Design of Primary & auxiliary equipment of Diethyl ether production plant. Process & mechanical design of Reactor, Heat exchanger, Distillation column.

1. 23
CHAPTER 5
EQUIPMENT DESIGN
In this chapter, detailed equipment design and mechanical design of
5.1 Fixed Bed Catalytic Reactor Process Design:
Reaction temperature =250 0
C ( 523K)
Catalyst: γ - alumina
Density of catalyst particle: 1392 kg/m3
[8]
Catalyst porosity: 0.52 [8]
Type of reactor: Shell and tube heat exchanger type in which catalyst is placed inside the
tube.
Reaction is exothermic: It is carried out in isothermal manner. Water is to be circulated in
liquid form on shell side to maintain the isothermal condition.
Mass of catalyst required in commercial scale plant = 6579.711 kg
Superficial velocity of feed gas V=0.802 m/s
Capacity of plant =50000 MTA of diethyl ether (DEE)
Let no. of working days per annum=340 days
Production rate of diethyl ether (DEE) = (50000*1000)/(340*24)
=6127.45 Kg/hr
!""=
#$%%&'()*
2
&'()*
2
+ #1&'()*&,-(%
(5.1) [3]
"./03"4"=
#%(567%8%&'()*
&'()*
2
+ #1&'()*&,-(% + #2&'()*
2
+ #9&,-(%
2
Design equation (5.2) [3]
:
;
= <
!>
?@AB
CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC?DE9B [4]

2. 24
In table 5.1 conversion of ethanol and rate of reaction data is given. Unit of rate of reaction
is mol/(gm catalyst sec)
Table 5.1: rate of reaction and conversion data
r (total) 1/r
Ethanol
conversion
2.77216E-06 360729.1 0
2.24531E-06 445373.6 0.1
1.81423E-06 551197.8 0.2
1.45502E-06 687277 0.3
1.15111E-06 868729.7 0.4
8.90654E-07 1122770 0.5
8.31259E-07 1202994 0.525
4.67523E-07 2138934 0.7
2.9333E-07 3409130 0.8
From the graph (appendix A)
Area= 340000 unit
Weight of catalyst= 6579711 gm
= 6579.711 Kg
Bulk density =0.9333 gm/cc [8]
Volume = 6579.711/9333
= 7.049942 m3
Feed rate = 0.1382 Kmol/sec
= 0.1382 x 43.312
= 5.99 Kg/sec

3. 25
Density = PM/RT
= (1500 x 43.312) / ( 8.314 x 523 )
= 14.94 Kg/m3
Feed rate = 5.99 / 14.94
= 0.401 m3
/sec
Superficial velocity = 0.805 m/sec
Total Crosse section area = feed rate / space
= 0.401 / 0.805
= 0.499 m2
MOC of tube = Stainless steel
Tube OD = 0.0508 m
Tube ID = 0.04328 m
Crosse section area of tube = (∏/4) x ID2
= (∏/4) x (0.04328)2
= 0.00147 m2
Total number of tube required
N = Total Crosse section area / Crosse section area of tube
= 0.499/0.00147
= 340
Length of the tube (L) =total volume / (N x Crosse section area of tube)
= 7.05 / (340 x 0.00147)
= 14 m

4. 26
Area = N x ∏ x OD x L
= 340 x ∏ x 0.0508 x 14
= 764.78 m2
Heat duty (Q) = 2445180.91 J/sec
Calculation of fixed bed side film coefficient hi ;
dp = diameter of catalyst
= 0.003 m
Pipe diameter
dt = 0.04328 m
dp/dt = 0.003/0.04328
= 0.06931
(hidt /k) =0.813 e-6dp/dt
( dp G/µ) 0.9
Thermal conductivity K = 0.04366 W/mK
Viscosity µ = 1.58235 x 10-5
pa.sec
Mass velocity G = 0.87 Kg/m2
sec
On calculation
hi = 416.32637 W/m2
K
hi dp/k = 3.6(dpG/µ ε)0.365
on calculation
hi = 49.789923 W/m2
K
Take lesser value
hi = 49.789923 W/m2
K

5. 27
Calculation of shell side heat transfer, h0
Shell side heat transfer coefficient calculated here [11]
Tube pitch Pt =1.25d0
=1.25 x 0.0508
= 0.0635 m
Type of arrangement = Equilateral triangular
Equivalent diameter de = 1.1/d0 (Pt – 0.907 d0
2
)
= 1.1/0.0508[0.06352
– 0.907*0.0508 2
]
= 0.03663 m
Shell side mass flow rate m ;
∆H = m*Cp*∆T
Here coolant used is dowtherm Q because operating temperature is 523 K and dowtherm Q is
stable up to 603 K ( Properties from dowtherm Q product technical data)
Properties of dowtherm Q
Cp = 1811 J/Kg K
Viscosity µ = 1.28 x 10-3
pa.sec
Thermal conductivity K = 0.1156 W/mK
∆T= 60 K
m = 2445180.91/(1811 x 60)
= 22.5 Kg/s
Density = 927.6 Kg/ m3
Circulation rate qv = (22.5/927.6)
= 0.024 m3
/sec

6. 28
Shell inside diameter, Ds :
Db =d0 (Nt /K1 )1/n1
K1 = 0.319 and n1 = 2.142
Db = 50.8(340/0.319)1/2.142
= 1.315m
Let clearance between shell internal dia and bundle (Db),
Db = 15 mm
Let Ds= 1.315 + 0.015 m
= 1.330 m
Baffle spacing
Bs= 0.4Ds
= 0.4 x 1.33
= 0.532m
Shell side flow area As = (Pt-d0)DsBs/Pt
= (0.0635-0.0508)/0.0635(1.330 x 0.532)
= 0.1416 m2
Gs = m/As
= 22.5 / 0.1416
= 158.83 kg/m2
sec
Reynolds number,
Re = deGs/µ
= 0.03669 x 158.83 / 0.00128
= 4545.36
Prandlt number,
Pr = Cp µ/K

7. 29
= 1811 x 0.00128 / 0.1156
= 20.05
(h0 de/k)= 0.027 Re0.8
Pr0.3
From calculation
h0 = 150.50 W/m2
K
Overall heat transfer coefficient U0 ;
1/ U0 =1/h0+1/h0d +d0 ln(d0 /di)/2Kw+d0 l/di hid +d0 l/di hi
=1/150.50 + 1/5000 + {0.0508 ln(0.0508/0.04328)}/(2*16) +
(0.0508/0.04328)*(1/5000) + 0.0508/(0.04328 x 49.78)
U0 = 37.06 W/m2
K
Shell side pressure drop
Ps =8 Jf(Ds/de)(L/Bs)(ρsus
2
/2)
Jf = 0.07 from Jf vs Nre graph [11]
us= Gs/ρs
= 158.83 / 927.6
= 0.171 m/sec
= 8*0.07 x (1.330/0.03663) x (14/0.5323) x ( 985.728 x 0.0692
/2)
= 7335.7 Pa
Tube Side pressure drop
Pt =8 Jf(L/di)(ρsus
2
/2)
Jf = 0.03 from Jf vs Nre graph [11]
=8 x 0.03 x (14/0.04328) x (14.95 x 0.8022
)/2
= 0.3760672 KPa
Pressure drop across the bed
Blake – plummer equation
!
="
1.75(1 # $)%&
'
$*+,
"
P = 18.07 KPa

8. 30
Total tube side pressure drop
Pt = 18.45 KPa
5.1.1 Mechanical Design of reactor
Shell and tube type reactor [6]
(a) Shell side
Material carbon steel - (Corrosion allowance- 3mm)
Number of passes – 1
Fluid – dowtherm Q
Working pressure – 0.3 N/mm2
Design pressure – 0.33 N/mm2
Inlet temperature – 25 0
C
Outlet temperature – 85 0
C
Segmental baffles (25% cut ) with tie rods and spacers
Maximum allowable stress - 80 N/mm2
Shell thickness; [6]
ts =PD/(2fJ+P)
= 0.33 x 1400/((2 x 80 x 0.85)+0.33) + 3 mm
= 6.38 mm
Nozzle thickness (diameter -75mm)
tn=PD/(2fJ-P)
= 0.33 x 75/( 2 x 80 – 0.33)
= 0.155 mm + 3 mm
= 3.155 mm
Head
Head thickness (th) = PCrW/2fJ
Crown radius = 1400 mm
Knuckle radius = 140 mm

9. 31
W=1/4(3+ (Rc/R1)1/2
)
= 1/4(3 + (1400/140)1/2
)
= 1.54
th = 0.33 x 1400 x 1.54 / (2 x 0.85 x 80) + 3mm
= 8.23mm
Transverse Baffles
Spacing between baffles= 0.4Ds
= 0.4 x 1.4
= 0.56m
Thickness of baffles = 5mm
Tube Side [6]
Tube and tube sheet material - stainless steel
Number of tubes – 340
Outside diameter – 50.8 mm
Length – 14m
Tube pitch - 0.0635m
Working pressure – 1.5 N/mm2
Design pressure – 1.65 N/mm2
Inlet temperature – 2500
C
Outlet temperature - 2500
C
Permissible stress – 74.5 N/mm2
tf =PD0/(2fJ+P)
= 1.65 x 50.8 / (2 x 74.5 x 0.85 + 1.65)
= 0.65 mm
No corrosion allowance, since the tubes are of stainless steel.
Design of Gasket and Bolt Size [6]
Gasket material – flat metal jacketed, asbestos fill (iron or soft steel)
Gasket factor, m= 3.75
Minimum design stress = 52.4 N/mm2

10. 32
Basic gasket seating width – b 0
Internal dia. Of Gasket – 1400 mm
Do/Di = ((Y-Pm)/(Y-P(m+1)))0.5
= ((52.4 – 0.33 x 3.75)/(52.4 – 0.33 x 4.75))0.5
= 1.0032
Do = 1.4045 m
N = (1.4045-1400)/2 = 0.0022648mm use 35mm
b0 = ½N = 0.0175mm
G= (1.4045+1400)/2
= 1.4022m
Effective Gasket seating width, b= 0.5b0
1/2
= 2.09 mm
Bolts
Minimum bolt load at atm. Condition, Wm1 = 3.14bGYa
= 3.14 x 2.09 x 1402.2 x 52.4
= 483360.87 N
At operating condition,
Wm2=3.14(2b)GmP+3.14G2
P
= 3.14 x 2 x 2.09 x 1402.2 x 3.75 x 0.33 +3.14 x 1402.22
x 0.33
= 532176.24 N
Wm1 < Wm2 so Wm2 is controlling load
Number of bolts = 1402.2/(2.5*10)
= 56
Am2= 532176.24/80 = 6652.203 mm2

11. 33
Diameter of bolts = [(Am2/no. of bolts) x 3.14/4]1/2
= [(6652.203)/56 x (4/3.14)]1/2
=12.29 mm
Bolt area, Ab = 2 x 3.14 x YaGN/fa
= 2 x 3.14 x 52.48 x 1402.2 x 35 / 80
=202204.36 mm2
Pitch of bolts = 4.75*18
= 85.6 mm
Pitch circle dia.= (85.6*56)/3.14
=1526.62mm
Flange Thickness,
K= 1/[0.3+1.5WmhG/HG]
= 1/[0.3 + 1.5 x 532176.24 x 62.52136 /( 509382.1 X 1402.2)]
= 2.7
tf = G(p/kf)1/2
+c
= 1402.2 x (0.33/2.7/80) ½
+ 3
= 70.62 mm
5.2 Heat exchanger Design
For heat exchanger tube side is waste water and shell side is cooling water is used. Here we
assume over all heat transfer coefficient (U) is 800 W/m2
K.In table 5.1 tube side and shell
side fluid inlet, outlet temperature and mass flowrate values given. [11]
Table 5.2: tube side and shell side flowrate and temperature
tube side shell side
flow rate(Kg/sec) 0.6714 6.12
inlet temperature(K) 401 308
outlet temperature(K) 310 318

12. 34
U=800 W/m2
K (assumed) [11]
LMTD= [(401-318)-(310-308)/ln((401-318)/(310-308))]
= 21.74 K
Q = 256454.44 J/sec
Q = UA(LMTD)
A=256454.44/(800 x 21.74)
= 14.74 m2
Material of construction (MOC) of tube = Stainless steel
Tube OD = 0.02 m
Tube ID = 0.016 m
Length of tube (L) = 5 m
Area of tube = ∏ x ID x L
= ∏ x (0.04328) x 5
= 0.303 m2
Total number of tube required
N = total area / area of tube
= 14.74/0.303
= 49
Tube side heat transfer coefficient
Cross section area = n x (∏/4) x ID2
= 49 x (∏/4) x (0.016)2
= 0.0098 m2
Velocity (u) = 0.000692/0.0098
= 0.0706 m/sec

13. 35
Density = 969.972 Kg/m3
Viscosity = 0.000345 Pa.sec
hi = 4200(1.35 + 0.02t)u0.8
/ID0.2
= 4200 (1.35 + 0.02 x 82.5) (0.0706)0.8
/(0.016)0.2
= 3466.1561
Shell side
Water flow rate = 6.12 Kg/sec
Pitch (P) = 1.25 x OD
= 1.25 x 0.02
= 0.025 m
Equivalent diameter de = 1.1/d0 (Pt – 0.907 d0
2
)
= 1.1/0.02[0.0252
– 0.907*0.022
]
= 0.0144 m
Shell inside diameter, Ds :
Db =d0 (Nt /K1 )1/n1
K1 = 0.319 and n1 = 2.142
Db = 0.02(49/0.319)1/2.142
= 0.21 m
Let clearance between shell internal dia and bundle (Db),
Db = 15 mm
Let Ds= 0.21 + 0.015 m
= 0.225 m
Baffle spacing
Bs= 0.4Ds
= 0.4 x 0.225 = 0.09 m

14. 36
Shell side flow area As = (Pt-d0)DsBs/Pt
= (0.025-0.02)/0.025(0.225 x 0.09)
= 0.00405 m2
Gs = m/As
= 6.12 / 0.00405
= 1530 kg/m2
s
Reynolds number,
Re = deGs/µ
= 0.0144 x 1530 / 0.000853
= 25815.515
Prandlt number,
Pr = Cp µ/K
= 4184 x 0.000853 / 0.610
= 5.85
(h0 de/k)= 0.023 Re0.8
Pr0.3
From calculation
h0 = 5594.0996 W/m2
K
Overall heat transfer coefficient U0 ;
1/ U0 =1/h0+1/h0d +d0 ln(d0 /di)/2Kw+d0 l/di hid +d0 l/di hi
=1/5594.0996 + 1/5000 + {0.02 ln(0.02/0.016)}/(2*16) +
(0.02/0.016) x (1/5000) + 0.02/(0.016 x 3466.1561)
U0 = 1648.18 W/m2
K
Shell side pressure drop
Ps =8 Jf(Ds/de)(L/Bs)(ρsus
2
/2)
Jf = 0.03
us= Gs/ρs
= 1530 / 1000
= 1.53 m/sec
= 8 x 0.07 x (0.225/0.0144) x (5/0.09) x (1000 x 1.532
/2) = 234.28 KPa

15. 37
Tube Side pressure drop
Pt = (8Jf(L/di) + 2.5)(ρtut
2
/2)
= ( 8 x 0.008 x (5/0.016) + 2.5)(969.69 x 0.0712
/2)
= 54.99 Pa
5.2.1 Mechanical Design for heat exchanger
Shell and tube type heat exchanger [6]
(a) Shell side
Material carbon steel - (Corrosion allowance- 3mm)
Number of passes – 1
Fluid – water
Working pressure – 0.4 N/mm2
Design pressure – 0.44 N/mm2
Inlet temperature – 25 0
C
Outlet temperature – 85 0
C
Segmental baffles (25% cut ) with tie rods and spacers
Shell thickness;
ts =PD/(2fJ+P)
= 0.44 x 300/((2 x 80 x 0.85)+0.44) + 3 mm
= 3.96 mm
Nozzle thickness (diameter -75mm)
tn=PD/(2fJ-P)
= 0.44 x 75/( 2 x 80 – 0.44)
= 0.21 mm + 3 mm
= 3.21 mm
Head
Head thickness (th) = PCrW/2fJ
Crown radius = 300 mm
Knuckle radius = 30 mm

16. 38
W=1/4(3+ (Rc/R1)1/2
)
= 1/4(3 + (300/30)1/2
)
= 1.54
th = 0.44 x 300 x 1.54 / (2 x 0.85 x 80) + 3mm
= 4.49 mm
Transverse Baffles
Spacing between baffles= 0.4Ds
= 0.4 x 0.3
= 0.12 m
Thickness of baffles = 5mm
Tube Side
Tube and tube sheet material - stainless steel
Number of tubes – 49
Outside diameter – 20 mm
Length – 5 m
Tube pitch - 0.025 m
Working pressure – 0.5 N/mm2
Design pressure – 0.55 N/mm2
Inlet temperature – 1280
C
Outlet temperature - 370
C
Permissible stress – 74.5 N/mm2
tf =PD0/(2fJ+P)
= 0.55 x 20 / (2 x 74.5 x 0.85 + 0.55)
= 0.086 mm
No corrosion allowance, since the tubes are of stainless steel.
Design of Gasket and Bolt Size [6]
Gasket material – flat metal jacketed, asbestos fill (iron or soft steel)
Gasket factor, m= 3.75

17. 39
Minimum design stress = 52.4 N/mm2
Basic gasket seating width – b 0
Internal dia. Of Gasket – 300 mm
Do/Di = ((Y-Pm)/(Y-P(m+1)))0.5
= ((52.4 – 0.44 x 3.75)/(52.4 – 0.44 x 4.75))0.5
= 1.0043
Do = 301.29 m
N = (301.29 - 300)/2 = 0.502 mm use 35mm
b0 = ½N = 0.0175 m
G= (301.29 + 300)/2
= 300.65 mm
Effective Gasket seating width, b= 0.5b0
1/2
= 2.09 mm
Bolts
Minimum bolt load at atm. Condition, Wm1 = 3.14bGYa
= 3.14 x 2.09 x 300.65 x 52.4
= 103635.28 N
At operating condition,
Wm2=3.14(2b)GmP+3.14G2
P
= 3.14 x 2 x 2.09 x 300.65 x 3.75 x 0.44 +3.14 x 301.652
x 0.44
= 131402.52 N
Wm1 < Wm2 so Wm2 is controlling load
Number of bolts= 300.65/(2.5*10)
= 12

18. 40
Am2= 131402.52/80
= 1642.53 mm2
Diameter of bolts= [(Am2/no. of bolts) x 3.14/4]1/2
= [(1642.53)/12 x (4/3.14)]1/2
=13.19 mm
Bolt area, Ab = 2 x 3.14 x YaGN/fa
= 2 x 3.14 x 52.48 x 300.65 x 35 / 80
= 43350.36 mm2
Pitch of bolts = 4.75*18
= 85.6 mm
Pitch circle dia.= (85.6*12)/3.14
= 327.13 mm
Flange Thickness,
K= 1/[0.3+1.5WmhG/HG]
= 1/[0.3 + 1.5 x 131402.52 x 13.4 /( 31221.65 X 300.65)]
= 1.75
tf = G(p/kf)1/2
+c
= 300.65 x (0.44/1.75/80) ½
+ 3
= 23.99 mm
Use 24 mm
5.3 Distillation column Design:
Operating pressure at top = 1 atm = 101.325 KPa
Reflux ratio = 3.49
Number of plates = 40
Distillation molar rate D = 0.0327 Kmol/sec
Liquid molar rate L= D x R
= 0.0327 x 3.49
= 0.114 Kmol/sec

19. 41
Vapor molar rate = D x (R + 1)
= 0.0327 x (3.49 + 1)
= 0.1468 Kmol/sec
Vapor density ρv = 3.91 Kg/m3
Liquid density ρl = 653.64 Kg/m3
Vapor and liquid flowrate is given in table 5.2
Table 5.3: vapor and liquid flowrate
vapor liquid
molar flow rate 0.1468 0.1141
mass rate 10.8649 8.4451
vol. rate 2.7750 0.0129
Vload = Q [ρv / (ρl - ρv)]0.5
= 2.77 [ 3.91/(653.64 – 3.91)]0.5
= 0.2154 m3
/sec
q = 0.0129 m3
/sec
Single pass
Dt = 1.7 m (from graph of Vload and liquid flowrate)
System factor S = 1
Flooding factor = 0.8 ( 80 % flooding)
Flow path length L = 0.75 x Dt / number of pass
= 0.75 x 1.7 / 1
= 1.275 m
C* = 0.125
C = S x C*
= 1 x 0.125
= 0.125
Aamin = [ vapor load + 1.36qL]/ (C x F)
= [ 0.2154 + 1.36 x 0.0129 x 1.275 ]/(0.125 x 0.8) = 2.37 m2

20. 42
U* = 0.170 m/sec
U* = 0.007(ρl - ρv)0.5
= 0.007 x (653.64 – 3.91)
= 0.178 m/sec
U* = 0.008 x (Ts (ρl - ρv)) 0.5
= 0.008 x ( 0.457 (653.64 – 3.91)) 0.5
= 0.137 m/sec
Use smallest value
U* = 0.137 m/sec
u = U* x S
= 0.137 x 1
= 0.137 m/sec
Admin = q/(u x f)
= 0.0129/(0.137 x 0.8)
= 0.1171 m2
Admin < 0.11 x Aa
0.1171 < 0.11 x 0.1171 m2
0.1171 < 0.2607 m2
Admin = 2 x 0.1171
= 0.2342 m2
At = Aamin + 2 Admin
= 2.37 + 2 x 0.2342
= 2.84 m2
Atmin = 1.28 Vload /(0.8 x 0.125)
= 1.28 x 0.2154/ (0.8 x 0.125)
= 2.75 m2
At > Atmin
Take At = 2.84 m2

21. 43
Diameter = (At x 4 / 3.14)0.5
= (2.84 x 4 / 3.14)0.5
= 1.9 m
Ad/(AtN) = 0.2342/(2.84 x 1)
= 0.0823
Weir length
Lw/Dt = 0.657
Lw = 0.657 x 1.9
= 1.25 m
Weir hight
H/ Dt = 0.12
H = 0.12 x 1.9
= 0.228 m
Number of valve units
Assume 120-175 units/ m2
active area
Active area = 2.37 m2
Number of units = 285 to 417 units/plate
Assume
Number of units = 350 units/plate
Holes area = 350/845
= 0.4142 m2
Pressure drop
Tray MOC – MS density = 7700 kg/m3
Thickness of tray = 14 gauge = 0.188cm
Type of valve V4 K1 = 2.73 K2 = 13.6
∆Pdry = 0.135 tn (ρm /ρl) + K1Vn
2
(ρv /ρl)
= 0.135 (0.188)(7700/653.64) + 2.73 (6.692
)(3.91/653.64)
= 1.032 cm liquid

22. 44
∆Pdry = K2Vn
2
(ρv /ρl)
= 13.6 (6.692
)(3.91/653.64)
= 3.65 cm liquid
∆Pt = ∆Pdry + 55.4(q/Lw)0.67
+ 0.04hw
= 3.65 + 55.4(0.0129/1.25)0.67
+ 0.04 x 50
= 8.44 cm liquid
= 0.076 psi
Hde = 55.4(q/Lw)0.67
+ 0.1 hw + (∆Pt + 1.66)( ρl / (ρl - ρv))
= 55.4(0.0129/1.25)0.67
+ 0.1 x 50 + (8.44 + 1.66)(653.64/(653.64-3.91))
= 17.96 cm liquid < 0.6 TS
%Flooding = Vload / (0.78ATC)
= 0.2154 / (0.78 x 2.84 x0.125)
= 77.60%
5.3.1 Mechanical design of distillation column
Mechanical design of distillation column including support. [14]
Operating pressure = 101.325 Kpa
Design pressure = 1.1 x 101.325 = 111.45 Kpa = 0.11145 N/mm2
Design temperature = 423 K
MOC = carbon steel
Diameter = 1900 mm
Thickness of the column
tc = PD/(2fJ - P)
= 0.44 x 300/((2 x 80 x 0.85) - 0.44) + 3 mm
= 3.065 mm
But take 8mm
Head
Torispherical head [6]
Head thickness (th) = PCrW/2fJ
Crown radius = 1900 mm

23. 45
Knuckle radius = 190 mm
W=1/4(3+ (Rc/R1)1/2
)
= 1/4(3 + (1900/190)1/2
)
= 1.54
th = 0.11145 x 1900 x 1.54 / (2 x 0.85 x 80) + 3mm
= 5.39 mm
Use 8 mm same as column diameter
Total vessel dead load
!=("!+0.8#$ )%&'
= 1.15 x 3.14 x 1.9 x (19 + 0.8 x 1.9) x 0.008 x 7700 x 9.81
= 119736.89 N
Column support design
Skirt diameter = 1900mm
Stress due to dead load
Fds = W/(D + t)t
= 119736.89/(3.14 x (1900 + t) x t)
Stress due to wind load
Fws = 11071.56/(3.14 x (1900 + t) x t)
Total compressive stess = Fds + Fws
Maximum stress = 0.125Et/D = Fds + Fws
E = 190 N/mm2
By solving this
t = 41.42 mm
So take thickness 45 mm
For this thickness
Fcompressive < Fs
Ftensile < Fs