EXPERIMENTAL ANALYSIS OF HEAT AND MASS TRANSFER IN A PACKED BED. Suryapet , India, Warangal , India
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1 Journal of Mechanical Engineering and Sciences (JMES) e-issn: ; Volume 1, pp , December 011 FKM, Universiti Malaysia ahang EXERIMENTL NLYSIS OF HET ND MSS TRNSFER IN KED BED K. V. Suryanarayana 1, G. Srinivasa Rao, D. M. Reddy rasad 3, K. V. Sharma 4 and. K. Sarma 1 1 Department of hemical Engineering, Sri Venkateswara Engineering ollege, Suryapet 50813, India, kagita_surya@yahoo.com Department of Mechanical Engineering, Kakatiya Institute of Technology and Science, Warangal , India 3 Faculty of hemical Engineering, Universiti Malaysia ahang, 6300 Gambang, Kuantan, ahang, Malaysia 4 Faculty of Mechanical Engineering, Universiti Malaysia ahang, Kuantan, ahang 5 International Director, GITM University, Visakhapatnam , India BSTRT Experiments have been conducted to study the effect of mass flow rate on heat and mass transfer coefficients in a packed bed. It has been observed that an increase in mass flow rate of water increases the heat and mass transfer coefficients by and times respectively at The diffusion of oxygen from packed bed inlet water obtained from experimental data can be used to estimate the mass transfer coefficients.the theoretical equation available in literature is compared and satisfactory agreement has been observed. The increase in inlet water temperature decreases both the heat and mass transfer coefficients by 60% and 5% due to the reduced driving force. The increase in oxygen concentration in inlet water has no significant effect on both heat and mass transfer coefficients. Keywords: acked bed, ondensation heat transfer coefficients, Diffusion mass transfer coefficients, Oxygen INTRODUTION Boiler feed water may contain significant amounts of dissolved oxygen, which causes pitting and iron deposition. acked beds are used to remove these dissolved and corrosive gases from boiler makeup feed water. The makeup water and the condensate are heated in the packed bed for removal of oxygen before entry into the boiler as even small amounts of dissolved gas can cause significant corrosion. The high temperature of boiler feed water will further increase the corrosivity due to dissolved oxygen, if left untreated. In packed bed, the incoming water falls on the top of the bed, the length of the this bed is 1. m and packed with 38 mm nominal size pall rings made of nylon. The bed is engulfed with steam at a pressure. Experiments are conducted at different flow rates, pressures and temperatures of packed bed water. Rapas et al. (1987) presented the experimental data on mass transfer coefficients of counter flow pall-ring packed bed. The authors have taken the data from full size packed bed operating at desalination plants, checked the mass transfer performance of two inch pall-ring packing and spray nozzle distribution system. The effects of antifoam and the stripping steam flow rate on the effluent oxygen concentration are not 14
2 Experimental analysis of heat and mass transfer in packed bed considered. Ferro et al. (00) observed oxygen concentration to decrease with increase in temperature of seawater at inlet of packed bed. osta et al. (006) observed the performance of the oxygen stripping of the packed bed when the steam flow rate is low. They concluded that maximum oxygen content in the outlet water to be 0 30 ppb even in the absence of steam. Heat and mass transfer studies with non-condensable gas such as oxygen getting stripped from boiler feed water is quite limited. Hence, it is proposed to conduct experiments to estimate the heat and mass transfer coefficients from packed bed at different mass flows rates, temperatures and its impact on oxygen stripping from the boiler feed water. FBRITION OF THE EXERIMENTL SETU The experimental setup consists of 0.15m dia column, and 1.m length of packed bed. 00 liters feed water storage tank, a steam jacket on the deaerator water inlet pipe for regulating its temperature and a pump for circulating water are other accessories. In the steam circuit a pressure regulator and steam trap are connected to a buffer tank for removal of water droplets after steam expansion in the pressure regulator. water bath of 5 liters capacity with a copper coil to regulate the temperature of sample water to 0-40 º connected to Dissolved Oxygen (DO) meter and condenser for increasing the temperature of inlet water are provided. The schematic diagram of the experimental setup is shown in Figure 1. Top packing retainer Vent Steam in ondenser DLR all ring acking L ondensate out Steam from RDS Buffer Tank Steam trap Bottom packing retainer Water Storage Tank DO Meter Water outlet Water inlet ump Water Bath DLR: Dome Loaded ressure Regulator; DO: Dissolved Oxygen Meter Figure 1. Schematic diagram of packed bed experimental set-up Estimation of Heat Transfer oefficients The energy balance equation for the packed bed can be estimated from the relation Q E L o i m T T (1) 15
3 Suryanarayana et al. / Journal of Mechanical Engineering and Sciences 1(011) Heat transfer coefficient is estimated using Q E and log mean temperature difference as the driving force in the packed bed QE h () T Estimation of Mass Transfer oefficients LN The mass transfer is governed by the rate equation given by J k, x (3) where L p LN xln is the log mean concentration difference and expressed as ( xi x ) ( ), i x x, 0, o, xln (4) ln ( x x ) ( x x ) i, i, Rabas et al.(1987) have calculated the equilibrium concentration of oxygen in water at the inlet and outlet of packed bed with the following equations ( D / H ) xi, 1 K M / M M / M ( s T / H ) / x (5) e N W o, p, i o, F fg i y M x (6) o, D H M V Equations (4) (6) are substituted in Eq. (3) to obtain an equation for mass transfer coefficient as V x x i, o, k (7) L, p x LN nother expression for determination of mass transfer coefficient has been given by osta. et al. (006) ' NTU LM L kl, (8) a L where NTU LM xi, ln. x o, The mass transfer coefficients are evaluated using Eqs. (7) and (8) which are applicable to packed beds. RESULTS ND DISUSSION The increase in mass flow rate of packed bed water increases heat transfer coefficients in the packed bed as shown in Figure. The rate of increase is more at inlet water temperature of 55 0 compared to 95 0 due to higher temperature potential between steam and water. 16
4 Experimental analysis of heat and mass transfer in packed bed Figure : Effect of mass flow rate of packed bed water on condensation heat transfer coefficient for two different inlet water temperatures The variation of experimental Nusselt number with Reynolds number is shown in Figure 3 along with the data of Kuznetsov et al. (1993) that has been done for upward gas-liquid flow in a tube filled with spheres. Experimental data with upward steam and downward water flow is not available in literature. The trend of the present experimental data for different inlet water temperatures is satisfactory when compared. The condensation heat transfer coefficient has no significant influence with inlet water Oxygen concentration as shown in Figure 5 Figure 3: omparison of present data with that of Kuznetsov et al. (1993) with porous systems and packing 17
5 Suryanarayana et al. / Journal of Mechanical Engineering and Sciences 1(011) The variation of condensation heat transfer coefficient with packed bed pressure is shown in Figure 4. The condensation heat transfer coefficient increases with increase in packed bed pressure at lower temperatures due to higher driving force between steam and water and remains constant at higher temperatures. Figure 4: Effect of pressure of packed bed on condensation heat transfer coefficient for two different inlet water temperatures Figure 5: Effect of Oxygen concentration in inlet water on condensation heat transfer coefficient for two different inlet water temperatures 18
6 Experimental analysis of heat and mass transfer in packed bed The increasing trends of mass transfer coefficient at different inlet water temperatures are shown in Figure 6. The increase in mass flow rate of water is similar to increase in heat transfer coefficients as can be seen from a comparison with Figure. The mass transfer coefficient has no significant influence with packed bed pressure as shown in Figure 7. The mass transfer coefficient has no significant influence with inlet water Oxygen concentration as shown in Figure 8. Figure 6: Effect of mass flow rate of packed bed water on mass transfer coefficient for two different inlet water temperatures Figure 7: Effect of pressure of packed bed on mass transfer coefficient for two different inlet water temperatures 19
7 Suryanarayana et al. / Journal of Mechanical Engineering and Sciences 1(011) Figure 8: Effect of Oxygen concentration in inlet water on mass transfer coefficient for two different inlet water temperatures ONLUSIONS The following conclusions can be drawn from the present analysis: a) The increase in mass flow rate of water in a packed bed increases the heat transfer coefficients. The values of heat transfer coefficient are in the range of W/m K for the experimental range tested. b) The increase in flow rate of water in packed bed increases the mass transfer coefficients c) The mass transfer coefficient in the packed bed estimated with the theoretical equation of osta et al. (006) is in good agreement with the present experimental values d) The increase in packed bed pressure increases the both heat and mass transfer coefficients by 5% and 1% at lower temperature and remains constant at higher temperatures e) The increase in inlet water temperature decreases the both heat and mass transfer coefficients due to decrease in driving force f) The increase in oxygen concentration of inlet water has no significant effect on both heat and mass transfer coefficients KNOWLEDGEMENT The financial support by the Universiti Malaysia ahang and DJR ollege of Engineering and Technology, Vijayawada, India are gratefully acknowledged. 130
8 Experimental analysis of heat and mass transfer in packed bed REFERENES Rabas, T.J., Inoue, S. and Shimizu, n update on the mass transfer of counter flow, packed deaerators containing pall-ring packing, Desalination 66,pp Ferro, E., Ghiazza, E., Bosio, B., and osta,. 00. Modeling of flash and stripping phenomena in deaerators for seawater desalination, Desalination 14,pp osta,., Ferro,., Ghiazza, E. and Bosio, B Seawater deaeration at very low steam flow rates in the stripping section, Desalination 01,pp Kuznetsov, V.V., and Dimov, S.V The influence of the geometrical parameters of a porous medium on two-phase filtration, 4 th Symp. Multiphase Transport in orous Media: rpc. SME Winter nnual Meeting, Nov. 7 30, pp Nomenclature a packing area per unit volume, m / m 3 surface area for heat transfer, m area of cross section for packed bed, specific heat, J kg K D diameter of the tank, m T F temperature drop or flashing at packing inlet, 0.3 to T LN log mean temperature difference, ( T T ) ( T T )] ln[( T T ) ( T T )] m [ S i S o S i S o W / m h heat transfer coefficient, K H Henry s law constant, N / m / ppb H latent heat of condensation, J / kg fg J molar flux of component, kg mol / m s k thermal conductivity of water, W / mk K ratio of oxygen to nitrogen mass at packing inlet ( 1.75) e k L mass transfer coefficient, m / s L length, m ' L superficial mass velocity of flowing liquid, kg / m s M molecular weight, kg / kg mol m mass flow rate of water, kg s NTU Lm number of liquid phase transfer units for mass transfer Nu Nusselt number, hd k Q heat transfer, W Re Reynolds number, 4 m D s mass flow rate ratio of stripping steam to the inlet water T temperature, K V volumetric flow rate of water into the deaerator, m 3 s x mole fraction of O in water 131
9 Suryanarayana et al. / Journal of Mechanical Engineering and Sciences 1(011) x equilibrium mole fraction of O in water y mole fraction of O in steam V Velocity of liquid, m s Greek symbols viscosity of water, kg m s Subscripts oxygen or non-condensable gas V average E energy balance i inlet L liquid N nitrogen o outlet packed bed V water vapor W water 13
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