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4-086-12 JUMEL ET AL 4. UNDERTAKING HIGH IMPACT ACTIONS: TECHNOLOGY AND ... at dead state is 20 °C. Condensation temperature is set at 30 °C. Hot air and cool water flow rate are sequentially 0.2 kg/s and 0.5 kg/s. Each component of these cycles was assumed to be adiabatic. The pressure drop and the heat loss in the pipes and the components of the cycle were neglected. The cycles work in steady flow conditions. The performance calculations and the cycle simulation were carried out by the Engineering Equation Solver (EES) (Klein 2012). The thermodynamic properties of the working fluid were calculated by the built-in functions of In the case without superheating, point 4’ will be removed and working fluid enters the turbine at vapour saturated state. Thus, equation (6) and (7) become: •••• Qin =QPreheat+QEvap =m(h4 −h2) (8) •••⎡• •⎤ I HTHEX = I Pr eheat + I Evap = T0 ⎢⎣mh (shso − shsi )+ m(s4(−9)s2 )⎥⎦ EESandtheinterfaceFluidProp-EESdeveloped•byTherm•ody- IHTHEX =IPreheat+IEvap =T⎢m(s −s )+m(s −s)⎥ (9) • ⎡ • • ⎤ namic Laboratory, University of Liege (Quoilin 2012). 0⎣hhso hsi 4 2⎦ Each component of system is considered to be a control vol- ume. The exergy destruction rate for a steady-flow process is calculated by equation (2). Heat received and exergy destruction rate of higher tempera- ture heat exchanger in supercritical cycle ⎛•⎞ ••⎜••Q⎟ •• Qin =m(h −h ) (2) •• 2,s1 η ••• W t = m(h − h )η = m(h − h(4))η η (without superheating) (13) (14) (15) WP =m(h2 −h1)= •• (4) 4 5 m,t (without superheating) 5,s s,t m,t ∑ ∑ ∑ I =T0 Sgen =T0⎜ ⎝⎠ struction rate is rewrote (3): ••⎛••⎞ IHTHEX =T0[mh(shso −shsi)+m(s3 −s2)] (11) Work created by vapour’s expansion and exergy destruction me s − e mi s − i Tkk ⎟ (2) For the case of an adiabatic process, the equation of exergy de- 32 (10) ••• I=T0Sgen=T0⎝ mese− misi⎠ (3) ⎜∑ ∑ ⎟ (3) The power input and exergy destruction rate of the pump are calculated by following equations for both of sub- and super- critical cycles (Equation 4 and 5). rate of turbine is calculated by equations below: Subcritical cycle ••• W t = m(h4' − h5 )ηm,t = m(h4' − h5,s )ηs,tηm,t (with su(1p2er)heating) • m(h −h) 5,s s,t m,t(without superheating) 4 5 m,t 4 5,s s,t m,t fluid from heat source can be imaginarily split into preheat- ing, evaporating and possibly superheating process (to avoid the condensation of working fluid during expansion process) illustrated in Figure 4. While, working fluid, in supercritical cycle, don’t pass two-phase region like in subcritical one. It is directly heated from point 2 to point 3 (Figure 5). Total heat received and exergy destruction rate are calculated by follow- ing equations: Subcritical cycle ••••• Qin =QPreheat+QEvap+Qsuperheat =m(h4' −h2) (6) It =m(s −s ))(withosutpseurpherahtienagti)ng) 5 4' ••••⎡••⎤ I HTHEX = I Pr eheat + I Evap + I superheat = T m (s (7−) s )+ m(s S−ubscr)itical cycle (7) 0⎢⎣hhso hsi 4' 2⎥⎦ ••⎡••⎤•••• IEvap+Isuperheat =T0⎢⎣mh(shso −shsi)+m(s4' −s2)⎥⎦ (7) Qout =QDesuperheat+QCond =m(h5 −h1) (16) 564 ECEEE 2012 SUMMER STUDY on EnERgY EffiCiEnCY in inDUSTRY ••• ••• (with superheating) Wt=m(h−h)η =m(h−h)ηη(withsuperheating) 4' 5 m,t 4' Wt=m(h−h)η =m(h−h)ηη s,p 4 (5) I t = m(s5 − s4' )(with superheating) IP =T0 m(s2 −s1) In subcritical cycle, the heat absorption process of working (5) •• • • (with superheating) •• I t = m(s5 − s4 ) (without superheating) (without superheating) Supercritical cycle ••• W t = m(h3 − h4 )ηm,t = m(h3 − h4,s )ηs,tηm,t •• It =m(s4 −s3) (6) Heat exchange and exergy destruction rate in lower tempera- ture heat exchanger: +PDF Image | Working Fluid selection and performance comparison of subcritical and supercritical organic Rankine cycle (ORC) for low temperature waste heat recovery
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