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</html>";s:4:"text";s:6760:"Hence, it must be emphasized that the local heattransfer coefficients at specific points needed in the Simpson method of integration mustfirst be corrected for the local velocity and temperature profile distortions by the propertyratio method and then used as local h values for the integration. Rev., Vol. Make appropriateidealizations and find the new length of the exchanger as:(a) 2 m (b) 3 m (c) 4 m (d) 5 m (e) can’t tell3.47 A 2-ton window air-conditioner needs to remove 8.4 kW of heat from its con- denser. 1, the counterflow exchanger effectiveness \" from Eq. 4.8, isdqconv: dqconv ¼ hP dx ðT À T1Þ ¼ hP dx ð4:77ÞHence, the total convective heat transfer rate qconv from the constant cross section fin,excluding the heat exchanged from the tip (to be included later), is found by integrating, 264 ADDITIONAL CONSIDERATIONS FOR THERMAL DESIGN OF RECUPERATORS T(x) T(x) dT = 0 T(x)T∞ T∞ dx T∞ ᐉ δ Insulated qe= he Ak(Tᐉ – T∞)xᐉ xᐉ xᐉ ᐉ/δ ∞ qx = ᐉ = –kf Ak dT = 0 qx = ᐉ = –kf Ak dT = qe (a) dx ᐉ dx ᐉ (b) (c)x qᐉ x Tᐉ (d) ᐉ (e) ᐉFIGURE 4.10 Five boundary conditions at x ¼ ‘ for the thin-fin problem: (a) very long fin; (b)adiabatic fin tip, (c) convection at the fin tip; (d) finite heat leakage at the fin tip, (e) temperaturespecified at the fin tip.this equation from x ¼ 0 to x ¼ ‘. (4.28) and re-arranging yields q ¼ U~A ÁTm ¼UA ÁTm ð4:33ÞThus, an overall heat transfer coefficient U which takes into account both the tempera-ture ðU~Þ and length effects () is given by U¼1 ð A UmðTÞ f ðx; yÞ dA ¼ U~ ð4:34ÞAs noted before, f ðx; yÞ ¼ f ðx*1 ; x*2 Þ is a pure position function. In industry, heat exchanger design and analysis calculations are performed almostexclusively using commercial and/or proprietary computer software. 1. Assume a negligible change in the specific heat of oil in the temperature range 110 to 1708C. 5.3 Heat Exchanger Design Methods The goal of heat exchanger design is to relate the inlet and outlet temperatures, the overall heat transfer coefficient, and the geometry of the heat exchanger, to the rate of heat transfer between the two fluids. Often, the changes ofheat transfer coefficients are not linear and the values calculated for the mean overall heattransfer coefficient determined using various approaches may be substantially different(Shah and Sekulic´ , 1998). For most heatexchangers, except liquid metal heat exchangers, Pe and x* are higher than the valuesindicated above. Arrange the following design alter- natives from higher to lower effectiveness P1. 4.7b is shown inFig. As discussed for Eq. The common trend in all three temperature distributions is that thetemperature gradient in the fin decreases continuously with increasing x when the finconvects heat to the ambient (T > T1). 4.10a on page 264, the fin is very longcompared to its thickness (‘= ! RQ3.26a and b represent the temperature profiles in twodifferent counterflow exchangers having the same cold fluids and the same coldfluid flow rate in each exchanger. Now consider that we use the same counterflow ÁTlm definition for aparallelflow exchanger [i.e., Eq. If thespecific heat is constant, the enthalpies can be replaced by temperatures in Eq.(4.42). In this figure, (a) sketch the variation of wall temperature with position (neglecting wall resis- tance) when ðhAÞh ) ðhAÞc. (4.29) with Uðx; T Þ instead of UðT Þ or ^ UUmðTÞ. The location of zero heattransfer rate in the axial direction of fin then can be determined where the temperaturegradient in the fin ðd=dxÞ ¼ 0. No such extension is available in the MTDmethod. What would the values be if the thermal resistance of the wall is neglected?3.4 Explain the physical reasoning why \" ¼ 1 À eÀNTU for all flow arrangements when C* ¼ 0.3.5 (a) For a typical counterflow heat exchanger, explain briefly the change in the effectiveness as the flow rate of the cold fluid is decreased slowly from some initial value to near zero. (4.50), as 1 1 1 2 1 1 1 U~ ¼ 6 120:1 W=m2 Á K þ 3 314:0 W=m2 Á K þ 6 393:6 W=m2 Á K ¼ 3:934 Â 10À3 m2 Á K=WSince the thermal entry length is negligible for liquids and zero for condensing steam, ¼ 0. Make a plot of this crossflow exchanger effectiveness as a function of the number of passes. 1-1 Counter-Current heat exchanger from Example #1 designed with 25% excess heat transfer area (UA=196,000 Btu/hr oF) Assume only sensible heat effects •C2+ NGL feed heat capacity –0.704 Btu/lb F In this method, notonly the variations in individual h’s due to the temperature effect are taken intoaccount, but the specific heat cp is considered temperature dependent. Consider cp for air and water as 1.01 and 4.19 kJ/kg Á K, respectively. However, if wecan come up with some reasonably accurate value of the overall U after approximately. To avoid possible confusion, we refer to f as the fin efficiencyand \" as the fin effectiveness. However, when it varies significantly as in a cryogenic heatexchanger, the third point calculated for the Cmax and Cmin fluid by Eq. Consider a counter- flow exchanger with crossflow headers as a three-pass exchanger (Fig. ";s:7:"keyword";s:41:"fundamentals of heat exchanger design pdf";s:5:"links";s:5183:"<a href="http://digiprint.coding.al/site/page.php?tag=41e064-coconut-palm-sugar">Coconut Palm Sugar</a>,
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