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T [C] 200 150 100 50 0 -50 T [°C] R142b 4-086-12 JUMEL ET AL 4. UNDERTAKING HIGH IMPACT ACTIONS: TECHNOLOGY AND ... 2.50E6 Pa 840 000 Pa 170000 P a 1 6000 Pa 0.2 0.4 0.6 0.8 Ammonia 1.500E7 Pa 1.000 E7 Pa 5.000E6 Pa 150 125 100 75 50 25 0 -25 -50 -75 hII hth I tot I HTHEX I LTHEX It IP Itot hII IHTHEX hth ILTHEX I t IP h 0.4 0.36 0.32 0.28 0.24 0.2 0.16 0.12 0.08 0.04 s [J/kg-K] Figure 8. Configuration of subcritical cycle using Ammonia (left) and R141b (right). h 2100 0.5 s [J/kg-K] I [W] 3500 3000 2500 2000 1500 1000 500 0 -100 0 1000 2000 3000 4000 5000 6000 7000 8000 500 750 1000 1250 1500 1750 2000 2250 2500 1800 1500 1200 900 600 300 0 0.45 0.4 0.35 0.3 0.25 0.2 0.15 0.1 0.05 0 Figure 9. Evolution of exergy destruction rate and second law efficiency in subcritical cycle (left) and supercritical (right) with different working fluids. In Figure 9, we can observe the evolution of total irrevers- ibility rate and of each component of the cycles. The exergy destruction in higher temperature heat exchanger contributes to the most important part in total exergy destruction. There- fore, curve appearance of iHTHEX is similar to one of itot. For the different fluids, exergy destruction rate in lower temperature heat exchanger and in the turbine stays approximately at the same value, while this is relatively different in higher tempera- ture heat exchanger. Pump exergy destruction has the lowest value of all exergy destructions. Second law efficiency grows up with the increase of thermal efficiency and the decrease of total exergy destruction rate. In Figure 10, we find that evaporating temperature, in sub- critical case, and higher pressure, in supercritical case, strongly influence on thermal efficiency. Thermal efficiency is remark- ably improved at higher evaporating temperature and higher pressure. This effect is also observed for second law efficiency because heat was being added to working fluid at higher aver- age temperature in these cases. The result is a reduction in the rate of entropy generation and an increase in the efficiency of the cycle. In Table 3, the results of the comparison between the sub- critical cycle and the supercritical one using R245fa are encap- sulated. A higher pressure Ph = 1.03Pcrit is applied for super- critical cycle. While, two evaporating temperatures at 140 °C and 150 °C were used in case of subcritical cycle to investigate cycle performance. Inlet turbine temperature and net power are consecutively set at 160 °C and 1 kW for three operating con- ditions. Back work ratio (bwr), which is defined as the power consumed by the cycle to the gross power produced by the cy- cle, and the quotient of the higher pressure to the lower one, tP, are also studied for two cycles. They are calculated by the equation (24) and (25). Wt tP = Ph/Pcond (for supercritical cycle) (25) or Pevap/Pcond (for subcritical cycle) According to these results, supercritical configuration presents numerous advantages such as lower exergy destruction, higher thermal and second law efficiency, less heat exchanger effec- tiveness required. In other hand, some drawbacks are observed for supercritical cycle, i.e. higher energy consumption, higher 566 ECEEE 2012 SUMMER STUDY on EnERgY EffiCiEnCY in inDUSTRY ⎛••⎞ ⎜Wt+WP,water ⎟ bwr=⎝ ⎠• (24) I [W] r125 r143a R1234yf r32 R227ea Propane R134a R1234ze R22 R236fa R124 R152a isobutane R142b Butane R245fa 0.0033 R227ea R1234yf Propane R1234ze R134a R236fa R124 isobutane R22 Butane R245fa R142b R152a R245ca n-Pentane R123 R141b ammoniaPDF 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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