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Condenser Q_c1⁄4m_rðh2h4Þ ð8Þ _ h4 h2 Ic1⁄4T0m_r ðs4s2Þ T ð9Þ L Refrigerant pump W_ rp 1⁄4 m_ rðh5s h4Þ=grp 1⁄4 m_ rðh5 h4Þ ð10Þ I_rp 1⁄4T0m_rðs5 s4Þ ð11Þ Thermal efficiency is defined as follows: g1⁄4ðW_ W_ Þ=Q_ ð12Þ I t rp h 2.2.2. Economical modeling It is desirable to use total electricity cost as the objective func- tion in the optimum design. But there is no much precise informa- tion about the current capital cost of the organic Rankine cycle power plant. However, it can be considered that the total cost of the heat exchangers (evaporator/vapor generator and condenser) contributes largely to the total ORC system cost in a low-tempera- ture geothermal power plant and is assumed to be representative of the complete system cost [1]. This is reasonable because 80– 90% of the system capital cost is assigned on the heat exchangers [42–44]. Two economic indicators are put forward by previous research and both are analyzed in the optimization procedure in this study. Firstly, the economic performance of the power plant is opti- mized using the criterion of APR given in Refs. [1,43], in which the ratio of total heat transfer area to total net power is considered to be the objective function. APR 1⁄4 Atot=W_ net ð21Þ where Atot is the total heat exchanger area of the system. Secondly, the levelized energy cost (LEC) [28–29,44], which is the ratio of the system cost to total net power output, is also used in the optimization process. The capital cost of each heat exchanger is determined by the fol- lowing general correlation [26,45]: lgCp 1⁄4 K1 þ K2lgA þ K3ðlgAÞ2 ð22Þ lgFp 1⁄4 C1 þ C2lgP þ C3ðlgPÞ2 ð23Þ CBM 1⁄4 CpFBM 1⁄4 CpðB1 þ B2FMFPÞ ð24Þ CCpl;1996 1⁄4 CBM;e þ CBM;c ð25Þ CCpl 1⁄4 CCpl;1996 CEPCI2008 =CEPCI1996 ð26Þ In this equation, Cp is the basic cost of the equipment assuming ambient operating pressure and carbon steel construction in the year of 1996. A fixed head shell and tube vapor generator in cast steel and a fixed head shell and tube condenser in stainless steel are chosen and the operating pressure of both heat exchanger are much higher than the ambient pressure. So the basic cost is cor- rected for the chosen material and for the working pressures by Eq. (23). CBM is the corrected cost. Then the cost of power plant is further converted from 1996 costs to 2008 costs by using Chemical Engineering Plant Cost Index(CEPCI) values, which is published in the Chemical Engineering Journal and allows adjusting process plant construction costs from one period to another. The Bi System total irreversibility: I_tot 1⁄4XIj 1⁄4Ih þIc þIt þIrp 1⁄4T0m_r h1 h5 h4 h2 ð13Þ Second law efficiency: gII 1⁄4g1=ð1T0=THÞ ð14Þ Recovery efficiency: gr 1⁄4 W_ net=W_ max ð15Þ W_ max is the maximum theoretical power produced by a Carnot en- gine operating between the heat source inlet temperature and ambient temperatures. W_ max 1⁄4 m_ w;hCp;wðth;wi t0Þð1 T0=Th;wiÞ ð16Þ Exergy destruction factor (EDF) Net power output of the system can be given: W_ wp;h 1⁄4 m_ h;wDPw=ðqw;hgwpÞ ð18Þ W_ wp;c 1⁄4 m_ c;wDPw=ðqw;cgwpÞ ð19Þ W_ net 1⁄4W_ t W_ rp W_ wp;h W_ wp;c ð20Þ where the W_ wp;h and W_ wp;c are the water pump input power in heat transfer fluid circulation and W_ net is the net power output of the ORC system. j THTL __ EDFcomponent 1⁄4 Icomponent=Wnet ð17Þ Z. Shengjun et al. / Applied Energy 88 (2011) 2740–2754 2743 Fig. 2. T–S diagram of the subcritical ORC and transcritical Rankine cycle. (a) T–S diagram of the subcritical ORC, (b) T–S diagram of the transcritical Rankine cycle. (a) (b)PDF Image | Performance comparison and parametric optimization of subcritical Organic Rankine Cycle (ORC) and transcritical power cycle system for low-temperature geothermal power generation
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