Shell and Tube Heat Exchanger Design Spreadshe Project Item No.
Light Base Oil Feed Exchanger E-101 Service Light Base Oil Feed Exchanger
Project No. STBE for E By
Step 1. Input flows, conditions and properties data for shellside and tubeside.
Step 4. Start configuring transfer coefficients to
Tu b e
Side
Shell
Used Lube Oil
Fluid Name
Light Base Oil
Av. Density Av. Viscosity Av. Heat Capacity Capacity
14,925.1 68 163.4 54.765 92.989 0.605
Flow (M), lb/h o Temp. in, F o Temp. out, F 3 r, lb/ft m, cP cp, Btu/ Btu/lb· lb· F
4,854.5 392 150.8 51.3158 8.767 0.613
Heat Exchanged Av. Thermal Conductivity Conductivity
861,007 0.095
Q, Btu/h k, Btu/h·ft Btu/h·ft·· F
717,769 0.1098
Fouling Resistance Prandtl No.
0.004 1426.38
R, ft ·h· F/Btu cpm/k
Uncorrected MTD Corrected MTD
143.6 108.3
Step 2. Input tubing OD, BWG and length (can be trial and error).
2
o
Tube OD BWG Tube ID, d = Tube Length, L = Flow area per tube, a t = Eff Effect ective ive trtransf ansfer er are area per per tube ube =
Step 3. Estimate the number of tubes per tube pass.
Reset tubes/p
0.004 118.44
Step 5. Select tube arra and estimate shell dia
o
F F
o
0.7500 16 0.620 8 0.302 1.57 1.5711
Eq
in. in. ft. 2 in. ft
Che
Tubes/pass = lb/h per tube =
129 116
Av. velocity, fps = Tubeside Reynolds No., N Re =
0.28 13
Tubeside Fr Frict iction Fa Factor, f = DP per pass, psi =
0.219 0.02
Step 6. Check tubeside adjust tube length, nu
Nusselt number, Nr =
9.09
baffle spacing. Reme
Inside Film Coefficient, h i =
168
required.
t stablishment SETH
Date/Time
7-Nov-12
BWG/Tube Wall Thicknesses . 9 0.148 0.017 10 0.134 0.014
12:07
the exchanger. Begin with the total calculated this point (i.e., not including shellside h): Ustart = On that basis, assumed U o = Then the required transfer A = Number of tubes required = ass (Step 3), then no. of passes = Total tube count = Tubeside DP (incl. returns) = Actual effective transfer area, A =
ngement eter
Tube Pitch Pattern
72 20 398 253 2 258 0.036 405
1 Sqr
Shell ID from Tube Count Tables Select Baffle Spacing Number of Baffles = Flow Area across Bundle, as = ivalent Diameter, d e (see table) = Mass Velocity, Gs = Shellside Reynolds No., NRe =
21 5 18 0.182 0.9476 26,631 240
Shellside Friction Factor = Shellside DP =
0.00421
Outside Transfer Factor, j h = Outside Film Coefficient, h o = Calculated Uo = ck: % difference, U calc. vs Uassum. = Uclean =
0.027 8.1 55 31.2 35.9% 41.6
2 o
11
0.120
0.014
2 o
12
0.109
0.011
13 14 15 16
0.095 0.083 0.072 0.065
0.014 0.012 0.011 0.007
Btu/h·ft · F Btu/h·ft · F ft
2
psi ft
MTD Correction Factors R = ( T 1 - T2 ) / ( t2 - t1 ) =
2.528
S = ( t2 - t1 ) / ( T1 - t1 ) =
0.294
in. in. in.
2
(R +1)
½
=
2.719
( 1 - S ) / ( 1 - RS ) =
2.761
18.20 ft in. 2
lb/h·ft
-
+
-
+ 2
2-S(R+1+(R +1)
=
1.762
)=
0.161
FT =
0.754
½
psi
elocity and DP, shellside DP. If too high or too low, ber of tubes per pass, number of passes, and/or shell ber to reset shell diameter from tube count tables, as