hex-302 0309
DESCRIPTION
Heat ExchTRANSCRIPT
Towler CH11Feed Feed 2Combined Feed Top D Bottom
T 140 38 140.253 143.8405P 6 4 4 4F 17.35608 12.68744 30.04352 30.04331 2.03E-04 kmol/hW 1791.609 464.1872 2255.7962 464.183 1791.613 kmol/hAC 13.30653 6.31E-03 1.33E+01 6.40E-03 13.30645 kmol/h
Total flow 1822.272 476.8809 2299.1529 494.2327 1804.92 kmol/hProcess
T 144 C F 16 kt/y 96.1 kg/kmolP 4 bar W 281 kt/y 18.0 kg/kmol
AC 80.3 kt/y 60.1 kg/kmolTotal 377.3 kt/y
Feed
Flow Ki zi Kizi zi/Ki Tc °CF 30 kmol/h 540478.25 0.01 7063 0.000 397W 2256 kmol/h 0.9461751 0.98 0.928 1.037 374AC 13 kmol/h 0.0017565 0.01 0.000 3.297 321.6Total 2299 kmol/h 1.00 7063 4.3Check >1.0 >1.0
H VapFlow xi hg hf hfg xi(hfg)
F 30 kmol/h 2.93E-08 x x #VALUE! #VALUE!W 2256 kmol/h 0.9745387 x x #VALUE! #VALUE!AC 13 kmol/h 0.0254612 x x #VALUE! #VALUE!Total 2299 kmol/h #VALUE!
Vap rateMr
L 19.085538 kg/mol density 967 viscosity 0.000185 From condenserV 19.335341 kg/mol 2.26 1.379E-05
ViscosityFraction vapourised 1.49 mPa.sW
Conc Datayi (mol frac top) xi (mol frac bot) yi (mol fracxi (mol frac bot)
F 0.06 0.00 0.012 0.00024W 0.94 0.99 0.987 0.96300AC 0.00 0.01 0.001 0.0367604kmol /h 494 1805 14010222 3473072
Flash CalcL/V 0.273825266493806 From distil 3.9
Ai=L/Vki Vi=Fzi/(1+Ai) yi=Vi/V xi=(Fzi-Vi)/L5.066351E-07 30.04 0.017 0.0000.2894023225 1749 0.983 0.975
156 0.08 0.000 0.025V calc 1780
L/V 0.29% diff 6.20
L 520
hfg 42.8 kJ/mol 42.82153 kJ/kg 2153 kJ/mol405 kJ/kg 24320 Mr 60.05
2254
From condenser
Design InputProcess Stream
Description Reboiler feed Vapour returnP (barg) 4 bargVapourisation rate 34844 kg/h
Physical PropertiesReboiler feed Vapour return
Boiling point 142.5 C 144Mr 19.6 Average, from DISTILTc 321.6 CLatent heat 2254 kJ/molSaturation temp - - - -
Mean overall T, areaMean overall T 37.5 CReduced temp 0.56Design heat flux, Fig 12.61 Towler 35000 W/m2Heat load (duty) 1,114,131 WArea required 32 m2
Tube ID tube 0.05 mOD tube 0.03 mL tube 1.83 mArea 1 tube 0.287 m2Number of tubes 111 -Pitch type SquarePitch 1.25Pass 1n1 2.207K1 0.215D bundle (sq) 0.508 m
Shell Type of tube sheet Fixed tube sheet, bcs vertical thermosiphonClearance, Fig 12.10 0.019 mID shell 0.527 m
Outlet pipeTotal tube CSA 0.217 m2D outlet pipe 0.53 m
PhasesLiquid density at base of HEX 967
Two-phase fluid density at tube exit Friction Loss
Static Pressure in TubesAvailable Head
dTlm 37.5 CRequired U 933 W/m2.CCalculated U BelowCheck calculated U>required U
Heat TransferCritical pressure F 55.02 barCritical pressure W 220.6 bar 22060000Critical pressure 55.02 bar 5502000 Pa
Nucleate boiling coefficienth_nb 194.1 W/m2.CVapor quality (mass vap/total), x 0.8Viscosity vapor 0.00001 Pa.sDensity vapor at tube exit 2.26 kg/m31/Xtt 49.63Pr L 1.12Mass flux, L only in tubes
Convective boiling coefficienth_cb
Design InputUtility Stream Flow bottoms (kt/y)
Liquid return Heat source T 289 Temp6 barg W 281 0.9723183 P (barg)
AC 8.03 0.0277855Physical Properties F 0.00289 0.00001
Liquid return Heat source Vapourisati 305 kt/y- - Mr 1.958E-05 kt/kmol- -- -- -
- - 180 CMean overall T, area
Tube generalID+thickness+corrosion 0.5 mmgeneral size, from 1.83m for vacuum service to 3.66m for pressure operation.
re: Tube layout sheetre: Tube layout sheet
Shell CHECK re: Fig 12.10
Outlet pipe
Phases
Friction LossStatic Pressure in Tubes
Available Head
Heat Transfer convective boiling coefficient Chen'smethod
This is for FU onlyNucleate boiling coefficient Mostinski eqn
From Condenser data
From condenser
Convective boiling coefficient
1444
293Average, from DISTIL
general size, from 1.83m for vacuum service to 3.66m for pressure operation.
P 31.66 bar P 11.71 barT 236.85 C 510 K T 186.85 C 460Hvap 1,773,000 J/kg Hvap 1,989,000 J/kgkf 0.631 W/mK kf 0.631 W/mKkg 0.0447 kg 0.0447
Duty 1,114,131 W Duty 1,114,131 WMass 0.628387 kg/s Mass 0.560146 kg/s
19.81682 17.66477 kt/y