11275 kg/h 11249.5Streams Hot Cold (Water)Tin 144 C, Tb 30 C kTout 142.5 C, Td 45 C cpxF @ 4 bar 0.057 mass Td 142.5 TbFlow 99 kt/y 98.40 kg/s miuQ 6,349,634 W From DP1 16,604,000 PrFouling factors 5,000 W/m2K 4.26E+03 W/m2K 2.35E-04Physical Properties F W g Wfrho 4.20882 kg/m3 2.35 kg/m3 919.1176Viscosity u 1.49E-03 Pa.s or Ns/m2 1.38E-05 Pa.s 1.85E-04Thermal cond, k 0.002 W/m.K 0.030 W/m.K 0.688Cp 1740 J/kgK 2291 J/kgK 4302Pr 1163 - 1.075 - 1.16Hvap 445416 J/kg 2123000 J/kg -

TEMA Type Serth CH11aisi 304, k 21.4 W/mK eg:50

Overall U estPerry 637 700 1000 Ulrich Table 4 500 600U 1100 J/m2K Trial 1 700dTLM Water dT 5-20dTH Dew pt 99 S 0.13157895dTC 112.5 R 0.1Top term -13.5 13.5 F 0.99Bottom -0.1 0.1 Actual dTLM 104.6dTLM 105.6 105.6A Q=FUAdTA 56 m2

HEX TypeLayout S&T Ulrich 194

U-Tube cheapest, removal bundle, tube cleaning outside and insideShell E smaller

Tube Side CoefficientTube material Steel 304 cp material 515 J/kg.K

kL, condensate thermal cond 0.688 W/mCInner d 0.019 m min 0.05 m max

Wall thickness 0.0026 tube pitch 0.0625Inner d 0.0474 m OD 0.0500 m

Lt 2.899767176275 m Nt 129 -Loading 0.154 kg/s m

Re,c 3338Figure 12.43 0.18 [] term 3.739708E-15

B-K method hc 7,978 W/m2C **hc CR717 3,578choose higher hc 7,978

Tube bundlePass 4KL, pitch constant 0.18 for 4 pass 0.25

nL 2.29 2.21Bundle d, Db 0.90 m

shell sidehead U tubeBaffle type double segmental less Pdropbaffle spacing 0.919 m 45 % cutBaffle cut 0.45Clearance 0.019 m 19 mmShell ID 0.919 m

Shell Side Coefficient: KBBFlow shell 101 kg/s

rhoL 1000 kg/m3Area for cross flow As 0.1688

Mass velocity, Gs 597Equivalent d sq 0.049

Re sq 33,183OR hs, w/o miuW triangle 4,228 KBB

Overall Uho 4,228 W/m2Khof 4255 W/m2Khi 7,978 W/m2Khif 5,000 W/m2KMaterial, kw 21.4 W/m2K1/U 8.8E-04U 1140.1 W/m2K

Compare U: within 30%dU 3.52 % limit -30 30Check 1.00 TRUE

Tube side dPu_t 6.08 m/s 5Tube L/D 61j_f 0.09 - 9 - re:12.23 sinnotmiu/miuw 1 Neglect viscosity correctiondP_t 7779 Pa 40,000 Pa guide:0.1*absPCheck 1.00

Shell side dPu_s 0.60 m/s 1 31-Dec 0.3j_f 0.43 -miu/miuw 1dP_s 33021 Pa TRUE

CW 185 kg/s5827 kt/y

BP50 W/mK F 100

4186 J/kg W 161.7144 Azeo 97.85 C @1atm

8.90E-040.07 Reboiler 18,918,000

m2.K/WWf Mixture g Mixture f g 9.81

kg/m3 2.26 kg/m3 967 kg/m3 Air rho 1.2754 kg/m3Pa.s 1.38E-05 Pa.s 1.85E-04 Pa.s Mr F 0.09609 kg/mol

W/m.K 0.030 W/m.K 0.688 W/m.K a 0.008322J/kgK 2260 J/kgK 4156 J/kgK b 0.4228

- - 1.12 - c 637.87- 2,027,378 J/kg d 520200

http://www.stainless-structurals.com/wp-co 0.0298Overall U est

Towler 799Ulrich pg 190

(t2-t1)/(T1-t1) 1: in(T1-T2)/(t2-t1)Perry 11-9, 1s 2t

HEX Type

cheapest, removal bundle, tube cleaning outside and inside Table 3.1 SerthTable 3.2 Serth

Tube Side Coefficient Eg 12.5 c&r

condensing h only or need to calc separate tube h?OD 16,20,25,30,38,501.6, 2, 2.6, 3.2 mm pg 645

5 10 Lt/Ds limitLt/Ds 3.15607 Lt 1.83 m, 2.44 m, 3.66 m, 4.88 m, 6.10 m, 7.32 m

0 1 2.899767

Tube bundle

for 2 pass CR Table 12.4

shell side

Serth pg 86baffle spacing, lB=Ds for condensersSinnot e.g.re:figure12.10 Sinnot

Shell Side Coefficient: KBB

miu Wall(pt-do)/pt: ratio clearance b/ntubes & distance tube centres

Gs*de/miu

Overall U

Compare U: within 30%

Tube side dP10 typical

re:12.23 sinnotNeglect viscosity correctionguide:0.1*absP

Shell side dP1 limit

re:12.20 si re: Fig 12.30 SinnotNeglect viscosity correction

35000 limit

Another source of pressure drop will be the flow expansion and contraction at theexchanger inlet and outlet nozzles. This can be estimated by adding one velocity head forthe inlet and 0.5 for the outlet, based on the nozzle velocities.

Towler

Another source of pressure drop will be the flow expansion and contraction at theexchanger inlet and outlet nozzles. This can be estimated by adding one velocity head for

Couper Walas //Towler 2013Silla 2003McMahon 2014One HEXA 600 sqftfd 0.585 fixed headfp 1.10 dependent on Ag1 0.82 steel 304g2 0.16fm 1.90 cs & 304 ssfp 1.00 dependent on PCb 15271CostUnit 1C per unit $22,656.65Total cost $22,656.65

Figure 12.3 Sinnot

Towler

Couper