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INNOVA2 FUNDED PROJECTS Figure 91 provides examples of the sort of experimental data acquired. It shows on the left the condensation of isopropanol on three stacked finned tubes made from stainless steel; on the right it depicts the operational be- haviour of a natural circulation evaporator made from pillow plates. In the left-hand panel, one sees the increase in the heat transfer coefficient for con- densation on the finned tubes relative to the value calculated on the basis of Nusselt’s theory for the equivalent smooth tube device. The finned tubes re- sult in a heat transfer coefficient some 3.5 to 4 times greater than that achiev- able with a conventional heat exchanger tubes. It is also apparent that the heat transfer coefficient decreases on moving from the first (uppermost) row in the stack to the third (lowest) row. This observed decrease in heat trans- fer is known as the inundation effect, but it is significantly less pronounced than would be seen in an equivalent bank of smooth tubes. The reason for this is the improved drainage of the condensate from the fins compared with drainage from a smooth surface. The condensate dripping down from the upper tube drains away more rapidly, causing only a minor increase, if any, in the thickness of the condensate layer on the tube below. The right-hand panel in Figure 91 presents a comparison of the operating window for a natural circulation evaporator using pillow plates and one for a standard smooth tube bundle evaporator for water at pabs = 200 mbar. Characteristic operating parameters include the apparent liquid level, i.e. the liquid level in the associated vapour condenser relative to tube length or plate height, and the temperature differential that drives heat transfer be- tween the heating side and the condensing side. In heat integration schemes, the magnitude of the temperature difference is determined by the process. The effectiveness of a heat integration scheme is higher the smaller the temperature difference required between the heat-releasing side (the heat source) and the heat-receiving side (the sink). As can be seen in Figure 91, the entire operating window for the pillow plate device is significantly larger than that for the tube bundle. At high apparent liquid levels, the required driving temperature difference in the pillow plate device is only about 60% of that in the tube bundle. This means that heat integration initiatives be- come feasible at driving temperature differences that would be too small if conventional tube bundle equipment were to be used. Similar results were found in the studies of evaporation on finned tubes, condensation in pillow plate condensers and for the multi-stream plate condenser. The computational approaches derived from the experimental data follow the established concept of using performance indices to facilitate calcula- tion of the heat transfer coefficients for the different heat exchanger designs. It was also demonstrated that by suitable transformation, a pillow-plate or finned tube device can be reduced to an equivalent configuration involving cylindrical smooth tubes, which allows the computational methods men- 215PDF Image | Chemical Processes and Use of CO2
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