Supercritical Carbon Dioxide Cycle Analysis

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generator designs should consider the effect of steam pressure on the overall heat transfer area (and therefore cost) of the steam generator tubing. This cost is significant because, although busbar costs will be reduced as steam pressure and efficiency increase, the additional capital cost of a larger steam generator may be a outweigh any gains achieved through the improvement of efficiency. 5.7 Chapter Summary It is clear that the S-CO2 cycle has an efficiency benefit over the Rankine cycle in the temperature range considered here. The S-CO2 cycle achieves efficiencies about 1.0 % higher than the traditional Rankine cycle for comparably sized heat exchangers, either PCHE or Shell- and-tube. PCHEs suffer from higher intermediate and primary fluid pump work requirements, but are very compact. The intermediate loop pump work for all of these designs is small and the only pumping requirements that will be significant to overall efficiency are those of the primary pumps and that associated with intermediate piping pressure drops. The PCHE S-IHXs modeled here did not require the whole available space. In other words, the PCHE designs always approached a pinch point prior to the size reaching the maximum allowed dimensions. However, the heat transfer coefficients have not been thoroughly studied for PCHE geometries and improved PCHE codes should be developed to model them more accurately if more data become available. The limiting factor for most of the design options was the cycle choice, rather than the S-IHX. Consistent with Dostal’s findings [Dostal, 2004], the S-CO2 cycle is slightly better than the Rankine cycle above a turbine inlet temperature of about 485 oC. For the lowest turbine inlet temperatures achieved, the cycles’ efficiencies are within 0.15 % of each other. When heat exchanger options raise the turbine inlet temperature higher, however, the S-CO2 cycle efficiency exceeds that of the Rankine cycle. The highest efficiencies are achieved with a S-CO2 cycle coupled to a shell-and-tube heat exchanger linked to primary sodium in a loop-type design, i.e. there is no intermediate loop present. The CO2 shell-and-tube S-IHX must incorporate enhanced tubes, however, as smooth tubes do not provide the heat transfer coefficient required. Rankine cycles and S-CO2 recompression cycles perform comparably at a core outlet temperature below 510 oC. At 510 oC, the S-CO2 cycle and the supercritical water cycle achieve comparable efficiencies which are, on the whole, a slight improvement over the traditional Rankine cycle. Clear differences in cycle efficiency become evident if the core outlet temperature reaches 530 oC when the S-CO2 cycle has a clear efficiency advantage. Eliminating the intermediate loop is only practical for loop-type designs. Eliminating the intermediate loop, though effective in increasing efficiency, has safety implications, and there are other options for increasing efficiency almost as much without the safety issues. If the loop 119

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