Cheat drivers ed. Counter strike 1.6. Calculation; we can ignore this in our calculations since we consider the overall air-side resistance to be constant for all of our calculations). The resistance of the heat exchanger tube is a function of the thickness of the tube s, the conductivity of the tube k, and the mean cross 2. Exactly the design value (eg. 20℃) when the condenser performance test carried on. Neither was the cooling wa-ter volume flow. The heat transfer coefficient correction equation was as follows: K. C (13) D v T. Whistling vivaldi pdf free. V F V (14) Table 1. The calculation of condenser cleanliness coefficient.
CONDENSER DESIGN Condensation on horizontal tubes (Nusselt theory) Heat transfer coefficient is obtained by h=0.728[kL3 ϸL(ϸL- ϸV)g ƛ /µL (Tv –TW) D] Where kL – thermal conductivity of liquid ϸL – density of liquid ϸV –density of vapour ƛ – latent heat of condensation of steam g- Gravitational acceleration =9.81m/s2 µL – viscosity of liquid TW – temperature of surface Tv –temperature of vapour D –diameter The above eqn applies for a single tube or single row of tubes. When tubes are stacked over each other the heat coefficient is calculated as H=h NR-1/6 Nr- no of rows of horizontal tubes
As the properties(kL, ϸL, µL) of the condensate changes with the temperature ,so some modifications are being done to compensate for that . Tf =βTw +(1- β)Tsat Where β-weight factor (recommended in the literature from 0.5 to 0.75) Condensate sub cooling The temp in the condensate film drops from Tsat at the liquid vapour interface to Tw at the wall. Therefore the avg condensate temperature, TL is less than Tsat, and hence the condensate leaving the surface is sub cooled. Accounting for sub cooling, the rate of heat transfer is Q=W ƛ +WCp,L (Tsat - TL)= Whfg*
Cp,L heat capacity of condensate W- condensation rate to account for both sub cooling and inertial effects h/hNu =(1+(0.683 -0.228 PrL-1)Ԑ)^0.25 hNu - heat transfer coeff by basic nusselt theory Ԑ- Cp,L (Tsat - Tw)/ƛ PrL - Cp,L µL/ kL above eqn is valid for Pr>0.6 Q=NhD0L∏(Tsat - Tw) Tw=…………… Then Tf can be obtained by the eqn given above Mass flow rate of water =ϸAu U –flow velocity A of tube can be calculated from the above eqn And the total area= N∏DL And the condensation rate –Q/hfg* Some FACTS to remember
In drop wise condensation Heat transfer coefficient is considerably high as compared to film condensation. The reason being the direct contact of vapor with the cooler surface. The effectiveness of a condenser can be calculated as (1 - eNTU) NTU=(UA/Cmin) Cmin=(mCp)min
References –process heat transfer principles and applications by ROBERT W SERTH Heat and mass transfer –cengel and ghajar
As the properties(kL, ϸL, µL) of the condensate changes with the temperature ,so some modifications are being done to compensate for that . Tf =βTw +(1- β)Tsat Where β-weight factor (recommended in the literature from 0.5 to 0.75) Condensate sub cooling The temp in the condensate film drops from Tsat at the liquid vapour interface to Tw at the wall. Therefore the avg condensate temperature, TL is less than Tsat, and hence the condensate leaving the surface is sub cooled. Accounting for sub cooling, the rate of heat transfer is Q=W ƛ +WCp,L (Tsat - TL)= Whfg*
Cp,L heat capacity of condensate W- condensation rate to account for both sub cooling and inertial effects h/hNu =(1+(0.683 -0.228 PrL-1)Ԑ)^0.25 hNu - heat transfer coeff by basic nusselt theory Ԑ- Cp,L (Tsat - Tw)/ƛ PrL - Cp,L µL/ kL above eqn is valid for Pr>0.6 Q=NhD0L∏(Tsat - Tw) Tw=…………… Then Tf can be obtained by the eqn given above Mass flow rate of water =ϸAu U –flow velocity A of tube can be calculated from the above eqn And the total area= N∏DL And the condensation rate –Q/hfg* Some FACTS to remember
In drop wise condensation Heat transfer coefficient is considerably high as compared to film condensation. The reason being the direct contact of vapor with the cooler surface. The effectiveness of a condenser can be calculated as (1 - eNTU) NTU=(UA/Cmin) Cmin=(mCp)min
References –process heat transfer principles and applications by ROBERT W SERTH Heat and mass transfer –cengel and ghajar
PROCESS DESIGN OF SHELL AND TUBE HEAT EXCHANGER, CONDENSER AND REBOILERS. Calculation of heat transfer co-efficient. Type of heat exchanger and design pressure. Downloads lagu opick taubat. The optimum thermal design of a shell and tube heat exchanger involves the. Tube heat exchangers calculations it is very important to remember some. Sandhya namam lyrics in malayalam pdf software. Tower Design Free Online eBook Collection at: www.pdftop.com/ebook/tower+design. Thermal design calculations of Shell & Tube condensers for horizontal condensers, vertical condensers including reflux condensers; main features: +Support S.I. Naruto shippuden torrent english dub all episodes.
Condenser Design Calculation Pdf Reader Free
CONDENSER DESIGN Condensation on horizontal tubes (Nusselt theory) Heat transfer coefficient is obtained by h=0.728[kL3 ϸL(ϸL- ϸV)g ƛ /µL (Tv –TW) D] Where kL – thermal conductivity of liquid ϸL – density of liquid ϸV –density of vapour ƛ – latent heat of condensation of steam g- Gravitational acceleration =9.81m/s2 µL – viscosity of liquid TW – temperature of surface Tv –temperature of vapour D –diameter The above eqn applies for a single tube or single row of tubes. When tubes are stacked over each other the heat coefficient is calculated as H=h NR-1/6 Nr- no of rows of horizontal tubes
As the properties(kL, ϸL, µL) of the condensate changes with the temperature ,so some modifications are being done to compensate for that . Tf =βTw +(1- β)Tsat Where β-weight factor (recommended in the literature from 0.5 to 0.75) Condensate sub cooling The temp in the condensate film drops from Tsat at the liquid vapour interface to Tw at the wall. Therefore the avg condensate temperature, TL is less than Tsat, and hence the condensate leaving the surface is sub cooled. Accounting for sub cooling, the rate of heat transfer is Q=W ƛ +WCp,L (Tsat - TL)= Whfg*
Cp,L heat capacity of condensate W- condensation rate to account for both sub cooling and inertial effects h/hNu =(1+(0.683 -0.228 PrL-1)Ԑ)^0.25 hNu - heat transfer coeff by basic nusselt theory Ԑ- Cp,L (Tsat - Tw)/ƛ PrL - Cp,L µL/ kL above eqn is valid for Pr>0.6 Q=NhD0L∏(Tsat - Tw) Tw=…………… Then Tf can be obtained by the eqn given above Mass flow rate of water =ϸAu U –flow velocity A of tube can be calculated from the above eqn And the total area= N∏DL And the condensation rate –Q/hfg* Some FACTS to remember
In drop wise condensation Heat transfer coefficient is considerably high as compared to film condensation. The reason being the direct contact of vapor with the cooler surface. The effectiveness of a condenser can be calculated as (1 - eNTU) NTU=(UA/Cmin) Cmin=(mCp)min
References –process heat transfer principles and applications by ROBERT W SERTH Heat and mass transfer –cengel and ghajar
As the properties(kL, ϸL, µL) of the condensate changes with the temperature ,so some modifications are being done to compensate for that . Tf =βTw +(1- β)Tsat Where β-weight factor (recommended in the literature from 0.5 to 0.75) Condensate sub cooling The temp in the condensate film drops from Tsat at the liquid vapour interface to Tw at the wall. Therefore the avg condensate temperature, TL is less than Tsat, and hence the condensate leaving the surface is sub cooled. Accounting for sub cooling, the rate of heat transfer is Q=W ƛ +WCp,L (Tsat - TL)= Whfg*
Cp,L heat capacity of condensate W- condensation rate to account for both sub cooling and inertial effects h/hNu =(1+(0.683 -0.228 PrL-1)Ԑ)^0.25 hNu - heat transfer coeff by basic nusselt theory Ԑ- Cp,L (Tsat - Tw)/ƛ PrL - Cp,L µL/ kL above eqn is valid for Pr>0.6 Q=NhD0L∏(Tsat - Tw) Tw=…………… Then Tf can be obtained by the eqn given above Mass flow rate of water =ϸAu U –flow velocity A of tube can be calculated from the above eqn And the total area= N∏DL And the condensation rate –Q/hfg* Some FACTS to remember
In drop wise condensation Heat transfer coefficient is considerably high as compared to film condensation. The reason being the direct contact of vapor with the cooler surface. The effectiveness of a condenser can be calculated as (1 - eNTU) NTU=(UA/Cmin) Cmin=(mCp)min
References –process heat transfer principles and applications by ROBERT W SERTH Heat and mass transfer –cengel and ghajar
Condenser Design Calculation Pdf Reader File
PROCESS DESIGN OF SHELL AND TUBE HEAT EXCHANGER, CONDENSER AND REBOILERS. Calculation of heat transfer co-efficient. Type of heat exchanger and design pressure. Nimbus controller windows 10. Downloads lagu opick taubat. The optimum thermal design of a shell and tube heat exchanger involves the. Tube heat exchangers calculations it is very important to remember some. Sandhya namam lyrics in malayalam pdf software. Tower Design Free Online eBook Collection at: www.pdftop.com/ebook/tower+design. Indesign cs4 free for mac. Thermal design calculations of Shell & Tube condensers for horizontal condensers, vertical condensers including reflux condensers; main features: +Support S.I.