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34 3 Numerical methods be noticed that this simplified calculation approach for the recuperator effectiveness is based only on the use of temperatures and does not take into account the possible signif- icant changes in the heat capacity on the vapor side, which should be taken into account in a more detailed design of the recuperator. The enthalpy change in the feed pump can be defined as ∆hfp = v(pfp,out − pfp,in). ηfp The feed pump power is defined as P = q v(pfp,out − pfp,in). fp m,wf ηfp The temperature rise in the feed pump can be defined as ∆Tfp = (1 − ηfp)hfp,out − hfp,in . cp The net electric power from the system can be calculated as Pe,net = (Pt − Pfp)ηgm − Pmis, if the feed pump is located on a turbine shaft. (3.6) (3.7) (3.8) (3.9) The net electric efficiency of the ORC process was defined by dividing the net electric power output by the evaporator heat rate ηe,net = Pe,net . (3.10) φev The pressure losses between the turbine and condenser were estimated in the simulations presented in Chapter 5. The pressure loss was estimated based on the turbine outlet ve- locity and working fluid density at the turbine outlet. The pressure loss after the turbine depends mostly on the flow velocity. The pressure loss between the turbine outlet and the condenser is estimated by ∆ppl = 0.5ρt,outc2t,outCd. (3.11) The drag coefficient Cd in Equation 3.11, is estimated based on the experience gained from measurements in a larger-scale commercial ORC power plant. It should be noted that an accurate estimation for the pressure losses would require detailed information about the geometry of the components, pipeline lengths, and the size of the flow passages.PDF Image | WORKING FLUID SELECTION AND DESIGN OF SMALL-SCALE WASTE HEAT RECOVERY SYSTEMS BASED ON ORGANIC RANKINE CYCLES
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