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Preheater Evaporator Superheater 5 Condenser 6 TABLE I: BASIC DATA FOR THE WORKING FLUIDS International Journal of Materials, Mechanics and Manufacturing, Vol. 1, No. 1, February 2013 Heat source 4 TH Turbine greater than the others so the whole temperature-entropy diagram for NH3 is not shown in the figure [12]. G Substance M(kg/kmol) NH3 17.031 Tc(K) Pc(bar) 405.65 112.78 380.00 36.90 369.30 49.71 408.14 36.48 386.60 44.99 346.25 37.58 425.18 37.97 460.43 33.81 469.65 33.69 0.252 0.239 0.219 0.177 0.263 0.253 0.199 0.228 0.249 3 Internal heat exchanger 2 Pump 1 TL R134a R22 iC4H10 R152a R143a C4H10 iC5H12 nC5H12 102.031 86.468 58.123 66.051 84.041 58.123 72.150 72.150 200 Fig. 1. Schematic diagram of the system. P RT a(T) vb v(vb)c(vb) R2T2 a(T) a c (T) Pc (1) (2) A low-grade sensible energy is supplied to the system and important assumptions used in this work are as follows. 1) The energy source is air at temperature of TS. 2) The working fluid leaves the condenser as saturated liquid at temperature of TL. 3) The evaporating temperature, TE is lower than the critical temperature of the fluid and the turbine inlet temperate becomes TS - ∆TH by the superheater. 4) The minimum temperature difference between the hot and cold streams in the regenerator is operated at a prescribed pinch point, ∆TPP. 5) Pressure drop and heat loss of the system are negligible. At point 1, the fluid is saturated liquid at T and the L corresponding saturated pressure PL is the low pressure of the system. When the turbine inlet pressure is PH, the corresponding saturation temperature TE is the evaporation temperature of the system. The thermodynamic properties at point 4 are determined with the temperature TH and the pressure PH. The thermodynamic properties at points 2 and 5 are determined with the isentropic efficiencies of pump and turbine, ηp and ηt, respectively. As the mass flow rate of working fluid for a given energy source increases, the temperature of source flow at preheater exit decreases, and finally the temperature difference between the source and the working fluid reaches the pinch point value ∆TPP when the mass flow rate of working fluid is increased to its maximum value. Then the ratio of mass flow rate of a working fluid to that of the source, rm, can be determined as RT bc (3) bP c RT cc (4) cP c 1NH3 89 2 R134a 3 R22 150 4 iso-C4H10 5 R152a 6 R143a 7 C4H10 100 8 iso-C5H12 9 n-C5H12 7 50 0 0.0 0.5 2 35 6 Entropy [kJ/kgK] 4 1.5 1 2.0 Temperature [oC] Fig. 2. Temperature-entropy diagrams of working fluids. (5) Ts,out T3 TPP (6) 1.0 rmmwf cpsTsTs,out m s h 4 h 3 The basic data of the fluids which are needed to calculate Patel-Teja equation are shown in TABLE I, where M, Tc, Pc and ω are molecular weight, critical temperature, critical pressure, and accentric factor, respectively [14]. The molecular weights of NH3 and iC4H10 are small, and those of R123 and C8H12 are large among the fluids. The critical temperatures of R143a and R22 are low and those of nC5H12 and iC5H12 are high. The critical pressures of nC5H12 and iC5H12 are low and those of NH3 and R22 are high. The temperature-entropy diagrams for the fluids are shown in Fig. 2.ItcanbeseenfromthefigurethatiCH ,CH ,iCH where subscripts wf and s denote the working fluid and the source fluid, respectively, and m the mass flow rate, T the temperature, h the specific enthalpy, cps the constant pressure specific heat of source fluid, and ∆TPP the pinch point temperature difference of the heat exchanger. 410 410 512 and nC5H12 belong to dry fluids, R134a and R143a to isentropic fluids, and NH3, R22 and R152a to wet fluids. Especially, the latent heat of vaporization of NH3 is much The rate of heat input and net work are obtained as Q m h h in wf 4 3 W W W m h h h h net t p wf 4 5 2 1 ( 7 ) ( 8 ) 42PDF Image | Exergy Analysis of Organic Rankine Cycle with Internal
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