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CHE 304

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Che 304 lab sheet
  1 CHE 304 Chemical Engineering Laboratory-III (Heat Transfer & Unit Operation) LIST OF EXPERIMENTS Experiment #1 Study of Double Pipe Heat Exchanger Experiment #2 Study of Steam Condensation on a Single Vertical Tube Experiment #3 Study of Shell and Tube Heat Exchanger Experiment #4 Study of Single Effect Evaporator Experiment #5 Study of Pressure in Masses of Particles Experiment #6 Study of Constant Pressure Filtration Experiment #7 i) Investigation of Liquid-Solid and Gas-Solid Fluidized bed. ii) Investigation of 2D and 3D Gas-Solid Fluidized beds Experiment #8 Study of Crushing and Grinding SCHEDULE FOR LEVEL-3, TERM-2 Group Week 1 2 3 4 5 6 7 8 9 10 11 12 1 INTRODUCTION 1 2 3 4 5 6 7 8 BOARDVIVA QUIZ 2 2 3 4 5 6 7 8 1 3 3 4 5 6 7 8 1 2 4 4 5 6 7 8 1 2 3 5 5 6 7 8 1 2 3 4 6 6 7 8 1 2 3 4 5  2 EXPERIMENT #1   STUDY OF HEAT TRANSFER COEFFICIENT IN A DOUBLE PIPE HEAT EXCHANGER 1.   OBJECTIVES a)   To obtain individual and overall heat transfer coefficients.  b)   To study the variation of heat transfer coefficient with Reynolds number (Re) and fluid velocity (v). c) To compare experimental and estimated heat transfer coefficients. 2.   EXPERIMENTAL SECTION 2.1   Double Pipe Heat Exchanger Heat exchangers are devices that facilitate the exchange of heat between two fluids that are at different temperatures while keeping them from mixing with each other. Heat transfer in a double pipe heat exchanger usually involves convection in each fluid and conduction through the wall separating the two fluids. (a) (b) Figure 1: (a) Schematic diagram of a double pipe heat exchanger and (b) Temperature profile of a double pipe heat exchanger.  3 The rate of heat transfer between the two fluids at a location in a heat exchanger depends on the magnitude of the temperature difference at that location, which varies along the heat exchanger. 2.2   Experimental Set-up Tube length = 7' 4'' Inner tube: Nominal diameter =1'' Schedule 40 2.3   Experimental Procedure 1   Set the thermometers in proper places and record the necessary data for this experimental system. 2   Pass water through the inner pipe. 3   Allow steam to flow through the annulus. Valve opening will determine the steam  pressure at the inlet. This is shown on the pressure gauge. 4   Fix the pressure at a convenient value and record the inlet and outlet water temperature. Also note the amount of water and condensate collected for a known interval of time. Keeping the steam pressure fixed, obtain all readings for different water flow rates. 5   Repeat step 4 for different steam pressures. 6   Enter the results in the table shown below. 2.1   Data Sheet Preparation Table 1: Observed data Steam pressure No. of obs. Water temperature Water Condensate P (psig) Inlet (T 1 ) (Unit) Outlet (T 2 ) (Unit) Weight (Unit) Time (Unit) Weight (Unit) Time (Unit)  4 3.   REPORT WRITING 3.1 Calculations Mass flow rate of water M w  = W w /t Mass flow rate of condensate M c  = W c /t Rate of heat taken up by water Q w  = M w C  p (T 2 - T 1 ) Rate of heat given up by steam Q c  = M c    s  Mean rate of heat flow Q m  = (Q w +Q c )/2 Saturation temperature of steam, T s , heat of vaporization,  s  Temperature difference at inlet,  T 1 =T s -T 1  Temperature difference at outlet,  T 2  = T s -T 2  Log mean temperature difference, )/ln( 21211 T T T T T  m   Outside area available for heat transfer, A o  Exptl. Overall heat transfer coefficient, U OE = omm  AT Q 1   Mean temperature of water, T m  = (T 1 +T 2 )/2 Tube wall temperature on steam side, T w = (T s +T M )/2 Water side heat transfer coefficient for turbulent flow using Dittus-Boelter euation h i = 0.023 3/18.0 (Pr)(Re) im  Dk   Film temperature, T F =T s    –  0.75(T s -T w ) Steam side heat transfer coefficient  Nusselt equation for film type condensation h o =0.725 4/1023 )(        f  w s s f   f   T T  D g k   (Laminar flow) The parameters  f   k  ,  f    , and  f     are to be evaluated at T F  . Overall heat transfer coefficient is estimated by U OT = 111 1       lm M oW oo  Dk  D xh D Dh  
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