+ All Categories
Home > Documents > HEX-302 0309

HEX-302 0309

Date post: 12-Dec-2015
Category:
Upload: qilaqrs
View: 269 times
Download: 4 times
Share this document with a friend
Description:
Heat Exch
16
Towler CH11 Feed Feed 2 ombined Fee Top D Bottom T 140 38 140.253 143.8405 P 6 4 4 4 F 17.35608 12.68744 30.04352 30.04331 2.03E-04 kmol/h W 1791.609 464.1872 2255.796 464.183 1791.613 kmol/h AC 13.30653 6.31E-03 1.33E+01 6.40E-03 13.30645 kmol/h Total flow 1822.272 476.8809 2299.153 494.2327 1804.92 kmol/h Process T 144 C F 16 kt/y 96.1 P 4 bar W 281 kt/y 18.0 AC 80.3 kt/y 60.1 Total 377.3 kt/y Feed Flow Ki zi Kizi zi/Ki F 30 kmol/h 540478.3 0.01 7063 0.000 W 2256 kmol/h 0.946175 0.98 0.928 1.037 AC 13 kmol/h 0.001756 0.01 0.000 3.297 Total 2299 kmol/h 1.00 7063 4.3 Check >1.0 >1.0 H Vap Flow xi hg hf hfg F 30 kmol/h 2.93E-08 x x #VALUE! W 2256 kmol/h 0.974539 x x #VALUE! AC 13 kmol/h 0.025461 x x #VALUE! Total 2299 kmol/h Vap rate Mr L 19.085538 kg/mol density 967 viscosity 0.000185 V 19.335341 kg/mol 2.26 1.38E-05 Viscosity Fraction vapourised 1.49 mPa.s W
Transcript

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

B10
Windows User: between bp and dp
D17
Nur Zulifle: Equilibrium

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

J13
Windows User: Assume very small
M13
Windows User: Assume very small

Conc Data

Flash Calc

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

B3
Nur Zulifle: Assumed same as bottoms stream 121
B10
Nur Zulifle: Take lowest?
B11
Nur Zulifle: take the mixture. Change units
B20
Nur Zulifle:
B22
Nur Zulifle:

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

H12
Nur Zulifle: 144!!

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

K

Towler

Towler

A 342.6397 sqftfd 0.608969 Utubefm 1.9 CS/304fp 1.1 4-6 barCb 11379.59C 17,640.67 $

0281

8.03289.03

0.000.970.03


Recommended