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still maintain the same temperature approach in the two evaporators and condensers. However, the overall area covered by these two rectangles is substantially greater than the for the single- stage cycle. It is possible to increase the number of stages to increase power yield from a given set of resources while maintaining a given set of approach temperatures. However, cost tradeoffs will limit the number of stages that can be economically used. Figure 1 Cycle temperature-entropy (T-S) diagram for a single and two-staged Carnot cycles (not to scale) While Figure 1 illustrates the principle for staging for Carnot cycles, the same arguments apply for the Rankine cycle as well. Baseline plant For the baseline plant, which was sized at a nominal 10 MWe net electrical power, we used a warm seawater flow rate of 50,000 kg/s and a cold seawater flow rate of 28,450 kg/s. Economic analyses indicate that because of the larger costs and pumping power requirements for the cold seawater, a proportionately higher flow rate of warm seawater is beneficial [Vega 1995]. Other assumptions, based on many prior design studies, made for the rest of the presented analyses are summarized in Table 1. Once again, since cold seawater is a more costly resource, the condenser minimum internal temperature approach (MITA) is set at 1oC as opposed to 1.2oC for the evaporator. Condenser and evaporator pressure losses are based on earlier studies. Overall system loss is consistent with a floating platform for the plant. 2PDF Image | Staging Rankine Cycles Using Ammonia for OTEC Power Production
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