(feasibility table)phd thesis hohmann done

8/11/2019 (Feasibility Table)PHD Thesis Hohmann Done

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OPTM NTWORKS FOR AT XCANG

b

wa Chals ohann J

A Disstation Psnt to t

FACLTY OF T GRADAT SCOOL


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NS F SN FN

TH E SHOOL

NIVERSITY PAR

LOS ANELES ALIFORIA 000

hs dssertaton, wrtten by

g

9._;* M!.-

under the drecton of h.i... Dssertaton om-mttee and approved by all ts members haseen presented to and accepted by he Graduate School n paral fulllment of requre-ments of the degree of

DOCTOR OF PHILOSOPHY

Date .Yn_:7J


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ACOWLDGMNTS

I wish to xss my gatit to all th ol

who hav hl in th oltion of this isstation

I a sially int to D F J Lokhat who hasgivn so fly of his tim ing th os of th

sah Th oth omitt ms D J Rtan D L L any hav also n vy hlfl

Aitionally I wol lik to aknowlg thfinanial hl fo Gilltt-Pa Mat oany ing th

io Coting svis ovi y th

Systs Silation Laoatoy at th nivsity of

Sothn Califonia a also gatly aknowlg


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TABLE OF CONTENTS

Page

ACOWLEDGMETS

LIST OF TABLES

LIST OF FIGURES

. . .

. . . . . . . . . .

. . . . . . .

ii

v

vii

NOME NCLATURE

ABSTRACT

CHAPTER

I.

xiii

INTRODUCTION

II ELEMENTS OF AT EXCHANGE NETWORKS

1

7

8A. Heat Exchangers

B. Uilities for Heating

c Uilities for Cooling

. .

. . .

. .

.

18

21


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Pe

V CASE SES EWORK ESGN 7A pe Ss te o f or Proces s Str es 7

B pe C Sste of Sx Process Stres 7 2

. pe Ss te o f S x Pro ce ss Str es 84

V HEA EXCHAGE EWORKS N OPERAOA SteStte Response to epertre

Chne s . . .

B Ste-Stte Response to Cpct RteChnes . .

. e rn Responses . .

V COCSOS . . .

REERECES . . . . .

APPECES

A Gossr . . .

93

93

100

02105

10

108

109


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Tbe

I

II

III

IV

VI

VII

VIII

LIST OF ABLES

DATA FOR SIMPLIFIED THEE STRE EMPLE

FEASIBILITY TABLE FOR TEE STREAM EPLECASE WITH mi 0 F

o

FEASIBILITY TABLE FOR THREE STREA EXMPLECASE 4 WITH min 20 F

FEASIBILITY TABL FOR HREE SRE EPLECASE 4 WITH Omin = 10

MINIM EA TABLE FOR

CASE 1 MINIM AREA TABLE FORCASE

MINI AREA TBLE FORCASE

Fo

THREE STREAM EPLE

THREE STREM EXPLE

THREE STRAM EXPLE

DATA FOR SREA CONTETION EXPLE

Pge

33

4

37

4

4

4

45


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Tbe Pge

III RATE SENSITIVITY F NETWRK SHWN INFIGURE 19 101

XIX EMPLE CALCUTIN USING RATE SENSITIVITY 103

D-I ECUTIE CPUTER PRGRA 132

D-II SUBRUTINE PSDATA 133

D-III SUBRUTINE DELTA 136

D-I SUBRTINE BALNCE 137

D-V SUBRUTINE RANGE 138

D-VI SUBRUTINE MIUTY 139

D-VII SUBRUTINE IN 13

D-VIII SUBRUTI CIG 147

D-IX SUBRUTINE PATH 152

D-X SUBRUTINE EXCHNG 155

D-XI SUBRUTINE DIVIDE 158


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Fige

!A

B

C

D

2

3

LIS OF FIGRES

Netwoks o Singe ocess Ste ype ASte Syste

Netwoks o One Soce n One Sink ocess

Ste ype B Ste System

A ossibe Netwok o One Soce n SeveSink ocess Stems o One Sink n SeveSoce ocess Stes ype C Ste Syste

A ossibe Netwok o Seve Soce nSeve Sink ocess Stes Type D Syste

epete Rnges o hee Ste ExmpeCse 2

Lck o Tepete Contentin in heeSte Expe Cse 1

Rnge o Tepete Contetion in hee

Ste Expe se 3

ge

28

28

2 9

29

3

0

40


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Fiue

14

1 5

1

1 7

18

19

2 0

2 1

Feasibe Netwok Space fo pe D SsteExape

Effect of Miniu epeate of Appoac onCosts fo pe D Sste Exape

Entap Dia fo pe D Sste Exape

Netwok Sntesis sin Entap Diaa ofpe D Sste Exape

Netwok Afte Lee et a

Netwok Snte s ized si n te EntapDiaa

Entap Diaa fo pe C Sste Exape

Netwok Afte Westbook

2 2 Feasibe Netwok Space fo pe C Sste

2 3

Exape

Netwok Sntesis wit Cude Stea Diided

into Fou Bances

Pae

7 0

7 1

73

74

7 5

75

7 8

79

8 0

8 2


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Figue

A-3

C-2

3

C-4

C-5

C-6

o eat Loa Loops Counte-Cuent eat ane

Thee Stea Counte-Cuent eat Tanse

ee Steam Syste with empeatueContention

Miniu Aea Netwok

A Stea Syste ich Reuies eatxchanges in Seies

A Steam Syste ih Reuies eatxcanges in Paallel

age

11423

2 3

24

125

26

26


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NOENCE

y f h rm d phr d h dr

hv b gv pc mg wh ppd

chg wrk h b cry c hr pry pcfc vcbry drb m f h

ccp dvpd Sm f h rm hv b dg

d by ymb d ppr h Nmcr; hwvr

fr p f h rm ppr

Gry ppd I

bc

h chgr c prmr

rfr r f chgr k


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M

N

- miniu nub o xangs qui to

onstut a at xang ntwok o agivn stam syst.

- nub o xangs qui o a ntwokwit t iniu total at tans aaA*.

oiints in t tpatu viationquation o sou stams

- oiints in t tatu viationquation o sink stams .

nub o sou stas in a givn sta

syst inluing utility stams .- nub o sink stams in a givn sta

syst inluing utility stams .

- nub o tans units in a givn xang .

- at tans in xang k


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Toutput

the deviation from the design value for the

temperature at point i,f tactual tdesign

input tperature of a given stream to aheat echange netork

outlet temperature of a given stream from a

heat echange netork

deviation of a stream's temperature from the

design value, = Tdesign - Tactual

overall heat transfer coefficient forstreams i and

eight rate of stream i

temperature dierenc at n point in anexchanger, tsource - tsink

smallest minim temperature of approach for

an exchanger in gven netork


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ABSTACT

Ecoomic operaion o mern chemical processes re

quires ha he pars o he process wih excess hea be

couple o hose ha requre hea is hermal couplin

is accomplishe hrouh he use o hea exchaners Te

hea exchaners, heaers a coolers in moern plans orm

hihl inerae an complex neworks

Te cos o such hea exchane neworks epens no

onl on he pairin a sequencin o sreams exchanin

hea, bu also on he amous o upplemenal heain an

cooli use perai coss are primaril a uncion o


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with het exchge etwrk t evep prctic

etwrk eig eth he reerch h hw tht there

exit " j uxtptiu r egi " i which if fere t eigs

ct be itiguihe cst bi becuse f t

ucertities itgibe Bus this regi c

be c cute " ecic ptiu etwrk es ig i

e whi ch ie withi thi j uxtptimu regi

Utiizig e f the theryic spect f the

prbe it i pibe t ccute bu fr etwrk e

ig Fir t eth h bee evepe fr eteri i g

the iiu ut temperture eve f utiity

tres require Se cy it i pibe t c c ute


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eork desgs ca be deermed by comparso o dea

ms addo o comparso o eac oer

o cocude e researc, severa meods o e

ork syess ere epored ad e bes pars o eac

amped Meods ere aso deveoped o mprove gve

eork desgs ad o predc e eec o sream

cages o eork operao Numerca eampes are used

o usrae e desg ad operao o ecoomc opm

eorks


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TE I

INTIN

I a oder peroe refer or ceca pa, a

arge fraco f o e a capa vee ad

e cog operag co ca e ared o e

pp ad reova of ea . To redce co

proce deger ae e of ea excage ewe e

o ad cod proce rea addo o eag ad

coog b e . Te reg grp of ea ex

cager, cooer, eaer, reoer, codeer ad/or

frace are p caed e excage ewor


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be rewarding to develop the best esigns Such is the

case, since cnsiderabe cost ifferences can result in

network designs depending on the pairing and sequencing

of the streams exchanging heat

2

e technica literature contains informative

articles on design and optimization of individua heat ex

changers but there is ittle practica information on de

sign or optimization of networks for heat exchange e

iterature that is availabe has been groupe in an anno

tated bibliography (Appendix

i dissertation divides the probe of heat ex

change network design int a number of parts for analysis:


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network, i.e. to find h changes i iput

variables affect outts for a iven fixed

etwork

3

T stucturing or synthesis of a network (Part (a)

of the process dsign problm) is very difficut in all

but the most simple cases is is a irect result of the

astonishing nuber of technically possible networks if

ore than three or four process streas are consided

Recently several authos have trid to foruate the nt

work synthesis probl so that it could b sov by opera

tions esearch technies Hever, these forlations


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4

opimiaio chiqu a w Herei ie ecod

difficuy for e proce gieer The ouio ech

iqu are im coumig v oug doe o hig pd

digia compur

e ecod par of h proce deig probem {b)

ca oy be aemped afr h work a b ruc

urd Ti probem i more coveioa ad chiqu

uch a dyamic prograig hav be ued o opii

giv ework Hever h copuig co for he

echique i ao uuay i hig

Par (c) of h proce eig probem provide h

i i d i Wih


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5

efe o an poin wihin his jua-opi egion as

he opiu e auho has developed seveal copue

aided echniques fo finding his ua-opiu egion fo

hea echange newos ese echniques ae fleile and

a e used a each sep of he design pocess o oain

he juaopi o he accuac pemied b daa and

ie liiaions

Realisicall, he acual design of a cheical

plan o a peoleu efine uni poceeds in seveal

seps and so s he design of an associaed hea echange

newo In he iniial o concepual sep he enginee


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emphaszes the ntal desgn of heat exchange networks

e last part of the network desgn proble con

sdered s not often nclded n optmzaton stdes

That s how does the nt respond to transents and/or

steady-state process changes? e "operablty of a

process can be of great mportance n ts start-p and

economc operaton Operablty shold be consdered

drng ntal desgn stages and not left as a problem to

be soled later e athor has ade a stdy of the ef

fect of process changes on heat exchange networks and has

deeloped me general crtera whch shold ad the

6


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CHAPER II

ELEMENS OF HEA EXCHANGE NEORKS

o fcilitt study ht xchng ntworks r

considred to b cposed of individul building blocks

or lmnts which opert on th ntwork procss strms

s lments hv bn grouped into four bsic typs nd

ch type is discussd in section of this chptr

individul lnt typs hve ben studid xtnsively

in the litrture but r reviewd re to surize thir

most importnt chrctristics In network t lemnts

do not oprte indpndently but th prformnc of ch


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8

detiled techniques cn be used to finlize the best design

for ech element Hoever it should be noted tht the

desgn ltitude is not ver gret in the finl project

engineer ing stges

Het xhnger s

Generl D scription

Het exchngers re unique group of netork ee

ments since the m be described s the nodes of the net

ork nd the onl plce ithin netor here het trns

fer is considered to tke plce A het exchnger m be

brodl defined s n pprtus in hich one fluid trns


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In ractice te first fuid fls troug a bunde of

tubes e te second fuid fls on te outside of te

ube bunde and is contaned by an outer se Actuay,

many variations of te basc se-and-tube design are

utiized as described by Perry (15) and oter sources

ese varations are made in an effort to otimize te de

sign of an individual excanger for te articuar service

anticiated Te tree most mortant factors affecting

tis otimization are usualy: eat transfer area, res

sure dro across te excanger, and maintenance costs

Maintenance costs are rimarily a functon of material of

i d f d bl d l i f


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value can hen be use o characerize he excanger for

iniial rocess cos evaluaions Exchanger ressure ro

is also usually esablishe so ha exchanger esign an

uing requireens can be deermined

ssuing a simlifie dble-ie moel for he

hea exchanger one can wrie for each ifferenial seg-

en of he excanger a seaysae hea conucion

equaion:

(II

I is also ossible o wrie a ea balance for boh fluis

in e ifferenial secion of he exchanger


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Solving Equation II for dq and substituting gives

d9U9d

9outlet - inlet>

qexcanger{II4)

fter rearrangement te wole excanger may be modeled as

outlet

d 9outlet inletue qexcanger

xchanger

d

(II5)

fter integration wit constant and rearrangemet

inlet - 9outletq U

l

n

i

n

l

t

o

u

t

l

t

UQ (II6)


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an compensate for ing an other effects

For esign cacuations invoving other than the

oube-pipe f geometry a correction factor F is

custoariy incue in Equation II6 to correct the og

mean terature ifference to the true integrate

temperature ifference for the new exchanger geometry

us Equation II6 becomes:

q = A9 II8)

eoreticay F may vary from to se ow vaue but

in practice few exchaners are buit with an F vaue ess

than 85 is is a resut of the reative costs esign


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3

ount of het trnsferre uh rtin or simution

utions ou be one usin ution however

n i nvove tr i n err or soution wou be r eui re

ortunte n e ff i ient ir ect soution r t in

metho hs been eveope b Ks n onon (7). he

het tns fer r te euti on ) n n energ eution

2 ) re the two esript ive eutions for het ex

hne r hese eutions m be roupe s bove or re

written usin sever imensioness roups t hve phsi

s in if ine xh nger het tr ns fer e f fetivenes s

e ) i s efine s the r t io of tu het trnsfer r te to

th th i i it i h t t f t


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14

smller strem cpcit rte (Cin> in the echnger under

considertion e number of het trnsfer units Ntu is

n epression of the het trnsfer size of the prticulr

echnger nd is defined by

lO UdA in

U

in(II10)

Cpcit rte rtio is the rtio of the smller to the

lrger of the strem ccit rtes Like echnger ef

fectiveness, cpcit rte rtio is never greter thn

unit nd equls zero if one of the two strems is vpor

izing or condensing


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15

1 0 exp u

l R

= R _ exp u l.OR) o 0 o R = 0 0 II2

o u s e h boe expes s on s n n exhn ng

lulon one hou po ollos:

l u o enon gen n

Eon II0

2 lule R o Eon II1

(3 Dene e o he pul oe u

n R lu es o s pl ouneu en

oub le ppe exh ne us e Equon I I2


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6

fr the sae fuids r frm a previus desin alulatin

three fat rs miht hane it ir st , i f vei t of the

f ui ds thruh the exhaner is hne , U w i l ar . A

r uh r ue is that U vr ies as the rat io f the st ream

rtes t the 0 8 pwer , with an inr ea se in rate eadin

t an increased The seond fatr is ar iat in in f u i

prper ti es due t a hne in fu id temper ature s . If fui

vis c si ty der eases , e o it thruh the exhaner w i l

either remain nstant r inrease for a fixed pressure

drp . hanes in issity an be pronouned with heav

petr eum i s . Lsty the ndit in of the heat ex

hner ( ean r fue d) hs a s in i f iant e ffe t n the


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As mentioned earlier these three facors are manipulaed

in he design o individual exchangers to ry ad arrive

at a minim cost for a given service Hever, they

may not always be reely varied and if, for examle,

stainless steel tubes are required because of corrosive

streams, exchanger cost wil be doubled In addition

shipping and installation can add significanty to the

initial cos of heat exchangers

I materials o construction are ixed, exchanger

17

cost can, as a first aproximaion, e related o area as:

D aA

b

c {II-13 E


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18

e ul o ppox e u he o el e o

nu o exhnge un well o he ne e

To o e le op e eono nl o h e ex

hnge newo nenne o o he exhnge

houl e n lue

B le o Heng

eleen o he exhnge ne wo u l e e

onee o poe n nee wh exenl oue

n n o he I h ou gh he u le o he

ng h he l ene g o he p o he n e

wo h e e h ghe epe u e ene g h n l


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1

ac le y ooe ( 1 saze s soe o he e s a

oea coseao s . Feely , las have hee

levels o sea hea avalale : hh es se (00 s ,

lo esse (100 s a eas hese levels o

seam esse ove a ealy eal hea e h

he eeae ae o ao 00 o 00F Seam

sally sasses all he hea e hs emea

e ae ecas e o s avalaly , saly , c os ,

h eaaso caacy , a s aey

ees a mehas ve cos es o ocess

les a s ees o oe ha se o

he hhe esse l evel hee s a e lave ly sal l cos


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0

syses ae eely se. Dhe A s a ola l

o hs ose e he age 00 o 0F . he cos

o ho ol syses s c os eal hghe ha ha o

sea ae o he la so sys e Fo he

ho ol syse s ec ess ay o have a seaae heae ,

ho lg a ae e sevos a s . Heve , o he

avaages o hghe eeae asece o ae (

soe a lcaos ho ol s se .A h ye o ly hch s oe se o

heag ocess seas o hgh eeaes s he ec

e heae. I eole eg he heae s calle

a e o es ll heae os heaes ae l h


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he ocess sea le es emeae s cease

o a xe le emeae o oose eecs ae

lace a salle heae ll e ee ecase less

hea s e ee , he le as es leave a a hhe

eeae h oe hea los he as . s , hee

1

s a ecooc ae o he eece sac as a

oces s sea eeae he ae l l vay o cos e ,

ee o hea a el coss A ossle movee

h e o ees heaes s o ha oe l coole col l hoh he covecve seco hle aohe

l hoe loe he aa seco.


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scsses he ee cool syses a soe o he

eas os o choos eee he .

heoyacally hea ss ae he o ae o

hea soces . he vale ee s o he ay o

eey he s ca ac ce he l oes eeae a hch

eey ca e accee a he chae s eeae

as ac ces eey . oeve shol e oe ha

h vay s a soce sea eeaes he o

le o ae o acco o he cos o eey as

ee a a ve hea exchae a eo s vey

cl.

I ece yeas a cool has cease avo


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23

ass o ecc lae hoh coo l es . Booe scsses soe o he ecoocs volve he s

o a cospo o ly ae lae pocess

plas . He caes ha ly ae ca cosly a

ha ae cosevao s poa oh he es

a opeao o plas .

Ocehoh cool ae s o se as ch as

oce as ecase o le soces . e a avaae

o ocehoh cool ae s s l epeae he

copae o close cycle cool ae hch ca eve e

coo le ha he e l a epeae . Paccally

ecclae cool ae s avalale eee 80 a


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wa o a cool a h cos cass aply as h

s pau s low Bcaus o hs ga

cool s us oly wh cssay a h a a pa

u ll us l ha ha u o h pocss

sa Ds a opao o h sys o po

ga cool usually cs uch ao

caus o h coss ol

D cocos

cocos s h oa m us o goup

h ls ha coy h pocs s sas houh a ha

xchag wo c lu hs oup a pp


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5

a o aly copa Gally , ppg a o

coss wll g o wos olg o a

cags us a s appoao mg o la

coco coss o um o a cags

ly , s s a oug sao u s oa

o cos sos sgca c coss

as soca a cag os .


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HAPTER III

ANAYSIS OF STREAM SYSTEMS

The purpse f ths chpter s t pvde n dey

fmewrk tht cn be used t vew nd pce n pespectve

the vbe s s s ted wth ne twks f het exchne

In ths context vbe i s bod def ned to en nt

n ths e quntt es tht v contnuus but s

thse which chne fom ne dscete stte to nothe

Identfctin nd chcteztion of vbe intec

t ins desc be the ste sste es ibe so ution spce

Once bounds hve been est bi sed n the s utn spce

netk desns cn be effcient ppsed nd ccutey


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7

spciid according to tpratur ll an possilyaxiu aounts aai lal or th syst rtr ic tions

ar coplt .

Onc a coplt st o syst rstrictions has n

g in a str a sys t can di nd . Th str a syst

is th coination o th gin procss stras plus th

chosn aounts o th aail al uti l it is . Thrmoynam

ic a ly th syst rs tr i ctions din a low syst y

spciying liitations iposd at th systsurroundings

oundary. aditional undrstoo spciication is that

thr is no hat low twn syst an surrounings x

cpt that coupld with sra low . That i s hat is onl y

xchangd at spci i hat xchangr s . Actually any


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SouceStream

S n Stream

ef ge ran t oo ng Wa te r

Process

Hot 0 St eam

F g ue A Ne twos fo a S n ge P roce ssSteam ype A Steam System

Pocess Process

P

2 8

A

F e dFunace


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D E

A

U t t y

F gu e A Po b e Netwo fo One Souce and

Sevea S i n Poce Steam One S n and SeveaSouce Poce Steam ype Steam Sytem

D E

2 9


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3

sour or sink procss stram A utility is usd to cool

or hat th str am i a pro css uti li xchagr . Thr

is no choic as to h xchangr ha load ut slction

o th typ o utility can ad As discussd i

Chapr ach typ o utility usually xcls or a

crtai tmpratur rang Howr this rang dpds

sowhat o currnt uility and xchangr costs ad will

ary ro plat to plan as wll as wih tim Prhas

th most ailiar xamp o Typ A stra syst optimiza

t ion is th choic tw air or ar coolr s

Stra s Tp B cosits o two rocss stras

o sourc stram a on sik stram plus chosn utili

t i s ) Th hat xchag works or syst Typ B


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3 1

hper IV.

Sr e s s t e pe n be ons der bl ore o

pied hn pes or B pe onssts o onesour e , se ve r s nk sr e s , nd t l i es or one s nk ,

se ver l sor e s r e s , nd u i e s . eworks o pe

sstes re r s he he exhne trn n rude

ds ti ll ton unts or s lqueon pl nts . Re t ve l

i e l i er ur e i s v bl e on the s nhes s nd opt

z on o pe nework s . Pe (14 ) for expe , pr e

sents so e q t i ve r ue s o be us ed i n the des n o

oolers whe Wesbrook (17 ) llus tr es the use o

dni pro r n o op ze i ven n etwork . he best

ppr o h ppe rs t o b e ht o Wh is tler (1) He uses


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3

three trem ytem The next two ection o thi

chpter be their dicuion o networ bounds on the

thre e str em exmple preented in Tble ote tht the

het lod of the two our ce s tre m A nd B) i eual i n

mgnitude to the het lod of the in tem (C) or the

exmpl e The term inl tepertur e given in Tble

de ine our exmple ce The igni i cnce o these

our ces nd the terminl tempertures given i di

cued l ter in thi chpter

B Syte Feii lit

The irst uetion tht should be nswered or

i t t i h th t it i ibl t


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3 3

TBE

DT O M ED THEE TEM EXME

Capac i t ate Heat oadteam C BTUH)

Q

MM BTUH)

70 , 000 7 . 00B 48,000 - 9 . 60

5 5 3 3 3 1 6 6 0

UC 0 0 BTUHt2 UBC

1 0 0 UHrt2

Termina Temperatre )

Cae 1 Cae 2 Cae 3 Cae 4tream n O t n O t n O t n O t

650 550 600 500 500 400 500 400 B 550 350 550 350 550 350 550 350

4 1 4 4 5


50/206

TBLE

E B L TY TBLE OR TREE TREM EXMLE CE 2 W T

9 = 20

mn

Rane#

1

2

3

4

5

oce team in teamTemp ame

( OF )

600550

5 50 - 500B

500450 B

450350 B

350 1 50

Q Temp ame Q QMM BTU) (0F ) MM BTH) Rane

3 5 0 5 30-5 80

3 5 0480-530 5 90 2 4 0

2 4 0 430480 2 4 0

4 8 0 330430 5 5 3 073

1 30330 1 1 0 7 1 1 0 7

Q Tota 0 0

Raneea i b i i t

0

0

0

0

0


51/206

3 5

ne f the tre in the rnge i l given A bln

indicte there re n trem in the given range Given

next t ech tre ne i the enthlpy chnge ( ) fr

the tre r the given teperture rnge.

Feibility tble re cntructed by tarting with

the highet teperture tre in the yte nd prgre

ing dwnwrd in teper tur e leve l A new r nge i tart ed

e ch tie tre (ur ce r ink) i encuntered . A

new r nge i l tr ted whenever the ter in l teper

ture f tre i reched. Figure give a pictrial

view f the f ive teper tur e r ange r Ce

The ttl het ld fr ech teperture rnge i

diplyed under the heding Q Rnge in the feibility


52/206

36

feaibi l ity colun i all e ro a in Table II then i t

i feaible to contruct a networ in which echanger

have at leat a F in iu tper ature of approach

On the other hand the range feaibilit column i

not alway all ero Table III contructed for Cae 4

of the Three Strea Eaple ha a te range feaibilit

column which annot be ade all ero Thi occur in

pite of the fact that the eaple i in overall heat

balance at the tabl e how i that in the fir t teper

ature r ange ther e i ore in capacit than can be ued

Liewie in the econd teperature range there i more

ource capacity than an be ued b an of the lower te

per atur e r ange Thu i t i impoibl e to contruct a


53/206

3 7

AB L E

FEAS B L Y ABLE FOR HREE SREAM EXAMPLE CASE 4 W H a . Fm n

Soue Steams S i n St eamsRange ems Name Q emps Name Q Q Range# ( F (MM BU/H ( F } MM BU/H} Range Fe as i b i i ty

B 4 480 - 530 2 . 77 . 7 . 7

4A 7 . 848 . 6 7 -0 . 37B 4 .8

400- 350 B .4 330- 380 . 77 . 7

4 . 5 . 53 Q o t a l .


54/206

38

tepe tue of ppoch The nbe o nges in e s i -

bi li t tble i s of no pt icul s igni ine , eet to

indicte the nbe of difeent te teinl tee

tues The eltionship ong iniu tepetues o

ppoch util it eui eents nd netwo costs is

discus sed in Sect ion D of thi chpte

The bove pocedue o deteining the esibilit

of constucting netwo fo given ste sste is

ppl ic le to sste with n ube of tes The

ethod cn be esily coded fo use on digitl coute

nd eecute uicl. ppendi D contins ORRN IV

pog n eple of fesibilit nd iniu utilit

te clcultion


55/206

nd hve the me overll het trner coeicient with

repect to iven in trem their potentil het lux

will be the me In uch ce the tre re id to

be in " temper tur e contention ht i ei ther one o

the could eliver het to the in t the me cot in

ter o het exchne re I i t exit thi teper

ture contention will hold over ome rne Fiure how

tht there i no temperture contention or Ce o the

hre e S tr em Exmpl e However or Ce the contention

exit over bro d r ne hon in Fiure Ce

lo h r ne o teperture contention ( to F

networ will hve the minium totl het trner

re i ech dierentil element o het or ll tre


56/206

7

4 8

nthapy (MM UHr

F i g u r e ac o emperature ontention n h ree S t rea m E xamp e a e

0

'


57/206

4

he pr ere s sr e h sr e s eq eper

re e e s r s fer he w h he sme he x m

per pr gr s hes ze s h ewr s b r f r

s ge pped x D . Expe r e b es r

pex s r e s s es r e s g e .

Fr s sses he re ewrk be

be e s e Tbe V ges he

r e ewr f r sr e s se wh h es he

eper re e . Tbes VI d VI I g e he

re ewr k f r w s s ems wh er e

s f epe r r e e .

Lke he fes b be e r e be

s mpse f eper re r ges e s r e


58/206

ABLE V 2

MIN IMM AREA ABLE FOR HREE STREAM EXAMPLE CASE 1

Source S rea S k S rea Exchager Ca cu a oRage ep Nae Q ep Nae Q 1 Area#

2

Rage#

2

( F ) ( F )

650550 A - 7 0 304430

550350 B -9 . 6 3 0 3 0 4

7 . 0

9 6

A B L E V

{ F ) ( F ) ( F ) ( F 2 )

00 220 247 233 300

0 0 2 4 7 2 2 0 2 3 3 4 1 2

E = 2 , = 22 0 A = 7 1 2

M N IMM AREA ABLE FOR HREE SREAM EXAMPLE CASE 2

Source S rea S k Srea Exchager Ca cu a o

ep Nae Q ep Nae Q 2 A Area F ) ( F ) ( F ) F ) { F ) (F2 )600550 A - 3 . 5 367430 3 . 5 1 0 0 7 0 1 83 1 7 7 1 9 8

550500 A - 3 . 5 260367 5 . 9 1 0 0 83 2 40 2 0 2 8 B 2 4

7 2 3 1 3 .


59/206

4

terinted so tht the het lost b the source stres

ust euls tht gi ned b the s in str es us the

rnge is in het blnce nd the vle of cn be deter

ine d ddit ionl r nges re fored unti l ll the stres

in the sste hve been included The finl rnge should

end with the lowest source stre outlet teperture nd

the lowest sin stre input teperture If overll het

trn sfer coeff ic ient vlues ( ' s re nown for e ch

str e cob intion n r e vlue cn be deterined fore ch r nge The su of these re vlues is then the

inium totl het exchnge re for the given stre

sste

Notice tht the miniu teperture of pproch for


60/206

4 4

ytem i n whi ch var iou tre am cobination have d i eren t

ove al l hea t trane coe i c ient For uch a c ase the

var iou trea may be in trea contention . t e

contention exit when the product U euals ue AC Table VIII give an example o a thee team system

in which two in tr eams are in tempe atu e contention

Figure 5 show that the contention exit ove the whole

tempeature range o both tre However the over all

heat tanser coeicient are dieent or the two

te am Thu tre am contention alo exi st There or e

to calculate a tr ue minimu are a netwo anges in the

minium area table mut be determined on the bai o

potential heat lux T able I X hows the con


61/206

Srea

A

B

400

ABLE V I I I

DAA FOR SREAM CONENION EXAMPLECapac y RaeC ( B/HrF )

20 000

1 55 0

4 4 5 0

eperaure ( )I Ou

400 .

259

259

320

320.

320

He aQ (M B/H)

5 86 . 0

7 0 4 6

8 8 4

4

AB E X


62/206

Rage

l

2

3

M IN IMM AREA ABE CON DR NG RAM CONEN ON

ource rea k rea E ch ager Ca lcu la o ep Nae Q ep Nae Q [ue ] 1 [ U a ] 2 2 Area

400-382 A - 3 5 6 289-320 B 3 5 6 79 30 . 9240 1 0 0 7 9 3 9 2 4 8 5 6 4 1 6

382- 3 39 - 8 4 3 259-289 B 349 9240 8030 1 0 0 9 2 4 8 0 3 86 . 3 4 0 4286-320 . 494 1 50 6 1 5 5 3 . 6 5 7 . 5 5 7 . 3

339-320 A - 3 8 7 259-286 3 8 7 8030 9 1 50 . 1 5 0 5 3 6 6 1 0 5 7 3 4 5 0 E = 4 , = 5 3 6 , A = 1 84 3

32 0 F

A400 O F

:

.

320 O F

259 F

I

A

2 89 F 2 5 9 FB

F i gu re 6 M i u Area Nework Co i der g Srea Coe o

E #

1

23

4

4


63/206

4

TAE X

M N MUM AREA TALE ONS DER N ONY TEMPERATURE ONTENT ON

Source StreamsRange Temps Name Q# O F

S in StreamsTemp s Name Q{OF

A

7

8 8

E x c a n g e a l c l a t o n s 91 9? Area

F

F

) { F ) ( F t

8

6 ]

8

E+

= ,+

6 8e = A = 1 m n

4 8


64/206

4 8

strea cotetio is oe which ust be ore thoroughly

ives tigate be fore it ca be cos iere to be neglig ible .

D . Mi ium eper at ur e of pproach

he theral r ivi g for ce or teper ature i ffer ence 9 ) wi ll vary fr o oe e of a exchager to the other ,

uless the source a sik streas have ietical capacity

rates. he iiu teper atur e o f appro ach 9i > for

a exchager is the smalest value of 9 for that exchager his value will usually occur at one of the es of the

exchager However , for soe ser vices the r ivig for ce

may be sa le st at a poi t i ter al to the exchager

9


65/206

the pertinent ot i required. The cot o dditionl

9

exhnger re ut be blnced gint the vlue o the

increed heting nd ooling tht would te plce. Thi

type o nlyi h been conduted by itler 8 ) nd

other. The nlyi depend on the reltive cot o

heting ool ing n d exhnger re but the eonomic

inimu teperture o pproch i lot lw le thn

2 F nd ore probbly 1 F onidering the high cot o

utilitie in tody plnt.

ctul ly te eonoi minimu temperture o p

proch i not ontnt but depend on the teperture

level t whih het being trnered. For re r iger

tion yte the eonomic inimu teperture o pproh

50


66/206

50

Ths calclatin f several feasibility tables

with varing min va es make it ps s ib le to e terine the

effec t f min imm temper atre f apprac n t i l i ty r e

qir ements fr any s tre am s ste . he r ange of intere s t

fr 9 vales i s fr 0 t perhaps 5 0 p. I f the str eammn

sstem is nt feasible at very lw in vale s then ti i

ties wi certain be neee in a netwrk. On he oter

han if the str eam s stem is fe as ible for a la rge in im

teperatre f apprach (greater than 5 0 ) aitiona

tiities are nt necessary.

btain a mre qantitative view of these inter

actins min im netwrk area an be cal cla te fr a

r ange f til ity strea r ates . plt f minim newrk


67/206

steam system is deined as:

E M + N - -2)

whee M is the nme o soce steams and N te nme

o si nks netwok s ing ony the as i-minimm ne

o echanges can e constcted o any steam system

that is easie see Section B ) Sch a netwok may e

ie si tting st eams ; howeve at each ecange in

the netwok one o the sys tem ste ams mst eac its ot

et teme ate discssion o te easiiity o net

woks containing ony ecanges is given in endi mati oat can e sed to visaize netwoks

with di e ent ne s o eat echanges The ee senta

5 2


68/206

5 2T A B L E X I

HE NMBER OF HEA EXCHANERS I NV A R I O U S NTWORKS FOR A SEVEN STREAM SSEM

SourcesA B D S i n Q

y : 3 . 3 3 oopt

S i n s F102 . 6 3 1 0 0

G 7 60 6 7 Source Q 30 40 70 . 60 200

A . Seven Exchangers W i l Resu t i n a Heat Load Loop

SourcesA B D S i n Q

.

30 3 3 3 S n s F 3 7 6 3 0 0

5 3


69/206

5 3

detemined and i t is not poss ible to ay an o the ex

hange heat loads without upsetting the system heat

balane . Howee othe s ix exhange netwoks an be

onstuted o the gien steam system o most steam

sys tems the bes t o these pos s ible netwoks annot be

ound by diet seah sine thee ae too many possibi

li ties to enume ate .

I oe than the quas i minimum numbe o exhange s

ae used Pa t o Tabl e XI a heat load loop will

eis t in the netwoks . The sign iiane o the loop is

that the exhange heat loads in the loop ay be alteed

without di stub ing the oea ll netwok he at balane . o

netwok s wi th head load loops opt iiz at ion o exhange

5


70/206

5

costa its The temeate eves o the ste ams i

vove mst be checke beoe oe ca say i it is ossibe

to costct etwok C .

I o iea eeec ie s exis t betwee te soce

a s ik steam sbsets it is io ss ib e to costct

a etwok with ewe ta the asi-miimm e o

heat exchage s S ice sch sbset eaity i s iey

o most ea s team systes E ay be geeay vieedas the acta miim me o exchages

* .


71/206

5


72/206

for network desin is presened.

. nthes i z in etwork Ds ins

he on de sr iption of the enthap di agr m or mor e

expiit the temperatureenthap diaram in the lira

ture appears at the end of an artie b ister 8 ) .

He indiates hat it is used b a nuber of eniners but

is not unier sa l epoed . Essential the dira in

ols pottin the streams to be inuded in a ntwor on

a epr atur e s enthap sa l . Th i s was don for the

exmpl es in Chapter I I I .

With the streams portrad in suh a fashion it is

re at ie ea s to snthes iz e ood networks . ine the

5 7


73/206

stat with the highest temeae soce and sin steam

te eciing how these shod e echange one ne

cons ide s the owes t teme at e ste ams hen ac o

the hi ghe temea e s again eventa y woing a d

the mide temeate ste ams ctay sevea ne

wos may aea to e good and it is then necessay to

comae etaied cacations o each

he steams isaye on the enhay diagam need

not have constant heat caacity ved ines can e

dawn and man iate j st as we a s st a ight ones .

Sitting a steam into a nme o anches is somewhat

awwa d on the enthay i agam owe caac ity ate

steams have a steee soe an so otaying anches

8700 r-


74/206

700

500

300

1000

Exchanger # 1

8

Enha l py (MM

F i g u r e 8 E n h a l p y D i a g ra m S t h es i s A l t e r na te A .

5 9


75/206

A

A Ser e F l ow

A

A

Ser e F l ow (A l erae)

60


76/206

hapter or the more omplex sstems , some sk i l l i sinole in s ing the enthalp iagr an a s might be

expete pr ati e impr oes one s fai l it with the tool

B Optimizing etwork Designs

One a network onf igur at ion has been sele te , the

inter nal temper atur es an r ates ma be a j us te to optimize

the requir e heat trans fer ar ea More aurate l , the

temperatures an rates shoul be ajuste to optimize net

work ost s i s uss e in hapter I I , ost shou l not

onl inlue the effet of network area but some ontribu

t ion epenent on the number o f heat exhanger s .

he f ir st in i ation as t o whether the interna l

TAB L E 6 1


77/206

Srea

A

D

TAB L E DAA FOR HEAT LOAD LOOP EAMPE

Capac y Re Teperare F ( BTU/HrF ) O

1 4 , 45 0 1 40 3 2 0

1 0 8 2 0 1 0 0 1 8 0

1 6 7 2 2 3 2 0 200

20 , 000 3 5 3 300

A 1 u eq a 1 5 0 BTU/HrF2 F

Heat oQ MM BTU/ r )

2 60

0 86

-2 00

1 46

6 2


78/206

A network has been proposed for ths sst ue 11)

and an optization of the nternal net tate

s es ire d . Str ic tly speakn g e minu tt to

area occurs when the temperature t 1 s at 23 r

iure 2 shows soe ore detail concerning total tk

are a . The slution sur face is rea lly qu ite flat fo a

teperature of t1

between 222 and the lmitn ta

ture of 25 2 Oer this range, the total area s th

2 of the mniu. Thus r athe tha chose th tepe a-

tures such that total network area s a im t s

bette to select t equal to 2 2. At th s alue ex

changer s 1 , 2 an carr the entir e network heat load

and exchanger 4 is not necessar.

63


79/206

i to the es i o exche etwos 6 ) pe sets

the ie o cobini ou esibe netwos into sie

supe etwok . Thi s supe etwok is the optimi z

iictes tht the upoitbe exches shou be

e ii te o the i optii e supe etwo . Ho

eve s ice Hw e tes etwok cost oy to e hi s

"optiu esin ivoves o the thitee exches

p e set in the o ii supe netwok The qus i iimu

ube o exches o this ste syste is oy ive

n so i t wou ppe tht soe o the exche s c ou

be esiy eiite. Uotutey s ic iet t e

ot pe set i the t ic e to check this hypothe s i s

Aothe expe om the itetue tht iictes

4


80/206

ranches which have the smaer teperature differences 6 Since the ranch rates are not in equal propotion to the

heat oad this procedure is caed disproportionate

stream spittin In Fiur e C the st ream s r anches

have een optiiz e This is shown y the fact tht the

outet tempertures of the two ranches are not equal

c Overa Stratey

he oa of a desin stratey s to present a pln

of attac that wi produce an econoic dsin ithn the

appicae time and re source constr aints To ad ths

desin proces s increas in ider u se has een made o

diita computers Coputers are not as yet ae to

6 5


81/206

- lc ra y

Dr Q a M Nbr of Ha Exchagr

C a l c l a O p U l y Ra ad M prar of pproach

ad o Crr Co

yhz Nwork U gE h a l p D a g r a


82/206

f a fw agr The strateg s nteracve n the

sense that the engneer ust ake the esgn ecsns

athugh the cuter can avse h f the cnseuences

f the ecsns.


83/206

CHAPTER V

CAS STUDES IN HEAT EXCHANG NETWRK D

Stues on tree fferent stream systems are

pre sente n ti s capter Tese sys ems er e selec ted

from to art cles n te i ter ature 1 17 and ar e n

cude to lu strate a ide var ety of esn probles an

so uti ons Most o f te ca lcul at ons for tese eampes

ere done it te computer prorams iven n Appen D

Representative roram output is iven for eac of te

eample s n te appen di ltou te pror ams ar e soe

at come tey eecute qu ickl y and not mor e tan

fifteen mnutes computaton tie as equre to cacuate

68


84/206

ProcessStrems

2

3

4

i i tyStrems

Stem

TAB L E X DATA FOR TYPE D SYSTEM O FOUR PROCESS STRS

Ref 1 0)

Cpc i ty Rte Tempertures F ) et o BTU/r ) Q {MM BTU/ r )

1 4 , 4 50 1 40 3 20 2 60

1 6 6 6 7 320 200 2 00

1 1 ' 5 3 0 240 500 3 0 0

20 , 000 480 2 8 0 -4 00

Descr i t i on

Sturted t 540 F tent het 6 5 6 6 BU/Lb

69


85/206

Fiue 14 umie the ccutios o iiu utiit

equi emet mi iu tot etwok e Tese c cu -

tio outie the eibe soutio pce o the sstem.

A ue o poit o the bou e iicte. ee-

i to Fiu e 14 po it bove the cuve i i the

eibe etwok spce whie it i ipoibe to costuct

e ibe etwok whi ch wou ie beow the cuve

ee et ive oe cot iue o het ex-

che e o the utii tie . U i the i imu e

cuve {Fiue 4 pu thei ccutio etho o te

e pout 8 h ow time ecooic evu

tio c be me o the optiu uti it tes . The opti

mu ste te i bout 26 TU with suiciet

Coo i g Ut i l i ty MM B U/ r 0 8 0 1 0 1 1 1 2


86/206

tworkAr

F t2

00

Boo

700

600

t

I

E = 1 3 9 =

5 F m

9 = 1 0 F m A E = 5 9 = 20 F m

I

, J

_

l

X i h

uu .

. 2

n

Rate % a bove n mum U t t es )5 0 100

7 1


87/206

7

6

Cost

$/Yr)

3

Tota Cost

5 0 100

n mu m e two r Area and E 5

7 2


88/206

data en n fea s be netwo space aps .

n enta daa s pesented n Fue 1 fo

te exape sot stud of te da w sues t a

pos s b e neto no n f e excanes Fue 1 7

sows ow te netwo was constucted on te aa

Lee ' s constant of 2 0 F tepeatue of appoac was an

taned so te snteszed netwo coud be copae to te

one pes ented n s at ce e to ne two s ae pe

sented n F ues 18 and 9 Lee s netwo eques a

tota of 59 ft2 of eat excane aea we te one

snteszed b te entap daa eques on 706 ft2

s s an 8% poeent a n about 6 % aboe te n u

ae a ese two netwos ae sown o n F ue 4 a s po n ts

Steam emperatre Leve


89/206

500

400

emperature

{ O F )

300

200

1000 2

Range of Coo i ng-Wate r

emperatre

3 4 5

Enthapy (MM BTU/Hr)

F i gu re 1 6 En tha py D i agram for ype D Sysem Examp l e .

7

.

w

Steam


90/206

500

400

Temperature

(OF )

300

200

1000 1 2 3 5

Enth al py (MM BTU/Hr)

F i gu re 1 7 Network Synthes i s Us i ng Entha l py D i agram f Type D System Example.

'

L

Stre S t rem 4 S tem7 5


91/206

Strem 3

Strem 1

C l n g Wter

4 0 F

1 80 F

5 4 0 F

F g re 8 Netwrk After Lee et l

7 6


92/206

rcessStreams

Ga s 1 i e

Kers i e

Gas 0 i 1

Gas O i 1

A s p h a l t

C rde

U t i l i t yStreams

2

T A B X V

DAA OR YE C SYSM O S IX PROCSS STRAMSRef 1 )

Capac i ty Rates emperatres oF Heat adC BTU/Hr ) I O t

Q

MM BTUHr )

3 2 3 0 0 2. 1 0 0 . -5 6

39 ,400 . 400. 1 0 0 . 1 1 . 8

0 4 0 0 00. 1 2 0 . 2 .

220 , 000 . 550 . 350 . 4 4 . 0

2 2 0 0 1 0 . 1 1 . 8

244 400 . 0 1 4 0 .

7 7


93/206

akes t uh easer to suaze and reeber strea

data

Westbrook s art e deas wth the use o dyna

progr ang to opt ze heat ehange network he network

he hose to opt ze s gen n Fgure 2 Thee are

seera ontradtons and errors n the tepeature d

gen n the arte but the teperatures n Fgure 21

appear to be those Westbrook ntended

The arge nuber o derent heat od oops n

the network akes or a op e opt z a on . esbr ook

dd not nude any unt oss o ehngers and so a

o the ehangers orgnay present are retaned n the

network ater h s " optz aton " Atua y the network

800

Ut i l t y H eat Leve l


94/206

700

Goo

sooI

Temperature( 0_ 400

300

200

100 l

00

Ut i l t y H eat Leve l

1 As ph a 1 t

Crude

Gaso I neI

Gas O 1 I

I

Co o ng-Wat erTemperatur Range

50 1 00 1 50 200 2 50 30 0

ntha l py (MM BTU/Hr)

F i gu re 20 Entha l py D iag ram for Type C Sysem Ex amp .-

(

G as l e Kerse Ga s 1 Gas 1 As p al t


95/206

C rude

75 F

C l gWater

7 5 f

G as l e

2 7 5

Kerse

4

Ga s 1

5

Gas 1

55

g r e 2 1 Nerk Afer Westbrk

As p al t

6 7 5

r e drace

6 5

C oo g U y MM BTU / r )

28

a

0 1 1

i

2

q


96/206

eworkArea

M 2 )

2 4

2

1 6

A E

I

f

6 , = 25 m

= 25 m

M mu U 1 y: for ea Baace

E r e Lo cu s

E+= 3 + = 25' m

C E = ,

=

m

1 2 -0 8 52 56 60

ea g U i y MM B TU r )

i gu re 22 Feas b e ework Space of Type C Syse Exmp e

i h i h

8


97/206

cooi ps excher costs eterine the ont o

ti it ies tht sho be se . Thi s wi l vry soewht

ro pt to p t with t ie . However te oti

tiities c be qicky ccte ro Fir once

costs re estbishe.

Westbrook s etwork ieti ie by on the igre

ses re ot o ti it ies . This is ot necessry

the ethpy ir c be se to constrct net

work withot y coo i wter . Figre sows sc

sythes i s . The cr e stre hs een s it ito or

brces . Fire 2 pi ctr es te network syntes i zed . The

retive sizes o the vrios cre stre brches were

chose to ive exchers o roy eq tepertres o

700


98/206

00

500Tempe ra tu re

F ) 400

300

200

100

00 2 5

CrudeBrancB

E 3

Gas0 i 1I

As

c

5 0 75 1 00

En ha l py MM BTUHr)

Furnace

Tal rudeSrea r

Suer

Branc 0

1 25 1 50

F i g u re 23 erk S yn es i s W i C r u de S rea D v ded n ur B rances .

G a so l i n e Gas 0 i 1 2


99/206

Branch A-

75 F \ 1 1 2 6 F\.

5 2 6 F

5 5 0 F f r '

Branch B

75 F 35 6 f

u

7 5 1 2

0

u F

r

os

i n

ranch C

75 f

1 5

o

f

s

F

4 4 8 f

Gas O i 1

Branch D

75 F

F igure 2 4 Network Synthes i zed Us i ng Entha l py D iagram .

4 8 4

6 5 0 F

Ow

Tpe D Sstem o S ix Pocess Stems

84


100/206

Tpe D Sstem o S ix Pocess Stems

The in exmpe in this chpte is anothe Tpe D

sstem om the tic e b ee et T e X gies the

stem inomtion This exmpe is consiea moe

compex thn the ist one pesente temeate

enap i g m Fige 2 5 shows the age mont o

tempete contention pesent

n n cs e the e sibe netwo sace cn e

etemine n this gives n ieiate iea o the inte-

e tionshis between eqie netwo e n ti itie s

Fige 26 shows that stem is eqie on i it is e-

s i e to s e moe thn the min imm mont o coo ing-wte

Point D on the ige shows the minimm e netwo con-

TABLE XV

8 5


101/206

PrcessStreams

3

4

5

6

t i l i t yStreams

TABLE XV

DATA FOR TYP D S Y S T M O F S I X PROCSS STRAMSRef ( 1 0 )

Capac i ty Rate Temper at ures 0 F) Heat adC ( B T /H r F ) n O u t

Q

(MM TU/H r)

1 6 , 0 0 0 0 0 . 4 3 0 . 5 . 8

8 0 0 0 . 440. 5 0 - 8

3 , 7 6 0 1 8 0 350 . 5 5 7

3 8 0 0 . 5 0 300. -5 . 24

6 3 5 0 00. 40 0 . 5 7

3 3 6 0 0 . 390 5 0 . 8 0 6

esc r i p t i o n

500

Steam emperature eve


102/206

400

emperature( F )

300

200

100

0

C i n g{WaterRange

2 4 68 0 2

n t h a p y MM B/Hr)

F ig u r e 25 n t h a p y D ia g r a m f r S x P r c ess S t r ea m y e D S yst em x a m p e

1 4

2 . 5

C oo l i n g U t i l i t y ( MM BTU / H r )

6 . 0

A E 6 a . = 4 0 F ' m n

B

E = 5 9 = 40 F" m n

6 . 5 7 . 0 7 . 5


103/206

NetworkArea

Ft2)

2 . 3

2 1

1 . 9

I C : E 7 a 20F1

m n

I

5 3 MM BTU /Hr Coo l i n g .I M i n i mum U t i l i ty fo r He a t B a l an ce .

_

a+

= 50 F-

m nT .I

II

I

I

En

t

i

r

e Locus

+ + E = 29, 9 . 50 Fm n

II

1 7 .

1 . 60 0 4 0 8 1 . 2

He a t i ng U t i l i ty (M M BTU/Hr)

2 . 0 2 4

F i gu r e 26 Feas i b le e t w or k S pac e f or S i x P r oce s s S t r eam Type D System Example.0-

88

for crtain procss sras, and thn as utility rat is


104/206

for crtain procss sras, and thn as utility rat is

incrased other procss sras ay aso b xand ih

the utilitis.

L ' s " optial ntork for th s tr ea syst on

tains sevn xchanrs and is desinatd as point in th

ntok space iure 2 7 pictures e ' s ntork. His

ntork uses on ore than th quasiiniu nuer of x

chanrs (E 3 + 4 - 1 6 It is possibl o construct a ntork usin only

th quasiiniu nuber of exchanrs ith th aid of th

tepraturnthalpy diara. Suh a ntork is prsntd

in igur 28 and reprsntd as point on th fasibl

nork spac . Hoevr , note that xchanr #3 is very

89


105/206

Stream 1

S t r e a m 2 Stream 4 S t r eam 6

9


106/206

Stram

Stram 6 Stram Stram 4

and ea ansfe aea equeen ae caned on

9


107/206

q

s fo e newo n F ue 8

Reducon of e ea excane equeen o fve

usaes e need fo nvenvenes s on e pa o f e

pocess desne S c spea n e n u nube

of excanes s e quas n u nube fo s exae.

No souce o s n sea subse s ae denc a equa

Howeve n pac ce e n u nube of ecanes can

be educe o fve and a newo consuced As o

wee o no newo B s e econoc coce depends on

coss assocaed w e nube of excanes n a

ne wo

9


108/206

S t e a m 3

S t e am 5

Steam

8 0 F

2 0 0 F

0 0 F

S t eam 2 S t eam 4

2 2 4 F

73 F

4 40 F 5 2 0 F

400F

2 5 2 F

4 3 0 o )


109/206

CHAPTE I

HEAT EXCHANGE NEOS IN OPTIO

Coiutio sythesis siig o the iiiu

eemets is oy pt o the iomtio poces eig-

e ees o compete het exche etwok esi He

shou so he kowee o the opeti chcte-

i st ic s o the etwok Thi s chpte ttept s to we

soe o the y questios tht the esige ight he:

1 ) s i t poss ibe o sm pocess chge to cuse

sti c ches i etwok pe omce? ) Whi ch

eemets o the etwok e most seitie to chge?

) D etwok s chcte ist ics hep o hie pt

9

V- )


110/206

V )

Fr the def init in f ef fi cienc in Eaton -a ne

a a wr ite :

-)

f the ave equatin are cined the eltng ex-

pein fr uce and ink ide f th exchange ae

t t - t > n u n u ce C e {tn rce in

Cin/R ) { tut - tin> ink

- t k )n n

ine

V-3)

VI- )

t e ) t + et V-7

9 5


111/206

tut suce

= e ) t n suce

+ et n snk V-7

/ tut snk eRtn suce

+ l eR ) t n snk V-8

hee tepeatues tten as " epesent ffeencesfrom the design values , i . e . t = tactual - tdes ign

nce nue ca l the capac t ate at R ) an

ef f cenc e th ust aas e eteen an an

changes ae n the net tepeatues f an exchange

l appea nshe n tes f changes that ccu nte utlet tepe atue s

Equatns V-7 an 8 can e e tten n the f:

< t t Fkt

+ Gkt k V-9

9 6


112/206

urce A

n

n D

rce B

4

9 7

s pstv and ust b lss than and so tpatu


113/206

changs n th nput to a ntwok cn on ppa as

dnshd changs f th sa algbac sg on ntwok

outt tp atus It shuld also b notd tt chang

n ntwok outlt d v d b nlt chang s cos tnt

Ths constant s cald th tpatu ss

facto

Tabl XVI lsts tpatu sst factos fo

th ntwok shwn n Fgu 9 pag 7 5 ) . hs factos

w coputd b subutn SENSIT n n Appnd D.

To us th tabl on s pl f nds h colun of th s t a

whos nt tpatu s vd and th ow of th ut

lt ntd at tp atu ds d. T fact at

AB XVI

8


114/206

#

# 2

O u t l e t #3

eperatueFactrs #4

c w

Stea

MPRAUR SS I I V I FACF O R W O R K S H O W I F U 9

Stea Whse I n l e t e p e a t u e I s#

. 1 39

0

#2 #3 #4

08

409" 0 00

2 3 8

0 8 3 9 7 042

8

2 4 2

c w .

3 4

0

0

V a iedSte

0

0

"

0

32 7 0 0 . 473 0

0 0 0 0 0 l

9

TABE XV I


115/206

EXAMP CALCULAT ON US I NG MPERAT R S E N S I T IV ITY FACTORS

A

S i m u l t i o nT C a l cu l a t ed F ro S en s i t i v i ty FactosStrea Due to 1 0 F0 Due to + 1 0 F0 Tot l C l . ",

Tout

C h n ge i n # 1 C h an ge i n #2 Chnge Both Chnges

1 3 9 + 1 . 08 0 3 1 0 3

2 -2 50 + 4 09 +1 . 59 + 1 5 9

3 0 0 0 0

4 3 . 0 6 + 2 3 8 - 0 6 8 - 0 6 8

c w . - 2 0 0 +3 2 7 2 7 + 2 7

.

tl - 3. 79 + 6 2 1 +2 42 +2 42

t2

- 5 63 + 4 3 8 + 1 25 + 1 . 2 5

100

points in a network can be qickly ientiie by ooking


116/206

for the larges t factors in the table . It al o qickly

seen where a change wil prouce no efect on a iven

strea teperatre (zero sensitivity actor ) .

B Steay-State Response to Capacity Rate Chane

For a oble-pipe heat exchanger o fixe ein

ef fic iency can be expre e in ters o stre a r ates

Combining Equations II-10 an II-12a ives:

e 1 . 0 - exp UA/Cmin - UA/Cax

Ci n/Cax - exp UA/Cmin - UA/Cmax(VI-11)

Ths ef iciency i a rather coplex nction o inivi ual


117/206

1

(page 7 5 ) . erentage strea ate hange is l iste d at the


118/206

top o eah oln ah ro in the tl oesponds to

an inte rnal or oe t str ea teperatr e hange . Note

that ost of the teperatre hanges ae ol linear

over the -1 % to +1 % r ate r ange . s ith tre

sen si tiv ity the ost sens i tive par ts of a neto e

deterined qiky by ooking for the largest ns in

the tab e . Notie that the teperate sensitivit nd

the r ate sens it iv ity of a netork ar e not th sa .

Gener al ly , the netork otlet tepetr of a str ea i s

ore sensitive to a hange in its o te ad less sensi

tive to a hange in its inpt teperare than are the

other streas in the netok

103

T A B L E X I X


119/206

EXAMPE CALCULAT ON US NG RAE SENS V I TY ABLE

T C a l c u l a t e d F rom R a te S en s i t i v i t i e s S i m u l a t i o nStream Due to -5% Due to +5 otal C a l c . f C h a n g e i n # C h an g e i n #2 Change Both Change

out

3 . 5 3 0 7 3 6 8 3 . 6 8

2 0 . 5 3 3 . 92 4 .45 4 4 5

3 0 0 0 0

4 3 4 0 . 3 8 3 9 3 8

c w . 0 . 4 3 2 0 2 4 4 2 4 2

1 0 8 2 69 3 . 5 0 3 . 4 7

2 3 60 69 3 8 5 3 86

04

London dvot a captr to t sary of 8 transint


120/206

rspons probls that av appard in th litratr

Th soltion to t probls ar prsntd in trs of

dins ionl ss qanti ti s c lik tos sd in t x

cangr r at ing ca lcl ation procdr . Coon to th so l

ti on o f a ll o f ths probl ms i s t act tat th dynamic

rspons o individal xcangrs to stp changs is

ovrdpd i no osci llations occr .

Addi tional ly t govrn ing dif fr ntial qations

ar s aid to b l inar within t sa l idal izations

Th s th tpr atr r spons to any pr trb atio ns otr

tan a stp nction can b obtaind by linar dynic

tcniqs Bcas ac indiv idal xcangr tnds to


121/206

REEREES


122/206

1 . Boas , A. H. , " Optza ton a Lnea and DnaPoan, " eal

Engn n,

7 0 , o . 4 8 5 - 8( 19 6 } .

. Booe , M. , "ate , " hemalEngn n , 1 ' o 1,

1 5 - 1 8 ( 19 7 0 .

. an , L . T . , and S . an , The Ds ete aumP ncpl ,

Jon Wle & Sons;n , ew Yo , 1964 .

4 . G az z , L . , a nd R . P as e o P o e ss oo l n S s tes , "Hdocabon Poc ssng,

49 , o 1 0 , 8-90 (197 .

5 . Happel , J . , heal Poess Eonoms , John le &Sons , n , ew Yo , 195

6. Hwa, s , " ppl aton of Math odels n . E Resea, Desn, and Poduton, A . . h . E . ns .h e . En s . , 4 Pape 4 1 , ondon eetn, 8 -8(June 1965

0

2 Mono L. S a Chal Engneen 7 7 No


123/206

2 334 (7 3 Nlson L . ol Refney Engneeng 4h

on MGawH ll Boo Co Nw Yo

4 ag M os l Cool ng Ts a NwAoah o as s Ds gn al

Engneeng

7 4 No 7 3 ( 67

John alEngnees

Hanboo 4h on MawHl l Boo o Nw Yo 63

6 s M an K D Thas lanDes

Eonos ChalEngnees

MGawHll Booo Nw Yo 6 8

7 sboo G T s T s Mho o S EahSag fo Bs a on Hyoaon oessn anol fn No 2 26 (6

s l A M Ha Exhangs as Mon s


124/206

A P P E N D C E S


125/206

PPENDIX

GOSSRY

Single Ste Tems

Steam Inteaction ems

System and etwok erms

0

This lossary ontains the seial ters and


126/206

hr ases used in thi s di ssert ation . t as neessa ry to

define these seialize ters sine there is at resent

no seifi voabulary in the literature that an be used

to desr ibe soe of the onets develoed The lo ss ar y

is divided into three setions ith the ters in eah

setion lsted alhabetially

INGL TR TRM

NTRNAL TRAM TMPRATUR - s tr ea teer at ure that

our s it hin the heat exhane netork . This ould

usually be at soe teerature beteen the terinal

SPLIING A SRE - dv dn a ea n w o e

1 1 1


127/206

banch tea a uated bew.

B Note: t ouA

1 n

deter ned by anentha py ba lancearound te summer

Fue A-1 . A Typca Tw-way Sea Sp .

SPLITING THE H LO OF A SRE - exchann h ea

b th th h

112

STREAM INTERIN TES


128/206

HEAT ECNGER ES IGN CALCULATIN - deten ng the a ea

equed o a heat exhange so that the soue and

snk steam tempeatues hange ove a speed

ange The tempeatues ae onsstent wth an

enthapy baane that gves the amount of heat to be

tansfeed

HEAT ECHNGER RATING CALCULATIN - detenng the st ea

outet tempeatues and the aount o heat tansfeed

n a heat exhange o a gven desgn a ea xed)

w th known st eam ne t tempe atue s A onvenent

det auaton atng method s the tansfe unt

ff th d K d L d

3

str e rou gout the r e o f te conten ti on the


129/206

two source stres wl be ble to supl etg

to the sink t the se cost ters of e.

Contention cn lso est for two snk stres d

sgle source o fo severl stres of ec tpe.

TEMPERATURE COTENTON - the s pl fed cs e of st e

conteton whee te effect of the overll et

trsfer coeffcient U i s ot cos idered . To o

oe souce streas re i teperture conteton

wt ec oter if ty e vlble for het echge ove coo tepe tur e nt er vl Sink

stres c lso be in tepeture coteton

TEMPERATURE SENS TVIT ACTOR - fo het ecnge et

114

steas in the stea syste

AT LOA LP t t i l th th t


130/206

AT LOA LP - a te se to es ie l oe pth that

st exist in a heat exhange network i or a ixe

strea syste the network are an e hange y

alteing only intenal teperates an/or anh

steam rates The loop st stat at one exhanger

an retrn to that sae exhange y ollowing strea

paths The loop my hange o oll owin g the path

o one steam to that o anothe only at heat ex

hangers In oth o the networks il ls tate elow

a loop an e ae thogh exhange s 1 3 4 2 an

ak to exhange 1 .

115

TA-OPTI REGION - that reion o the ea sible solu

ti h i h b t t i ti


131/206

tion space , wh ich becau se o ata uncert ain ties

an intanibles is as oo as the optium or esin

purpose s . Any attempt to reine a esin beyon this

near optial reion is not economically justiie

because the mathematical oel use in the optiiza

tion simply oes not escribe the real solution

space (or system) any ore accurately .

MINM AREA ETWORK - or a spec i ie s tre a sys te a

network in which the total heat transer area (A*

}

is a inimum

MINIM UTILITY STREAM SYSTEM - a s tr eam syste compose

o a ien set o process streas plus the inimu

6

QUS MNIMUM BR OF HT XCHGRS st ic t def ined

M + N Si ifi f E i th t it i th


132/206

as M + N 1 Sinificance of E is that it is theini nbe of heat echanes eqied to con

stct a feasibe netwok fo soce and sink stea

sets that ae inea indeendent That i s no

soce stea sbset is identical eqa in anitde to an sink stea sbset Fo sch a sste

thee st be a ini of M + N heat echanes

STRM S TM the cob inat ion of the iven oces s

steas and the chosen aonts of availabe tilitiesas iven b the sste estictions Stea sstes

can be classified into fo basic tpes deendin on

the nbe of soce and sink ocess steas


133/206

PPENDIX B

N NNOTTED BIBIORPHY ONHET EXNE NERS

Netok SnthesiNetok tiization

118

An extensve search o the engneerng lteratre

( nclu ng ASA publc aton s ) was concte Th s sea rch


134/206

( nclu ng ASA publc aton s ) was concte . Th s sea rch

showe that a relatvely sall nuer o artcles s-

css e heat exchange networks . These artcles are lste

be low n two grops

ETWORK STHESIS

1 Ke s le r M . G . an P o Parker "Optal etwors o Heat Exchange . Che Enq . Pr or Sypos iu Seres 5 o . 92 , 111-120 (199)

General scusson o network synthessus ng a o e as s gnent al gor th Thetechnqe breaks each network strea ntounts o 1 M BU an operates on thesents One exaple s gven .

2 L K F A H M F R "B h

A r ia an er ror approa for r uur inga i ru ai ng waer em Ef fe of ooin g ower o i a o in ue ne expe


135/206

in g ower o i a o in ue . ne expeiurae e eniue

5 Ru D F Te Snei of Syem De ign I Eeenary Deopoiion Teor A. I E .Journa No 2 { 68 ) .

A aeaia approa o yneiing anework for a ipe re a em Te ing eeape given i rgy in erm ofgeneraize mo

6 i ter A M "Hea Exanger a MoneMaker " Peroeu Refiner 2 No 8386 8 )

Ti arie iue e eonomi forone proe -pr oe exanger However een of e arie rief menion eeperaure-enapy iagra an iuraei ue wi a Tpe C rea e

120

3 Hwa, c s , "Applcaton of Mth Mols n ChERsarch, Dsgn an Proucton A. I . Ch E .

I n s Ch. Engrs 4 Ppr . 12 Lonon Mtng83 88 ( 196 )


136/206

I n s Ch. Engrs 4 Ppr . 12 Lonon Mtng ,83 -88 (Jun 196 )

Gnral scusson of sparl lnarprogr mng Tchnqu s ppl to onlar ge (many xchangr ntwork Howr , n suffcnt ata prohts dtal nlyssof th rsults

4 . J ns s n, s K , "Hat Exchngr Optmzton , "Chcal Engineering Proress, 6 No 9 6 6 ( 1 9 69 )

Ths artcl scusss th optzatonof prs sur rop n a ha t xchangr Ex

changr cost appars to e rltly nsnstv to pressur drop

Rud, D F an c C Watson St r ateg ofProcss

Engineering

John Wley Sons , Inc Nw York , 19 68

Wesbrk T , "Use Thi s th S iz eEach Sae fr Bes Opa tion ,

Hydrcarbon

Ptre Ri ner , 0 No. 92 0 1 2 0 6 1 9 6 1 )

2 1


137/206

Prc ssing & Ptre Ri ner , 0 No. 9 2 0 1 -2 0 6 1 9 6 1 ) .Genera

prrminsme eta i .he ext anddiffic

discssin f he se dynamic exampes are presen inSeera incnsistencis beween

ires akes he exampesinterpre


138/206

AEDIX

SUORTIG REASOIG OR EASIB SOUTIOSACE BOUDIG AGORITS

Mu Aea etosQuasu ube oHeat Exchaes

1 2 3

MINIMUM OK

F t t t th t il h t


139/206

For a two strea sste the est possile heat

excane "network" is a conter-crrent aranent as

so in Fie C-1 .

emp.

E n h a y

Fi e C-1 Conter -C ent Heat rans fe

he avantae of sch a stea arraneent is that eac


140/206

25

A


141/206

i n k n i n k O u t

B

Figr e C-4 i i Are a Newrk

This arrageen is he ni area newrk fr he

hree s reas

m n

26


142/206

Tm

ntha y

m nc

Fire C-5 A Sream Syse hich eqiresea xchaers i Ser ies

Fire 6 as shws a feasibe srea sysem

weer i hi s cas e he w sr ce sr e ams chae erhe same emper are ee Aai he sr ce sr eam

eria emperares are js 9mi abe he sik srea

The y feasibe ewrk fr sch a sysem ies he

1 2 7

Anasis of the reqireent for feasiiit shows

that a feaie tream te fa eteen these two


143/206

worst case . ence i t i s a wa poie to constr ct

a feaie networ with the qasi-in ner of heat

exchaner s .


144/206

ANDIX D

AUTOTION OF HAT XHNGENTWORK AUATIONS

9

Thi s aeni is opose o a ser ies o taes .

The TAN IV oter prors se or network cac


145/206

at os are ie . so se s o the ott or the

three eames presete in Chater V are ice.

The MAIN coter proram (Tae DI ) is an

eecte r or am that contr o s the network ca c at ions .The cacatios ca be iie to three basc types

) Determ i etwork bos 2 esnin or sizn

echaer s for networks an 3 Sati the effect of

temeratre a/

or r ate chanes o etworks . s te

beow ar e the fctios o f each sbrot ie .

SDATA - eas roe an str ea ata a per fors

soe nit a ca c atos sch as

3 0

MIY - Ti s sbrtin clcats fasi bi iy

ab fr a n stra sst an


146/206

mpr ar f appra c It n rmins

ility rqirnt an if rqs

AMIN

i incls ncssary iliis in

sra sysmTis sbrin caclas ini nwrk

ara sin cnc f rar

cnnin

CONFIG as an sins sr sc if i nwrksf a xcanrs I cntrs

r a in f nx fr sbr i ns

ATH T calcain rr fr CONFIG s in

SENS IT - Netwrk rte n temper tre senst t

c ctns re sper ise by th sb t Lik COIG t th

3


147/206

sbrtne Like COIG t r eq re s the

se f TH S n DIVIDE

NTC - Het echaner r tn r s m tn

cactns are ne b ths sbrtne

when t s ce b SENSIT

Tb es D- I I thr h D-XIV e the sr ce prr ams fr

ech f the be sbr tne s

Tpc prram tpt fr three eampes s pre

sente n Tabes D-X D-XVI a n D-XI I I The tpt s

r e s e f-ep antr n shws the etent t wh ch

netwrk ccatns he been tmte fr ths re

lV

h P; VRS !N 3, V E L D IE T H U Y 13t

E MAI N PAM FUR C L T I O S IM EYRK fRUT fXCiNE THE OiM S N l T RQ CAUL OD ) ! A SPI F t IN Ht RAY "Lr' T PRuRA . $l( h H O P N H E : P u A HE!t. CU NC lMu"T T fLLW ABL W L IA DeJ M u : b T S

PAGE 0

R A N , 8 L c A H ( 3 ) I 1 4 ,

'18" ; ( T b , RN E 7 N u T l d , A M I 9 " flf , t N

eN 5 A 3 l T N Y . Hh Hc 1 9 7 .


148/206

001

02

0 0 3O


149/206

0

0 0 0 1 4

5 0 1 7

c M M Y TX CMN -40 L

EAD T h AR A NA L E . I F I = NT C RTI E I 1 H I = I A M = I M N T M 4 21 = 3 I AM N C L M 3 ) f v M T M : O PR < MS 7 5 , 2 5 o 0 5 t

'

NA M o L , T E M P W T A 4 , X , X, 4 . 0l

W R E 1 F O K. A T l t i l

W R : l P M E kMA O T b t 1 o H A CHNGE NEOK CCI 1 1 l / T 5 ' R M )T A T t M E N T F A / l

R E EAM N f MAT N AN L eA T R N C E J C E T R M AM M$ 1-8

C AT / CU! *

Ub 202 TM ( M 2 - A PA T M L HA T TA E F ' M 44-b *0 C N C AT A R E R eA S N SrAM NMA N U M F O R A T A A B V E T 3 C* M N I C A A T I R A M *

* N O R A C H C E I N T R AM C OMB AT N ARE N E * E STEM AR EAM T A T Pt R NEN E t H C N I T I AL AN N AL MP EA A AL AN E A T E T E A T O *

Vc N N I N T A F tA T A A I

ww

RN l

O v 0 0

o

0 0 !

O l

0 0 3

O 4

005

0 0

0 008 2 03000

Mh DI (ontin)V E I N 3 L EV E A E t U H 0 2 N R E l l l

.AO 5 2 0 N S U R E NS RCE I I l 5 U R C N RC e, C l l O

20 u F 1 . 0 , f : X 0 F . O X ; S C RCE , - U RCE RC E ,

, 8 = C R L C E N RC 1 l i F $ o i , = i C * S U C E ! RC 1

2 S 1 C k

l 9 , = 0 N K N S I N I t : l 5 JK N I K 1 h K Al i , f U . F 5 0 1 = N S I N 4 )

AGE 0002


150/206

00 0

OH

0 3 4

0 5

O b

O O 7

0 0

1 5 F + F T ( -1 l1

c 1 5 5 T ( o i I , l o , 2 > A t 2 X l O F O l Xl

A l

tEIG

AA R EU I EN T S A

TRA 1 V

0 0 0 1

0002 0 0 0 4050 0 6 0 7

! 0 9 0 0

cc

ABLE D II I SUBROUNE ELTAO P V E R S I O N r V A E T h iAY 3 1 1 A s ITH IS f U N CT O SB M CLUA E E OG MA AV RAGt O FA' W P O T V U t R . E UC L TRN TE VAvE FZ F t K A 6 C S E T E R GA T E

f C . 0 - 0 0 0 O 0 A / F A J l A = d / A ( A U 0 0 0 H J F f L A

= i / A A 1 0 L A /

/

1


152/206

0 0

0 A 0

D HTA C R U A 6 Y T

R T R V

0 0 0

00020 0 0

000

006

O O b0 0 0 O '

B D B 4 V E R I N L E V E 3 D E M AY ,

W a U I N c AL ' T H S R T N E AD U S T S H E R E T H E S T R E H H E R G E C C H G E T H P T G S T T H I S HE A E R N T E o l f N E T M M A SS A T E I S U " P C I I E D o I T S A L U T E D

; A H A T AAN N S E M . w T E . H H M N N - u s c . H E M NG D P . - 1 7 0

K uE O t 8 , N 0 8l NSC E NK t , Sl L A

T S E M E U S T F\ 1H&h : O

O = NSRE ) . O . O \U l o ( l t . H U T D S i

G E 0 0 0


153/206

0 0 1 00

L 0 0 0 0 0 50

0 0 7

001 8 0 9

00< 0.doo, 0 0

004O i ! 2

oo 0 0 O J 0 0 3

O O

OvO 0

0 0 3

Q O j oOO0 "

S i , 0 N U E

, N ! F S l t l , . O . O G T N L T H 1 A S I ,

U E

1 6 I I

d7

I l

A MT T S RAM ATE ETH CHNGE S EE RE L AS TA HA HAGE R UE R SI S T R E M S

1 F T . T 0H C H S G , E H N K

= s +S U B I G F d 1 E I I G , / RC E ! l G 6 * S C E I Ux

C , = - S CE l / URCE I G 7 t f

0 H S I N K I I G I B I , x E I N

H S I i I N l T

d , N I N G , S , E

B r N l l / K l I G o 7 EN

R E E U I < S 0 0 d 0 Y T E

w

TA V

0 0 0

000 0 0

00O O O O b

TL DV SUBUINE NGDEL 9 S S N L E D AT E T Y E 000

c T E A u i T E A , T I , T , S T M T M C T H I S U B T INE C L CU L AT e EXT E T THE CE N STREA TPET kAN R USIEAT N A T E A T I T h EC K . A ET TJ T T R A U N T N T ! N .C T N B MN U . H N G t T - T A N T A I N T NC T Ht M T T H T MP RT R RA NGEC - L < L T T H T M P E T AN A Y w l T T A M N H E RA E M N T T H \ M N C T T Tr N F T M N H ARR T

N T O M 0 8

\L R T GHT TM TP AA A F T N . O v l u 20 1 0 I 1 T 1 0 = ,


154/206

O O b0 0

0 0 0 8000

0 0 1 0

0 0 0 1 2o

0 0 1

O O o0 0 1 0 0 80 1 90 0 0

0 2 00 OOd0 0 2 4

0 0 2 5002 60 0 7

0 2 80 0 2 9

0 0 00 0 3 10 0 0 0 3

000 3 5OO

1 0 , 0 I T K T l f L T R ( l

C CHE F T ANE S NE I N F N S M A L E T 20 =

M LR T f L A L I T f EW ANGE

n L w T f NW RANE A CE I S N T E S A L E E

c 0 N T F T i R A I E S T R A , 5 . A . T I EQ . T

. . R l GU T 3 0

+

TL = T R AM , 4 0 CM E F O l 5T

F F I T E E X E N T 5 f = o o

0 NS T 4 =

0 ) T . T L AN . EA L T T l l T L R EAM i C H A


155/206

0 0 w P N AM , J I O O ; f UR T H 1 0 , l L U Y A N D E A I T Y T A E FUR lA4/

' M M i'K A F A U A I N A E ' f . . /

O O l , O b A n ' , o ' R E A ' t , S I N K T E A S '

O O 0 5

0

1 190 0 20 0 2

O

(feasibility table)phd thesis hohmann done

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