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
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. Photoshop cs2 on windows 10.
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Sl no Condenser Heat addition Items Mkcals/hr 1 Heat added by main steam 330.76 2 Heat added CRH 38.703 Total 369.463 HEAT ADDED BY MAIN STEAM Main steam flow = 514.75 T/hr (Since main steam flow is inclusive of Attemperation flow, separate Attemperation quantity is not taken into account in heat load calculation) Steam pressure: 98.1 kg/cm2.g.
Feb 27, 2019 Air Cooled Condenser Design Spreadsheet - Download as Excel Spreadsheet (.xls), PDF File (.pdf). Condenser Design Shell and Tube Condenser Design (CnD) is a software that is made to demonstrate thermal analysis and design calculations required for designing shell and tube condensers. This software can design, horizontal shell side condensers.
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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. V F V (14) Table 1. The calculation of condenser cleanliness coefficient.