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divided into several types based on their means for heat transfer augmentation: fins, plates, matrices etc. In our case the cycle requires three different heat exchangers: the high and low temperature recuperators and the precooler. The high temperature recuperator is the simplest one to design since it operates far from the critical point in the region where the change of the fluid properties is not very significant. The performance calculations can be done using the mean logarithmic temperature difference or the ε - NTU method [Kays and London, 1984]. The low temperature recuperator operates closer to the critical point and the change of fluid properties significantly affects its temperature difference. When proceeding from the hot inlet, the temperature difference at first increases then reaches its maximum and starts to decrease, ending at about the same value at the cold end as at the hot end. This behavior is caused by the variation of specific heat. Thus the heat exchanger size cannot be evaluated by the simple mean logarithmic temperature difference or ε - NTU method. Instead, the heat exchanger has to be split into several axial nodes and every node has to be evaluated based on the node mean temperature difference. This should also capture the variation of the heat transfer coefficient due to the variation of fluid transport properties. Once developed, this method can be used for the high temperature recuperator as well, in order to obtain more accurate values of heat transfer coefficients. The last heat exchanger in the cycle is the precooler. This heat exchanger has a different medium on each side: the hot side is CO2 the cold side is water. This heat exchanger operates close to the CO2 critical point since it cools the CO2 that leaves the low temperature recuperator to the compressor inlet temperature, which is only about one degree centigrade above the critical temperature. For certain cycle pressure ratios the pressure is very close to the critical pressure. If the precooler operates close to the critical point it takes advantage of improved heat transfer coefficients around the critical point as shown in Figure 9.1, where the normalized heat transfer coefficient (at a velocity of 5 m/s, hydraulic diameter of 0.015 m and pressure of 7.5 MPa) is plotted. It was normalized to the CO2 heat transfer coefficient at 66oC (~ 3000 W/m2K) in order to 202PDF Image | Supercritical Carbon Dioxide Cycle for Next Generation Nuclear Reactors
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