Section 25 - Equilibrium Ration (K) Data

7/25/2019 Section 25 - Equilibrium Ration (K) Data

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FIG. 25-1

Nomenclature

= P* =

L = R =

N = mole fraction in the total mixture or system T =

= acentric factor V =

P = absolute pressure, psia =

= convergence pressure, psia =

Subscripts i =

KEY

= Example calculation from the boo

= !pplication "orsheet for user to fill out

= Numbers that must be fille# in accor#ing to the user$s #ata an# specific situation

'i

e(uilibrium ratio, yi)x

i

ratio of moles of li(ui# to moles of totalmixture

xi

P

yi


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vapor pressure, psia

temperature, R or +

component

%also inclu#es numbers from graphs an# charts&

universal gas constant,

%psia cu ft&)%lbmole R&

ratio of moles of vapor to moles of totalpressure

mole fraction of component in the li(ui#phase

mole fraction of component in the vaporphase


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! mixture is put un#er the follo"ing con#itions-

.omponent / 0ethane = 12 lb moles

.omponent 3 Ethane = 42 lb moles

Temperature = 5/36 +

Pressure = 62 psia

7o" many moles are in the vapor phase an# ho" many in the li(ui# phase8

= /2 Page 365/2

= 29:6 Page 365/2

= /2

= 29:6

29:6 an# /2

;olving the above e(uations simultaneously-

= 2921


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n no event "ill the AP! or AP;! an# their members be liable for any #amages "hatsoever %inclu#ing "it

These calculation sprea#sheets are provi#e# to provi#e an FGperational levelH of accuracy calculation base


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Application 25-1 -- Binary System Calculation

! mixture is put un#er the follo"ing con#itions-

.omponent / 0ethane = 12 lb moles

.omponent 3 Ethane = 42 lb moles

Temperature = 5/36 +

Pressure = 62 psia

7o" many moles are in the vapor phase an# ho" many in the li(ui# phase8

= /2 Page 365/2

= 29:6 Page 365/2

= /2

= 29:6

29:6 an# /2

;olving the above e(uations simultaneously-

= 2921


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out limitation, those resulting from lost profits, lost #ata or business interruption& arising from the use, ina

# on rather broa# assumptions %inclu#ing but not limite# toI temperatures, pressures, compositions, imperia


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the gas processing in#ustry9 !ll information an# calculation formulae has been compile# an# e#ite# in

luntary an# the AP! an# AP;! #o not guarantee the accuracy, completeness, efficacy or timeliness of s

a particular purpose or non5infringement of intellectual property9


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ility to , reference to or reliance on the information in thes Publication, "hether base# on "arranty, con

curves, site con#itions etc& an# #o not replace #etaile# an# accurate ?esign Engineering taing into ac


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cooperation "ith Aas Processors !ssociation %AP!&9

uch information9 Reference herein to any specific commercial pro#uct, calculation metho#, process, or


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tract, tort or any other legal theory an# "hether or not a#vise# of the possibility of such #amages9

count actual process con#itions, flui# properties, e(uipment con#ition or fo"ling an# actual control set5


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service by tra#e5name, tra#emar, an# service mar manufacturer or other"ise #oes not constitute or i


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oint #ea#5ban# limitations9


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ply en#orsement, recommen#ation or favoring by the AP! an#)or A


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Temperature = 532 +

Pressure = 122 psia

Bhat is the ratio of moles of li(ui# to the moles of the total mixture un#er these con#itions8

Solution Steps

.omponent

.olumn

/ 3 : 4 6 1

Trial values of L %note- V C L = /& =

3222 2923 2924 2921

292/2 :9< 29344 2936411 :91/22

292/21 /93: 2922>14 2922>1< 2922> 29//32: 29433 29/>1:: 29/64> 292 29213>

292246 2923: 29/26 2926 292122/ 292:6:2 2923622 292:>36

2922/ 29226> 292 2924/


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2922243

29222/4

The sample calculations, e(uations an# sprea#sheets presente# herein "ere #evelope# using examples publ

Bhile every effort has been ma#e to present accurate an# reliable technical information an# calculation spr

The .alculation ;prea#sheets are provi#e# "ithout "arranty of any in# inclu#ing "arranties of accuracy

n no event "ill the AP! or AP;! an# their members be liable for any #amages "hatsoever %inclu#ing "it

These calculation sprea#sheets are provi#e# to provi#e an FGperational levelH of accuracy calculation base

.

* .22 psia

perature at "hich the gas starts to con#ense9 %?e" Point&

eps

.olumn

/ 3 : 4 6

+ee# /222 /222

562 + 542 +

29>64 3936 29:>2 39: 29:44 29212

2921: 293 29/26 29:26

= /9222 /923/ 2942

54

* '.G3

= s(9rt9 %'./

K '.3

&

Linear interpolation- T#e"

=

e heaviest "o$ponent is uite i$portant in de' point "al"ulations.$ple) $i)tures# the "hara"teri6ation of the heav& fra"tion as aonent su"h as he)ane or o"tane 'ill have a signifi"ant effe"t on

al"ulations.


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ublishe# in the Engineering ?ata @oo as publishe# by the Aas Processor ;uppliers !ssociation as a service to th

sprea#sheets base# on the AP;! Engineering ?ata @oo sample calculations, the use of such information is volu

cy or reasonableness of factual or scientific assumptions, stu#ies or conclusions, or merchantability, fitness for a

ithout limitation, those resulting from lost profits, lost #ata or business interruption& arising from the use, inabili

ase# on rather broa# assumptions %inclu#ing but not limite# toI temperatures, pressures, compositions, imperial c


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e gas processing in#ustry9 !ll information an# calculation formulae has been compile# an# e#ite# in co

ntary an# the AP! an# AP;! #o not guarantee the accuracy, completeness, efficacy or timeliness of suc

articular purpose or non5infringement of intellectual property9

ty to , reference to or reliance on the information in thes Publication, "hether base# on "arranty, contra

rves, site con#itions etc& an# #o not replace #etaile# an# accurate ?esign Engineering taing into acco


33/39


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operation "ith Aas Processors !ssociation %AP!&9

h information9 Reference herein to any specific commercial pro#uct, calculation metho#, process, or se

ct, tort or any other legal theory an# "hether or not a#vise# of the possibility of such #amages9

nt actual process con#itions, flui# properties, e(uipment con#ition or fo"ling an# actual control set5poi


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vice by tra#e5name, tra#emar, an# service mar manufacturer or other"ise #oes not constitute or impl

nt #ea#5ban# limitations9


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en#orsement, recommen#ation or favoring by the AP! an#)or AP;


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These "harts sho' the vapor-liuid euilibriu$ ratio# Ki# for use in e)a$ple and appro)i$ateflash "al"ulations. The "harts do not give a""urate ans'ers# parti"ularl& in the "ase of nitrogen.The& are in"luded onl& for illustrative purposes and to support e)a$ple flash "al"ulations andui"k esti$ation of K-values in other hand "al"ulations. These "harts should not be used indesign "al"ulations.

Previous editions of this data book presented e)tensive sets of K-data based upon the 8P(Convergen"e Pressure# Pk# $ethod. ( "o$ponent9s K-data is a strong fun"tion of te$peratureand pressure and a 'eaker fun"tion of "o$position. The "onvergen"e pressure $ethod re"ogni6es"o$position effe"ts in predi"ting K-data. The "onvergen"e pressure te"hniue "an be used inhand "al"ulations# and it is still available as "o$puter "orrelations for K-data predi"tion.

(vailabilit& of "o$puters# "oupled 'ith the $ore refined Kvalue "orrelations in $odern pro"esssi$ulators# has $ade the previous 8P( "onvergen"e pressure "harts outdated. Co$plete sets ofthese "harts are available fro$ 8P( as a Te"hni"al Paper# TP-22.

For e)a$ple 25-2# Kivalues used and in Fig. 25-3 are found in the K-Data Charts at the end ofChapter 25. These data are for P

k 3!!! psia although the "harts spe"ifies P

k 2!!! psia. The

pressures refer to "onvergen"e pressure# Pk# of the "harts fro$ the Tenth %dition of this data book.

The& should not be used for design 'ork or related a"tivities. (gain# their retention in thisedition is for illustration and appro)i$ation purposes onl& ho'ever# the& "an be ver& useful insu"h a role. The "riti"al lo"us "hart used in the "onvergen"e pressure $ethod has also beretained +Fig. 25-,.

For e)a$ple 25-3# note that the heaviest "o$ponent is uite i$portant in de' point "al"ulations.For $ore "o$ple) $i)tures# the "hara"teri6ation of the heav& fra"tion as a pseudo"o$ponentsu"h as he)ane or o"tane 'ill have a signifi"ant effe"t on de' point "al"ulations.

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Section 25 - Equilibrium Ration (K) Data