immediate neighborhood of the wall.
The bubbles condense owing to the sub-cooled water around it.
This process is known as sub-cooled boiling.
There is no steam generation in this process.
As the water is heated close to its saturation temperature the steam bubbles will not collapse and move up through the water as bubbles.
This is called nucleate boiling.
The heat transfer coefficient is very high.
This bubbly type of flow continues till the steam fraction in the mixture is low.

8. Boiling Map

9. Historical trend of furnace heat release rates for coal-fired boilers

10. Towards Matured & Sustainable SC Technology

11. Departure from Nucleate Boiling and Critical Heat Flux
In practice, if the heat flux is increased, the transition from nucleate boiling to film boiling occurs suddenly, and the temperature difference increases rapidly.
The  point  of  transition  from  nucleate  boiling  to  film  
boiling  is  called  the  point  of departure from nucleate boiling, commonly written as DNB.  
The heat flux associated with DNB is  commonly  called  the  critical  heat  flux  (CHF).    
CHF  is  an  important parameter.  

12. An increase in heat flux beyond the critical heat flux leads to the occurrence of DNB.
The  temperature  difference  required  for heat transfer from the tube surface to boiling fluid increases  greatly.    
The temperature increase causes the TUBE to exceed its design limits, a failure will occur.
The amount of heat transfer by convection can only be determined after the local heat transfer coefficient  is  determined.   
Such  determination  must  be  based  on  available  experimental  data.
Experimental data is to be correlated by dimensional analysis.
An   equation   for   the   HTC curve is drawn using the correlation.

13. Flow Boiling
Flow boiling occurs when all the phases are in bulk flow together in a channel; e.g., vapor and liquid flow in a pipe.
The multiphase flow may be classified as adiabatic or diabatic, i.e., without or with heat addition at the channel wall.
Void fraction and Pressure drop are two important parameters in real flow boiling.

14. Adiabatic Flow Through A Pipe

15. Diabatic Flow Through A Pipe

16. Selection of Flow rate in Flow Boiling
This process may either be forced convection or gravity driven.
At relatively low flow rates at sufficient wall superheats, bubble nucleation at the wall occurs such that nucleate boiling is present within the liquid film.
At high qualities and mass flow rates, the flow regime is normally annular.
As the flow velocity increases, convection in the liquid film is augmented.
The wall is cooled below the minimum wall superheat necessary to sustain nucleation.
Nucleate boiling may thus be suppressed, in which case heat transfer is only by convection through the liquid film and evaporation occurs only at its interface.