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ME 415 Energy Systems Design Tutorial

ME 415 Energy Systems Design Tutorial. This is a classic thermal systems design course. It is application intensive and covers flow in pipes and piping systems, pumps and pumping systems, heat exchangers and heat exchanger design, and thermal system simulation. Course Material.

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ME 415 Energy Systems Design Tutorial

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  1. ME 415 Energy Systems Design Tutorial

  2. This is a classic thermal systems design course. It is application intensive and covers flow in pipes and piping systems, pumps and pumping systems, heat exchangers and heat exchanger design, and thermal system simulation. Course Material

  3. The ME 415 Add-In offers several unique ‘user-defined’ functions for application of course material in the Excel environment. As a result, students are able to solve complex problems through elimination of cumbersome hand calculations or reading of charts and graphs. Application through Excel

  4. These ‘user-defined’ functions are utilized in the Excel Spreadsheet. • The functions can be invoked by several methods. • Call directly from the cell • Requires known function name and argument constraints (specific units, range sizes, etc.) • Call from the user ribbon (Excel 2007) • Provides function descriptions and input boxes Application through excel

  5. This method requires the user to highlight desired cell(s) for output and type =‘Function Name(Arg1,Arg2,…)’ • For example, we desire to know the Nusselt number for turbulent flow in a tube. Direct Cell call method This method requires knowing what arguments the function needs to compute the desired output. Direct cell call method becomes useful when user has gained experience with a specific function or group of functions.

  6. This method uses the ‘user ribbon’ and the ‘Insert –Function’ button located at the top of the Excel 2007 window. • Advantages of this method are function lists and descriptions that provide details on each argument’s requirements . • Highlight cell(s) for desired output and select the formulas tab on the user-ribbon as seen on following slide. • Then click either ‘Insert-Function’ button User Ribbon call method

  7. From the ‘Insert-Function’ pop up window displayed on the right, select ‘User Defined’ from the function category list. User ribbon call method Either ‘Insert-Function’ button will work

  8. User can select the correct function by scrolling through each function and its description. Once function is selected, spaces are provided for each argument. Some arguments can be optional such as the ‘Quiet’ argument on the ‘NuDTurbTube’ function. User ribbon call method

  9. The ME 415 Add-In provides tools for several special design calculations. • Heat Transfer Fin Efficiency • Heat Exchanger Effectiveness-Number of Transfer Units (NTU) Method • Pump Performance Correction for Viscous Fluids • Hardy-Cross Flow and Hazen-Williams Head Loss Analysis • Friction Factor Calculator (Swamee-Jain and Churchill) • Nusselt Number ME 415 Add-in Features

  10. The function fin_eff uses known fin parameters m, l, ri , and ro. • m = SQRT(h/kδ) • l is total fin length • ri is inner radius (circular fins) • ro is outer radius (circular fins) • The function call from the Excel spreadsheet is =fin_eff(Index,m,l,ri,ro) or =fin_eff_fintype(m,l,ri,ro) which will provide an equivalent result for an Index corresponding to the same fin type. Fin efficiency

  11. Study of finned surfaces in heat exchanger design requires analysis of fin efficiency. Calculation of fin efficiency can become cumbersome with complex fin geometries. With known fin dimensions, the ‘user-defined’ function fin_eff readily calculates fin efficiency. From calculation of fin efficiency, further analysis of finned surface properties such as total surface effectiveness can be easily determined. Fin Efficiency

  12. When using the =fin_eff_fintype function call, the following function names should be used for each specific fin geometry. • Straight Rectangular Fins • =fin_eff_rect(m, l) • Straight Triangular Fins • =fin_eff_tri(m, l) • Circular Rectangular Fins • =fin_eff_rect_c(m, l, ri, ro) • ri and ro are required arguments here • Rectangular Spines (Circular cross-section) • “Round Pin Fin” • =fin_eff_pin_R(m, l) • Rectangular Spines (Square cross-section) • “Square Pin Fin” m = Sqrt(2*h/k/δ) • =fin_eff_pin_S(m,l) • Triangular Spines (Circular “Cone” cross-section) • “Cone Pin Fin” • =fin_eff_pin_C(m,l) Fin efficiency

  13. An Index value of 1,2,3,4,5, or 6 should be supplied for the appropriate fin geometry. • 1– Straight Rectangular Fins • =fin_eff(1,m, l) • 2– Straight Triangular Fins • =fin_eff2,m, l) • 3– Circular Rectangular Fins • =fin_eff(3,m, l, ri, ro) • ri and ro are required arguments • 4 – Rectangular Spines (circular cross-section) • “Round Pin Fin” • =fin_eff(4,m, l) • 5 - Rectangular Spines (square cross-section) • “Square Pin Fin” m = Sqrt(2*h/k/δ) • =fin_eff(5,m,l) • 6– Triangular Spines (Circular “Cone” cross-section) • “Cone Pin Fin” • fin_eff(6,m,l) FIN EFFICIENCY

  14. Function arguments ri and ro are provided as optional. When Index 3 is used for a circular rectangular fin, ri and ro are required. Otherwise, they should not be supplied. Fin efficiency

  15. The function calls from the Excel spreadsheet are =Hx_eff( Index,NTU,Cmin ,Cmax ,Passes) and =Hx_NTU( Index,eff, Cmin ,Cmax ,Passes). • The function Hx_eff uses known parameters NTU, Cmin, Cmax, and No. of Passes to calculate heat exchanger effectiveness. • NTU=UA/Cmin. • Cmin is the smaller of the two capacities Ch and Cc. • Cmax is the larger of the two capacities Ch and Cc. • Passes is an optional argument (specific to certain heat exchanger types). • The function Hx_NTU uses known parameters effectiveness, Cmin, Cmax, and No. of Passes to calculate NTU. • Where Cmin, Cmax, and Passes are same as above. Ntu method

  16. Heat exchanger analysis where only inlet conditions are known uses the Number of Transfer Units (NTU) Method to determine heat exchanger effectiveness. Effectiveness – NTU relations for some heat exchanger types require iterative calculation which is simplified by ‘user-defined’ functions Hx_eff and Hx_NTU. NTU Method

  17. An Index value of 1-8 should be supplied for the appropriate heat exchanger type. • 1 – Parallel flow: single pass • 2 – Counterflow: single pass • 3 – Shell and tube (one shell pass; 2,4,6, etc., tube passes) • 4 – Shell and tube (n shell passes; 2n, 4n, 6n, etc., tube passes) - - Passes argument required • 5 – Cross flow (both streams unmixed) • 6 – Cross flow (both streams mixed) • 7 – Cross flow (stream Cmin unmixed) • 8 – Cross flow (stream Cmax unmixed) • Index 4 requires input of the No. of passes. All other indexes should not have No. of passes supplied. Ntu method

  18. The direct cell call method uses =Hx_eff( Index,NTU,Cmin ,Cmax ,Passes) and =Hx_NTU( Index,eff, Cmin ,Cmax ,Passes). The ‘user-ribbon’ call method is shown in the figure below. Ntu method

  19. The function calls from the Excel spreadsheet are =Vis_pump_QHE(QHE_Matrix,Vis) and =Vis_pump_CF(QBE, HBE, Vis). • The function Vis_pump_QHE uses a pre-calculated QHE matrix and viscosity of the pumping fluid to provide corresponding flow and head values for the high viscosity fluid. The user can then generate (plot) a new pump curve with the supplied output. • The function Vis_pump_CF uses known best efficiency point (BEP) flow and head values along with the viscosity of the pumping fluid to provide correction factors that ‘correct’ the pump curve data. The user can multiply these correction factors with original pump data to find corresponding flow and head values for the high viscosity fluid. Viscous pump

  20. Because pump performance is greatly affected by highly viscous fluids, a correction method must be used to estimate performance when manufacturer’s data is not available. These pump corrections can be found from charts but is simplified through ‘user-defined’ functions Vis_pump_QHE and Vis_pump_CF. With the known best efficiency point (BEP) of a specific pump, the correction factors for efficiency, flow, Head0.6Q, Head0.8Q, Head1.0Q, and Head1.2Q can be found. Both ‘user-defined’ functions use a BEP to calculate and output the new data for a high viscosity pumping fluid. Viscous Pump

  21. The function Vis_pump_QHE uses a pre-calculated QHE Matrix and known viscosity. • The QHE matrix is a 4 x 3 matrix that the user must generate for input into the Vis_pump_QHE function. • From a given pump curve (water), determine the BEP (highest efficiency). From this point, the user determines the flow and head at the pump’s best efficiency. • The 4 x 3 matrix is then generated as follows. • Q H E (efficiency) 0.6*QBE Head@0.6QBE Efficiency@0.6QBE 0.8*QBE Head@0.8QBE Effficiency@0.8QBE 1.0*QBE Head@1.0QBE Efficiency@1.0QBE 1..2*QBE Head@1.2QBE Efficiency@1.2QBE • Viscosity (SSU – Saybolt Seconds Universal) Viscous pump

  22. Vis_pump_QHE outputs a matrix of cells. To execute the function, the user must highlight the expected output of cells. The output is the same size as the input QHE matrix (4 x 3). • Highlight any open cells in a 4 x 3 matrix. • Call =Vis_pump_QHE( QHE_Mat(4 x 3),Vis). Once all arguments are entered, the keystroke command Ctrl+Shift+Enter (Do NOT press OK) must be used to obtain the desired corrected pump curve data. Viscous pump

  23. The output of the cells is corrected pump curve data for the high viscosity fluid. Viscous pump Ctrl+Shift+Enter (Do not ‘click’ OK)

  24. The function Vis_pump_CF uses known BEP arguments flow (QBE), head (HBE), and viscosity. • Flow (GPM) • Head (‘ft’) • Viscosity (SSU – Saybolt Seconds Universal) • Vis_pump_CF outputs an array of cells. To execute the function, the user must highlight the expected array of six cells in any column and call =Vis_pump_CF( Flow,Head,Vis). Once all arguments are entered, the keystroke command Ctrl+Shift+Enter (Do NOT press OK) must be used to obtain the desired correction factors. Viscous pump

  25. Output array: • Cη • CQ • CH (0.6 x QNW) • CH (0.8 x QNW) • CH (1.0 x QNW) • CH (1.2 x QNW) Viscous pump Ctrl+Shift+Enter(Do NOT ‘click’ OK)

  26. For flows equal to or less than 100 GPM, correction factors for 0.6, 0.8, 1.0, and 1.2 flow rates will be equal. Otherwise, correction factors will vary. Viscous pump Final array output

  27. The function calls from the Excel spreadsheet are • =Hardy_Darcy(RngL,RngD,RngQ,RngN,RngE,rho,vis) • =Darcy(RngL,RngD,RngQ,RngE,rho,vis) and • =Hardy_Hazen(RngL,RngD,RngQ,RngN,RngC,tol,k1) • =HazenWill(RngL,RngD,RngQ,k1,RngC) • Darcy-Weisbach and Hazen-Williams are two methods for calculating head loss through pipes. They use unique parameters to determine friction and head-loss through piping systems. With appropriate input arguments, these two methods will provide approximately the same solution. Hardy-cross analysis

  28. Hardy-Cross formulation is an iterative method for obtaining the steady-state solution for any generalized series-parallel flow network. It can be systematically applied to any fluid flow network. While Hardy-Cross flow values can be obtained using ‘solver’ in Excel, an alternative method that employs ‘user-defined’ functions Hardy_Darcy and Hardy_Hazen supplies the same solution. Hardy-Cross analysis

  29. The function Hardy _Darcy uses system geometry, initial guesses for line flow rates, loop-node analysis, pipe roughness, density, and dynamic viscosity to determine flow through the system. Corresponding to the number of pipes in the system, the user should supply a range of lengths (RngL), diameters (RngD), initial flow guesses (RngQ), and epsilon values coefficients (RngE). The user also supplies a n-connection matrix (RngN), a density, and a dynamic viscosity. The function call from the Excel spreadsheet is =Hardy_Darcy(RngL,RngD,RngQ,RngN,RngE,rho,vis). Hardy-cross and darcy-weisbach

  30. The user must input a rho (density)and vis (dynamic viscosity). Typical units for each are lbm/ft3 and ft2/sec, respectively, when units of Q are ft3/sec. Hardy_Darcy outputs an array of cells. To execute the function, the user must highlight the expected array of cells (No. of pipes in system) in any column and call =Hardy_Darcy(RngL,RngD,RngQ,RngN,RngE,rho,vis). Once all arguments are entered, the keystroke command Ctrl+Shift+Enter (Do NOT press OK) must be used to obtain the desired Hardy flow values. Hardy-cross and darcy-weisbach

  31. Hardy-cross and darcy-weisbach Ctrl+Shift+Enter (Do not ‘click’ OK)

  32. The final array output Hardy _Darcy flow values are shown above. Darcy-Weisbachhead lossvalues through each pipe can then be found with these known flow rates. Hardy-cross and darcy-weisbach Final array output

  33. The ‘user-defined’ function Darcy uses the same system geometry and the calculated Hardy_Darcy flow values to find the head loss through each pipe. The function call from the Excel spreadsheet is =Darcy(RngL,RngD,RngQ,RngE,rho,vis). Since the Darcy function also uses range inputs, the keystroke command Ctrl+Shift+Enter must again be used to obtain the expected array Darcy head lossvalues. Hardy-cross and darcy-weisbach

  34. Hardy-cross and darcy-weisbach RngQ uses new Hardy_Darcy flow values

  35. The function Hardy _Hazen uses system geometry, initial guesses for line flow rates, and loop-node analysis to determine flow through the system. Corresponding to the number of pipes in the system, the user should supply a range of lengths (RngL), diameters (RngD), initial flow guesses (RngQ), and Hazen-Williams coefficients (RngC). The user also supplies a n-connection matrix (RngN), a tolerance value (tol), and a K1 value (k1). The function call from the Excel spreadsheet is =Hardy_Hazen(RngL,RngD,RngQ,RngN,RngC,tol,k1). Hardy-cross and Hazen-Williams

  36. Typical values for tol and k1 are .0001 and 4.727 respectively when units of Q are ft3/sec. Hardy_Hazen outputs an array of cells. To execute the function, the user must highlight the expected array of cells (No. of pipes in system) in any column and call =Hardy(RngL,RngD,RngQ,RngN,RngC,tol,k1). Once all arguments are entered, the keystroke command Ctrl+Shift+Enter (Do NOT press OK) must be used to obtain the desired Hardy flow values. Hardy-cross and hazen-williams

  37. Hardy-cross and hazen-williams Ctrl+Shift+Enter(Do NOT ‘click’ OK)

  38. The final array output Hardy_Hazen flow values are shown above. Hazen-Williams head lossvalues through each pipe can then be found with these known flow rates. Hardy-cross and hazen-williams Final array output

  39. The ‘user-defined’ function HazenWill uses the same system geometry and the calculated Hardy_Hazen flow values to find the head loss through each pipe. • The function call from the Excel spreadsheet is =HazenWill(RngL,RngD,RngQ,k1,RngC). • k1 is 4.727 when units for Q are ft3/sec • Since HazenWill also uses range inputs, the keystroke command Ctrl+Shift+Enter must again be used to obtain the expected array Hazen-Williams head loss values. Hardy-cross and hazen-Williams

  40. Hardy-cross and hazen-williams RngQ uses new Hardy_Hazen flow values

  41. The function calls from the Excel spreadsheet are • =fric_Swamee(Eps_Dia, ReD) • =fric_Churchill(Eps_Dia, ReD) • Eps_Dia is the relative roughness = ε/D • ReD is the Reynolds number = ρ*V*D/μ • Swamee-Jain and Churchill are two methods for calculating friction factors, a value necessary for calculating head loss through piping. Each function must be used with caution, as they each represent friction factors for different flow regions. Friction factor

  42. The Swamee-Jain friction factor calculation is appropriate for use only in a region of turbulent flow. • For piping flows • Turbulent region ReD > 2300 • Darcy-Weisbach is used for ReD<2300 • f = 64.0/ReD • The Churchill friction factor calculation is appropriate for use in any region of flow • Useful in • Laminar • Transition • Turbulent Friction factor

  43. Since Reynolds number ≈ 4000, either fric_Churchill or fric_Swamee can be used Friction factor

  44. Optional Inputs in italics NuxPlate(Re, Pr, Rexc, Quiet) NuBarPlate(Re, Pr, Rexc, Quiet) NuDBarCyl(Re, Pr, Quiet) NuDBarSphere(Re, Pr, mu_mus, Quiet) NuDBarTubes(Re, Pr, St_D, Sl_D, Aligned, Nl, Quiet) NuDBarZTubes(Re, Pr, Prs, St_Sl, Aligned, Nl, Quiet) NuDBarLamTube(Re, Pr, D_L, Thermal, mu_mus, Quiet) NuDTurbTube(Re, Pr, Quiet) NuDLiqMetals (Re, Pr, UniformT, Quiet) Nusselt numbers

  45. Functions return the local (Nu) or average (NuBar) Nusselt number The functions are reliable only over certain ranges. An answer will be returned, but it is up to the user to decide if it is adequate. A warning will appear for values outside the reliable range for the function. Quiet - Each function has an optional Quiet input. True or 1 will turn off the warnings. False if omitted. Nusselt numbers

  46. V, T∞ Turbulent Laminar x Ts • NuxPlate(Re, Pr, Rexc, Quiet) • Returns the local Nusselt number at x • Inputs based on the film temperature, Tf = (Ts+T∞)/2 • Re - Reynolds number, Rex = V x / ν • Pr - Prandtl number, Pr = Cpμ/ k = ν/ α • Rexc - Critical Reynolds number. Reynolds number at transition point from laminar to turbulent. If Re < Rexc, then laminar calculation. Otherwise, the calculation is for turbulent flow. If omitted, Recx = 5 X 105 • Ranges • For laminar, Pr ≥ 0.6 • For turbulent, Rex ≤ 108, 0.6 ≤ Pr ≤ 60 Nusselt: Flat Plate, Local

  47. NuBarPlate(Re, Pr, Rexc, Quiet) • Returns the average Nusselt number from 0 to x • Inputs based on the film temperature, Tf = (Ts+T∞)/2 • Re - Reynolds number, Rex = V x / ν • Pr - Prandtl number, Pr = Cpμ/ k = ν/ α • Rexc – Critical Reynolds number. Reynolds number at transition point from laminar to turbulent. If Re < Rexc, then laminar calculation. Otherwise, the calculation is for a mix of laminar and turbulent. If omitted, Recx = 5 X 105 • Ranges • For laminar, Pr ≥ 0.6 • For mixed, ReL ≤ 108, 0.6 ≤ Pr ≤ 60 Nusselt: Flat Plate, Mean Rex, c V, T∞ Turbulent Laminar x Ts

  48. NuDBarCyl(Re, Pr, Quiet) • Returns the average Nusselt number for crossflow over a cylinder • Inputs based on the film temperature, Tf= (Ts+T∞)/2 • Re - Reynolds number, ReD = V D / ν • Pr - Prandtl number, Pr = Cpμ/ k = ν/ α • Range • ReD Pr ≥ 0.2 Nusselt: Cylinder in crossflow

  49. NuDBarSphere(Re, Pr, mu_mus, Quiet) • Returns the average Nusselt number for flow over a sphere • Inputs based on the ambient fluid temperature, T∞, except μs • Re - Reynolds number, ReD = V D / ν • Pr - Prandtl number, Pr = Cpμ/ k = ν/ α • mu_mus - μ/ μs; viscosity ratio calculated from T∞ and Ts at the surface • Range • 0.71 ≤ Pr ≤ 380 • 3.5 ≤ ReD ≤ 7.6 X 104 Nusselt: Sphere

  50. Staggered Aligned SD St St Sl Sl Rows Rows • NuDBarTubes(Re, Pr, St_D, Sl_D, Aligned, Nl, Quiet) • Returns the average Nusselt number for crossflow over a bank of tubes • Inputs based on the film temperature, Tf = (Ts+T∞)/2 • Re - Reynolds number, ReD, max = Vmax D / ν • Pr - Prandtl number, Pr = Cpμ/ k = ν/ α • St_D - Transverse spacing / Diameter, St / D • Sl_D - Longitudinal spacing / Diameter, Sl / D • Aligned - True or 1 for Aligned tubes, False or 0 for Staggered tubes. Aligned if omitted. • Nl - Number of rows, if less than 10. Allows for correction factor if there are less than 10 rows. If omitted, Nl ≥ 10 • Vmax • Aligned - Vmax = St V / (St-D) • Staggered • if 2 SD > St +D, same as aligned • else Vmax = ½ V St / (SD-D) • Ranges • Pr ≥ 0.7 • 2000 ≤ ReD, max ≤ 40,000 Nusselt: Bank of Tubes

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