WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Table of contents Table of contents ........................................................................................................................................................................................... 1 Thermal and hydraulic design of shell and tube heat exchangers ................................................................................................................. 2 Design of the tube sheet Determination of the tube sheet data .................................................................................................................. 4 Properties of water........................................................................................................................................................................................ 6 Properties of water........................................................................................................................................................................................ 7 Heat transfer in pipe flow .............................................................................................................................................................................. 8 Shell-side heat transfer in baffled shell and tube heat exchangers ............................................................................................................. 11 Corrected log. mean temperature difference (CLMTD) and temperature distribution ............................................................................... 14 Tube bundle vibration analysis .................................................................................................................................................................... 15 Tube-side pressure loss in shell and tube heat exchangers......................................................................................................................... 16 Pressure loss on the shell-side of shell and tube heat exchangers .............................................................................................................. 18 CAD program for shell and tube heat exchangers ....................................................................................................................................... 20 MS Excel Specification Sheet ....................................................................................................................................................................... 21 CAD created by WTSC .................................................................................................................................................................................. 22 3D Tube sheet created by Alibre Design from SPIE .................................................................................................................................... 23 Layout Input values: Calculated values: Critical values: Estimated values: Lauterbach Verfahrenstechnik GmbH 1.234 1.234 1.234 1.234 or or or or 1.234 1.234 1.234 1.234 1 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Thermal and hydraulic design of shell and tube heat exchangers Tube-side: Medium: Shell-side: Water Water Mass flow Volume flow Pressure in (abs) Inlet temperature Outlet temperature Mean temperature mi Vi Pi ϑei ϑai ϑmi 158730 323.7 0.04351 176 131 153.5 Actual inlet temperature outlet temperature ϑei ϑai 176 132.3 Heat duty Heat loss Qi -7144853 Fouling resistance Density ρi Specif. heat capacity cpi Thermal conductivity λi Dynamic viscosity ηi lb/hr gpm ksi °F °F °F ma Va Pa ϑea ϑaa ϑma 198903 398.9 0.05801 68 104 86 °F °F ϑea ϑaa 68 103 Btu/hr Qa Qva 7144853 0 0 ft²hr°F/Btu 61.13 1 0.3799 1.011 lb/ft³ Btu/lb °F Btu/hr ft°F lb/ft hr Geometry: From tubesheet library: Installation position: Horizontal Bare tubes Straight tubes with fixed tubesheets Shell outside diam. Do Shell inside diam. Di Bundle-shell distance Tube outside diam. do Tube inside diam. di Tube pitch (crosswise) Pitch angle Φ Central baffle spacing Inlet baffle spacing Baffle borehole Sealing strips pairs 16 15.31 0.543 0.9843 0.8268 1.26 60 7.48 11.42 1.016 0 in in in in in in ° in in in - ρa cpa λa ηa lb/hr gpm ksi °F °F °F °F °F Btu/hr Btu/hr 0 ft²hr°F/Btu 62.17 0.9978 0.3555 1.93 lb/ft³ Btu/lb °F Btu/hr ft°F lb/ft hr Bare tubes Segmental baffles Shell wall thickness s 0.3465 in Min. bundle-shell dist. Tube wall thickness si 0.4724 0.07874 in in 1.091 1.929 19 15.19 20 in in in % Tube pitch(lengthwise) Pass lane width b Number of baffles/pass Baffle diameter Baffle cut Tube material Thermal conductivity of tube material λ Number of passes 8.667 Btu/hr ft°F Tube-side 2 - Number of serial exchangers 1 Shell-side 1 - — Lauterbach Verfahrenstechnik GmbH 2 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Evaluation: Heat transfer area Bundle length A l Required 40811 165 in² in Aa la Results: Number of tubes Heat transfer coefficient (inside) Heat transfer coefficient (outside) Overall heat transfer coefficient Logarithmic mean temperature diff. LMTD FN Factor (Correction factor for LMTD) Total fouling resistance Tube-side: Velocity (tube-side) Reynolds number Pressure drop Mean wall temp. 4.837 Re 72550 ∆pi 0.002596 134 ϑwi Inlet nozzle Nominal width Outside diameter Inside diameter Velocity 5.185 4.919 Outlet nozzle Nominal width Outside diameter Inside diameter Velocity 5.185 4.919 ft/s ksi °F in in ft/s in in ft/s Final 38956 157.5 N αi αo k ∆ϑ FN Rf 80 1034 396.5 67.4 0.9433 0 Inlet nozzle Nominal width Outside diameter Inside diameter Velocity ρ ·v² inlet nozzle 6.272 4.143 1588 in in ft/s kg/(m·s²) Outlet nozzle Nominal width Outside diameter Inside diameter Velocity 6.272 4.143 in in ft/s Heat balance shell-side: Qa = ma · cpa · (ϑaa - ϑea ) = Btu/hr 7144853 2093942 - 0 ) = -7144853 Overall heat transfer coefficient: 1 1 do do ln(do/di) = + fi · + k di 2 · λ αi 1 + 0 Btu/hr 1 + do + fo ; Rf = fi · αo · + fo di 0.025 ln( 0.025 = Btu/ft²hr°F Btu/ft²hr°F Btu/ft²hr°F °F ft²hr°F/Btu ft/s ft/s ksi °F Btu/hr = -( Overdesign -4.55 % Shell-side: Velocity (shell-side) 3.357 Velocity (window zone) 6.719 Reynolds number Re 43225 Pressure drop ∆pa 0.006568 Mean wall temp. 111.9 ϑwa Equations: Heat balance tube-side: Qi = mi · cpi · (ϑai - ϑei ) = -7144853 Heat balance: Qi = -(Qa - Qva ) in² in 0.025 / 0.021) + 0.021 2 · 15 1 + + 0 5870 k = 396.5 Btu/ft²hr°F Q = k · A · ∆ϑ · FN = 2251 · 26.33 · Lauterbach Verfahrenstechnik GmbH 37.44 · 0.9433 = -7144853 3 Btu/hr 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Design of the tube sheet Determination of the tube sheet data Name of type: Baffle-type: Segmental baffles Design = D; Rating / Simulation = R < R Outside shell diameter Inside shell diameter Bundle diameter Bundle diameter at cross flow zone > Do Di Db Dbc 16 15.31 14.22 12.69 in in in in Minimum distance bundle - shell Distance between bundle - shell Dm D 0.4724 0.543 in in Outside tube diameter Inside tube diameter Pitch crosswise to direction of flow Pitch in direction of flow Pitch angle da di sq sl Φ 0.9843 0.8268 1.26 1.091 60 in in in in ° Baffle diameter Height of the window in the baffles Height of the window in % of diameter Dl H 15.19 3.061 20 in in % Tube pattern: aligned = a / staggered = s Adapt window height Yes = Y / No = N < S < Arrangement: around central tube = 0 staggered by 1/2 pitch = 1 No tubes in window? Yes = 1 < 0 > - < 0 > - Number of tube-side passes Number of shell-side passes Bundle type Tube lane width (horizontal) Tube lane width (vertical) > > 2 1 < 1 > 1.929 1.929 Outside head diameter Bolt-circle diameter Number of bolts on the bolt-circle Rotation angle for bolt-hole pattern Da Dt in in in in ° Number of tubes Number of dummy tubes Number of tie rods Total number of tubes, dummy tubes and tie rods Number of tubes in the windows Number of tubes in the cross flow zone Number of boundary tubes required/actual RR n nB nZ nG nF nS - / 80 0 0 80 19 61 50 Number of tube rows in a window Number of tube rows in the cross flow zone Number of tube rows in the end zone nRF nW nWE 1.5 7 8.5 - Sum of the shortest connecting paths in the center Shortest connecting path between tube and tube Shortest connecting path between tube and shell Number of connecting paths Mean distance boundary tubes-envelope circle centre Le e e1 nV rh 5.096 0.2756 1.308 9 5.48 in in in in — Lauterbach Verfahrenstechnik GmbH 4 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Number of tubes, dummy tubes and tie rods per pass Pass-No. 1 2 3 4 5 40 0 0 0 40 Final tube length Total area Number of baffles per shell-side path Distance between the baffles Distance between head and baffle Diameter of the baffle borehole Number of sealing strips pairs Number of exchangers in series la A N S1 S2 nD 5 7 0 8 0 in in² in in in - Tube-side 5.185 in 5.185 in Nozzles: Inside diameter of the inlet nozzle Inside diameter of the outlet nozzle Lauterbach Verfahrenstechnik GmbH 157.5 38956 19 7.48 11.42 1.016 0 1 6 0 Shell-side 6.272 in 6.272 in 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Properties of water Properties of Water and Steam State 1 Calculation for saturation? (Yes = Y / No = N) < N ϑ1 p1 Temperature Pressure State 2 > < N 153.5 0.04351 ϑ1 p2 °F ksi Properties of liquid water or superheated steam: State 1 Liquid Density Spec.isob.heat capacity Thermal conductivity Dynamic viscosity Kinematic viscosity Prandtl number Thermal diffusivity Specific volume Spec.isoc.heat capacity Specific enthalpy Spec. internal energy Specific entropy Compressibility Surface tension C. of therm. expansion Isentropic exponent Speed of sound Dielectric constant Characteristics: Molar mass Gas constant Critical temp. Critical pressure Critical density M R Tc pc ρc Lauterbach Verfahrenstechnik GmbH ρ cp λ η ν Pr a v cv h u s Z σ β κ w ε lb/ft³ Btu/lb °F Btu/hr ft°F lb/ft hr m²/s m²/s ft³/lb Btu/lb °F Btu/lb Btu/lb Btu/lb °F lbf/in 1E-6/°F ft/s - 61.13 0.9998 0.38 1.011 4.267E-7 2.66 1.604E-7 0.01636 0.9398 121.6 121.4 0.2207 0.001949 0.000371 316.1 7918 5110 64.52 18.02 0.1102 705.1 3.2 20.1 lb/lbmol Btu/lb °F °F ksi lb/ft³ 6 > 134 0.04351 °F ksi State 2 Liquid ρ cp λ η ν Pr a v cv h u s Z σ β κ w ε 61.49 0.9986 0.3742 1.186 4.979E-7 3.166 1.573E-7 0.01626 0.953 102.1 102 0.1885 0.002001 0.000382 278.8 7908 5092 67.81 Validity: 0.01 °C ≤ ϑ 0.00612 bar 0.01 °C ≤ ϑ 0.00612 bar ≤ ≤ ≤ ≤ lb/ft³ Btu/lb °F Btu/hr ft°F lb/ft hr m²/s m²/s ft³/lb Btu/lb °F Btu/lb Btu/lb Btu/lb °F lbf/in 1E-6/°F ft/s - 800 °C p ≤ 1000 bar 2000 °C p ≤ 500 bar 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Properties of water Properties of Water and Steam State 1 Calculation for saturation? (Yes = Y / No = N) < N ϑ1 p1 Temperature Pressure State 2 > < N 86 0.05801 ϑ1 p2 °F ksi Properties of liquid water or superheated steam: State 1 Liquid Density Spec.isob.heat capacity Thermal conductivity Dynamic viscosity Kinematic viscosity Prandtl number Thermal diffusivity Specific volume Spec.isoc.heat capacity Specific enthalpy Spec. internal energy Specific entropy Compressibility Surface tension C. of therm. expansion Isentropic exponent Speed of sound Dielectric constant Characteristics: Molar mass Gas constant Critical temp. Critical pressure Critical density M R Tc pc ρc Lauterbach Verfahrenstechnik GmbH ρ cp λ η ν Pr a v cv h u s Z σ β κ w ε lb/ft³ Btu/lb °F Btu/hr ft°F lb/ft hr m²/s m²/s ft³/lb Btu/lb °F Btu/lb Btu/lb Btu/lb °F lbf/in 1E-6/°F ft/s - 62.16 0.9982 0.3554 1.929 8.006E-7 5.416 1.478E-7 0.01609 0.9832 54.21 54.04 0.1043 0.002871 0.000407 168.4 5687 4959 76.65 18.02 0.1102 705.1 3.2 20.1 lb/lbmol Btu/lb °F °F ksi lb/ft³ 7 > 111.9 0.05801 °F ksi State 2 Liquid ρ cp λ η ν Pr a v cv h u s Z σ β κ w ε 61.84 0.9979 0.3664 1.457 6.082E-7 3.969 1.532E-7 0.01617 0.9675 80.03 79.86 0.1505 0.002755 0.000393 232 5863 5048 71.76 Validity: 0.01 °C ≤ ϑ 0.00612 bar 0.01 °C ≤ ϑ 0.00612 bar ≤ ≤ ≤ ≤ lb/ft³ Btu/lb °F Btu/hr ft°F lb/ft hr m²/s m²/s ft³/lb Btu/lb °F Btu/lb Btu/lb Btu/lb °F lbf/in 1E-6/°F ft/s - 800 °C p ≤ 1000 bar 2000 °C p ≤ 500 bar 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Heat transfer in pipe flow Constant wall temperature Circular pipes ϑe ϑa ϑm ρ cp λ η ν Pr PrW Inlet temperature Outlet temperature Mean temperature Density of the fluid Specific heat capacity of the fluid Thermal conductivity of the fluid Dynamic viscosity of the fluid Kinematic viscosity of the fluid Prandtl number Prandtl number at wall temperature 61.13 1 0.3799 1.011 4.267E-7 2.661 3.166 Fluid: liquid <0> or gas <1> 0 = Circular pipes, 1 = Non-circular pipes < < Pipe length Inside diameter of the pipe Cross sectional area of the pipe Perimeter of the pipe ⇒ Hydraulic diameter l di f u dh = Total mass flow Total volume flow Number of pipes with parallel flow ⇒ Mass flow per pipe ⇒ Velocity ⇒ Reynolds number Mg Vg Z M = w = Re = Q = Mg · cp · (ϑa - ϑe ) Balance: °F °F °F lb/ft³ Btu/lb °F Btu/hr ft°F lb/ft hr m²/s - 0 > 0 in in in² in in 157.5 0.8268 0.5369 2.597 0.8268 lb/hr gpm lb/hr ft/s - 3968 4.837 72550 = Btu/hr Results: Constant wall temperature Nu · λ ⇒ α = Re = 295.6 · 0.6575 = = dh w · dh · ρ = = = = Btu/ft²hr°F 1.474 · 301.3 0.021 · 979.2 = = η / 1000 Nu_m_ϑ Nu_m_ϑ Nu_m_T Nu_m 1630 0.021 72550 0.4179 / 1000 (laminar non-disturbed flow Re < 2300) (laminar entrance flow Re < 2300) (turbulent flow Re > 10000) (transition zone 2300 ≤ Re ≤ 10000) [6] [12] [26] [29] Factor K: 0.11 Liquids: Gases: K = (Pr/PrW ) n K = (T/TW ) Nu = Nu_m(_ϑ,T) · K = Heat transfer: Q ⇒ Wall temperature ϑW = 0.9811 = for n = 0 [40,41] 295.6 = α · = 9257 · = 134 A · ∆ϑlog · °F — Lauterbach Verfahrenstechnik GmbH 8 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Calculations: Re < 2300 Laminar flow: Laminar non-disturbed flow: HW = Re · Pr · dh/l = 1014 1/3 Nu_m_ϑ_2 = 1.615 · HW 3 Nu_m_ϑ = 3.66 3.66 [5] 3 + 0.7 3 = = 3 = [6] 3 + 0.7 1/3 Nu_m_ϑ_2 - 0.7 + 3 + 1/3 - 0.7 = Laminar entrance flow: 1/6 2 Nu_m_ϑ_3 = · HW = 1 + 22 Pr 1/6 2 = · 1 + 22 · 3 Nu_m_ϑ = 3.66 3 + 0.7 3 = 3.66 Turbulent flow: 3 Nu_m_ϑ_2 - 0.7 + [11] 3 3 + 1/3 + Nu_m_ϑ_3 3 + 0.7 = 1014 2.661 - 0.7 = [12] 3 1/3 + = Re > 10000 -2 ξ = [1.8 · log Re - 1.5] -2 = [ 1.8 · log 72550 - 1.5 ] = 0.01903 [27] 2/3 ξ /8 · Re · Pr Nu_m_T = dh · 1 + 2/3 1 + 12.7 · ξ /8 · (Pr = l -1) [26] 2/3 0.01903 /8 · 72550 · 2.661 = 0.021 · 1 + 12.7 · Nu_m_T = 0.01903 /8 · ( 2/3 -1) 2.661 1 + 4 301.3 — Lauterbach Verfahrenstechnik GmbH 9 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Transition zone: 2300 ≤ Re ≤ 10000 1/3 Nu_m_ϑ_2_2300 = 1.615 · (2300 · Pr · dh/l) = [32] 5.135 1/6 2 Nu_m_ϑ_3_2300 = · 2300 · Pr · dh/l = [33] 3.22 1 + 22 Pr 3 Nu_m_L_2300 = 49.371 Nu_m_L_2300 = 5.539 + Nu_m_ϑ_2_2300 - 0.7 3 1/3 + Nu_m_ϑ_3_2300 [31] 2/3 (0.0308/8) · 10000 · Pr dh Nu_m_T_10000 = · 2/3 1 + 12.7 · 0.0308/8 · (Pr 1 + l -1) [37] Nu_m_T_10000 = 61.15 Re - 2300 γ = 72550 - 2300 = 10000 - 2300 = Nu_m = (1 - γ ) · Nu_m_L_2300 + γ · Nu_m_T_10000 = Lauterbach Verfahrenstechnik GmbH [30] 10000 - 2300 10 [29] 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Shell-side heat transfer in baffled shell and tube heat exchangers Geometric data Tube arrangement: Staggered Inside diameter of the shell Diameter of the tube bundle at cross flow zone Di DB 15.31 12.69 in in Outside diameter of the tubes Tube pitch crosswise to direction of flow Tube pitch in direction of flow da s1 s2 0.9843 1.26 1.091 in in in Diameter of the baffle Height of the window in a baffle Diameter of the bore-holes for the tubes in the baffle Baffle spacing Dl H dB 15.19 3.061 1.016 in in in S 7.48 in Number of tubes including blanks and support tubes Number of tubes in the upper and lower windows n 80 - nF 19 - Number of main resistances in a cross-flow zone Number of connection lines Number of sealing strip pairs nW nV nS 7 9 0 - Number of shell-side passes Tube lane width (only for ND = 2) ND b 1 1.929 Fluid Mass flow Volume flow m V Fluid: liquid <0> or gaseous <1> 198903 398.9 < in lb/hr gpm 0> Inlet temperature Outlet temperature Mean wall temperature ϑE ϑA ϑW Density Spec. heat capacity Thermal conductivity of the fluid Dynamic Viskosity Kinematic viscosity of the fluid Prandtl number Prandtl number at wall temperature 62.17 ρ cp 0.9978 0.3555 λ 1.93 η 8.009E-7 ν Pr 5.416 PrW 3.969 68 104 111.9 °F °F °F lb/ft³ Btu/lb °F Btu/hr ft°F lb/ft hr m²/s - Results fW = fG · fL · fB Nu0,AW α = 1.093 · = fW · Nu0,Bundle Nu0,AW α = = · λ 0.5031 · 358.3 · · K π /2 · da 1068 = 0.8555 · 0.538 = 712.1 = 358.3 0.6152 = · π /2 · 0.5031 1.081 0.025 Btu/ft²hr°F Lauterbach Verfahrenstechnik GmbH — 11 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Calculation of Nu0,Bundle a = s1 /da = b = s2 /da = 1.28 ψ = 1- π /4a (for b ≥ 1) Reψ ,1 1.109 ψ = 1- π /4ab (for b < 1) = 43225 ψ = 0.3864 3 Nu1,lam = 0.664 · Reψ ,1 · Pr 3 242.4 = 0.664 · Nu1,turb 43225 · 5.416 0.037 · Reψ ,1 = 1 + 2.443 · Reψ ,1 0.037 · -0.1 0.8 · Pr · (Pr(2/3) 0.8 43225 - 1) · 5.416 · ( 5.416 372.4 = 1 + 2.443 · 43225 2 Nu1,0 = 0.3 + (2/3) - 1) 2 Nu1,lam 444.7 = 0.3 + Nu0,Bündel -0.1 + Nu1,turb 242.4 = fA · Nu1,0 = 2 + 372.4 1.601 · 2 444.7 = 712.1 2 fA = 1 + = 1.601 3 · b Calculation of fG RG = nF / (n / ND) fG = 1 - RG + 0.524 · RG 1.093 = 1 - ⇔ 0.2375 = 19 / ( 80 / 1) 0.32 0.2375 + 0.524 · 0.2375 0.32 — Lauterbach Verfahrenstechnik GmbH 12 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Calculation of fL e = 0.2756 in e1 = 1.308 in LE (e ; e1 ) = dB = 1.016 in da = 0.9843 in n = n ASRU π (dB nF = - · ND 2 2 - da 80 = π · (Di 2 nF = 19 3.488 0.3858 ) = 106.7 in² 4 γ = 2 arccos(1- 2·H/D1 ) = 2 arccos(1 - 2 · 0.07776 / ASMU in ) = 2 5.096 - D1 2 (360 - γ ) ) · 4 = in² 1.99 360 · ND = π /4 · ( 2 0.3888 + ASMU = - 0.3858 ASG = ASRU AE = S · LE = 0.19 · RL = ASG = 0.003534 / fL = 0.4 / AE 2 ) · (360- 0.00225 + 0.001284 = ASRU 106.7) / (360 · 5.478 in² 0.1294 = 38.12 in² 0.02459 = 0.1437 1) ASRU + 1 - 0.4 ASG exp(-1.5 · RL ) ASG 0.00225 0.00225 0.8555 = 0.4 + 1 - 0.4 exp(-1.5 · 0.003534 0.1437 ) 0.003534 Calculation of fB AB = S · (Di - DB - e) = 17.51 RB = AB / AE 0.02459 = = 0.01129 / in² for e <(Di - DB ) else AB = 0 0.4592 3 fB = exp - ß · RB 1 - for nS ≤ nW / 2 2 nS / nW 3 0.538 = exp fB = 1 - ß · 0.4592 1 - 2 · 0 / 7 for nS > nW / 2 Lauterbach Verfahrenstechnik GmbH 13 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Corrected log. mean temperature difference (CLMTD) and temperature distribution Corrected logarithmic mean temperature difference (CLMTD) and distribution with cell method for shell and tube heat exchangers Tube-side inlet temperature Shell-side inlet temperature ti1 ta1 176 68 Tube-side mass flow Shell-side mass flow Specific heat capacity tube-side Specific heat capacity shell-side mi ma cpi cpa 158730 198903 1 0.9978 Heat capacity flow tube-side (mi·cpi) Heat capacity flow shell-side (ma·cpa) Wwi Wwa 46532 58165 Sheet plus shell type Number of tube-side passes Number of shell-side passes Number of baffles Nt NS NZ Actual overall heat transfer coefficient Actual heat transfer area Number of tube rows per cell 1 2 1 19 k A 396.5 38956 4 Flow pattern: countercurrent = 1; cocurrent = 2 Tube flow: countercurrent = 1; cocurrent = 2 0 = unmixed; 0.5 = mixed 101 1 0 Tube-side outlet temperature Shell-side outlet temperature ti2 ta2 LMTD countercurrent flow CLMTD corrected log. mean temp. difference FN factor ∆TGeg ∆Tm FN Number of cells Product k·A Product k·A per cell Lauterbach Verfahrenstechnik GmbH timax tamax timin tamin tinv 14 W/°F W/°F Btu/ft²hr°F in² - °F °F 68.57 64.69 0.9433 °F °F - 0.4047 0.3237 0.01664 0.01331 Maximum tube-side temperature Maximum shell-side temperature Minimum tube-side temperature Minimum shell-side temperature Max. temperature inversion in one cell lb/hr lb/hr Btu/lb °F Btu/lb °F 132.3 103 40 31437 785.9 Tube-side efficiency Shell-side efficiency Tube-side cell efficiency Shell-side cell efficiency °F °F 176 103 132.3 68 32 W/°F W/°F °F °F °F °F °F 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Tube bundle vibration analysis General formulation Outside diameter of the tubes Wall thickness of the tubes Inside tube diameter da s di Pitch (crosswise) Pitch (lengthwise) Transverse pitch ratio Longitudinal pitch ratio 0.9843 0.07874 0.8268 t l t/da l/da in in in 1.26 in 1.091 in 1.28 1.109 - Cross-sectional area of the tubes Second moment of area of the tubes A J 0.2239 0.02309 Modulus of elasticity Effective density E ρ 29007 490.1 in² in^4 ksi lb/ft³ Support for the tubes: Selected support for the tubes: Factor for the support Factor for additional forces 1 fixed-jointed C 3.93 Cf 1 - Arrangement of the tubes (1-3) Selected arrangement: → Strouhal number of the bundle 1 Staggered bare tubes Sr 0.2219 - Final span Velocity in the narrowest cross section L we 11.42 4.143 Natural frequency of the tubes fR Safety factor S Allowable excitation frequency fz = fR/S fz Excitation frequency of the flow ferr in ft/s 1203 1/s 1.5 802.3 1/s 11.21 1/s 18.9 3.357 in ft/s 439.3 1/s 292.9 9.081 1/s 1/s in² Vibration probable, when ferr > fz Equations di = da - 2 · s = 25 - 2 · 2 = 0.8268 in A = π /4 · (da2 - di2 ) = π /4 · ( 25 2 - 21 2 ) = 0.2239 J = π /64 ·(da4 - di4 ) = π /64 ·( 25 4 - 21 4 ) = 0.02309 106 fR = C 2 · E · J · 2·π ρ · A 106 3.93 · 2 da/1000 9611 7850 · 144.4 · 290 ⇔ 802.3 = ⇔ 11.21 = Sr · we ferr = 200000 · · 2·π fz = fR / S ⇔ · Cf L 1203 = in^4 Lauterbach Verfahrenstechnik GmbH 1203 / 1.5 0.2219 · 1.263 1 25 / 1000 15 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Tube-side pressure loss in shell and tube heat exchangers Properties Inlet temperature Outlet temperature Mean temperature Pressure at the inlet Density of the fluid Specific heat capacity Thermal conductivity Dynamic viscosity of the fluid Fluid: liquid = 0, gas = 1 Fluid ϑe ϑa ϑ Pe ρ cp λ η 176 131 153.5 0.04351 61.13 1 0.3799 1.011 0 Acceleration due to gravity Type (straight tube=1; U-tube=2) Inside diameter of inlet nozzle Inside diameter of outlet nozzle Number of tube-side passes Number of tubes per pass Length of one tube Inside tube diameter Outside tube diameter Tube wall thickness Mass Mean Mean Mean °F °F °F 134 ksi lb/ft³ 61.19 Btu/lb °F Btu/hr ft°F lb/ft hr 1.186 g 9.81 °F lb/ft³ lb/ft hr m/s² 1 flow velocity in the inlet nozzle velocity in the outlet nozzle velocity in the tube Reynolds-Number Prandtl-Number Grashof-Number Pressure loss factor Friction coefficient Correction factor for the viscosity Correction factor for the convection Friction factor (ξ is · Φ · ψ) DTNI DTNO NTP N L DI DO t = 5.185 5.185 2 40 157.5 0.8268 0.9843 0.07874 W Vni = Vno = Vt = 158730 4.919 4.919 4.836 lb/hr ft/s ft/s ft/s Re = Pr = Gr = 72537 2.661 498913 - = 3.2 = 0.0059 = 1.025 = 1 = 0.006047 - = = = = = = ksi ksi ksi ksi ksi Ke ξ is Φ ψ ξ Pressure loss (inlet nozzle) Pressure loss (outlet nozzle) Pressure loss (inlet, outlet and baffle) Pressure loss (friction) Fouling factor Total pressure loss (∆Pn + ∆Pe + Ft·∆Pt) Lauterbach Verfahrenstechnik GmbH Wall 16 ∆Pni ∆Pno ∆Pe ∆Pt Ft ∆P 0.000144 0.000144 0.000494 0.001421 1.277 0.002596 in in in in in in — 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Equations t = 1/2 · ( DO - DI ) ⇔ 0.002 = 1/2 · ( ⇔ 1.499 = 1.273 · W Vni = 1.273 · DTNI2 · ρ ⇔ DTNO2 · ρ 20 2 979.2 1.273 · 20 1.499 = 0.1317 1.273 · W 2 · 979.2 1.273 · ⇔ Vt = DI2 · N · ρ Re = 0.021 ) · 0.1317 1.273 · W Vno = 0.025 - 0.021 Vt · DI · ρ 2 · 40 · 1.474 · ⇔ η/1000 20 1.474 = 979.2 0.021 · 979.2 72537 = 0.000418 Pr = η/1000 · Cp / λ ⇔ g · DI3 Gr = 2.661 = 0.000418 · 4188 / 0.6575 ρ - ρW · ( η/1000 / ρ )² ρ 9.81 · 0.021 3 979.2 - 498913 = 980.2 · ( 0.000418 / 979.2 )² 979.2 Pressure drop factor for: Straight tubes: one pass multiple passes U-tubes: two passes four or more passes ξ is = ξ is( Re ) = Φ ( Re ; η/ηW ) Φ = ψ ( Re ; Gr·Pr·η/ηW ) ψ ∆PnE = ρ E ·VnE ² / 2.224 = ∆PnA = ρ A ·VnA ² / 2.224 = ∆Pe = Ke·ρ ·Vt² / 2.0 ∆Pt = 2 · ξ · = = = Ke Ke Ke Ke = = = = 0.0059 = ξ is( 1.025 = Φ ( 1 = ψ ( 989.8 = 989.8 = 979.2 · 979.2 · 3404 = 3.2 · = 0.9 1.6 · NTP 0.9 0.8 · NTP NTP = 2 Ke = 3.2 72537 ) 72537 ; 72537 ; 0.852 ) 1131300 ) 1.499 ² / 2.224 1.499 ² / 2.224 979.2 · 1.474 ² / 2.0 ρ · Vt² · NTP · L DI 979.2 · 1.474 ² · 2 · 4 9801 = 2 · 0.006047 · 0.021 DO - 2·t 5 Ft = DO - 2.2·t - 0.00182 · DO 0.3 0.025 - 2 · 5 0.002 1.277 = 0.025 - 2.2 · Lauterbach Verfahrenstechnik GmbH 0.002 - 0.00182 · 17 0.025 0.3 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Pressure loss on the shell-side of shell and tube heat exchangers Tube-bundle heat exchanger with baffles Geometric variables: Shell inside diameter Tube bundle diameter at cross flow zone Di DB 15.31 12.69 in in Tube outside diameter Tube pitch crosswise to direction of flow Tube pitch lengthwise to direction of flow Pitch angle da sq sl 0.9843 1.26 1.091 60 in in in ° Baffle diameter Number of baffles Height of the window in a baffle Diameter of the bore holes for the tubes in the baffles Baffle spacing Distance between the tubesheet and the 1st baffle Dl nU H dB 15.19 19 3.061 1.016 in in in S SE 7.48 11.42 in in Number of tubes including blanks and support tubes Number of tubes in the upper and lower windows Number of tube rows in a window Number of main resistances in the crossflow zone Number of main resistances in the end zone Number of connection lines Distance between boundary tubes and shell Number of sealing strip pairs n nF nRF nW nWE nV e1 nS 80 19 1.5 7 8.5 9 1.308 0 in - Number of shell-side passes Tube lane width (only for ND = 2) ND b 1 1.929 in Inside nozzle diameter (inlet) Inside nozzle diameter (outlet) dSi dSo 6.272 6.272 in in Fluid: Mass flow Volume flow m V 198903 398.9 Fluid: liquid = 0 or gas = 1 0 Inlet pressure Inlet temperature Outlet temperature Mean temperature Density Dynamic viscosity Specific heat capacity Thermal conductivity Prandtl number Mean wall temperature Dynamic viscosity at mean wall temperature Friction loss on the shellside of the heat exchanger 1 · 0.000022 ∆p = (nU -1) · ND · ∆pQ = ( 19 - 1) · + 2 · ∆pQ_E = 2 · 0.000023 + nU · ND · ∆pF = 19 · 1 · 0.000310 + ∆pS = 0.000230 ∆p = 0.006568 lb/hr gpm PE ϑE ϑA ϑ ρ η cp λ Pr ϑW ηW ksi ksi ksi ksi 0.05801 68 104 86 62.17 1.93 0.9978 0.3555 5.416 111.9 1.457 ksi °F °F °F lb/ft³ lb/ft hr Btu/lb °F Btu/hr ft°F °F lb/ft hr Cross-flow zone End zone Window zone Nozzles ksi Lauterbach Verfahrenstechnik GmbH — 18 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers Results a = 1.28 e = 0.2756 in Cross-flow zone L_E = 5.096 in f_a_l_f = 223.4 f_a_t_v = - b = 1.109 - A_E = 38.12 in² - f_a_t_f = 0.6963 5.485 - f_z_l = Xi_l = 0.006994 - 1.28 w_e = 3.357 ft/s - f_a_l_v = 223.4 - 0.9875 - f_z_t = 0.9615 - Xi_t = 0.4103 - Xi = 0.4014 - A_SMU = 1.99 A_SG = 5.478 3.488 R_M = 0.3633 - R_L = 0.1437 - r = 0.5955 - γ = 106.7 ° Re = 31937 - ß = 3.7 - R_S = 0 - R_B = 0.4592 - A_B = 17.51 in² f_L = 0.5649 - f_B = 0.1828 - ∆p_Q_0 = 0.000212 ksi - A_E_E = 58.19 in² ∆p_QE_0 = 0.000124 ksi ∆p_QE = 0.000023 ksi Window zone A_FG = 26.92 in² w_p = 6.497 d_g = 1.806 End zone Re_E = 20924 A_FR = 7.228 ft/s w_z = 4.67 in U_F = 43.63 ksi ∆p_F = 0.000310 ksi w_S_o = 4.143 ∆p_S = 0.000230 in² ksi ∆p_F_l = 0.000295 Shell nozzles w_S_i = 4.143 in² - A_SRU = ∆p_Q = 0.000022 in² c = in² ft/s w_e_E = 2.199 A_F = 19.7 n_WF = 2.245 ft/s in² - in ∆p_F_t = 0.000490 ksi ft/s ∆p_S_i = 0.000115 ksi ft/s ∆p_S_o = 0.000115 ksi ksi Lauterbach Verfahrenstechnik GmbH 19 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers CAD program for shell and tube heat exchangers Tube-side TEMA type AEL TEMA: Front end: A Medium Inlet pressure Pressure stage Inlet temperature Outlet temperature Mean temperature Design temperature Design pressure Shell: Shell-side E Rear end: Water pi ϑe,i ϑa,i ϑm,i L Water 0.04351 0.2321 176 131 153.5 212 0.05801 ksi ksi °F °F °F °F ksi pa ϑe,a ϑa,a ϑm,a 0.05801 0.2321 68 104 86 122 0.07252 ksi ksi °F °F °F °F ksi Inlet nozzle: Flange connection n.w.* Outside diameter Nozzle wall thickness Inside diameter DN 125 5.185 DN in in in 150 6.272 in in in Outlet nozzle: Flange connection n.w.* Outside diameter Nozzle wall thickness Inside diameter DN 125 5.185 DN in in in 150 6.272 in in in * n.w. = nominal width Geometry: Shell outside diam. Do Shell inside diam. Di Bundle - shell distance Tube outside diam. do Tube pitch (crosswise) Pitch angle Φ Central baffle spacing Inlet baffle spacing Baffle borehole Sealing strips pairs 16 15.31 0.543 0.9843 1.26 60 7.48 11.42 1.016 0 in in in in in ° in in in - Shell wall thickness sa 0.3465 in Tube inside diameter di Tube pitch(lengthwise) Pass lane width b Number of baffles/pass Baffle diameter Baffle cut 0.8268 1.091 1.929 19 15.19 20 in in in in % Number of passes (tube-side) Number of passes (shell-side) 2 1 Final bundle length Final shell length la la Number of tubes Expansion joint diameter Plate thickness (fixed plate) Plate thickness (free plate) R Lauterbach Verfahrenstechnik GmbH 157.5 157.5 in in 80 1.181 1.181 20 in in in 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers MS Excel Specification Sheet 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 55 56 57 58 59 60 61 Customer Job No. Reference No Proposal No. Date Adress Plant Location PERFORMANCE OF ONE UNIT Shell Side Water kg/s 25,06 kg/s kg/s Fluid Allocation Fluid Name Fluid Quantity, Total Vapour (In / Out) Liquid (In / Out) Steam Water Noncondensables Temperature (In / Out) °C 20 Density kg/m³ 995,9 Viscosity mPa·s 0,7976 Molecular Wt, Vapour kg/kmol Molecular Wt, Noncondensables kg/kmol Specific Heat J/(kg·K) 4177,6 Thermal Conductivity W/(m·K) 0,6152 Latent Heat J/kg Inlet Pressure (abs.) bar 4 Velocity m/s Pressure Drop, Allow./Calc. Pa Fouling Resistance m²·K/W Heat Exchanged kW 2093,9 Transfer Rate, Service W/(m²·K) 2250,9 MTD (Corrected) K (diff) 35,32 Heat Transfer Area m² 25,1 CONSTRUCTION OF ONE SHELL Shell Side Design / Test Pressure Pa Design Temperature °C No. Passes per Shell 1 Corrosion Allowance mm Connections in DN 150 Size & out DN 150 Rating Intermediate Tube Length mm 4000 Tube Dimensions (OD x Thk) mm 25 x 2 Pitch Cross mm 32 Shell ID mm 388,8 Channel or Bonnet Tubesheet-Stationary Floating Head Cover Baffles-Cross mm 385,8 Baffles Spacing mm 190 Bypass Seal Arrangement Expansion Joint ρ · v² Bundle Entrance kg/(m·s²) 1588 Gaskets-Shell Side - Floating Head Code Requirements Weight / Shell kg Weight / Bundle kg Remarks Lauterbach Verfahrenstechnik GmbH 40 28.01.2013 Tube Side Water 20 80 979,2 0,4179 55 4187,9 0,6575 3 1,02 1,47 45288 17898 0 0 Sketch (Bundle/Nozzle Orientation) Tube Side 2 DN 125 DN 125 Material No. of Tubes Pitch Long Shell Dimensions (OD x Thk) Channel Cover Tubesheet-Floating Impingement Protection % Cut Number of baffles / Shell-side path 80 27,7 406,4 x 8,8 20 19 Type ρ · v² Bundle Exit Tube Side TEMA Class Filled with Water 21 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers CAD created by WTSC Lauterbach Verfahrenstechnik GmbH 22 2013 WTS Sample Printout 2013 Thermal and Hydraulic Design of Shell and Tube Heat Exchangers 3D Tube sheet created by Alibre Design from SPIE Required: • LV Strength Calculation Software • Alibre Design 3D-CAD Lauterbach Verfahrenstechnik GmbH 23 2013
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