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34 Chapter 3 Heat exchanger design and construction two streams of the same fluid, Cmin=CmQX' and with negligible longitudinal conduction, the temperature vs. length profiles of both streams will be necessarily identical though slightly shifted, ie. the temperature difference between the hot stream and the cold stream, Th,rTc,o, is constant over the length of the heat exchanger (Kays and London[71,p34]). The heat transferred is given by U A ( T h , i - T c ) = C ( T c , o - T c ) = C ( T h , i - T h) ( 3 . 2 5 ) Mtu, the number of transfer units for each temperature increment, then becomes 3.5.2 Pressure drop 3.5.3 General approach to the sizing problem i1Ntu- (Tc,o-TJln = T .-T h,1 C,O I1T T .-T (3.26) The core pressUre drop IS derived from the relation gIven by Kays and London[71,p36] . nG2 08 11P=-(4J-+k +k) 2p d c e (3.27) For matrix surfaces the entrance and exit effect is usually included in the friction factor then referred to as the equivalent friction factor or drag coefficient, wherein the drag coefficient is defined as 81 (3.28) 'f:.=2J-+-(k +k) ':l d 2 c e The required effectiveness of the heat exchanger is the starting point for the sizing problem. For a user specified geometry the total surface area required and hence the volume, number ofplates and pressure drop can be calculated using equations (3.22), (3.26) and (3.27). The schematic approach to this sizing procedure is shown in Table 3.2. Temperature dependant fluid properties are read in from a file and interpolated if necessary. A listing of the source code is given in appendix A. 3.6 Matrix heat exchanger - construction Several methods for construction of MHE's have been used since they were first made in 1950 by McMahon et al.[70]. Venkatarathnam and Sarangi's excellent review[72] of matrix heat exchangers covers the various methods and hence these are h,1 c,oPDF Image | CO2 removal from air for alkaline fuel cells operating with liquid H2
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