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U. Drescher, D. Bru ̈ggemann / Applied Thermal Engineering 27 (2007) 223–228 225 Fig. 2. T ; H_ – diagram for the standard (a) and an improved (b) plant design for an ORC without superheating (state 5 and 6 are equal). PP = pinch point. The small difference between states 1 and 2 is neglected in the diagrams. Fig. 3. Typical T, S-diagram for ORC with superheating. order to avoid the constriction of the pinch point at state 4 (Fig. 2(b)). This design allows to consider also fluids with high vaporization enthalpy at maximum process tempera- ture. Therefore, the suggested plant design simplifies fluid selection. Now thermal efficiency can be used for fluid eval- uation instead of total heat recovery efficiency. 3. Methods We developed a calculation method which needs follow- ing basic data for each substance: • molecular weight, • critical temperature, • critical pressure, • acentric factor, • melting point, • autoignition temperature, • vapor pressure of the liquid, • heat of vaporization, • heat capacity of the liquid, • heat capacity of ideal gas. These thermodynamic properties have been extracted from the database of the Design Institute for Physical Properties (DIPPR) [8,9] which includes nearly 1800 sub- stances. The calculation method has to cover the range from liquid phase to superheated gas (Fig. 3). Specific enthalpy difference h3 h2 is the recovered heat provided by the recuperator using h7 h8. The difference h6 h1 is input enthalpy, h7 h6 gained work wturbine and h8 h1 waste heat which may be used for space heating. State 6 can be in the gas phase or on the dew line (then state 5 equals state 6). The maximum temperature Tmax is the turbine inlet temperature (state 6) and the minimum temperature Tmin is the condenser temperature (state 1 and 9). The states 1, 2, 3, 4, 5 and 9 are calculated directly from the DIPPR database. In the case of minimum process pres- sure below 0.1 MPa, states 7s, 7 and 8 are calculated from state 9 using ideal gas heat capacity. Otherwise, these states as well as state 6 are obtained from an isothermal change of state starting from the 0.1 MPa – isobar using Peng–Rob- inson–EOS [10,11]. The thermal efficiency g is defined by g1⁄4h6 h7 jwpumpj ð1Þ h6 h3 with the feed pump work 1 Zpmax wpump1⁄4g vdp ð2Þ pump pmin Feed pump work is calculated neglecting the fluid com- pressibility which influences enthalpy only marginally. The efficiency of the internal heat exchanger is gihe 1⁄4 h3 h2 ð3Þ h7 h8 and turbine efficiency is given by h6 h7 gturbine 1⁄4 h h ð4Þ 6 7s In order to validate the calculation procedure, a compari- son with the software Fluidcal [12] which is based on an analysis by Lemmon et al. [13] was carried out for toluenePDF Image | Fluid selection for the Organic Rankine Cycle (ORC) in biomass
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