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ðĖð ðĄ =SteammassflowrateofHRSG hð 2= Enthalpy of steam after the evaporator hðððð= Enthalpy at approach point temperature ðĄð2 can be calculated by using equation 15, mĖ cĖ ïŋ―t -t ïŋ―=mĖ ïŋ―h -h ïŋ― gas p g2 g3 st s2 appr h =enthalpyofsaturatedsteamat17bar hð 2 = 4.18x (196.3) = 820.7 ðððð 90x1.05 (ðĄð2-222.6) =3.727x (2795-820.7) ðĄð2=300.5oC Heat balance over super heater: mĖ cïŋ― ïŋ―t -t ïŋ―=mĖ (h -h )................................................................................(16) gasp g1 g2 st sh s2 ðĖ ððð = Flue gas mass flow rate from six diesel engines ððĖ = specific heat of flue gas ðĄð1= Flue gas input temperature to HRSG ðĄð2= Flue gas temperature after economizer ðĖð ðĄ =SteammassflowrateofHRSG hð h = Enthalpy of super heated steam hð 2= Enthalpy of steam after the evaporator For optimization pinch point temperature should fall between 8 0C and 160C. It is apparent that when the optimization is done with the pinch point temperature close to 80C the power output from HRSG is higher but the large scale size and high cost makes it uneconomical. On the other hand when the pinch point temperature gets closer to 160C the power output of HRSG gets limited. Above calculation indicate that exhaust gas out from HRSG is 194.4 oC. This means we can recover more energy. Therefore, in order to investigate the attainable maximum possible power output with steam temperature at 2800C and 17 bar, the following trial runs were carried out using EES. 29PDF Image | waste heat recovery steam power system for ACE Embilipitiya
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