Thiết kế mô phỏng - Lê Thị Như Ý

Thiãút kãú mä phoíng 1/1

MUÛC LUÛC 1 Giåïi thiãûu täøng quan ................................................................................................3

1.1 Muûc âêch, vai troì cuía thiãút kãú mä phoíng.........................................................3 1.2 Caïc pháön mãöm mä phoíng trong cäng nghãû hoïa hoüc .......................................4

2 Pháön mãöm PRO/II....................................................................................................4 2.1 Lénh væûc sæí duûng .............................................................................................4 2.2 Quaï trçnh mä phoíng bàòng pháön mãöm PRO/II..................................................5

3 Caïc khaïi niãûm cå baín vãö chæng cáút .........................................................................5 3.1 Thiãút bë ngæng tuû âènh thaïp .............................................................................5 3.2 Thiãút bë âun säi âaïy thaïp .................................................................................6

4 Lyï thuyãút nhiãût âäüng hoüc .........................................................................................8 4.1 Phæång phaïp phæång trçnh traûng thaïi ..............................................................8

4.1.1 Phæång trçnh báûc ba täøng quaït .....................................................................9 4.1.2 Phæång trçnh Soave-Redlich-Kwong...........................................................9

5 Læûa choün mä hçnh nhiãût âäüng................................................................................10 5.1 Cå såí læûa choün ...............................................................................................10 5.2 Caïc æïng duûng cuû thãø ......................................................................................13

5.2.1 Caïc quaï trçnh loüc dáöu vaì chãú biãún khê .......................................................13 5.2.2 Caïc quaï trçnh hoïa dáöu ................................................................................13

6 Caïc pháön cå baín cuía PROII...................................................................................14 6.1 Giao diãûn cuía PROII .....................................................................................14

6.1.1 Qui æåïc ban âáöu.........................................................................................14 6.1.2 Cæía säø PRO/II............................................................................................15

7 Caïc thao taïc thæåìng duìng trong mä phoíng bàòng PRO/II ......................................16 7.1 Måí mäüt chæång trçnh mä phoíng måïi (Opening a New Simulation) .............16 7.2 Måí mäüt chæång trçnh mä phoíng âaî coï (Opening an Existing Simulation) ...16 7.3 Ghi mäüt file mä phoíng âang hiãûn haình (Saving the Current Simulation) ....16

7.3.1 Ghi mäüt file mä phoíng âang hiãûn haình.....................................................16 7.3.2 Ghi mäüt file mä phoíng våïi mäüt tãn khaïc...................................................17

7.4 Xoïa mäüt chæång trçnh mä phoíng (Deleting a Simulation)............................17 7.5 Sao cheïp mäüt chæång trçnh mä phoíng (Copy a Simulation) .........................17 7.6 Thay âäøi daûng âæåìng viãön caïc doìng (Modifying the Flowsheet Stream Border Style)..............................................................................................................17 7.7 Hiãøn thë tênh cháút cuía doìng trãn så âäö mä phoíng..........................................18 7.8 Sæí duûng Flash Hot-Key Tool.........................................................................19 7.9 Xuáút mäüt så âäö mä phoíng ra cæía säø læu træî taûm (Exporting the PFD to the Windows Clipboard) .................................................................................................19

ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa


7.10 Nháûp mäüt file PRO/II coï sàón (Importing a PRO/II Keyword Input File) .....20 7.11 Xaïc âënh caïc tênh cháút vãö cán bàòng loíng - håi cuía caïc hãû 2 cáúu tæí (Display BVLE) 20

8 BAÌI TÁÛP AÏP DUÛNG.............................................................................................22 8.1 Baìi toaïn 1: Mä phoíng så âäö cäng nghãû cuía phán xæåíng taïch Meïthane........22

8.1.1 Phæång phaïp tiãún haình ..............................................................................23 8.1.2 Mä phoíng vuìng 1.......................................................................................23

8.2 Baìi toaïn 2: Mä phoíng thiãút bë taïch khê - loíng ...............................................61 8.2.1 Baìi toaïn......................................................................................................61 8.2.2 Kãút quaí: .....................................................................................................62

8.3 Baìi toaïn 3: Tênh nhiãût âäü säi cuía mäüt häùn håüp hai pha åí mäüt aïp suáút nháút âënh 70

8.3.1 Baìi toaïn......................................................................................................70 8.3.2 Giaíi quyãút baìi toaïn.....................................................................................70 8.3.3 Så âäö baìi toaïn ............................................................................................70 8.3.4 Kãút quaí: .....................................................................................................71

8.4 Baìi toaïn 4: Mä phoíng thaïp taïch propane ......................................................78 8.4.1 Baìi toaïn......................................................................................................78 8.4.2 Så âäö baìi toaïn ............................................................................................79 8.4.3 Caïc bæåïc mä phoíng ...................................................................................79

8.5 Baìi toaïn 5: Xaïc âënh âéa naûp liãûu täúi æu cho thaïp taïch propane bàòng cäng cuû Optimiser ...................................................................................................................92

8.5.1 Baìi toaïn......................................................................................................92 8.5.2 Sæí duûng cäng cuû Optimiser .......................................................................93 8.5.3 Giaíi quyãút baìi toaïn.....................................................................................94 8.5.4 Tiãún haình mä phoíng vaì xem kãút quaí ........................................................95

8.6 Baìi toaïn 6: Xaïc âënh säú âéa lyï thuyãút täúi thiãøu vaì chè säú häöi læu täúi thiãøu cho thaïp taïch propane bàòng phæång phaïp shortcut ..........................................................95

8.6.1 Baìi toaïn......................................................................................................95 8.6.2 Tiãún haình mä phoíng vaì xem kãút quaí ........................................................97



1 Giåïi thiãûu täøng quan

1.1 Muûc âêch, vai troì cuía thiãút kãú mä phoíng • Thiãút kãú mä phoíng laì quaï trçnh thiãút kãú våïi sæû tråü giuïp cuía maïy tênh våïi caïc pháön

mãöm chuyãn nghiãûp

• Caïc tæì khoaï thæåìng âæåüc sæí duûng trong thiãút kãú mä phoíng laì :

- Simulation, process simulation : mä phoíng, quaï trçnh mä phoíng

- Dynamic simulation : mä phoíng âäüng

- Simulator : thiãút bë mä phoíng

- Equation of state (EOS) : phæång trçnh traûng thaïi

- Steady-state simulation : mä phoíng traûng thaïi bãön væîng

- To proceed by trial and error : Tiãún haình bàòng caïch moì máùm

- Model : mä hçnh

- Modelling : mä hçnh hoïa

• Mä phoíng laì mäüt cäng cuû cho pheïp ngæåìi kyî sæ tiãún haình cäng viãûc mäüt caïch hiãûu quaí hån khi thiãút kãú mäüt quaï trçnh måïi hoàûc phán têch, nghiãn cæïu caïc yãúu täú aính hæåíng dãún mäüt quaï trçnh âang hoaût âäüng trong thæûc tãú.

• Täúc âäü cuía cäng cuû mä phoíng cho pheïp khaío saït nhiãöu træåìng håüp hån trong cuìng thåìi gian våïi âäü chênh xaïc cao hån nãúu so våïi tênh toaïn bàòng tay. Hån næîa, chuïng ta coï thãø tæû âäüng hoïa quaï trçnh tênh toaïn caïc så âäö cäng nghãû âãø traïnh viãûc phaíi thæûc hiãûn caïc pheïp tênh làûp khäng coï cå såí hoàûc moì máùm. Vê duû, chuïng ta coï thãø sæí duûng mäüt mä hçnh máùu âãø nghiãn cæïu sæû váûn haình cuía mäüt phán xæåíng khi thay âäøi nguäön nguyãn liãûu hoàûc caïc âiãöu kiãûn váûn haình cuía caïc thiãút bë aính hæåíng âãún hiãûu suáút thu vaì cháút læåüng saín pháøm nhæ thãú naìo ? Âiãöu naìy seî âån giaín, nhanh choïng vaì tiãút kiãûm hån nhiãöu so våïi thæí trãn phán xæåíng thæûc tãú. Vç ràòng cå såí tênh toaïn caïc cäng cuû mä phoíng thæåìng dæûa trãn caïc bäü cå såí dæî liãûu chuáøn hoïa, nãn mäüt khi âaî xáy dæûng mäüt mä hçnh håüp lyï thç báút kyì mäüt kyî sæ naìo cuîng coï thãø sæí duûng noï âãø tênh toaïn vaì cho caïc kãút quaí chênh xaïc.

• Thiãút kãú mä phoíng thæåìng âæåüc sæí duûng âãø :

- Thiãút kãú (Designing) mäüt quaï trçnh måïi

- Thæí laûi, kiãøm tra laûi (Retrofitting) caïc quaï trçnh âang täön taûi

- Hiãûu chènh (Troubleshooting) caïc quaï trçnh âang váûn haình

- Täúi æu hoïa (Optimizing) caïc quaï trçnh váûn haình



• Âãø xáy dæûng mäüt mä hçnh mä phoíng hiãûu quaí, chuïng ta phaíi xaïc âënh âuïng muûc tiãu. Bæåïc âáöu tiãn trong báút cæï mäüt quaï trçnh mä phoíng naìo laì læåüng hoïa caïc muûc tiãu caìng nhiãöu caìng täút. Caïc kãút quaí âaût âæåüc thæåìng phuû thuäüc vaìo caïc yãu cáöu âàût ra. Nhæ váûy, træåïc khi mä phoíng mäüt quaï trçnh nãn âàût ra caïc cáu hoíi sau :

- Muûc âêch sæí duûng cäng cuû mä phoíng trong træåìng håüp naìy âãø laìm gç ?

- Quaï trçnh mä phoíng seî thæûc hiãûn nhæîng viãûc gç ?

- Sæû phæïc taûp coï cáön thiãút khäng ?

- Cáön thiãút phaíi tçm ra caïc kãút quaí naìo tæì quaï trçnh mä phoíng ?

• Cáön nhåï ràòng caïc giaï trë thu âæåüc tæì kãút quaí mä phoíng phuû thuäüc ráút nhiãöu vaìo nhæîng læûa choün ban âáöu maì chuïng ta âaî nháûp vaìo.

1.2 Caïc pháön mãöm mä phoíng trong cäng nghãû hoïa hoüc • Trong cäng nghãû hoïa hoüc, ngæåìi ta sæí duûng ráút nhiãöu caïc pháön mãöm mä phoíng :

- DESIGN II (WINSIM) : sæí duûng trong cäng nghiãûp hoïa hoüc noïi chung

- PRO/II (SIMSCI) : sæí duûng trong cäng nghiãûp hoïa hoüc, cäng nghiãûp loüc - hoïa dáöu

- PROSIM : sæí duûng trong cäng nghiãûp hoïa hoüc

- HYSIM (HYSYS) : sæí duûng trong cäng nghiãûp chãú biãún khê

• Trong caïc pháön mãöm kãø trãn, pháön mãöm PRO/II laì pháön mãöm näøi tiãúng nháút, âæåüc sæí duûng räüng raîi nháút trong nhiãöu lénh væûc cäng nghiãûp.

2 Pháön mãöm PRO/II

2.1 Lénh væûc sæí duûng • Pháön mãöm PRO/II laì pháön mãöm tênh toaïn chuyãn duûng trong caïc lénh væûc cäng

nghãû hoïa hoüc noïi chung, âàûc biãût trong lénh væûc loüc dáöu, hoïa dáöu, polymer, hoïa dæåüc, ... Âáy laì pháön mãöm tênh toaïn ráút chênh xaïc caïc quaï trçnh chæng cáút. Laì saín pháøm cuía SIMSCI, hçnh thaình tæì nàm 1967 vaì âæåüc chênh thæïc sæí duûng vaìo nàm 1988 sau nhiãöu láön âæåüc caíi tiãún. Hiãûn nay, chuïng ta âang sæí duûng phiãn baín PRO/II 7.0

• PRO/II váûn haình theo caïc modul liãn tiãúp, mäùi thiãút bë âæåüc tênh riãng leî vaì láön læåüt tênh cho tæìng thiãút bë.

• PRO/II bao gäöm caïc nguäön dæî liãûu phong phuï : thæ viãûn caïc cáúu tæí hoïa hoüc, caïc phæång phaïp xaïc âënh caïc tênh cháút nhiãût âäüng, caïc kyî xaío váûn haình caïc thiãút bë hiãûn âaûi âãø cung cáúp cho caïc kyî sæ cäng nghãû caïc kyî nàng âãø biãøu diãùn táút caí caïc



tênh toaïn cán bàòng váût cháút vaì nàng læåüng cáön thiãút khi mä phoíng caïc traûng thaïi dæìng cuía caïc så âäö cäng nghãû.

• Pháön mãöm PRO/II âæåüc sæí duûng theo nhàòm 2 muûc âêch :

- Thiãút kãú mäüt phán xæåíng måïi (Sizing)

- Mä phoíng mäüt phán xæåíng âaî âæåüc xáy dæûng trong thæûc tãú âãø nghiãn cæïu caïc yãúu täú aính hæåíng âãún sæû váûn haình cuía noï (Rating) nhæ : thay âäøi nguäön nguyãn liãûu, âiãöu kiãûn váûn haình hoàûc tiãu chuáøn kyî thuáût cuía saín pháøm, ...

2.2 Quaï trçnh mä phoíng bàòng pháön mãöm PRO/II • Træåïc khi tiãún haình mä phoíng, chuïng ta phaíi diãùn âaût caïc dæî liãûu tæì så âäö thæûc tãú

thaình mä hçnh mä phoíng. Quaï trçnh naìy bao gäöm caïc bæåïc sau :

- Xaïc âënh hãû âån vë âo : coï 3 hãû âån vë âo : hãû Anh, hãû Meït vaì hãû SI. Tuyì træåìng håüp, chuïng ta choün hãû âån vë âo cho thêch håüp, thäng thæåìng choün hãû Meït;

- Xaïc âënh thaình pháön cáúu tæí coï trong hãû : âæåüc choün tæì nguäön dæî liãûu phong phuï caïc cáúu tæí cuía PROII;

- Læûa choün caïc phæång trçnh nhiãût âäüng thêch håüp : trãn cå såí thaình pháön hoïa hoüc cuía nguyãn liãûu vaì âiãöu kiãûn váûn haình cuía thiãút bë ;

- Læûa choün caïc doìng nguyãn liãûu vaì saín pháøm : xaïc âënh thaình pháön, traûng thaïi nhiãût cuía caïc doìng;

- Xaïc âënh caïc dæî liãûu vãö thiãút bë vaì âiãöu kiãûn váûn haình cho caïc thiãút bë.

• Hån næîa, trong nhiãöu træåìng håüp chuïng ta phaíi thay âäøi så âäö cäng nghãû thæûc tãú sang muûc âêch mä phoíng. Màûc duì coï sæû tæång æïng giæîa så âäö cäng nghãû thæûc tãú vaì så âäö mä phoíng nhæng váùn coï nhæîng sæû khaïc biãût cáön chuï yï.

• Vç cäng cuû mä phoíng chè mä taí traûng thaïi dæìng nãn trong så âäö mä phoíng khäng nãn bäú trê caïc thiãút bë âiãöu khiãøn, kiãøm tra

3 Caïc khaïi niãûm cå baín vãö chæng cáút

3.1 Thiãút bë ngæng tuû âènh thaïp PRO/II màûc âënh Condenser âæåüc xem laì mäüt báûc thay âäøi näöng âäü (mäüt âéa lyï thuyãút) vaì coï 4 daûng Condenser :

• Partial : Loíng åí âéa 2 âæåüc laìm laûnh vaì chè ngæng tuû mäüt pháön. Loaûi Condenser naìy thæûc sæû laì mäüt báûc thay âäøi näöng âäü. Nhiãût âäü trong Condenser chênh laì nhiãût âäü âiãøm sæång cuía häùn håüp håi cán bàòng Gäöm 2 loaûi :



- loaûi Distillat vapor : loíng ngæng tuû chè âãø häöi læu vãö âènh thaïp, coìn saín pháøm láúy ra åí thãø håi âæåüc goüi laì Overhead.

- Loaûi Distillat mixe : loíng ngæng tuû mäüt pháön âãø häöi læu vãö âènh thaïp, coìn laûi láúy ra laìm saín pháøm ⇒ saín pháøm âènh gäöm 2 loaûi laì saín pháøm håi vaì saín pháøm loíng.

• Bubble Temperature : Loíng åí âéa 2 âæåüc âæåüc laìm laûnh âãún nhiãût âäü âiãøm säi cuía häùn håüp vaì ngæng tuû hoaìn toaìn, mäüt pháön cho häöi læu vãö âéa 2 åí âènh thaïp, pháön coìn laûi láúy ra daûng saín pháøm loíng, âæåüc goüi laì Fixe Rate Draw. Nhiãût âäü trong Condenser chênh laì nhiãût âäü âiãøm säi cuía häùn håüp loíng cán bàòng

- Subcooled, Fixe Temperature : Loíng åí âéa 2 âæåüc âæåüc laìm laûnh dæåïi nhiãût âäü âiãøm säi cuía häùn håüp loíng. Loíng naìy goüi laì loíng quaï laûnh.

- Subcooled, Fixe Temperature Drop : Loaûi Condenser naìy cuîng giäúng nhæ loaûi trãn nhæng âäü quaï laûnh cuía häùn håüp loíng âæåüc xaïc âënh båíi mäüt giaï trë naìo âoï.

LoíngLoíng

HåiHåi

a- Daûng Partial

Distillate vapor Distillate mixe

b- Daûng Bubble

3.2 Thiãút bë âun säi âaïy thaïp PRO/II màûc âënh Reboiler âæåüc xem laì mäüt báûc thay âäøi näöng âäü vaì coï 3 daûng Reboiler :

- Daûng Kettle : âæåüc màûc âënh (qui chuáøn)

- Thermosiphon without baffles

- Thermosiphon with baffles



210

300

?

?

?

?

50

4 Lyï thuyãút nhiãût âäüng hoüc Caïc tênh cháút nhiãût âäüng laì cå såí dæî liãûu quan troüng nháút cho viãûc tênh toaïn quaï

trçnh phán taïch toaìn hãû thäúng.

Coï nhiãöu phæång phaïp tênh toaïn caïc tênh cháút naìy, trong âoï, quan troüng nháút laì 2 phæång phaïp :

- Phæång phaïp tæång quan : API vaì Rackett

- Phæång phaïp phæång trçnh traûng thaïi : phæång trçnh báûc ba täøng quaït, cäng thæïc Alpha, caïc qui luáût häùn håüp, phæång trçnh SRK, phæång trçnh PR, phæång trçnh SRKP, SRKM, SRKS, ...

Phæång phaïp API vaì Rackett tênh toaïn khaï chênh xaïc tè troüng cuía pha loíng, coìn caïc tênh cháút nhiãût âäüng khaïc nhæ : enthalpie, entropie loíng vaì håi, tè troüng pha håi, ... thç âæåüc tênh toaïn ráút chênh xaïc bàòng caïc phæång trçnh traûng thaïi nhæ : SRK, SRKM, ...

4.1 Phæång phaïp phæång trçnh traûng thaïi Phæång phaïp tênh cán bàòng pha naìy coï thãø aïp duûng trong mäüt khoaíng räüng nhiãût

âäü vaì aïp suáút. Ngoaìi ra, coìn âãø tênh toaïn caïc tênh cháút nhiãût âäüng nhæ Enthalpie vaì Entropie. Traûng thaïi tham khaío cho caí hai pha loíng-håi laì khê lyï tæåíng, caïc chãnh lãûch



cuía hãû thæûc so våïi hãû lyï tæåíng âæåüc xaïc âënh bàòng caïch tênh hãû säú hoaût aïp cho caí hai pha.

Cuû thãø âäúi våïi caïc phæång trçnh traûng thaïi báûc ba, caïc âiãöu kiãûn tåïi haûn vaì quaï tåïi haûn âæåüc tênh toaïn khaï chênh xaïc. Bàòng caïch sæí duûng mäüt haìm theo nhiãût âäü biãøu diãùn læûc háúp dáùn giæîa caïc phán tæí, haìm thãø têch, quy luáût häùn håüp, caïc phæång trçnh traûng thaïi báûc ba âaî âæåüc váûn duûng khaï thaình cäng âãø tênh cán bàòng loíng - håi caïc hãû phi lyï tæåíng låïn.

4.1.1 Phæång trçnh báûc ba täøng quaït

Phæång trçnh gäöm 2 tham säú a vaì b âæåüc biãøu diãùn dæåïi daûng sau :

( )22 wbubvv

Tabv

RTP++

−−

=

Trong âoï : P : aïp suáút

T : nhiãût âäü tuyãût âäúi

v : thãø têch mol

u, w : hàòng säú, daûng säú nguyãn

Caïc giaï trë cuía u vaì w seî xaïc âënh daûng cuía phæång trçnh traûng thaïi báûc ba nhæ baíng dæåïi âáy :

u w Phæång trçnh traûng thaïi

0

1

2

0

0

-1

Van der Waals (vdW)

Redlich-Kwrong (RK)

Peng-Robinson (PR)

4.1.2 Phæång trçnh Soave-Redlich-Kwong

Âãún nàm 1972, âãø caíi thiãûn tênh chênh xaïc khi tênh aïp suáút håi cuía cáúu tæí tinh khiãút vaì tênh cán bàòng loíng - håi cuía hãû âa cáúu tæí, Soave âaî xaïc âënh : ( ) ( ) ( )cTaTTa .α=

( ) ( )[ ]221rT1M1T /−+=α

217605741480M ω−ω+= ,,,

Trong âoï :

a (T) : hãû säú phuû thuäüc vaìo nhiãût âäü



α (T) : haìm phuû thuäüc vaìo nhiãût âäü, âàûc træng cho læûc háöp dáùn giæîa caïc phán tæí

Tc : nhiãût âäü tåïi haûn

Acentricsäú hàòng:

goün ruït âäü nhiãût :

ω

=c

r TTT

5 Læûa choün mä hçnh nhiãût âäüng

5.1 Cå såí læûa choün • Læûa choün mä hçnh nhiãût âäüng thêch håüp cho mäüt æïng duûng cuû thãø âoïng mäüt vai troì

ráút quan troüng, aính hæåíng låïn âãún âäü chênh xaïc cuía kãút quaí mä phoíng

• Mäùi phæång phaïp nhiãût âäüng cho pheïp tênh caïc thäng säú sau :

- Hàòng säú cán bàòng pha K : thãø hiãûn sæû phán bäú cáúu tæí giæîa caïc pha åí âiãöu kiãûn cán bàòng

- Enthapie cuía caïc pha loíng vaì pha håi : xaïc âënh nàng læåüng cáön thiãút âãø chuyãøn mäüt hãû tæì traûng thaïi nhiãût âäüng naìy sang traûng thaïi khaïc

- Enthapie cuía caïc pha loíng vaì pha håi : nhàòm phuûc vuû viãûc tênh toaïn caïc maïy neïn, thiãút bë giaín nåí vaì nàng læåüng tæû do täúi thiãøu åí caïc thiãút bë phaín æïng

- Tè troüng cuía pha loíng vaì pha håi : âãø tênh toaïn quaï trçnh truyãön nhiãût, tråí læûc vaì xaïc âënh kêch thæåïc thaïp chæng cáút

• Âãø læûa choün mä hçnh nhiãût âäüng thêch håüp, nãn dæûa vaìo caïc yãúu täú sau :

- Baín cháút cuía caïc âàûc træng nhiãût âäüng cuía hãû nhæ : Hàòng säú cán bàòng loíng-håi (VLE : Vapor Liquid Equilibrium) cuía caïc quaï trçnh chæng cáút, cä âàûc hoàûc bäúc håi, quaï trçnh trêch ly, ...

- Thaình pháön cuía häùn håüp

- Phaûm vi nhiãût âäü vaì aïp suáút

- Tênh sàón coï cuía caïc thäng säú hoaût âäüng cuía caïc thiãút bë

• Cuû thãø, ta coï thãø dæûa vaìo så âäö sau :



5.2 Caïc æïng duûng cuû thãø

5.2.1 Caïc quaï trçnh loüc dáöu vaì chãú biãún khê

• Hãû thäúng aïp suáút tháúp (thaïp chæng cáút aïp suáút khê quyãøn vaì chán khäng) : Trong nguyãn liãûu cuía caïc hãû thäúng naìy noïi chung coï khoaíng ≥ 3 % thãø têch pháön nheû ⇒ coï thãø choün mä hçnh BK10 hoàûc GS vaì caïc biãún thãø cuía noï. Khi haìm læåüng pháön nheû låïn (nháút laì thaình pháön C1) ⇒ nãn choün EOS: SRK, PR

• Hãû thäúng aïp suáút cao (thaïp chæng phán âoaûn saín pháøm cuía phán xæåíng cracking, cäúc hoïa, ...) Trong hãû thäúng naìy, haìm læåüng pháön nheû noïi chung låïn hån ⇒ Caïc mä hçnh nãn choün : GS, SRK, PR

• Caïc quaï trçnh chãú biãún khê thiãn nhiãn : trong thaình pháön thæåìng coï chæïa N2, khê acide (CO2, H2S) vaì caïc hydrocarbon nheû :

- Våïi loaûi khê chæïa êt hån 5% N2, CO2, H2S vaì khäng coï cáúu tæí phán cæûc naìo khaïc ⇒ nãn choün SRK, PR hoàûc Benedict - Webb - Rubin - Starling (BWRS)

- Våïi loaûi khê chæïa nhiãöu hån 5% N2, CO2, H2S nhæng khäng coï cáúu tæí phán cæûc naìo khaïc ⇒ nãn choün SRK, PR vaì ngæåìi sæí duûng nãn âæa vaìo caïc thäng säú tæång taïc âãø thu âæåüc kãút quaí täút hån

- Våïi hãû thäúng xæí lyï khê thiãn nhiãn coï láùn næåïc laìm viãûc åí aïp suáút cao (trong træåìng håüp naìy âäü hoaì tan cuía hydrocarbon trong næåïcseî tàng lãn) ⇒ nãn choün caïc biãún thãø cuía caïc phæång trçnh traûng thaïi nhæ : SRKM, PRM hay SRKS, SRKKD (Kabadi - Danner Modification to SRK)

- Khi khê thiãn nhiãn chæïa caïc cáúu tæí phán cæûc nhæ meïthanol ⇒ SRKM, PRM hay SRKS

5.2.2 Caïc quaï trçnh hoïa dáöu

• Quaï trçnh xæí lyï hydrocarbon nheû :

- ÅÍ aïp suáút tháúp : SRK, PR

- ÅÍ aïp suáút cao : SRKKD

• xæí lyï hydrocarbon thåm :

- P < 2 bars : IDEAL

- P > 2 bars : GS, SRK, PR

• Xæí lyï häùn håüp hydrocarbon thåm vaì hydrocarbon khaïc : NRTL, UNIQUAC, UNIFAC



6 Caïc pháön cå baín cuía PROII

6.1 Giao diãûn cuía PROII

6.1.1 Qui æåïc ban âáöu

Khi khåíi âäüng PROII, âáöu tiãn seî xuáút hiãûn mäüt cæía säø giao diãûn qui æåïc ban âáöu nhæ sau:

Caïc nuït hoàûc caïc biãøu tæåüng trong mäüt vaìi træåìng håüp âæåüc viãön quanh båíi 1 trong 6 maìu sau : âoí, xanh luûc, xanh dæång, vaìng, náu vaì âen. YÏ nghéa cuía mäùi maìu nhæ sau :

• Âoí : dæî liãûu yãu cáöu cáön phaíi nháûp

• Xanh luûc : dæî liãûu màûc âënh hoàûc læûa choün

• Xanh dæång : dæî liãûu baûn væìa cung cáúp thoaí maîn yãu cáöu

• Vaìng : baïo ràòng säú liãûu baûn væìa nháûp ngoaìi khoaíng cho pheïp

• Náu : dæî liãûu khäng coï giaï trë

• Âen : dæî liãûu khäng yãu cáöu nháûp vaìo



6.1.2 Cæía säø PRO/II

Tæì File menu ⇒ Choün New : mäüt cæía säø View1 seî xuáút hiãûn cho chuïng ta mäüt flowsheet måïi nhæ sau:

Maìn hçnh bao gäöm :

• Doìng trãn cuìng goüi laì Application Title Bar (Thanh tiãu âãö æïng duûng), åí âoï coï tãn cuía æïng duûng laì PRO/II with PROVISION, keìm theo laì Document Title Bar (Thanh tiãu âãö taìi liãûu) åí âoï coï tãn cuía chæång trçnh mä phoíng âang thæûc hiãûn (chàóng haûn laì View 1 - laì tãn nguyãn cuía taìi liãûu khi måïi khåíi âäüng PRO/II)

• Doìng thæï hai goüi laì Menu Bar (Thanh trçnh âån) gäöm 10 muûc tæì File âãún Help ;

• Doìng thæï ba goüi laì Standard Tool Bar (Thanh cäng cuû chuáøn) chæïa biãøu tæåüng cuía caïc lãûnh thæåìng duìng

• Bãn phaíi vaì phêa dæåïi maìn hçnh laì thanh træåüt doüc vaì thanh træåüt ngang

• Bãn phaíi maìn hçnh, bãn ngoaìi thanh træåüt doüc laì thanh cäng cuû floating PFD (Pipe Flow Diagram). Nãúu thanh cäng cuû PFD khäng hiãøn thë thç ta coï thãø goüi noï nhæ sau :

- click vaìo biãøu tæåüng Show or Hide PFD Palette trãn Standard Tool Bar

- hoàûc tæì View ⇒ Palettes ⇒ nhàõp choün (hoàûc khäng) PFD

• Ngoaìi ra coìn coï thanh cäng cuû Run. Âãø laìm xuáút hiãûn hoàûc biãún máút thanh cäng cuû naìy cuîng tæì View ⇒ Palettes ⇒ nhàõp choün (hoàûc khäng) Run



7 Caïc thao taïc thæåìng duìng trong mä phoíng bàòng PRO/II

7.1 Måí mäüt chæång trçnh mä phoíng måïi (Opening a New Simulation)

• Tæì File Menu ⇒ New

• Nãúu baûn muäún PRO/II luän luän âæåüc måí våïi mäüt chæång trçnh mä phoíng måïi ⇒ Options Menu ⇒ New File on Startup

7.2 Måí mäüt chæång trçnh mä phoíng âaî coï (Opening an Existing Simulation)

Baûn coï thãø måí báút kyì mäüt chæång trçnh mä phoíng naìo âaî âæåüc ghi træåïc âoï âãø chènh sæía, xem hoàûc in. Qui trçnh :

• Tæì File Menu ⇒ Open ⇒ hiãøn thë cæía säø Open Simulation .

• Âaïnh tãn chæång trçnh vaìo hoàûc choün tãn file mä phoíng

• OK hoàûc Enter ⇒ hiãøn thë file Simulation cáön thiãút

7.3 Ghi mäüt file mä phoíng âang hiãûn haình (Saving the Current Simulation)

7.3.1 Ghi mäüt file mä phoíng âang hiãûn haình

• Tæì File Menu ⇒ Save ⇒ nãúu baûn chæa ghi chæång trçnh mä phoíng naìy láön naìo thç seî hiãøn thë cæía säø Save as ⇒ nháûp tãn ⇒ Choün OK hoàûc nhàõp Enter. Coìn sau láön ghi âáöu tiãn, muäún ghi laûi file âang hiãûn haình ⇒ nhàõp vaìo biãøu tæåüng Save

• Chæång trçnh PRO/II seî tæû âäüng neïn 3 file dæî liãûu (*.pr1, .pr2, .pr3) vaì 1 file flowsheet biãøu âäö caïc doìng (*.sfd) thaình mäüt file âån *.prz. Vç váûy, bãn caûnh viãûc giaím kêch thæåïc cuía caïc file læu træî coìn âaím baío ràòng viãûc caìi âàût file âaî hoaìn thaình mäùi khi chuïng ta ghi caïc chæång trçnh mä phoíng

• Chæïc nàng Autosave cuía PRO/II seî tæû âäüng taûo mäüt file sao cheïp dæû phoìng (backup file). Nãúu baûn âoïng hoàûc thoaït ra chæång trçnh mä phoíng maì khäng ghi thç file naìy seî bë xoïa. Haîy choün Options / simulation Defaults / Autosave tæì menu bar ⇒ hiãøn thë cæía säø Autosave Options ⇒ nhàõp choün Automatic Save File every ⇒ nháûp chu kyì save (phuït) ⇒ OK



7.3.2 Ghi mäüt file mä phoíng våïi mäüt tãn khaïc

Tæì File Menu ⇒ choün Save as ⇒ hiãøn thë cæía säø Save as ⇒ Nháûp tãn måïi cho chæång trçnh mä phoíng ⇒ Choün OK hoàûc nhàõp Enter

7.4 Xoïa mäüt chæång trçnh mä phoíng (Deleting a Simulation)

• Tæì File Menu ⇒ choün Delete ⇒ PRO/II seî hiãøn thë mäüt danh saïch caïc file mä phoíng âaî coï

• Nháûp hoàûc choün tãn cuía flie muäún xoïa (Baûn khäng thãø xoïa mäüt chæång trçnh mä phoíng âang hiãûn haình)

• Choün OK hoàûc nhàõp Enter ⇒ PRO/II seî xoïa táút caí caïc file liãn kãút våïi chæång trçnh mä phoíng naìy

7.5 Sao cheïp mäüt chæång trçnh mä phoíng (Copy a Simulation)

• PRO/II coï thãø copy táút caí caïc file liãn kãút våïi chæång trçnh mä phoíng (3 file dæî liãûu vaì 1 flowsheet) vaìo mäüt file mä phoíng måïi hoàûc âang hiãûn haình. Nãúu baûn muäún copy vaìo mäüt file mä phoíng âang hiãûn haình ⇒ PRO/II seî hoíi baûn coï muäún viãút âeì lãn file hiãûn haình naìy khäng ?

• Tæì File Menu ⇒ choün Copy ⇒ PRO/II seî hiãøn thë cæía säø Select File to Copy ⇒ Haîy choün tãn file cáön copy (Baûn khäng thãø copy mäüt chæång trçnh mä phoíng âang hiãûn haình) ⇒ Nháûp tãn file âêch (target) ⇒ OK

7.6 Thay âäøi daûng âæåìng viãön caïc doìng (Modifying the Flowsheet Stream Border Style)

• Thäng thæåìng âæåìng viãön caïc doìng thæåìng coï daûng hçnh chæî nháût ⇒ Chuïng ta coï thãø thay âäøi thaình âæåìng viãön daûng troìn. Qui trçnh nhæ sau :

- Right-click vaìo doìng âæåüc choün ⇒ hiãøn thë cæía säø læûa choün

- Choün Display ⇒ xuáút hiãûn cæía säø Stream Style

- Choün Circle tæì drop-down list box cuía Stream Label Border

- click OK ⇒ âæåìng viãön doìng âæåüc choün tæì daûng hçnh chæî nháût chuyãøn thaình âæåìng viãön daûng troìn

• Våïi caïch nhæ trãn, baûn coï thãø thay âäøi daûng âæåìng viãön cho tæìng doìng riãng leî. Coìn nãúu muäún, baûn coï thãø click chuäüt traïi vaì queït choün mäüt hçnh chæî nháût bao



xung quanh caïc doìng muäún thay âäøi daûng âæåìng viãön räöi tiãún haình qui trçnh nhæ trãn. Hoàûc baûn coï thãø màûc âënh daûng âæåìng viãön cho táút caí caïc doìng ngay tæì âáöu theo qui trçnh sau :

- Tæì Options Menu ⇒ Drawing Defauts ⇒ Stream Display ⇒ hiãøn thë cæía säø Stream Style

- Choün Circle tæì drop-down list box cuía Stream Label Border. Vaì læûa choün naìy chè coï giaï trë khi chuïng ta choün Name åí muûc Stream Label Type ⇒ OK

7.7 Hiãøn thë tênh cháút cuía doìng trãn så âäö mä phoíng • Qui trçnh nhæ sau :

- Right-click vaìo doìng âæåüc choün ⇒ hiãøn thë cæía säø læûa choün


- Choün Properties tæì drop-down list box åí muûc Stream Label Type

- Màûc âënh åí muûc Property List laì Property Label List ⇒ seî hiãøn thë tãn, nhiãût âäü, aïp suáút vaì læu læåüng doìng ⇒ OK



7.8 Sæí duûng Flash Hot-Key Tool • PRO/II coï mäüt cäng cuû hæîu êch cho pheïp hiãøn thë nhanh choïng caïc tênh toaïn flash

cuía báút kyì doìng naìo âæåüc choün ⇒ Âoï laì cäng cuû Flash Hot-Key, cung cáúp mäüt phæång tiãûn nhanh choïng, dãù daìng âãø xaïc âënh haìm læåüng vaì thaình pháön cuía pha loíng vaì pha håi cuía báút kyì doìng naìo

• Haîy thæí våïi doìng S1 :

- click choün doìng S1

- click vaìo biãøu tæåüng Do flash ⇒ seî xuáút hiãûn trãn Programmer’s File Editor : file [S1.000]

7.9 Xuáút mäüt så âäö mä phoíng ra cæía säø læu træî taûm (Exporting the PFD to the Windows Clipboard)

Tæì Clipboard, baûn coï thãø daïn mäüt caïch âån giaín hçnh veî lãn báút kyì mäüt chæång trçnh soaûn thaío naìo nhæ trong Microsoft Word. Qui trçnh nhæ sau :

• Tæì Menu ⇒ File ⇒ Export

• Choün Flowsheet Drawing



• Click OK ⇒ PRO/II seî hiãøn thë mäüt häüp häüi thoaûi âãø khàóng âënh ràòng flowsheet âaî âæåüc xuáút ra cæía säø læu træî taûm

7.10 Nháûp mäüt file PRO/II coï sàón (Importing a PRO/II Keyword Input File)

Baûn coï thãø nháûp mäüt file keyword Input cuía PRO/II daûng *.inp coï sàón vaìo giao diãûn PRO/II âang hiãûn haình. PRO/II seî tæû âäüng chuyãøn âäøi file naìy thaình mäüt så âäö tênh toaïn vaì chuïng ta coï thãø tiãún haình mä phoíng nhæ mä phoíng trãn mäüt så âäö PFD, tæì âoï chuïng ta coï thãø chènh sæía theo yï mçnh

• Tæì Menu ⇒ File ⇒ Import

• Nháûp hoàûc choün tãn cuía flie muäún nháûp

• Choün OK hoàûc nhàõp Enter

7.11 Xaïc âënh caïc tênh cháút vãö cán bàòng loíng - håi cuía caïc hãû 2 cáúu tæí (Display BVLE)

Giaí sæí ta coï hãû 2 cáúu tæí: propane vaì butane. Âãø xaïc âënh caïc tênh cháút vãö bàòng loíng - håi cuía caïc hãû 2 cáúu tæí naìy åí aïp suáút thæåìng (1 atm) hay åí mäüt aïp suáút báút kyì naìo âoï, ta sæí duûng cäng cuû Display BVLE.

Qui trçnh nhæ sau :

• Choün hãû âån vë

• Choün cáúu tæí

• Choün mä hçnh nhiãût âäüng thêch håüp

• Nhàõp choün biãøu tæåüng Display BVLE ⇒ Choün caïc cáúu tæí, choün aïp suáút vaì nhàõp choün Calculate ⇒ Ta seî âæåüc 5 loaûi biãøu âäö:

• Biãøu âäö X - Y

• Biãøu âäö T - X - Y

• Biãøu âäö hãû säú Fugacity

• Biãøu âäö hàòng säú cán bàòng K thay âäøi theo thaình pháön mol

• Biãøu âäö hàòng säú cán bàòng K thay âäøi theo



8 BAÌI TÁÛP AÏP DUÛNG

8.1 Baìi toaïn 1: Mä phoíng så âäö cäng nghãû cuía phán xæåíng taïch Meïthane

Thaïp Demethanizer âãø taïch methane ra khoíi häùn håüp khê trong så âäö sæí duûng turbo-expander.

Læu læåüng doìng khê nguyãn liãûu : 8 m3/s

Nhiãût âäü : 120 oF

Aïp suáút : 602,7 psia (pound per square inch absolute)

(1 psi = 0,06896 bar; 602,7 psia = 588,2 psig)

Thaình pháön cuía häùn håüp khê ban âáöu nhæ sau :

Cáúu tæí % mol Cáúu tæí % mol

N2

CH4

C2H6

C3H8

i-C4H10

7,91 73,05 7,68 5,69 0,99

n-C4H10

i-C5H12

n-C5H12

C6H14

C7H16

2,44 0,69 0,82 0,42 0,31

Så âäö nhæ sau : (Hçnh I-1)

ThS. Lã Thë Nhæ YÏ Âaûi H

125 psia

oüc Baïch Khoa


Haîy xaïc âënh: 1. Cäng suáút thæûc cuía maïy neïn C1? 2. Thaình pháön, nhiãût âäü vaì aïp suáút cuía caïc doìng saín pháøm khê vaì loíng?

8.1.1 Phæång phaïp tiãún haình

Chuïng ta seî chia så âäö trãn thaình 2 vuìng :

• Vuìng 1 : Chuïng ta seî mä phoíng 3 thiãút bë (Hçnh 1-1) âãø laìm quen våïi pháön mãöm PROII

• Vuìng 2 : Chuïng ta seî mä phoíng toaìn bäü quaï trçnh âãø tçm hiãøu nhæîng âiãøm æu viãût cuía pháön mãöm PROII

8.1.2 Mä phoíng vuìng 1

• Vuìng 1 bao gäöm 3 thiãút bë : thiãút bë taïch, van giaím aïp loíng vaì turbo-expander

• Så âäö nhæ sau (Hçnh 1-1)

• Caïc bæåïc tiãún haình mä phoíng :

8.1.2.1 Måí mäüt flowsheet måïi :

Tæì File menu ⇒ Choün New : mäüt cæía säø View1 seî xuáút hiãûn cho chuïng ta mäüt flowsheet måïi, trãn âoï, chuïng ta seî tiãún haình xáy dæûng caïc så âäö bàòng cäng cuû floating PFD

8.1.2.2 Xaïc âënh hãû âån vë âo cho quaï trçnh mä phoíng :

• Nhàõp vaìo biãøu tæåüng caïi thæåïc âo (Input UOM) trãn doìng Standard Tool Bar (hoàûc tæì Menu ⇒ Input ⇒ Input of Measure)

• Xuáút hiãûn baíng Defaut Units of Measure for Problem Data Input

• Choün Initialize from UOM library

• Choün hãû ENGLISH-SET1 hoàûc METRIC-SET1. Giaí thiãút choün hãû ENGLISH-SET1. Tuy nhiãn, chuïng ta coï thãø thay âäøi âån vë âo cho tæìng âaûi læåüng bàòng caïch nhàõp vaìo caïc drop-down list vaì choün

• Nãúu nhàõp vaìo Standard Vapor Conditions... (âiãöu kiãûn tiãu chuáøn cuía pha håi) ⇒ hiãøn thë cæía säø Problem Standard Vapor Conditions. Tuyì theo hãû âån vë maì âiãöu kiãûn naìy seî khaïc nhau. Caïc giaï trë tiãu chuáøn âæåüc màûc âënh trong PRO/II laì :

Hãû âån vë Nhiãût âäü Aïp suáút Thãø têch khê

English

Metric

60oF

0oC

14.696 psia

1.0332 kg/cm2

379.48 ft3/lbmol

22.414 m3/kgmol



SI 273.15 K 101.32 kPa 22.414 m3/kgmol

• Nãúu nhàõp vaìo TVP and RVP Conditions... (âiãöu kiãûn xaïc âënh aïp suáút håi baîo hoìa thæûc vaì aïp suáút håi baîo hoìa Reid ) ⇒ hiãøn thë cæía säø Problem TVP and RVP Conditions, trong âoï PRO/II màûc âënh : TVP âæåüc xaïc âënh åí 100oF vaì RVP âæåüc xaïc âënh theo caïc phæång phaïp API Naphta, API Crude, ... ⇒ OK

• Âãø hiãøn thë thæ viãûn caïc âån vë âo ⇒ Tæì Options / Units of Measure List ⇒ xuáút hiãûn cæía säø Units of Measure Library cung cáúp 3 hãû âån vë âo chênh : English, Metric vaì SI ⇒ ta coï thãø taûo måïi, copy, xoïa, ... caïc loaûi âån vë

8.1.2.3 Thiãút láûp caïc thiãút bë coï trong så âäö :

• Cäng cuû floating PFD coï thãø dëch chuyãøn âãún báút kyì nåi naìo trãn giao diãûn PROII

• Click vaìo biãøu tæåüng thiãút bë cáön thiãút trãn cäng cuû floating PFD räöi click laûi mäüt láön næîa vaìo vë trê muäún âàût thiãút bë trãn så âäö

• Sau khi âaî click vaìo biãøu tæåüng 1 thiãút bë naìo âoï maì chæa âàût noï vaìo trong så âäö, nãúu khäng muäún choün thiãút bë naìy næîa ⇒ right-click

• Muäún xoïa boí mäüt thiãút bë coï trong så âäö ⇒ click vaìo thiãút bë muäún xoïa ⇒ xung quanh thiãút bë âoï seî coï mäüt âæåìng viãön âæït ⇒ báúm Delete hoàûc right-click ⇒ nhàõp choün Delete

• Våïi vuìng 1, ta click choün 3 thiãút bë : thiãút bë taïch F1, van giaím aïp loíng V1 vaì turbo-expander EX1

8.1.2.4 Thiãút láûp caïc doìng læu thãø chuyãøn âäüng ra vaìo caïc thiãút bë :

• Click vaìo nuït Streams trãn cäng cuû floating PFD ;

• Khi âoï, trãn caïc thiãút bë seî xuáút hiãûn caïc cæía vaìo vaì ra cuía caïc doìng læu thãø. Caïc cæía vaìo vaì ra yãu cáöu cáön phaíi coï (required) seî coï maìu âoí, nãúu khäng seî coï maìu xanh ;

• Veî caïc doìng læu thãø cáön thiãút S1, S2, S3, S4, S5

• Xong, click laûi vaìo nuït Streams hoàûc nhàõp Esc âãø thoaït khoíi viãûc thiãút láûp caïc doìng læu thãø

8.1.2.5 Xaïc âënh thaình pháön cáúu tæí coï trong hãû :

Nguyãn liãûu bao gäöm caïc paraffine tæì meïthane âãún heptane vaì nitrogen. Táút caí caïc cáúu tæí naìy âãöu âæåüc tçm tháúy tæì ngán haìng dæî liãûu (databanks) phong phuï caïc cáúu tæí cuía PROII



• Click vaìo biãøu tæåüng phán tæí benzeìne âæåüc viãön âoí (dæî liãûu yãu cáöu phaíi nháûp vaìo) trãn thanh cäng cuû âãø choün caïc cáúu tæí (hoàûc click vaìo Input (Menu) ⇒ choün Component Selection)

• Coï thãø nháûp træûc tiãúp vaìo ä Component, hoàûc coï thãø nhàõp choün Select from list ⇒ Hydrocarbon lightents ⇒ Choün cáúu tæí cáön thiãút : N2 ⇒ Add component ⇒ Choün CH4 ⇒ Add component ⇒ C2H6, C3H8, i-C4H10, ... âãún C7H16 ⇒ Sau khi âaî choün xong ⇒ OK

8.1.2.6 Læûa choün caïc phæång trçnh nhiãût âäüng thêch håüp :

• Click vaìo biãøu tæåüng biãøu âäö pha âæåüc viãön âoí (dæî liãûu yãu cáöu phaíi nháûp vaìo) trãn thanh cäng cuû âãø choün caïc mä hçnh nhiãût âäüng thêch håüp (hoàûc click vaìo Input (Menu) ⇒ choün Thermodynamic Data) ⇒ Choün Most Commonly Used tæì Category ⇒ Choün Peng-Robinson tæì Primary Method âãø tênh giaï trë K vaì choün API âãø tênh tè troüng loíng

• Click Add âãø xaïc âënh phæång phaïp tênh nhiãût âäüng PR01 cho hãû ⇒ OK

8.1.2.7 Xaïc âënh thaình pháön, traûng thaïi cuía caïc doìng, xaïc âënh caïc dæî liãûu vãö thiãút bë

• Doìng S1, thiãút bë F1, V1 vaì EX1 âæåüc viãön âoí (dæî liãûu yãu cáöu phaíi nháûp vaìo)

• Choün thiãút bë hoàûc doìng bàòng caïch click choün noï (hoàûc click vaìo Input (Menu) ⇒ choün Data Entry)

a- Doìng S1

• Double click doìng S1 ⇒ ⇒ hiãøn thë baíng Stream Data ⇒ ÅÍ muûc Description baûn coï thãø nháûp tãn FEED (nguyãn liãûu) cho doìng naìy ⇒ click choün Flowrate and Composition ⇒ choün Total Fluid Flowrate ⇒ nháûp vaìo giaï trë 8. Chuï yï, læu læåüng nguyãn liãûu âæåüc tênh bàòng m3/s, maì åí âáy âån vë laì LB-MOL/HR ⇒ click UOM ⇒ xuáút hiãûn baíng Convert Unit of Measure ⇒ choün Vap. Vol ⇒ M3 ⇒ SEC ⇒ nhàõp Change Units

• Nháûp thaình pháön caïc cáúu tæí cuía doìng S1 : Nháûp giaï trë 7.91 cho cáúu tæí 1 ⇒ nhàõp nuït TAB ⇒ nháûp 73.05 cho cáúu tæí 2, ... âãún 0.69 cho cáúu tæí cuäúi cuìng ⇒ nhàõp OK âãø quay laûi cæía säø chênh Stream Data

• xaïc âënh nhiãût âäü vaì aïp suáút cuía doìng S1 åí muûc Thermal Condition : ÅÍ doìng First Specification ⇒ choün Temperature ⇒ nháûp giaï trë -84. Xong nhàõp choün Pressure åí muûc Second Specification ⇒ nháûp giaï trë 587.7 psia (= 602.7 - 10 - 5) ⇒ OK

b- Thiãút bë F1



• Double click vaìo thiãút bë F1 ⇒ nháûp tãn SEPARATOR

• Læu yï : dæî liãûu ä Pressure Drop (tråí læûc) âæåüc viãön xanh ⇒ khäng yãu cáöu nháûp, nãúu chuïng ta khäng nháûp säú liãûu vaìo ä naìy, PROII seî màûc âënh nháûp giaï trë 0

• Click vaìo Unit Specification ⇒ choün Duty (nhiãût læåüng). ÅÍ âáy, giaï trë naìy âæåüc màûc âënh bàòng 0

• Quan saït tháúy khäng coìn vuìng naìo âæåüc viãön âoí ⇒ viãûc nháûp dæî liãûu cho thiãút bë äöan thaình ⇒ OK

• Âãø ghi laûi caïc säú liãûu væìa nháûp vaìo flowsheet âang laìm viãûc ⇒ Tæì File menu ⇒ choün Save As ⇒ nháûp tãn SESSION1 cho chæång trçnh mä phoíng vuìng 1 ⇒ OK

c- Thiãút bë V1

• Double click vaìo thiãút bë F1 ⇒ nháûp tãn VALVE

• Choün Outlet Pressure tæì muûc Operating Parameter ⇒ nháûp giaï trë 125 ⇒ OK

d- Thiãút bë EX1

• Double click vaìo thiãút bë F1 ⇒ nháûp tãn EXPANDER

• Choün Outlet Pressure tæì muûc Pressure and Work Specifications ⇒ nháûp giaï trë 125

• Thay giaï trë màûc âënh 100% cuía Adiabatic Efficiency (hiãûu suáút âoaûn nhiãût) thaình 80% ⇒ OK

⇒ Báy giåì, khäng coï mäüt biãøu tæåüng naìo trãn doìng Toolbar, mäüt thiãút bë hoàûc mäüt doìng naìo âæåüc viãön âoí ⇒ Âiãöu âoï coï nghéa laì táút caí caïc säú liãûu yãu cáöu nháûp vaìo flowsheet âãöu hoaìn toaìn thoaí maîn ⇒ Haîy ghi laûi file bàòng caïch nhàõp vaìo biãøu tæåüng Save

8.1.2.8 Chaûy pháön mãöm mä phoíng

• Click vaìo biãøu tæåüng Run trãn Toolbar

• Sau vaìi giáy, haîy sàón saìng nháûn kãút quaí :

- Nãúu thaình cäng, toaìn bäü dáy chuyãön seî chuyãøn tæì maìu xanh luûc nhaût sang maìu xanh dæång âáûm ⇒ OK

- Nãúu khäng ⇒ toaìn bäü seî chuyãøn thaình maìu âoí

8.1.2.9 Xem kãút quaí mä phoíng

• Click vaìo biãøu tæåüng Generate Report trãn Toolbar

• Kãút quaí cuía quaï trçnh mä phoíng seî tæû âäüng xuáút hiãûn trong cæía säø Programmer’s File Editor nhæ sau:



$ Generated by PRO/II Keyword Generation System <version 7.0> $ Generated on: Wed Aug 10 09:05:47 2005 TITLE DIMENSION ENGLISH, TIME=SEC, VAPVOL=M3 SEQUENCE SIMSCI COMPONENT DATA LIBID 1,N2/2,METHANE/3,ETHANE/4,PROPANE/5,IBUTANE/6,BUTANE/ & 7,IPENTANE/8,PENTANE/9,HEXANE/10,HEPTANE, BANK=PROCESS,SIMSCI THERMODYNAMIC DATA METHOD SYSTEM=PR, SET=PR01, DEFAULT STREAM DATA PROPERTY STREAM=S1, TEMPERATURE=-83.999, PRESSURE=587.7, PHASE=M, & RATE(GV)=8, COMPOSITION(M)=1,7.91/2,73.05/3,7.68/4,5.69/ & 5,0.99/6,2.44/7,0.69/8,0.82/9,0.42/10,0.31 NAME S1,FEED UNIT OPERATIONS FLASH UID=F1, NAME=SEPARATOR FEED S1 PRODUCT V=S2, W=S3 ADIABATIC VALVE UID=V1, NAME=VALVE FEED S3 PRODUCT M=S5 OPERATION PRESSURE=125 EXPANDER UID=EX1, NAME=EXPANDER FEED S2 PRODUCT V=S4 OPERATION PRES=125, EFF=80 END



SIMULATION SCIENCES INC. R PAGE H-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM CALCULATION HISTORY 08/10/05 ========================================================================= *** PROBLEM SOLUTION BEGINS FEED FLASH COMPLETE UNIT 1 SOLVED - 'F1 ' UNIT 3 SOLVED - 'V1 ' UNIT 2 SOLVED - 'EX1 ' *** PROBLEM SOLUTION REACHED *** THIS RUN USED 12.74 PRO/II SIMULATION UNITS *** RUN STATISTICS STARTED 09:05:28 08/10/05 NO ERRORS FINISHED 09:05:28 08/10/05 NO WARNINGS RUN TIMES NO MESSAGES INTERACTIVE 0 MIN, 0.00 SEC CALCULATIONS 0 MIN, 0.13 SEC TOTAL 0 MIN, 0.13 SEC



SIMULATION SCIENCES INC. R PAGE I-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT INDEX 08/10/05 ============================================================================== PAGE CONTENTS ------ ---------------------------------------------------------------- 1 COMPONENT DATA 2 CALCULATION SEQUENCE AND RECYCLES 3 FLASH DRUM SUMMARY 4 VALVE SUMMARY EXPANDER SUMMARY 5 UNIT 2, 'EX1', 'EXPANDER' 6 STREAM MOLAR COMPONENT RATES 7 STREAM SUMMARY



SIMULATION SCIENCES INC. R PAGE P-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COMPONENT DATA 08/10/05 ========================================================================= COMPONENT COMP. TYPE PHASE MOL. WEIGHT API --------------------- ----------- ----------- ----------- ----------- 1 N2 LIBRARY VAP/LIQ 28.013 43.600 2 METHANE LIBRARY VAP/LIQ 16.043 340.167 3 ETHANE LIBRARY VAP/LIQ 30.070 265.526 4 PROPANE LIBRARY VAP/LIQ 44.097 147.208 5 IBUTANE LIBRARY VAP/LIQ 58.124 119.788 6 BUTANE LIBRARY VAP/LIQ 58.124 110.629 7 IPENTANE LIBRARY VAP/LIQ 72.151 95.727 8 PENTANE LIBRARY VAP/LIQ 72.151 92.747 9 HEXANE LIBRARY VAP/LIQ 86.178 81.602 10 HEPTANE LIBRARY VAP/LIQ 100.206 74.109 COMPONENT NBP CRIT. TEMP. CRIT. PRES. CRIT. VOLM. F F PSIA FT3/LB-MOL --------------------- ----------- ----------- ----------- ----------- 1 N2 -320.440 -232.420 492.314 1.4433 2 METHANE -258.682 -116.680 667.195 1.5858 3 ETHANE -127.534 90.140 708.344 2.3707 4 PROPANE -43.726 206.006 616.348 3.2518 5 IBUTANE 10.886 274.964 529.054 4.2129 6 BUTANE 31.100 305.600 551.098 4.0847 7 IPENTANE 82.130 369.032 490.403 4.9017 8 PENTANE 96.933 385.700 488.641 4.8696 9 HEXANE 155.732 453.560 430.591 5.9268 10 HEPTANE 209.174 512.600 396.790 6.9200 COMPONENT ACEN. FACT. HEAT FORM. G FORM. BTU/LB-MOL BTU/LB-MOL --------------------- ----------- ----------- ----------- 1 N2 0.04500 0.00 0.00 2 METHANE 0.01040 -32066.21 -21726.14 3 ETHANE 0.09860 -36120.21 -13810.45 4 PROPANE 0.15290 -44650.04 -10139.64 5 IBUTANE 0.17720 -57870.16 -9121.45 6 BUTANE 0.20130 -54072.23 -7169.22 7 IPENTANE 0.22900 -66411.44 -6372.53 8 PENTANE 0.25060 -62968.62 -3672.87 9 HEXANE 0.29430 -71771.28 -34.39 10 HEPTANE 0.34990 -80693.47 3477.00



SIMULATION SCIENCES INC. R PAGE P-2 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT CALCULATION SEQUENCE AND RECYCLES 08/10/05 ========================================================================= CALCULATION SEQUENCE SEQ UNIT ID UNIT TYPE --- ------------ ---------- 1 F1 FLASH 2 V1 VALVE 3 EX1 EXPANDER



SIMULATION SCIENCES INC. R PAGE P-3 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT FLASH DRUM SUMMARY 08/10/05 ========================================================================= FLASH ID F1 NAME SEPARATOR FEEDS S1 PRODUCTS VAPOR S2 LIQUID S3 TEMPERATURE, F -84.000 PRESSURE, PSIA 587.700 PRESSURE DROP, PSI 0.000 MOLE FRAC VAPOR 0.67532 MOLE FRAC LIQUID 0.32468 DUTY, MM BTU/SEC 0.00000 FLASH TYPE ADIABATIC-P



SIMULATION SCIENCES INC. R PAGE P-4 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT VALVE SUMMARY 08/10/05 ========================================================================= VALVE ID V1 NAME VALVE FEEDS S3 PRODUCTS MIXED S5 TEMPERATURE, F -136.293 PRESSURE, PSIA 125.000 PRESSURE DROP, PSI 462.700 MOLE FRAC VAPOR 0.35862 MOLE FRAC LIQUID 0.64138



SIMULATION SCIENCES INC. R PAGE P-5 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT EXPANDER SUMMARY 08/10/05 ========================================================================= UNIT 2, 'EX1', 'EXPANDER' Feeds S2 Products Mixed S4 OPERATING CONDITIONS INLET ISENTROPIC OUTLET ----------- ----------- ----------- TEMPERATURE, F -84.00 -185.87 -179.53 PRESSURE, PSIA 587.70 125.00 125.00 ENTHALPY, MM BTU/SEC -0.0002 -0.0005 -0.0005 ENTROPY, BTU/LB-MOL-F 39.2708 39.2708 39.8039 MOLE PERCENT VAPOR 100.0000 90.8080 93.4667 MOLE PERCENT LIQUID 0.0000 9.1920 6.5333 ACT VAP RATE, M FT3/MIN 0.1473 ADIABATIC EFF, PERCENT 80.00 WORK, HP THEORETICAL 524.81 ACTUAL 419.85



SIMULATION SCIENCES INC. R PAGE P-6 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM MOLAR COMPONENT RATES 08/10/05 ========================================================================= STREAM ID S1 S2 S3 S4 NAME FEED PHASE MIXED VAPOR LIQUID MIXED FLUID RATES, LB-MOL/SEC 1 N2 0.0589 0.0552 3.6693E-03 0.0552 2 METHANE 0.5438 0.4280 0.1159 0.4280 3 ETHANE 0.0572 0.0159 0.0413 0.0159 4 PROPANE 0.0424 3.1439E-03 0.0392 3.1439E-03 5 IBUTANE 7.3703E-03 1.8398E-04 7.1864E-03 1.8398E-04 6 BUTANE 0.0182 2.9577E-04 0.0179 2.9577E-04 7 IPENTANE 5.1369E-03 2.5434E-05 5.1115E-03 2.5434E-05 8 PENTANE 6.1047E-03 2.5738E-05 6.0790E-03 2.5738E-05 9 HEXANE 3.1268E-03 2.5617E-06 3.1242E-03 2.5617E-06 10 HEPTANE 2.3079E-03 4.6998E-07 2.3074E-03 4.6998E-07 TOTAL RATE, LB-MOL/SEC 0.7445 0.5028 0.2417 0.5028 TEMPERATURE, F -84.0000 -84.0000 -84.0000 -179.5267 PRESSURE, PSIA 587.7000 587.7000 587.7000 125.0000 ENTHALPY, MM BTU/SEC -7.7696E-04 -1.7329E-04 -6.0367E-04 -4.7003E-04 MOLECULAR WEIGHT 22.5095 18.0233 31.8404 18.0233 MOLE FRAC VAPOR 0.6753 1.0000 0.0000 0.9347 MOLE FRAC LIQUID 0.3247 0.0000 1.0000 0.0653 STREAM ID S5 NAME PHASE MIXED FLUID RATES, LB-MOL/SEC 1 N2 3.6693E-03 2 METHANE 0.1159 3 ETHANE 0.0413 4 PROPANE 0.0392 5 IBUTANE 7.1864E-03 6 BUTANE 0.0179 7 IPENTANE 5.1115E-03 8 PENTANE 6.0790E-03 9 HEXANE 3.1242E-03 10 HEPTANE 2.3074E-03 TOTAL RATE, LB-MOL/SEC 0.2417 TEMPERATURE, F -136.2925 PRESSURE, PSIA 125.0000 ENTHALPY, MM BTU/SEC -6.0367E-04 MOLECULAR WEIGHT 31.8404 MOLE FRAC VAPOR 0.3586 MOLE FRAC LIQUID 0.6414



SIMULATION SCIENCES INC. R PAGE P-7 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 08/10/05 ========================================================================= STREAM ID S1 S2 S3 S4 NAME FEED PHASE MIXED VAPOR LIQUID MIXED ----- TOTAL STREAM ----- RATE, LB-MOL/SEC 0.744 0.503 0.242 0.503 M LB/SEC 1.676E-02 9.061E-03 7.696E-03 9.061E-03 STD LIQ RATE, FT3/SEC 0.709 0.424 0.285 0.424 TEMPERATURE, F -84.000 -84.000 -84.000 -179.527 PRESSURE, PSIA 587.700 587.700 587.700 125.000 MOLECULAR WEIGHT 22.509 18.023 31.840 18.023 ENTHALPY, MM BTU/SEC -7.770E-04 -1.733E-04 -6.037E-04 -4.700E-04 BTU/LB -46.364 -19.124 -78.436 -51.872 MOLE FRACTION LIQUID 0.3247 0.0000 1.0000 0.0653 REDUCED TEMP (KAYS RULE) 0.9533 1.1072 0.7395 0.8257 PRES (KAYS RULE) 0.9113 0.9058 0.9230 0.1927 ACENTRIC FACTOR 0.0401 0.0181 0.0857 0.0181 WATSON K (UOPK) 16.647 17.187 16.010 17.187 STD LIQ DENSITY, LB/FT3 23.629 21.350 27.026 21.350 SPECIFIC GRAVITY 0.3789 0.3423 0.4333 0.3423 API GRAVITY 241.971 281.844 195.026 281.844 -------- VAPOR --------- RATE, LB-MOL/SEC 0.503 0.503 N/A 0.470 M LB/SEC 9.061E-03 9.061E-03 N/A 8.262E-03 M M3/SEC 6.953E-05 6.953E-05 N/A 2.810E-04 STD VAP RATE(1), M M3/SEC 5.403E-03 5.403E-03 N/A 5.050E-03 SPECIFIC GRAVITY (AIR=1.0) 0.622 0.622 N/A 0.607 MOLECULAR WEIGHT 18.023 18.023 N/A 17.582 ENTHALPY, BTU/LB -19.124 -19.124 N/A -41.746 CP, BTU/LB-F 0.709 0.709 N/A 0.503 DENSITY, LB/M M3 130315.717 130315.717 N/A 29399.106 Z (FROM DENSITY) 0.7120 0.7120 N/A 0.8781 -------- LIQUID -------- RATE, LB-MOL/SEC 0.242 N/A 0.242 3.285E-02 M LB/SEC 7.696E-03 N/A 7.696E-03 7.996E-04 FT3/SEC 0.174 N/A 0.174 1.996E-02 GAL/MIN 78.017 N/A 78.017 8.958 STD LIQ RATE, FT3/SEC 0.285 N/A 0.285 3.582E-02 SPECIFIC GRAVITY (H2O=1.0) 0.4333 N/A 0.4333 0.3579 MOLECULAR WEIGHT 31.840 N/A 31.840 24.343 ENTHALPY, BTU/LB -78.436 N/A -78.436 -156.500 CP, BTU/LB-F 0.597 N/A 0.597 0.622 DENSITY, LB/FT3 44.277 N/A 44.277 40.060 Z (FROM DENSITY) 0.1048 N/A 0.1048 0.0253 (1) STANDARD VAPOR VOLUME IS 379.49 FT3/LB-MOLE (60 F AND 14.696 PSIA)



SIMULATION SCIENCES INC. R PAGE P-8 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 08/10/05 ============================================================================== STREAM ID S5 NAME PHASE MIXED ----- TOTAL STREAM ----- RATE, LB-MOL/SEC 0.242 M LB/SEC 7.696E-03 STD LIQ RATE, FT3/SEC 0.285 TEMPERATURE, F -136.293 PRESSURE, PSIA 125.000 MOLECULAR WEIGHT 31.840 ENTHALPY, MM BTU/SEC -6.037E-04 BTU/LB -78.436 MOLE FRACTION LIQUID 0.6414 REDUCED TEMP (KAYS RULE) 0.6365 PRES (KAYS RULE) 0.1963 ACENTRIC FACTOR 0.0857 WATSON K (UOPK) 16.010 STD LIQ DENSITY, LB/FT3 27.026 SPECIFIC GRAVITY 0.4333 API GRAVITY 195.026 -------- VAPOR --------- RATE, LB-MOL/SEC 8.669E-02 M LB/SEC 1.473E-03 M M3/SEC 6.205E-05 STD VAP RATE(1), M M3/SEC 9.315E-04 SPECIFIC GRAVITY (AIR=1.0) 0.587 MOLECULAR WEIGHT 16.994 ENTHALPY, BTU/LB -8.985 CP, BTU/LB-F 0.511 DENSITY, LB/M M3 23741.035 Z (FROM DENSITY) 0.9105 -------- LIQUID -------- RATE, LB-MOL/SEC 0.155 M LB/SEC 6.223E-03 FT3/SEC 0.151 GAL/MIN 67.936 STD LIQ RATE, FT3/SEC 0.210 SPECIFIC GRAVITY (H2O=1.0) 0.4748 MOLECULAR WEIGHT 40.142 ENTHALPY, BTU/LB -94.877 CP, BTU/LB-F 0.479 DENSITY, LB/FT3 41.114 Z (FROM DENSITY) 0.0352



(1) STANDARD VAPOR VOLUME IS 379.49 FT3/LB-MOLE (60 F AND 14.696 PSIA)Mä phoíng vuìng 2

8.1.2.10 Xáy dæûng flowsheet cho toaìn bäü quaï trçnh (required)

Chuïng ta seî xáy dæûng mäüt flowsheet cho toaìn bäü quaï trçnh trãn cå såí flowsheet cuía vuìng 1 theo caïc bæåïc sau :

• Tæì File menu ⇒ Open ⇒ Choün file SESSION1.PRZ

• PRO/II seî ghi tiãúp tuûc caïc dæî liãûu måïi vaìo file naìy ⇒ nghéa laì trong SESSION1.PRZ chuïng ta seî duìng cäng cuû floating PFD âãø làõp âàût thãm 2 thiãút bë trao âäøi nhiãût E1 vaì E2, 1 maïy neïn C1 vaì 1 thaïp chæng cáút T1 vaìo så âäö

• Chuï yï : Khi muäún làõp âàût nhiãöu thiãút bë cuìng loaûi vaìo så âäö (Vê duû 2 thiãút bë trao âäøi nhiãût) ⇒ click vaìo thiãút bë mong muäún trãn thanh cäng cuû PFD ⇒ nháún giæî nuït Shift ⇒ click vaìo caïc vë trê muäún âàût thiãút bë trong så âäö

• Khi choün biãøu tæåüng thaïp chæng cáút trãn cäng cuû PFD ⇒ seî xuáút hiãûn mäüt cæía säø yãu cáöu nháûp säú âéa (lyï thuyãút) ⇒ Haîy choün mäüt thaïp 10 âéa kãø caí thiãút bë âun säi laûi (laì mäüt âéa) vaì khäng coï thiãút bë ngæng tuû âènh thaïp

• Chuï yï : PRO/II coï thãø måí nhiãöu viewport cho cuìng mäüt baìi toaïn mä phoíng, cho pheïp chuïng ta quan saït så âäö åí nhiãöu goïc âäü khaïc nhau. Muäún váûy, coï nhiãöu caïch :

- Tæì Window menu ⇒ choün New View ⇒ taûo View 2

- Click vaìo biãøu tæåüng New View trãn Standard Tool Bar ⇒ taûo View 2

- Tæì Window menu ⇒ choün Tile Horizontally ⇒ taûo 2 Viewport theo chiãöu ngang

- Tæì Window menu ⇒ choün Tile Vertically ⇒ taûo 2 Viewport theo chiãöu doüc

• Biãøu tæåüng Zoom Full : cho pheïp quan saït toaìn bäü så âäö trãn toaìn maìn hçnh

• Biãøu tæåüng Zoom In : cho pheïp quan saït mäüt pháön så âäö âæåüc choün trãn toaìn maìn hçnh

• Click vaìo biãøu tæåüng Streams trãn thanh cäng cuû PFD vaì xáy dæûng caïc doìng sau :

- Doìng (håi) âi ra tæì âènh cuía thaïp Demethaniser vaì vaìo thiãút bë trao âäøi nhiãût E1

- Doìng âi ra tæì thiãút bë trao âäøi nhiãût E1 vaìo maïy neïn C1

- Doìng saín pháøm âi ra khoíi maïy neïn C1

- Doìng âi ra tæì thiãút bë trao âäøi nhiãût E1 vaìo thiãút bë trao âäøi nhiãût E2

- Doìng saín pháøm âi ra khoíi thiãút bë trao âäøi nhiãût E2



- Doìng saín pháøm ra tæì thiãút bë âun säi laûi cuía thaïp

• Chuïng ta nháûn tháúy ràòng : thaình pháön cuía doìng nguyãn liãûu vaìo thiãút bë trao âäøi nhiãût khê - khê E1 (gas-gas heat exchanger) chênh laì thaình pháön cuía doìng khê nguyãn liãûu vaìo thiãút bë taïch F1. Âãø traïnh viãûc nháûp dæî liãûu làûp laûi vaìo caïc doìng, ta seî tiãún haình näúi laûi caïc doìng theo âuïng så âäö (I-1) nhæ sau :

- Rã chuäüt âãún âáöu muîi tãn cuía doìng S1 ⇒ Nhàõp chuäüt traïi vaì giæî nguyãn, rã âãún âáöu vaìo cuía thiãút bë E1 ⇒ Buäng chuäüt ra ⇒ Báy giåì doìng nguyãn liãûu S1 seî âi vaìo thiãút bë E1

- Tiãún haình tæång tæû ⇒ Âæa doìng S10 âi ra tæì E2 âãún vaìo thiãút bë F1

- Doìng S4 vaìo âéa 1 cuía thaïp Demethaniser, doìng S5 vaìo âéa 3 cuía thaïp Demethaniser. Chuïng ta âaî hoaìn thaình viãûc thiãút láûp toaìn bäü så âäö nhæ sau:

• Chuï yï : Trãn så âäö, khäng coï doìng naìo âæåüc viãön âoí ⇒ Træåïc khi tiãún haình mä phoíng, chè coìn viãûc thay âäøi nhiãût âäü vaì aïp suáút cuía doìng S1 vaì nháûp dæî liãûu cho caïc thiãút bë âæåüc viãön âoí : E1, E2, C1 vaì T1



8.1.2.11 Thay âäøi nhiãût âäü vaì aïp suáút cuía doìng S1 (required)

Tiãún haình thay âäøi nhiãût âäü cuía doìng S1 tæì -84oF âãún 120oF vaì aïp suáút tæì 587.7 psia thaình 602.7 psia nhæ sau :

• Double-click doìng S1 ⇒ xuáút hiãûn cæía säø Stream Data

• Thay âäøi nhiãût âäü tæì -84oF thaình 120oF

• Thay âäøi aïp suáút tæì 587.7 psia thaình 602.7 psia

8.1.2.12 Nháûp dæî liãûu cho E1 (required)

• Thiãút bë naìy yãu cáöu âäü chãnh nhiãût âäü giæîa læu thãø noïng vaìo vaì læu thãø laûnh ra laì 10 oF vaì tråí læûc phêa læu thãø noïng laì 10 psi vaì tråí læûc phêa læu thãø laûnh laì 5 psi

• Double-click E1 ⇒ xuáút hiãûn cæía säø Heat Exchanger

• ÅÍ muûc Description nháûp tãn GAS-GASS HX

• Click vaìo muûc Process Stream âãø xaïc âënh doìng noïng vaì doìng laûnh cho thiãút bë ⇒ xuáút hiãûn cæía säø Heat Exchanger- Process Stream ⇒ click vaìo muûc Hot hoàûc Cold tæång æïng våïi caïc doìng ⇒ OK âãø vãö laûi cæía säø Heat Exchanger

• Choün Specification ⇒ xuáút hiãûn cæía säø Heat Exchanger-Specifications ⇒ choün Hot Inlet-Cold Outlet Temperature Approach vaì nháûp giaï trë 10oF ⇒ OK âãø vãö laûi cæía säø Heat Exchanger

• ÅÍ muûc Pressure Drop (tråí læûc) : nháûp giaï trë 10 psi cho Hot Side vaì 5 psi cho Cold Side ⇒ OK ⇒ hoaìn thaình viãûc nháûp dæî liãûu cho E1

8.1.2.13 Nháûp dæî liãûu cho E2 (required)

• Thiãút bë naìy yãu cáöu laìm laûnh doìng S9 xuäúng nhiãût âäü laì -84oF vaì tråí læûc phêa læu thãø noïng laì 5 psi

• Double-click E2 ⇒ xuáút hiãûn cæía säø Heat Exchanger

• ÅÍ muûc Description nháûp tãn CHILLER

• Choün Specification ⇒ xuáút hiãûn cæía säø Heat Exchanger-Specifications ⇒ choün Hot Product Temperature vaì nháûp giaï trë -84oF ⇒ OK âãø vãö laûi cæía säø Heat Exchanger

• ÅÍ muûc Pressure Drop (tråí læûc) : nháûp giaï trë 5 psi cho Hot Side ⇒ OK ⇒ hoaìn thaình viãûc nháûp dæî liãûu cho E2

8.1.2.14 Nháûp dæî liãûu cho C1 (required)

• Double-click vaìo C1 ⇒ xuáút hiãûn cæía säø Compressor

• ÅÍ muûc Description nháûp tãn COMPRESSOR



• Nháûp giaï trë 75% cho muûc Efficiency or Temperature Specification

• Chuï yï ràòng cäng suáút cuía maïy neïn C1 seî âæåüc cung cáúp båíi cäng suáút thu âæåüc tæì expander EX1 nãn seî chênh bàòng cäng suáút cuía EX1

• Choün Work tæì muûc Pressure, Work or Head Specification

• Click choün muûc Define åí doìng Toolbar ⇒ xuáút hiãûn cæía säø Definition ⇒ click choün muûc Set Up Definition for Compressor Work ⇒ click choün thäng säú Parameter âæåüc viãön âoí ⇒ xuáút hiãûn cæía säø Parameter

• Click choün thiãút bë Expander EX1 tæì muûc Constant/Stream/Unit

• click choün Parameter âæåüc viãön âoí ⇒ xuáút hiãûn cæía säø Parameter Selection ⇒ choün Actual Work ⇒ OK âãø tråí vãö cæía säø Parameter

• OK ⇒ tråí vãö cæía säø Definition ⇒ OK tråí vãö cæía säø Compressor ⇒ OK ⇒ nháûp xong dæî liãûu cho C1

8.1.2.15 Nháûp dæî liãûu cho T1

• Double-click vaìo C1 ⇒ xuáút hiãûn cæía säø Column

• ÅÍ muûc Description nháûp tãn TOWER

• Nhàõp choün vaìo ä thæï hai âæåüc viãön âoí Feeds and Products ⇒ xuáút hiãûn cæía säø Column - Feeds and Products ⇒ ÅÍ baíng trãn, xaïc âënh doìng S4 âæåüc naûp vaìo âéa 1 vaì S5 âæåüc naûp vaìo âéa 3 : nháûp giaï trë 1 tæång æïng våïi doìng S4 ⇒ Tab ⇒ nháûp giaï trë 3 tæång æïng våïi doìng S5 ⇒ ÅÍ baíng dæåïi, nháûp giaï trë læu læåüng 500 lbmol/hr cho doìng håi saín pháøm âènh S6 ra tæì âéa 1 (1 libra = 1 pound = 453,6 g)

• ÅÍ muûc Feed Flash Convention : coï 2 læûa choün :

- Vapor and liquid to be the feed tray : âæåüc màûc âënh

- Flash the feed adiabatically, vapor onto the tray above and liquid onto the feed tray : læûa choün naìy chè âæåüc choün khi naûp liãûu åí âéa cuäúi cuìng åí âaïy thaïp

• Nhàõp choün vaìo ä thæï nháút âæåüc viãön âoí Pressure Profile ⇒ xuáút hiãûn cæía säø Column - Pressure Profile ⇒ Nháûp giaï trë 125 psia laì aïp suáút åí âéa trãn cuìng cuía thaïp åí muûc Overall Specification ⇒ OK âãø tråí vãö cæía säø Column

• Chuï yï ràòng : yãu cáöu cháút læåüng cuía saín pháøm âaïy laì tè lãû C1/C2 = 0.015

• ÅÍ muûc Performance Specification ⇒

- Nhàõp choün ⇒ xuáút hiãûn cæía säø Column - Specifications and Variables ⇒ click vaìo ä choün Add Specifications and Variables ⇒ click vaìo parameter (chæî âoí vaì gaûch dæåïi âoí) trong muûc Specifications ⇒ xuáút hiãûn cæía säø



Parameter ⇒ choün Stream åí muûc Stream/Unit vaì choün doìng S11 åí muûc Stream Name laì doìng saín pháøm âaïy cuía thaïp

- Click vaìo Parameter (chæî tràõng trãn nãön âoí) ⇒ xuáút hiãûn cæía säø Parameter selection ⇒ choün Flowrate åí muûc Parameter ⇒ choün Selected Components åí muûc Flowrate ⇒ choün METHANE laì cáúu tæí âáöu vaì cáúu tæí cuäúi ⇒ OK âãø tråí vãö cæía säø Parameter ⇒ OK : hoaìn thaình cæía säø Parameter ⇒ tråí vãö cæía säø Column - Specifications and Variables

- ÅÍ muûc Specifications ⇒ nhàõp vaìo dáúu ‘= ‘ træåïc chæî Value maìu âoí ⇒ xuáút hiãûn caïc læûa choün +, -, /, * Parameter ⇒ choün ‘/ ‘

- Tiãúp tuûc nhàõp choün Parameter maìu âoí cuîng åí muûc Specifications ⇒ xuáút hiãûn cæía säø Parameter ⇒ choün Stream åí muûc Stream/Unit vaì choün doìng S11 åí muûc Stream Name ⇒ Click vaìo Parameter (chæî tràõng trãn nãön âoí) ⇒ xuáút hiãûn cæía säø Parameter selection ⇒ choün Flowrate åí muûc Parameter ⇒ choün Selected Components åí muûc Flowrate ⇒ choün ETHANE laì cáúu tæí âáöu vaì cáúu tæí cuäúi ⇒ OK âãø tråí vãö cæía säø Parameter ⇒ OK : hoaìn thaình cæía säø Parameter ⇒ tråí vãö cæía säø Column - Specifications and Variables

- click vaìo Value ⇒ nháûp giaï trë 0.015

- click vaìo parameter (chæî âoí vaì gaûch dæåïi âoí) trong muûc Variables ⇒ xuáút hiãûn cæía säø Parameter Selection ⇒ Choün Heat Duty (nàng suáút nhiãût) ⇒ ÅÍ muûc Heater seî xuáút hiãûn REBOILER ⇒ OK : quay laûi cæía säø Variables ⇒ OK : quay laûi cæía säø Column - Specifications and Variables ⇒ OK : hoaìn thaình viãûc nháûp dæî liãûu cho T1

• ÅÍ muûc Condenser : choün daûng Bubble

• ÅÍ muûc Reboiler : Choün daûng Kettle : âæåüc màûc âënh (qui chuáøn)

8.1.2.16 Tiãún haình mä phoíng (required) va ì xem kãút quaí mä phoíng

• Click vaìo biãøu tæåüng Run trãn Toolbar. Sau vaìi giáy, toaìn bäü dáy chuyãön seî chuyãøn tæì maìu xanh luûc nhaût sang maìu xanh dæång âáûm ⇒ OK

• Click vaìo biãøu tæåüng Generate Report trãn Toolbar

• Kãút quaí cuía quaï trçnh mä phoíng seî tæû âäüng xuáút hiãûn trong cæía säø Programmer’s File Editor våïi tãn file laì SESSION2.OUT nhæ sau:



$ Generated by PRO/II Keyword Generation System <version 7.0> $ Generated on: Fri Jul 29 17:16:30 2005 TITLE PRINT INPUT=REFP, STREAM=ALL, RATE=M, ION=NONE DIMENSION ENGLISH, TIME=SEC, VAPVOL=M3 SEQUENCE SIMSCI COMPONENT DATA LIBID 1,N2/2,METHANE/3,ETHANE/4,PROPANE/5,BUTANE/6,IBUTANE/ & 7,IPENTANE/8,PENTANE/9,HEXANE/10,HEPTANE, BANK=PROCESS,SIMSCI THERMODYNAMIC DATA METHOD SYSTEM=PR, SET=PR01, DEFAULT STREAM DATA PROPERTY STREAM=S1, TEMPERATURE=120, PRESSURE=602.7, PHASE=M, & RATE(GV)=8, COMPOSITION(M)=1,7.91/2,73.05/3,7.68/4,5.69/ & 5,2.44/6,0.99/7,0.69/8,0.82/9,0.42/10,0.31 UNIT OPERATIONS HX UID=E1 HOT FEED=S1, M=S6, DP=10 COLD FEED=S8, M=S9, DP=5 CONFIGURE COUNTER OPER HICO=10 HX UID=E2 HOT FEED=S6, M=S7, DP=5 OPER HTEMP=-83.999 FLASH UID=F1 FEED S7 PRODUCT V=S2, W=S3 ADIABATIC EXPANDER UID=EX1 FEED S2 PRODUCT V=S4 OPERATION PRES=139.7, EFF=80 VALVE UID=V1 FEED S3 PRODUCT M=S5 OPERATION PRESSURE=125 COLUMN UID=T1 PARAMETER TRAY=10,IO FEED S4,1/S5,3 PRODUCT OVHD(M)=S8,0.61703, BTMS(M)=S11 DUTY 1,10,,REBOILER PSPEC PTOP=125 PRINT PROPTABLE=PART SPEC STREAM=S11, RATE(LBM/H), COMP=2,WET, DIVIDE, STREAM=S11, & RATE(LBM/S), COMP=3,WET, VALUE=0.015 VARY DUTY=1 REBOILER TYPE=KETTLE COMPRESSOR UID=C1 FEED S9 PRODUCT V=S10 OPERATION CALCULATION=ASME, EFF=75 DEFINE WORK(HP) AS EXPANDER=EX1, WORK(HP) END



SIMULATION SCIENCES INC. R PAGE H-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM CALCULATION HISTORY 07/29/05 ============================================================================== *** PROBLEM SOLUTION BEGINS FEED FLASH COMPLETE Loop 1 BEGINS - 'LOOP1 ' UNIT 4 SOLVED - 'E1 ' UNIT 5 SOLVED - 'E2 ' UNIT 1 SOLVED - 'F1 ' UNIT 3 SOLVED - 'EX1 ' UNIT 2 SOLVED - 'V1 ' INNER 0 : E(ENTH+SPEC) = 1.199E-01 CALCULATING NEW MATRIX INNER 1 : E(ENTH+SPEC) = 3.419E-02 ALPHA = 1.0000 INNER 2 : E(ENTH+SPEC) = 1.792E-02 ALPHA = 1.0000 INNER 3 : E(ENTH+SPEC) = 1.094E-02 ALPHA = 1.0000 INNER 4 : E(ENTH+SPEC) = 5.204E-03 ALPHA = 1.0000 ITER 1 E(K) = 3.341E-01 E(ENTH+SPEC) = 5.204E-03 E(SUM) = 5.032E-01 DAMP = 1.000E+00 INNER 0 : E(ENTH+SPEC) = 8.921E-02 INNER 1 : E(ENTH+SPEC) = 3.142E-02 ALPHA = 1.0000 INNER 2 : E(ENTH+SPEC) = 1.191E-02 ALPHA = 1.0000 INNER 3 : E(ENTH+SPEC) = 6.228E-03 ALPHA = 1.0000 INNER 4 : E(ENTH+SPEC) = 3.958E-03 ALPHA = 1.0000 INNER 5 : E(ENTH+SPEC) = 2.226E-03 ALPHA = 1.0000 INNER 6 : E(ENTH+SPEC) = 1.198E-03 ALPHA = 1.0000 INNER 7 : E(ENTH+SPEC) = 1.647E-04 ALPHA = 1.0000 ITER 2 E(K) = 2.624E-01 E(ENTH+SPEC) = 1.647E-04 E(SUM) = 2.944E-01 DAMP = 1.000E+00 INNER 0 : E(ENTH+SPEC) = 1.747E-02 INNER 1 : E(ENTH+SPEC) = 5.165E-03 ALPHA = 1.0000 INNER 2 : E(ENTH+SPEC) = 1.897E-03 ALPHA = 1.0000 INNER 3 : E(ENTH+SPEC) = 1.923E-04 ALPHA = 1.0000 INNER 4 : E(ENTH+SPEC) = 1.529E-05 ALPHA = 1.0000 ITER 3 E(K) = 6.510E-02 E(ENTH+SPEC) = 1.529E-05 E(SUM) = 5.026E-02 DAMP = 1.000E+00 INNER 0 : E(ENTH+SPEC) = 2.025E-03 INNER 1 : E(ENTH+SPEC) = 1.309E-03 ALPHA = 1.0000 INNER 2 : E(ENTH+SPEC) = 1.587E-04 ALPHA = 1.0000 INNER 3 : E(ENTH+SPEC) = 3.035E-05 ALPHA = 1.0000 INNER 4 : E(ENTH+SPEC) = 4.536E-06 ALPHA = 1.0000 ITER 4 E(K) = 9.692E-03 E(ENTH+SPEC) = 4.536E-06 E(SUM) = 1.653E-02 DAMP = 1.000E+00 INNER 0 : E(ENTH+SPEC) = 3.218E-04 INNER 1 : E(ENTH+SPEC) = 1.346E-04 ALPHA = 1.0000 INNER 2 : E(ENTH+SPEC) = 4.222E-05 ALPHA = 1.0000 INNER 3 : E(ENTH+SPEC) = 8.643E-06 ALPHA = 1.0000 ITER 5 E(K) = 1.797E-03 E(ENTH+SPEC) = 8.643E-06 E(SUM) = 1.637E-03 DAMP = 1.000E+00 INNER 0 : E(ENTH+SPEC) = 9.981E-05 INNER 1 : E(ENTH+SPEC) = 1.655E-05 ALPHA = 1.0000 ITER 6 E(K) = 1.194E-03 E(ENTH+SPEC) = 1.655E-05 E(SUM) = 6.014E-04 DAMP = 1.000E+00 INNER 0 : E(ENTH+SPEC) = 3.066E-05 INNER 1 : E(ENTH+SPEC) = 6.049E-06 ALPHA = 1.0000 ITER 7 E(K) = 0.000E+00 E(ENTH+SPEC) = 6.049E-06 E(SUM) = 9.042E-05



SIMULATION SCIENCES INC. R PAGE H-2 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM CALCULATION HISTORY 07/29/05 ============================================================================== UNIT 7 SOLVED - 'T1 ' MAX ERRORS: X=4.25E-6 (S9) T=-.000403 (S6) P=0. Loop 1 SOLVED after 1 trials UNIT 6 SOLVED - 'C1 ' *** PROBLEM SOLUTION REACHED *** THIS RUN USED 133.88 PRO/II SIMULATION UNITS *** RUN STATISTICS STARTED 17:16:18 07/29/05 NO ERRORS FINISHED 17:16:18 07/29/05 NO WARNINGS RUN TIMES NO MESSAGES INTERACTIVE 0 MIN, 0.00 SEC CALCULATIONS 0 MIN, 0.21 SEC TOTAL 0 MIN, 0.21 SEC



SIMULATION SCIENCES INC. R PAGE I-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT INDEX 07/29/05 ============================================================================== PAGE CONTENTS ------ ---------------------------------------------------------------- 1 FLASH DRUM SUMMARY 2 VALVE SUMMARY EXPANDER SUMMARY 3 UNIT 3, 'EX1' COMPRESSOR SUMMARY 4 UNIT 6, 'C1' HEAT EXCHANGER SUMMARY 5 UNIT 4, 'E1' 6 UNIT 5, 'E2' COLUMN SUMMARY 7 UNIT 7, 'T1' 8 TRAY RATES AND DENSITIES 9 STREAM MOLAR COMPONENT RATES 11 STREAM SUMMARY



SIMULATION SCIENCES INC. R PAGE P-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT FLASH DRUM SUMMARY 07/29/05 ============================================================================== FLASH ID F1 NAME FEEDS S7 PRODUCTS VAPOR S2 LIQUID S3 TEMPERATURE, F -84.000 PRESSURE, PSIA 587.700 PRESSURE DROP, PSI 0.000 MOLE FRAC VAPOR 0.67532 MOLE FRAC LIQUID 0.32468 DUTY, MM BTU/SEC 0.00000 FLASH TYPE ADIABATIC-P



SIMULATION SCIENCES INC. R PAGE P-2 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT VALVE SUMMARY 07/29/05 ============================================================================== VALVE ID V1 NAME FEEDS S3 PRODUCTS MIXED S5 TEMPERATURE, F -136.293 PRESSURE, PSIA 125.000 PRESSURE DROP, PSI 462.700 MOLE FRAC VAPOR 0.35862 MOLE FRAC LIQUID 0.64138



SIMULATION SCIENCES INC. R PAGE P-3 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT EXPANDER SUMMARY 07/29/05 ============================================================================== UNIT 3, 'EX1' Feeds S2 Products Mixed S4 OPERATING CONDITIONS INLET ISENTROPIC OUTLET ----------- ----------- ----------- TEMPERATURE, F -84.00 -180.50 -174.39 PRESSURE, PSIA 587.70 139.70 139.70 ENTHALPY, MM BTU/SEC -0.0002 -0.0005 -0.0005 ENTROPY, BTU/LB-MOL-F 39.2708 39.2708 39.7596 MOLE PERCENT VAPOR 100.0000 91.3409 93.7547 MOLE PERCENT LIQUID 0.0000 8.6591 6.2453 ACT VAP RATE, M FT3/MIN 0.1473 ADIABATIC EFF, PERCENT 80.00 WORK, HP THEORETICAL 490.45 ACTUAL 392.36



SIMULATION SCIENCES INC. R PAGE P-4 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COMPRESSOR SUMMARY 07/29/05 ============================================================================== UNIT 6, 'C1' Feeds S9 Products Vapor S10 OPERATING CONDITIONS INLET ISENTROPIC OUTLET ----------- ----------- ----------- TEMPERATURE, F 110.00 149.54 161.83 PRESSURE, PSIA 120.00 160.72 160.72 ENTHALPY, MM BTU/SEC 0.0011 0.0013 0.0014 ENTROPY, BTU/LB-MOL-F 46.8354 46.8354 47.0180 CP, BTU/LB-MOL-F 8.8613 9.1682 CV, BTU/LB-MOL-F 6.7339 7.0281 CP/(CP-R) 1.2888 1.2765 CP/CV 1.3159 1.3045 MOLE PERCENT VAPOR 100.0000 100.0000 100.0000 MOLE PERCENT LIQUID 0.0000 0.0000 0.0000 ACT VAP RATE, M FT3/MIN 1.8599 ADIABATIC EFF, PERCENT 75.0000 POLYTROPIC EFF, PERCENT 75.8049 ISENTROPIC COEFFICIENT, K 1.2952 POLYTROPIC COEFFICIENT, N 1.4287 ASME "F" FACTOR 1.0001 HEAD, FT ADIABATIC 14970.67 POLYTROPIC 15131.34 ACTUAL 19960.90 WORK, HP THEORETICAL 294.27 POLYTROPIC 297.43 ACTUAL 392.36 NOTE: POLYTROPIC AND ISENTROPIC COEFFICIENTS CALCULATED FROM ASME EQUATIONS



SIMULATION SCIENCES INC. R PAGE P-5 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT HEAT EXCHANGER SUMMARY 07/29/05 ============================================================================== UNIT 4, 'E1' OPERATING CONDITIONS DUTY, MM BTU/SEC 1.448E-03 LMTD, F 56.989 ** WARNING ** The LMTD correction factor (FT) has been set to 0.0001. F FACTOR (FT) 1.000E-04 MTD, F 5.699E-03 U*A, BTU/HR-F 9.145E+08 HOT SIDE CONDITIONS INLET OUTLET ----------- ----------- FEED S1 MIXED PRODUCT S6 VAPOR, LB-MOL/SEC 0.744 0.663 M LB/SEC 1.676E-02 1.309E-02 CP, BTU/LB-F 0.545 0.569 LIQUID, LB-MOL/SEC 8.109E-02 M LB/SEC 3.671E-03 CP, BTU/LB-F 0.567 TOTAL, LB-MOL/SEC 0.744 0.744 M LB/SEC 1.676E-02 1.676E-02 CONDENSATION, LB-MOL/SEC 8.109E-02 TEMPERATURE, F 120.000 8.081 PRESSURE, PSIA 602.700 592.700 COLD SIDE CONDITIONS INLET OUTLET ----------- ----------- FEED S8 VAPOR PRODUCT S9 VAPOR, LB-MOL/SEC 0.617 0.617 M LB/SEC 1.081E-02 1.081E-02 CP, BTU/LB-F 0.501 0.506 TOTAL, LB-MOL/SEC 0.617 0.617 M LB/SEC 1.081E-02 1.081E-02 CONDENSATION, LB-MOL/SEC 0.000 TEMPERATURE, F -164.112 110.000 PRESSURE, PSIA 125.000 120.000



SIMULATION SCIENCES INC. R PAGE P-6 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT HEAT EXCHANGER SUMMARY 07/29/05 ============================================================================== UNIT 5, 'E2' OPERATING CONDITIONS DUTY, MM BTU/SEC 1.386E-03 HOT SIDE CONDITIONS INLET OUTLET ----------- ----------- FEED S6 MIXED PRODUCT S7 VAPOR, LB-MOL/SEC 0.663 0.503 M LB/SEC 1.309E-02 9.061E-03 CP, BTU/LB-F 0.569 0.709 LIQUID, LB-MOL/SEC 8.109E-02 0.242 M LB/SEC 3.671E-03 7.696E-03 CP, BTU/LB-F 0.567 0.597 TOTAL, LB-MOL/SEC 0.744 0.744 M LB/SEC 1.676E-02 1.676E-02 CONDENSATION, LB-MOL/SEC 0.161 TEMPERATURE, F 8.081 -84.000 PRESSURE, PSIA 592.700 587.700



SIMULATION SCIENCES INC. R PAGE P-7 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COLUMN SUMMARY 07/29/05 ============================================================================== UNIT 7, 'T1' TOTAL NUMBER OF ITERATIONS IN/OUT METHOD 7 COLUMN SUMMARY ---------- NET FLOW RATES ----------- HEATER TRAY TEMP PRESSURE LIQUID VAPOR FEED PRODUCT DUTIES DEG F PSIA LB-MOL/SEC MM BTU/SEC ------ ------- -------- -------- -------- --------- --------- ------------ 1 -164.1 125.00 0.0 0.5M 0.6V 2 -127.7 125.00 0.0 0.1 3 -106.5 125.00 0.2 0.1 0.2M 4 -40.8 125.00 0.2 0.1 5 -12.5 125.00 0.2 0.1 6 -6.4 125.00 0.2 0.1 7 -4.9 125.00 0.2 0.1 8 -3.3 125.00 0.2 0.1 9 2.9 125.00 0.2 0.1 10R 29.8 125.00 0.1 0.1L 0.0007 FEED AND PRODUCT STREAMS TYPE STREAM PHASE FROM TO LIQUID FLOW RATES HEAT RATES TRAY TRAY FRAC LB-MOL/SEC MM BTU/SEC ----- ------------ ------ ---- ---- ------ ------------ ------------ FEED S4 MIXED 1 0.0595 0.50 -0.0005 FEED S5 MIXED 3 0.6414 0.24 -0.0006 PROD S8 VAPOR 1 0.62 -0.0003 PROD S11 LIQUID 10 0.13 0.0000 OVERALL MOLE BALANCE, (FEEDS - PRODUCTS) -1.0708E-16 OVERALL HEAT BALANCE, (H(IN) - H(OUT) ) -5.7084E-09 SPECIFICATIONS SPECIFICATION PARAMETER TRAY COMP SPECIFICATION SPECIFIED CALCULATED NUMBER TYPE NO NO TYPE VALUE VALUE ------------- --------- ---- ------ ------------- ---------- ---------- 1 (ACTIVE) STRM S11 10 2 MOL RATIO 1.500E-02 1.500E-02



SIMULATION SCIENCES INC. R PAGE P-8 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COLUMN SUMMARY 07/29/05 ============================================================================== UNIT 7, 'T1' (Cont) TRAY NET VAPOR RATES AND DENSITIES --------------- RATES --------------- TRAY MW ACTUAL DENS Z FROM STANDARD ACTUAL LB/M3 DENSITY M LB/SEC M M3/SEC M M3/SEC ---- -------- ------------ -------- ----------- ----------- ----------- 1 17.515 27.35704 0.89106 1.081E-02 6.630E-03 3.950E-04 2 17.660 24.12515 0.90699 2.555E-03 1.554E-03 1.059E-04 3 17.908 22.67159 0.92003 2.494E-03 1.497E-03 1.100E-04 4 24.069 26.12170 0.90484 1.415E-03 6.318E-04 5.417E-05 5 29.592 31.04322 0.87690 2.620E-03 9.513E-04 8.439E-05 6 31.041 32.43253 0.86855 3.350E-03 1.160E-03 1.033E-04 7 31.343 32.70092 0.86700 3.529E-03 1.210E-03 1.079E-04 8 31.498 32.73882 0.86714 3.563E-03 1.216E-03 1.088E-04 9 31.960 32.70827 0.86889 3.569E-03 1.200E-03 1.091E-04 10 34.001 32.62859 0.87578 3.562E-03 1.126E-03 1.092E-04 TRAY NET LIQUID RATES AND DENSITIES --------------- RATES --------------- TRAY MW ACTUAL DENS Z FROM STD LIQ ACTUAL LB/FT3 DENSITY M LB/SEC FT3/SEC GAL/MIN ---- -------- ------------ -------- ----------- ----------- ----------- 1 26.611 41.273 0.02541 8.088E-04 3.543E-02 8.795 2 29.907 40.434 0.02595 7.485E-04 3.150E-02 8.309 3 39.548 38.308 0.03405 7.365E-03 0.257 86.296 4 39.681 33.890 0.03256 8.570E-03 0.306 113.503 5 39.514 32.006 0.03216 9.300E-03 0.336 130.420 6 39.491 31.597 0.03212 9.479E-03 0.344 134.656 7 39.546 31.532 0.03212 9.514E-03 0.345 135.416 8 39.810 31.570 0.03218 9.519E-03 0.343 135.336 9 40.964 31.790 0.03245 9.513E-03 0.335 134.305 10 46.689 32.835 0.03384 5.950E-03 0.191 81.337



SIMULATION SCIENCES INC. R PAGE P-9 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM MOLAR COMPONENT RATES 07/29/05 ============================================================================== STREAM ID S1 S2 S3 S4 NAME PHASE VAPOR VAPOR LIQUID MIXED FLUID RATES, LB-MOL/SEC 1 N2 0.0589 0.0552 3.6693E-03 0.0552 2 METHANE 0.5438 0.4280 0.1159 0.4280 3 ETHANE 0.0572 0.0159 0.0413 0.0159 4 PROPANE 0.0424 3.1439E-03 0.0392 3.1439E-03 5 BUTANE 0.0182 2.9577E-04 0.0179 2.9577E-04 6 IBUTANE 7.3703E-03 1.8398E-04 7.1864E-03 1.8398E-04 7 IPENTANE 5.1369E-03 2.5434E-05 5.1115E-03 2.5434E-05 8 PENTANE 6.1047E-03 2.5738E-05 6.0790E-03 2.5738E-05 9 HEXANE 3.1268E-03 2.5617E-06 3.1242E-03 2.5617E-06 10 HEPTANE 2.3079E-03 4.6998E-07 2.3074E-03 4.6998E-07 TOTAL RATE, LB-MOL/SEC 0.7445 0.5028 0.2417 0.5028 TEMPERATURE, F 120.0000 -84.0000 -84.0000 -174.3890 PRESSURE, PSIA 602.7000 587.7000 587.7000 139.6959 ENTHALPY, MM BTU/SEC 2.0568E-03 -1.7329E-04 -6.0367E-04 -4.5060E-04 MOLECULAR WEIGHT 22.5095 18.0233 31.8404 18.0233 MOLE FRAC VAPOR 1.0000 1.0000 0.0000 0.9375 MOLE FRAC LIQUID 0.0000 0.0000 1.0000 0.0625 STREAM ID S5 S6 S7 S8 NAME PHASE MIXED MIXED MIXED VAPOR FLUID RATES, LB-MOL/SEC 1 N2 3.6693E-03 0.0589 0.0589 0.0589 2 METHANE 0.1159 0.5438 0.5438 0.5438 3 ETHANE 0.0413 0.0572 0.0572 0.0141 4 PROPANE 0.0392 0.0424 0.0424 2.0029E-04 5 BUTANE 0.0179 0.0182 0.0182 1.2819E-06 6 IBUTANE 7.1864E-03 7.3703E-03 7.3703E-03 1.5859E-06 7 IPENTANE 5.1115E-03 5.1369E-03 5.1369E-03 1.1927E-08 8 PENTANE 6.0790E-03 6.1047E-03 6.1047E-03 9.0828E-09 9 HEXANE 3.1242E-03 3.1268E-03 3.1268E-03 5.0102E-11 10 HEPTANE 2.3074E-03 2.3079E-03 2.3079E-03 8.8805E-13 TOTAL RATE, LB-MOL/SEC 0.2417 0.7445 0.7445 0.6170 TEMPERATURE, F -136.2925 8.0805 -84.0000 -164.1125 PRESSURE, PSIA 125.0000 592.7000 587.7000 125.0000 ENTHALPY, MM BTU/SEC -6.0367E-04 6.0915E-04 -7.7696E-04 -3.2188E-04 MOLECULAR WEIGHT 31.8404 22.5095 22.5095 17.5152 MOLE FRAC VAPOR 0.3586 0.8911 0.6753 1.0000 MOLE FRAC LIQUID 0.6414 0.1089 0.3247 0.0000



SIMULATION SCIENCES INC. R PAGE P-10 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM MOLAR COMPONENT RATES 07/29/05 ============================================================================== STREAM ID S9 S10 S11 NAME PHASE VAPOR VAPOR LIQUID FLUID RATES, LB-MOL/SEC 1 N2 0.0589 0.0589 7.1637E-14 2 METHANE 0.5438 0.5438 1.7952E-07 3 ETHANE 0.0141 0.0141 0.0431 4 PROPANE 2.0029E-04 2.0029E-04 0.0422 5 BUTANE 1.2819E-06 1.2819E-06 0.0182 6 IBUTANE 1.5859E-06 1.5859E-06 7.3687E-03 7 IPENTANE 1.1927E-08 1.1927E-08 5.1369E-03 8 PENTANE 9.0828E-09 9.0828E-09 6.1047E-03 9 HEXANE 5.0102E-11 5.0102E-11 3.1268E-03 10 HEPTANE 8.8805E-13 8.8805E-13 2.3079E-03 TOTAL RATE, LB-MOL/SEC 0.6170 0.6170 0.1274 TEMPERATURE, F 110.0000 161.8332 29.7636 PRESSURE, PSIA 120.0000 160.7205 125.0000 ENTHALPY, MM BTU/SEC 1.1258E-03 1.4031E-03 -1.4771E-05 MOLECULAR WEIGHT 17.5152 17.5152 46.6888 MOLE FRAC VAPOR 1.0000 1.0000 0.0000 MOLE FRAC LIQUID 0.0000 0.0000 1.0000



SIMULATION SCIENCES INC. R PAGE P-11 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 07/29/05 ============================================================================== STREAM ID S1 S2 S3 S4 NAME PHASE VAPOR VAPOR LIQUID MIXED ----- TOTAL STREAM ----- RATE, LB-MOL/SEC 0.744 0.503 0.242 0.503 M LB/SEC 1.676E-02 9.061E-03 7.696E-03 9.061E-03 STD LIQ RATE, FT3/SEC 0.709 0.424 0.285 0.424 TEMPERATURE, F 120.000 -84.000 -84.000 -174.389 PRESSURE, PSIA 602.700 587.700 587.700 139.696 MOLECULAR WEIGHT 22.509 18.023 31.840 18.023 ENTHALPY, MM BTU/SEC 2.057E-03 -1.733E-04 -6.037E-04 -4.506E-04 BTU/LB 122.739 -19.124 -78.436 -49.728 MOLE FRACTION LIQUID 0.0000 0.0000 1.0000 0.0625 REDUCED TEMP (KAYS RULE) 1.4710 1.1072 0.7395 0.8408 PRES (KAYS RULE) 0.9345 0.9058 0.9230 0.2153 ACENTRIC FACTOR 0.0401 0.0181 0.0857 0.0181 WATSON K (UOPK) 16.647 17.187 16.010 17.187 STD LIQ DENSITY, LB/FT3 23.629 21.350 27.026 21.350 SPECIFIC GRAVITY 0.3789 0.3423 0.4333 0.3423 API GRAVITY 241.971 281.844 195.026 281.844 -------- VAPOR --------- RATE, LB-MOL/SEC 0.744 0.503 N/A 0.471 M LB/SEC 1.676E-02 9.061E-03 N/A 8.294E-03 M M3/SEC 1.926E-04 6.953E-05 N/A 2.542E-04 STD VAP RATE(1), M M3/SEC 8.000E-03 5.403E-03 N/A 5.065E-03 SPECIFIC GRAVITY (AIR=1.0) 0.777 0.622 N/A 0.608 MOLECULAR WEIGHT 22.509 18.023 N/A 17.596 ENTHALPY, BTU/LB 122.739 -19.124 N/A -40.189 CP, BTU/LB-F 0.545 0.709 N/A 0.510 DENSITY, LB/M M3 86987.591 130315.705 N/A 32626.860 Z (FROM DENSITY) 0.8854 0.7120 N/A 0.8690 -------- LIQUID -------- RATE, LB-MOL/SEC N/A N/A 0.242 3.140E-02 M LB/SEC N/A N/A 7.696E-03 7.673E-04 FT3/SEC N/A N/A 0.174 1.924E-02 GAL/MIN N/A N/A 78.017 8.633 STD LIQ RATE, FT3/SEC N/A N/A 0.285 3.427E-02 SPECIFIC GRAVITY (H2O=1.0) N/A N/A 0.4333 0.3590 MOLECULAR WEIGHT N/A N/A 31.840 24.438 ENTHALPY, BTU/LB N/A N/A -78.436 -152.832 CP, BTU/LB-F N/A N/A 0.597 0.624 DENSITY, LB/FT3 N/A N/A 44.277 39.891 Z (FROM DENSITY) N/A N/A 0.1048 0.0280 (1) STANDARD VAPOR VOLUME IS 379.49 FT3/LB-MOLE (60 F AND 14.696 PSIA)



SIMULATION SCIENCES INC. R PAGE P-12 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 07/29/05 ============================================================================== STREAM ID S5 S6 S7 S8 NAME PHASE MIXED MIXED MIXED VAPOR ----- TOTAL STREAM ----- RATE, LB-MOL/SEC 0.242 0.744 0.744 0.617 M LB/SEC 7.696E-03 1.676E-02 1.676E-02 1.081E-02 STD LIQ RATE, FT3/SEC 0.285 0.709 0.709 0.518 TEMPERATURE, F -136.293 8.081 -84.000 -164.112 PRESSURE, PSIA 125.000 592.700 587.700 125.000 MOLECULAR WEIGHT 31.840 22.509 22.509 17.515 ENTHALPY, MM BTU/SEC -6.037E-04 6.091E-04 -7.770E-04 -3.219E-04 BTU/LB -78.436 36.350 -46.364 -29.783 MOLE FRACTION LIQUID 0.6414 0.1089 0.3247 0.0000 REDUCED TEMP (KAYS RULE) 0.6365 1.1870 0.9533 0.8776 PRES (KAYS RULE) 0.1963 0.9190 0.9113 0.1919 ACENTRIC FACTOR 0.0857 0.0401 0.0401 0.0158 WATSON K (UOPK) 16.010 16.647 16.647 17.516 STD LIQ DENSITY, LB/FT3 27.026 23.629 23.629 20.847 SPECIFIC GRAVITY 0.4333 0.3789 0.3789 0.3343 API GRAVITY 195.026 241.971 241.971 291.810 -------- VAPOR --------- RATE, LB-MOL/SEC 8.669E-02 0.663 0.503 0.617 M LB/SEC 1.473E-03 1.309E-02 9.061E-03 1.081E-02 M M3/SEC 6.205E-05 1.313E-04 6.953E-05 3.950E-04 STD VAP RATE(1), M M3/SEC 9.315E-04 7.129E-03 5.403E-03 6.630E-03 SPECIFIC GRAVITY (AIR=1.0) 0.587 0.681 0.622 0.605 MOLECULAR WEIGHT 16.994 19.726 18.023 17.515 ENTHALPY, BTU/LB -8.985 50.817 -19.124 -29.783 CP, BTU/LB-F 0.511 0.569 0.709 0.501 DENSITY, LB/M M3 23741.034 99668.712 130315.705 27357.042 Z (FROM DENSITY) 0.9105 0.8253 0.7120 0.8911 -------- LIQUID -------- RATE, LB-MOL/SEC 0.155 8.109E-02 0.242 N/A M LB/SEC 6.223E-03 3.671E-03 7.696E-03 N/A FT3/SEC 0.151 0.102 0.174 N/A GAL/MIN 67.936 45.762 78.017 N/A STD LIQ RATE, FT3/SEC 0.210 0.114 0.285 N/A SPECIFIC GRAVITY (H2O=1.0) 0.4748 0.5148 0.4333 N/A MOLECULAR WEIGHT 40.142 45.279 31.840 N/A ENTHALPY, BTU/LB -94.877 -15.215 -78.436 N/A CP, BTU/LB-F 0.479 0.567 0.597 N/A DENSITY, LB/FT3 41.114 36.010 44.277 N/A Z (FROM DENSITY) 0.0352 0.1485 0.1048 N/A (1) STANDARD VAPOR VOLUME IS 379.49 FT3/LB-MOLE (60 F AND 14.696 PSIA)



SIMULATION SCIENCES INC. R PAGE P-13 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 07/29/05 ============================================================================== STREAM ID S9 S10 S11 NAME PHASE VAPOR VAPOR LIQUID ----- TOTAL STREAM ----- RATE, LB-MOL/SEC 0.617 0.617 0.127 M LB/SEC 1.081E-02 1.081E-02 5.950E-03 STD LIQ RATE, FT3/SEC 0.518 0.518 0.191 TEMPERATURE, F 110.000 161.833 29.764 PRESSURE, PSIA 120.000 160.721 125.000 MOLECULAR WEIGHT 17.515 17.515 46.689 ENTHALPY, MM BTU/SEC 1.126E-03 1.403E-03 -1.477E-05 BTU/LB 104.170 129.830 -2.482 MOLE FRACTION LIQUID 0.0000 0.0000 1.0000 REDUCED TEMP (KAYS RULE) 1.6915 1.8455 0.7289 PRES (KAYS RULE) 0.1842 0.2467 0.2038 ACENTRIC FACTOR 0.0158 0.0158 0.1576 WATSON K (UOPK) 17.516 17.516 15.067 STD LIQ DENSITY, LB/FT3 20.847 20.847 31.188 SPECIFIC GRAVITY 0.3343 0.3343 0.5001 API GRAVITY 291.810 291.810 151.452 -------- VAPOR --------- RATE, LB-MOL/SEC 0.617 0.617 N/A M LB/SEC 1.081E-02 1.081E-02 N/A M M3/SEC 8.778E-04 7.154E-04 N/A STD VAP RATE(1), M M3/SEC 6.630E-03 6.630E-03 N/A SPECIFIC GRAVITY (AIR=1.0) 0.605 0.605 N/A MOLECULAR WEIGHT 17.515 17.515 N/A ENTHALPY, BTU/LB 104.170 129.830 N/A CP, BTU/LB-F 0.506 0.523 N/A DENSITY, LB/M M3 12312.378 15106.319 N/A Z (FROM DENSITY) 0.9861 0.9867 N/A -------- LIQUID -------- RATE, LB-MOL/SEC N/A N/A 0.127 M LB/SEC N/A N/A 5.950E-03 FT3/SEC N/A N/A 0.181 GAL/MIN N/A N/A 81.337 STD LIQ RATE, FT3/SEC N/A N/A 0.191 SPECIFIC GRAVITY (H2O=1.0) N/A N/A 0.5001 MOLECULAR WEIGHT N/A N/A 46.689 ENTHALPY, BTU/LB N/A N/A -2.482 CP, BTU/LB-F N/A N/A 0.584 DENSITY, LB/FT3 N/A N/A 32.835 Z (FROM DENSITY) N/A N/A 0.0338 (1) STANDARD VAPOR VOLUME IS 379.49 FT3/LB-MOLE (60 F AND 14.696 PSIA)



Dæûa vaìo caïc säú liãûu kãút quaí trong Program File, ta xaïc âënh âæåüc:

1. Cäng suáút thæûc cuía maïy neïn C1:

ÅÍ P-4: Cäng suáút thæûc cuía maïy neïn C1 laì 392,36 HP

2. Thaình pháön, nhiãût âäü vaì aïp suáút cuía caïc doìng saín pháøm khê vaì loíng: Ở P-10: Ta có S10 (sản phẩm khí) S11 (sản phẩm lỏng) FLUID RATES, LB-MOL/SEC 1 N2 0.0589 7.1637E-14 2 METHANE 0.5438 1.7952E-07 3 ETHANE 0.0141 0.0431 4 PROPANE 2.0029E-04 0.0422 5 BUTANE 1.2819E-06 0.0182 6 IBUTANE 1.5859E-06 7.3687E-03 7 IPENTANE 1.1927E-08 5.1369E-03 8 PENTANE 9.0828E-09 6.1047E-03 9 HEXANE 5.0102E-11 3.1268E-03 10 HEPTANE 8.8805E-13 2.3079E-03 TOTAL RATE, LB-MOL/SEC 0.6170 0.1274 TEMPERATURE, F 161.8332 29.7636 PRESSURE, PSIA 160.7205 125.0000



8.2 Baìi toaïn 2: Mä phoíng thiãút bë taïch khê - loíng

8.2.1 Baìi toaïn

Cho vaìo thiãút bë taïch khê loíng mäüt doìng nguyãn liãûu våïi caïc dæî liãûu sau:

• Læu læåüng : 100 kmol/h

• t = 300C

• P = 10 bar

• Thaình pháön hoïa hoüc: Meïthane : 13 kmol/h

Ethane : 22 kmol/h

Propane : 38 kmol/h

Butane : 22 kmol/h

Pentane : 5 kmol/h

Âiãöu kiãûn laìm viãûc cuía thiãút bë taïch: 300C vaì 7 bar

Haîy xaïc âënh:

1. Pháön mol bay håi cuía nguyãn liãûu trong âiãöu kiãûn cuía bçnh taïch?

2. Thaình pháön cuía loíng vaì håi ra khoíi thiãút bë taïch?

3. Nàng suáút nhiãût cuía thiãút bë taïch?



8.2.2 Kãút quaí: $ Generated by PRO/II Keyword Generation System <version 7.0> $ Generated on: Sun Jul 24 18:48:32 2005 TITLE DIMENSION METRIC, PRES=BAR, STDTEMP=0, STDPRES=1.01325 SEQUENCE SIMSCI CALCULATION RVPBASIS=APIN, TVP=37.778 COMPONENT DATA LIBID 1,METHANE/2,ETHANE/3,PROPANE/4,BUTANE/5,PENTANE, & BANK=PROCESS,SIMSCI THERMODYNAMIC DATA METHOD SYSTEM=SRK, ENTHALPY(L)=LK, SET=SRK01, DEFAULT STREAM DATA PROPERTY STREAM=S1, TEMPERATURE=30, PRESSURE=10, PHASE=M, & RATE(M)=100, COMPOSITION(M)=1,13/2,22/3,38/4,22/5,5 UNIT OPERATIONS FLASH UID=F1 FEED S1 PRODUCT V=S2, W=S3 ISO TEMPERATURE=30, PRESSURE=7 END



SIMULATION SCIENCES INC. R PAGE H-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM CALCULATION HISTORY 07/24/05 ============================================================================== *** PROBLEM SOLUTION BEGINS FEED FLASH COMPLETE UNIT 1 SOLVED - 'F1 ' *** PROBLEM SOLUTION REACHED *** THIS RUN USED 3.12 PRO/II SIMULATION UNITS *** RUN STATISTICS STARTED 18:48:16 07/24/05 NO ERRORS FINISHED 18:48:16 07/24/05 NO WARNINGS RUN TIMES NO MESSAGES INTERACTIVE 0 MIN, 0.00 SEC CALCULATIONS 0 MIN, 0.19 SEC TOTAL 0 MIN, 0.19 SEC



SIMULATION SCIENCES INC. R PAGE I-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT INDEX 07/24/05 ============================================================================== PAGE CONTENTS ------ ---------------------------------------------------------------- 1 COMPONENT DATA 2 CALCULATION SEQUENCE AND RECYCLES 3 FLASH DRUM SUMMARY 4 STREAM MOLAR COMPONENT RATES 5 STREAM SUMMARY



SIMULATION SCIENCES INC. R PAGE P-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COMPONENT DATA 07/24/05 ============================================================================== COMPONENT COMP. TYPE PHASE MOL. WEIGHT DENSITY, KG/M3 --------------------- ----------- ----------- ----------- ----------- 1 METHANE LIBRARY VAP/LIQ 16.043 299.704 2 ETHANE LIBRARY VAP/LIQ 30.070 356.049 3 PROPANE LIBRARY VAP/LIQ 44.097 507.199 4 BUTANE LIBRARY VAP/LIQ 58.124 583.824 5 PENTANE LIBRARY VAP/LIQ 72.151 630.378 COMPONENT NBP CRIT. TEMP. CRIT. PRES. CRIT. VOLM. C C BAR M3/KG-MOL --------------------- ----------- ----------- ----------- ----------- 1 METHANE -161.490 -82.600 46.001 0.0990 2 ETHANE -88.630 32.300 48.839 0.1480 3 PROPANE -42.070 96.670 42.496 0.2030 4 BUTANE -0.500 152.000 37.997 0.2550 5 PENTANE 36.074 196.500 33.691 0.3040 COMPONENT ACEN. FACT. HEAT FORM. G FORM. KCAL/KG-MOL KCAL/KG-MOL --------------------- ----------- ----------- ----------- 1 METHANE 0.01040 -17814.56 -12070.08 2 ETHANE 0.09860 -20066.78 -7672.47 3 PROPANE 0.15290 -24805.58 -5633.13 4 BUTANE 0.20130 -30040.13 -3982.90 5 PENTANE 0.25060 -34982.56 -2040.48



SIMULATION SCIENCES INC. R PAGE P-3 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT FLASH DRUM SUMMARY 07/24/05 ============================================================================== FLASH ID F1 NAME FEEDS S1 PRODUCTS VAPOR S2 LIQUID S3 TEMPERATURE, C 30.000 PRESSURE, BAR 7.000 PRESSURE DROP, BAR 3.000 MOLE FRAC VAPOR 0.94580 MOLE FRAC LIQUID 0.05420 DUTY, M*KCAL/HR 0.09956 FLASH TYPE ISOTHERMAL



SIMULATION SCIENCES INC. R PAGE P-4 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM MOLAR COMPONENT RATES 07/24/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED VAPOR LIQUID FLUID RATES, KG-MOL/HR 1 METHANE 13.0000 12.9676 0.0324 2 ETHANE 22.0000 21.7330 0.2670 3 PROPANE 38.0000 36.5869 1.4131 4 BUTANE 22.0000 19.5760 2.4240 5 PENTANE 5.0000 3.7169 1.2831 TOTAL RATE, KG-MOL/HR 100.0000 94.5803 5.4197 TEMPERATURE, C 30.0000 30.0000 30.0000 PRESSURE, BAR 10.0000 7.0000 7.0000 ENTHALPY, M*KCAL/HR 0.2869 0.3813 5.1601E-03 MOLECULAR WEIGHT 41.8527 41.0332 56.1538 MOLE FRAC VAPOR 0.7211 1.0000 0.0000 MOLE FRAC LIQUID 0.2789 0.0000 1.0000



SIMULATION SCIENCES INC. R PAGE P-5 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 07/24/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED VAPOR LIQUID ----- TOTAL STREAM ----- RATE, KG-MOL/HR 100.000 94.580 5.420 K*KG/HR 4.185 3.881 0.304 STD LIQ RATE, M3/HR 8.620 8.085 0.535 TEMPERATURE, C 30.000 30.000 30.000 PRESSURE, BAR 10.000 7.000 7.000 MOLECULAR WEIGHT 41.853 41.033 56.154 ENTHALPY, M*KCAL/HR 0.287 0.381 5.160E-03 KCAL/KG 68.540 98.238 16.955 MOLE FRACTION LIQUID 0.2789 0.0000 1.0000 REDUCED TEMP (KAYS RULE) 0.8673 0.8766 0.7323 PRES (KAYS RULE) 0.2330 0.1622 0.1807 ACENTRIC FACTOR 0.1380 0.1347 0.1942 WATSON K (UOPK) 15.179 15.289 13.771 STD LIQ DENSITY, KG/M3 485.517 480.022 568.495 SPECIFIC GRAVITY 0.4860 0.4805 0.5691 API GRAVITY 159.655 162.987 117.157 -------- VAPOR --------- RATE, KG-MOL/HR 72.108 94.580 N/A K*KG/HR 2.730 3.881 N/A K*M3/HR 0.160 0.308 N/A NORM VAP RATE(1), K*M3/HR 1.616 2.120 N/A SPECIFIC GRAVITY (AIR=1.0) 1.307 1.417 N/A MOLECULAR WEIGHT 37.861 41.033 N/A ENTHALPY, KCAL/KG 95.813 98.238 N/A CP, KCAL/KG-C 0.459 0.444 N/A DENSITY, KG/K*M3 17009.778 12581.288 N/A Z (FROM DENSITY) 0.8831 0.9058 N/A -------- LIQUID -------- RATE, KG-MOL/HR 27.892 N/A 5.420 K*KG/HR 1.455 N/A 0.304 M3/HR 2.749 N/A 0.552 GAL/MIN 12.105 N/A 2.432 STD LIQ RATE, M3/HR 2.657 N/A 0.535 SPECIFIC GRAVITY (H2O=1.0) 0.5483 N/A 0.5691 MOLECULAR WEIGHT 52.172 N/A 56.154 ENTHALPY, KCAL/KG 17.373 N/A 16.955 CP, KCAL/KG-C 0.611 N/A 0.600 DENSITY, KG/M3 529.312 N/A 550.967 Z (FROM DENSITY) 0.0391 N/A 0.0283 (1) NORMAL VAPOR VOLUME IS 22.414 M3/KG-MOLE (0 C AND 1 ATM)



Tæì kãút quaí cuía Programme file, ta xaïc âënh âæåüc:

1. Pháön mol bay håi cuía nguyãn liãûu trong âiãöu kiãûn cuía bçnh taïch

Theo kãút quaí åí P-3: MOLE FRAC VAPOR 0.94580

Váûy: Pháön mol bay håi cuía nguyãn liãûu trong âiãöu kiãûn cuía bçnh taïch laì 0,9458 hay 94,58%

2. Thaình pháön cuía loíng vaì håi ra khoíi thiãút bë taïch:

- Trãn Flowsheet, Right-click vaìo doìng S2 vaì S3 ⇒ hiãøn thë cæía säø læûa choün


- Choün Properties tæì drop-down list box åí muûc Stream Label Type

- Màûc âënh åí muûc Property List laì Materiel Balance List ⇒ seî hiãøn thë tãn, traûng thaïi doìng, nhiãût âäü, aïp suáút, læu læåüng vaì thaình pháön cuía doìng ⇒ OK



3. Nàng suáút nhiãût cuía thiãút bë taïch:

Theo kãút quaí åí P-3: DUTY, M*KCAL/HR 0.09956

Váûy: Nàng suáút nhiãût cuía thiãút bë taïch laì 99560 kCal/h

8.3 Baìi toaïn 3: Tênh nhiãût âäü säi cuía mäüt häùn håüp hai pha åí mäüt aïp suáút nháút âënh

8.3.1 Baìi toaïn

Nguyãn liãûu coï thaình pháön, aïp suáút vaì nhiãût âäü nhæ baìi toaïn 2, læu læåüng = 5500 kg/h.

Haîy xaïc âënh:

1. Nhiãût âäü säi cuía häùn håüp nguyãn liãûu naìy åí aïp suáút 7 bar?

2. Hàòng säú cán bàòng pha cuía caïc cáúu tæí ?

3. Thaình pháön häùn håüp håi cán bàòng våïi loíng?

4. Nàng suáút nhiãût cuía thiãút bë taïch?

8.3.2 Giaíi quyãút baìi toaïn

Âãø giaíi quyãút baìi toaïn trãn, ta tiãún haình caïc bæåïc:

• Giaí thiãút cho häùn håüp nguyãn liãûu naìy âi vaìo mäüt bçnh taïch laìm viãûc åí aïp suáút laì 7 bar.

• Tiãún haình mä phoíng nhæ baìi toaïn 2

• Vç muäún xaïc âënh nhiãût âäü säi cuía häùn håüp ⇒ åí cæía säø Flash Drum, åí muûc Second Specification ⇒ Choün Bubble point åí muûc Unit Specification

• Do phaíi xaïc âënh hàòng säú cán bàòng pha cuía caïc cáúu tæí ⇒ åí cæía säø Flash Drum, åí muûc Print Option ⇒ Choün Include Component K - values

8.3.3 Så âäö baìi toaïn



8.3.4 Kãút quaí: $ Generated by PRO/II Keyword Generation System <version 7.0> $ Generated on: Sun Jul 24 20:11:07 2005 TITLE PRINT INPUT=REFP, ION=NONE DIMENSION METRIC, PRES=BAR, STDTEMP=0, STDPRES=1.01325 SEQUENCE SIMSCI CALCULATION RVPBASIS=APIN, TVP=37.778 COMPONENT DATA LIBID 1,METHANE/2,ETHANE/3,PROPANE/4,BUTANE/5,PENTANE, & BANK=PROCESS,SIMSCI THERMODYNAMIC DATA METHOD SYSTEM=SRK, ENTHALPY(L)=LK, SET=SRK01, DEFAULT STREAM DATA PROPERTY STREAM=S1, TEMPERATURE=30, PRESSURE=10, PHASE=M, & RATE(WT)=5500.01, COMPOSITION(M)=1,13/2,22/3,38/4,22/5,5 UNIT OPERATIONS FLASH UID=F1, KPRINT FEED S1 PRODUCT W=S3, V=S2 BUBBLE PRESSURE=7 END



SIMULATION SCIENCES INC. R PAGE H-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM CALCULATION HISTORY 07/24/05 ============================================================================== *** PROBLEM SOLUTION BEGINS FEED FLASH COMPLETE UNIT 1 SOLVED - 'F1 ' *** PROBLEM SOLUTION REACHED *** THIS RUN USED 3.12 PRO/II SIMULATION UNITS *** RUN STATISTICS STARTED 20:10:52 07/24/05 NO ERRORS FINISHED 20:10:52 07/24/05 NO WARNINGS RUN TIMES NO MESSAGES INTERACTIVE 0 MIN, 0.00 SEC CALCULATIONS 0 MIN, 0.11 SEC TOTAL 0 MIN, 0.11 SEC



SIMULATION SCIENCES INC. R PAGE I-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT INDEX 07/24/05 ============================================================================== PAGE CONTENTS ------ ---------------------------------------------------------------- 1 FLASH DRUM SUMMARY 2 STREAM MOLAR COMPONENT RATES 3 STREAM SUMMARY



SIMULATION SCIENCES INC. R PAGE P-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT FLASH DRUM SUMMARY 07/24/05 ============================================================================== FLASH ID F1 NAME FEEDS S1 PRODUCTS VAPOR S2 LIQUID S3 TEMPERATURE, C -78.756 PRESSURE, BAR 7.000 PRESSURE DROP, BAR 3.000 MOLE FRAC VAPOR 0.00000 MOLE FRAC LIQUID 1.00000 DUTY, M*KCAL/HR -0.62892 FLASH TYPE BUBBLE-P VAPOR-LIQUID COMPOSITIONS AND K-VALUES FOR UNIT 1, 'F1' COMPONENT VAPOR LIQUID K-VALUE ------------------- ---------- ---------- ---------- 1 METHANE 0.93087 0.13000 7.1605E+00 2 ETHANE 0.05887 0.22000 2.6761E-01 3 PROPANE 0.00969 0.38000 2.5507E-02 4 BUTANE 5.4730E-04 0.22000 2.4877E-03 5 PENTANE 1.8438E-05 0.05000 3.6877E-04



SIMULATION SCIENCES INC. R PAGE P-2 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM MOLAR COMPONENT RATES 07/24/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED VAPOR LIQUID FLUID RATES, KG-MOL/HR 1 METHANE 17.0838 0.9309 17.0838 2 ETHANE 28.9110 0.0589 28.9110 3 PROPANE 49.9371 9.6926E-03 49.9371 4 BUTANE 28.9110 5.4730E-04 28.9110 5 PENTANE 6.5707 1.8438E-05 6.5707 TOTAL RATE, KG-MOL/HR 131.4135 0.0000 131.4135 TEMPERATURE, C 30.0000 -78.7564 -78.7564 PRESSURE, BAR 10.0000 7.0000 7.0000 ENTHALPY, M*KCAL/HR 0.3770 0.0000 -0.2519 MOLECULAR WEIGHT 41.8527 17.1648 41.8527 MOLE FRAC VAPOR 0.7211 1.0000 0.0000 MOLE FRAC LIQUID 0.2789 0.0000 1.0000 (1) EQUILIBRIUM VAPOR FROM BUBBLE FLASH - STREAM RATE IS ZERO



SIMULATION SCIENCES INC. R PAGE P-3 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 07/24/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED VAPOR LIQUID ----- TOTAL STREAM ----- RATE, KG-MOL/HR 131.414 0.000 131.414 K*KG/HR 5.500 0.000 5.500 STD LIQ RATE, M3/HR 11.328 0.000 11.328 TEMPERATURE, C 30.000 -78.756 -78.756 PRESSURE, BAR 10.000 7.000 7.000 MOLECULAR WEIGHT 41.853 17.165 41.853 ENTHALPY, M*KCAL/HR 0.377 0.000 -0.252 KCAL/KG 68.540 0.000 -45.809 MOLE FRACTION LIQUID 0.2789 0.0000 1.0000 REDUCED TEMP (KAYS RULE) 0.8673 0.9759 0.5562 PRES (KAYS RULE) 0.2330 0.1517 0.1631 ACENTRIC FACTOR 0.1380 0.0171 0.1380 WATSON K (UOPK) 15.179 19.384 15.179 STD LIQ DENSITY, KG/M3 485.517 308.164 485.517 SPECIFIC GRAVITY 0.4860 0.3085 0.4860 API GRAVITY 159.655 327.219 159.655 -------- VAPOR --------- RATE, KG-MOL/HR 94.759 0.000 N/A K*KG/HR 3.588 0.000 N/A K*M3/HR 0.211 0.000 N/A NORM VAP RATE(2), K*M3/HR 2.124 0.000 N/A SPECIFIC GRAVITY (AIR=1.0) 1.307 0.593 N/A MOLECULAR WEIGHT 37.861 17.165 N/A ENTHALPY, KCAL/KG 95.813 10.123 N/A CP, KCAL/KG-C 0.459 0.504 N/A DENSITY, KG/K*M3 17009.778 7894.784 N/A Z (FROM DENSITY) 0.8831 0.9416 N/A -------- LIQUID -------- RATE, KG-MOL/HR 36.654 N/A 131.414 K*KG/HR 1.912 N/A 5.500 M3/HR 3.613 N/A 8.792 GAL/MIN 15.907 N/A 38.711 STD LIQ RATE, M3/HR 3.491 N/A 11.328 SPECIFIC GRAVITY (H2O=1.0) 0.5483 N/A 0.4860 MOLECULAR WEIGHT 52.172 N/A 41.853 ENTHALPY, KCAL/KG 17.373 N/A -45.809 CP, KCAL/KG-C 0.611 N/A 0.534 DENSITY, KG/M3 529.312 N/A 625.550 Z (FROM DENSITY) 0.0391 N/A 0.0290 (1) EQUILIBRIUM VAPOR FROM BUBBLE FLASH - STREAM RATE IS ZERO (2) NORMAL VAPOR VOLUME IS 22.414 M3/KG-MOLE (0 C AND 1 ATM)



Tæì kãút quaí cuía Programme file, ta xaïc âënh âæåüc:

1. Nhiãût âäü säi cuía häùn håüp nguyãn liãûu naìy åí aïp suáút 7 bar?

ÅÍ P -1: FLASH ID F1 NAME FEEDS S1 PRODUCTS VAPOR S2 LIQUID S3 TEMPERATURE, C -78.756 PRESSURE, BAR 7.000

Váûy nhiãût âäü säi cuía häùn håüp nguyãn liãûu naìy åí aïp suáút 7 bar laì -78,7560C

2. Hàòng säú cán bàòng pha cuía caïc cáúu tæí vaì thaình pháön häùn håüp håi cán bàòng våïi loíng?

Cuîng åí P - 1, ta tçm âæåüc: VAPOR-LIQUID COMPOSITIONS AND K-VALUES FOR UNIT 1, 'F1' COMPONENT VAPOR LIQUID K-VALUE ------------------- ---------- ---------- ---------- 1 METHANE 0.93087 0.13000 7.1605E+00 2 ETHANE 0.05887 0.22000 2.6761E-01 3 PROPANE 0.00969 0.38000 2.5507E-02 4 BUTANE 5.4730E-04 0.22000 2.4877E-03 5 PENTANE 1.8438E-05 0.05000 3.6877E-04

3. Nàng suáút nhiãût cuía thiãút bë taïch

ÅÍ P -1: DUTY, M*KCAL/HR -0.62892

Váûy nàng suáút nhiãût cuía thiãút bë taïch laì -628920 kCal/h



8.4 Baìi toaïn 4: Mä phoíng thaïp taïch propane

8.4.1 Baìi toaïn

Tênh cho thaïp Depropanizer våïi caïc dæî liãûu ban âáöu nhæ sau :

• Nguyãn liãûu :

- nàng suáút : 400 táún/ngaìy

- P = 18 bar

- coï thaình pháön 40% håi gäöm : 26% khäúi læåüng propane vaì 74 % khäúi læåüng butane

• Thaïp :

- 22 âéa lyï thuyãút

- naûp liãûu åí âéa 11

- aïp suáút âènh : 16,5 bar

- tråí læûc : 10 mbar/âéa lyï thuyãút

- thiãút bë ngæng tuû hoaìn toaìn

- aïp suáút bçnh taïch : 16,2 bar

• Chè tiãu cháút læåüng sau :

- saín pháøm âènh : coï 1% khäúi læåüng C4

- saín pháøm âaïy : coï 2% khäúi læåüng C3

⇒ Haîy xaïc âënh :

- Chè säú häöi læu ?

- Nàng suáút nhiãût cuía thiãút bë âun säi laûi vaì thiãút bë ngæng tuû (MkCal/ngaìy)

- Læu læåüng saín pháøm âènh vaì saín pháøm âaïy ?



8.4.2 Så âäö baìi toaïn

8.4.3 Caïc bæåïc mä phoíng

8.4.3.1 Xaïc âënh hãû âån vë âo

Choün hãû âån vë METRIC

1 ton = 1014.04 kilograms

2000 pounds = 1 short ton = 0.907 tonne

2240 pounds = 1 long ton = 1.016 tonne

⇒ Choün kg

8.4.3.2 Xaïc âënh thaình pháön cáúu tæí coï trong hãû

Hãû 2 cáúu tæí : Propane vaì Butane

8.4.3.3 Læûa choün caïc phæång trçnh nhiãût âäüng thêch håüp

Choün hãû GS (Grayson-Streed)



8.4.3.4 Thiãút láûp caïc thiãút bë coï trong så âäö vaì caïc doìng ra vaì vaìo caïc thiãút bë

• Thiãút bë : Thaïp ⇒ click choün biãøu tæåüng thaïp tæì floating PFD ⇒ hiãøn thë cæía säø Column Configuration ⇒ nhàõp choün Condenser vaì Reboiler ⇒ nháûp giaï trë 22 åí muûc Number Theoretical Trays ⇒ OK

• Caïc doìng :

- Thiãút láûp doìng nguyãn liãûu S1 naûp vaìo âéa thæï 11 cuía thaïp ;

- Doìng saín pháøm âènh S2 laì doìng loíng âi ra tæì âaïy bçnh taïch sau khi âaî cho häöi læu mäüt pháön vãö âènh thaïp (ngæng tuû hoaìn toaìn)

- Doìng saín pháøm âaïy S3

8.4.3.5 Xaïc âënh thaình pháön, traûng thaïi cuía caïc doìng, xaïc âënh caïc dæî liãûu vãö thiãút bë

Ta nháûn tháúy ràòng : chè coï doìng S1, thaïp T1 laì âæåüc viãön âoí ⇒ yãu cáöu nháûp dæî liãûu

a- Doìng S1 :

• Double click doìng S1 ⇒ ⇒ hiãøn thë baíng Stream Data ⇒ ÅÍ muûc Description baûn coï thãø nháûp tãn FEED (nguyãn liãûu) cho doìng naìy ⇒ click choün Flowrate and Composition ⇒ choün Total Fluid Flowrate ⇒ nháûp vaìo giaï trë 400. Chuï yï, læu læåüng nguyãn liãûu âæåüc tênh bàòng táún/ngaìy, maì åí âáy âån vë laì KG-MOL/HR ⇒ click UOM ⇒ xuáút hiãûn baíng Convert Unit of Measure ⇒ choün Mass ⇒ TON ⇒ DAY ⇒ nhàõp Change Units

• Nháûp thaình pháön caïc cáúu tæí cuía doìng S1 : Nháûp giaï trë 26 cho cáúu tæí 1 ⇒ nhàõp nuït TAB ⇒ nháûp 74 cho cáúu tæí 2 ⇒ nhàõp OK âãø quay laûi cæía säø chênh Stream Data

• Xaïc âënh nhiãût âäü vaì aïp suáút cuía doìng S1 åí muûc Thermal Condition : ÅÍ doìng First Specification ⇒ choün Pressure ⇒ nháûp giaï trë 18. Xong nhàõp choün Liquid Weight Fraction åí muûc Second Specification ⇒ nháûp giaï trë 0.6 ⇒ OK

b- Thaïp T1

• Double-click vaìo C1 ⇒ xuáút hiãûn cæía säø Column

• ÅÍ muûc Description nháûp tãn DEPROP

• Nhàõp choün vaìo ä thæï hai âæåüc viãön âoí Feeds and Products ⇒ xuáút hiãûn cæía säø Column - Feeds and Products ⇒ ÅÍ baíng trãn, xaïc âënh doìng S1 âæåüc naûp vaìo âéa 11 ⇒ ÅÍ baíng dæåïi, våïi doìng S2 ⇒ choün Fixed Rate Draw åí muûc Type of Product ⇒ choün Liquid åí muûc Phase ⇒ nháûp giaï trë 1 åí muûc Tray ⇒ nháûp giaï trë læu læåüng 104 ⇒ Chuï yï, læu læåüng saín pháøm âæåüc tênh bàòng táún/ngaìy, maì åí âáy âån vë laì KG-MOL/HR ⇒ click UOM ⇒ xuáút hiãûn baíng Convert Unit of Measure ⇒ choün Mass ⇒ TON ⇒ DAY ⇒ nhàõp Change Units ⇒ OK



• Nhàõp choün vaìo ä thæï nháút âæåüc viãön âoí Pressure Profile ⇒ xuáút hiãûn cæía säø Column - Pressure Profile ⇒ Nháûp giaï trë 16.5 bar laì aïp suáút åí âéa trãn cuìng cuía thaïp åí muûc Overall Specification ⇒ ÅÍ muûc Pressure Drop ⇒ choün muûc Per Tray ⇒ nháûp giaï trë 0,01 (bar) ⇒ OK âãø tråí vãö cæía säø Column

• ÅÍ muûc Condenser : nhàõp choün Bubble Temperature åí muûc Condenser Type ⇒ nháûp giaï trë 16.2 (bar) åí muûc Pressure trong cæía säø Condenser Data

• ÅÍ muûc Performance Specification ⇒

- Nhàõp choün ⇒ xuáút hiãûn cæía säø Column - Specifications and Variables ⇒ click vaìo ä choün Add Specifications and Variables ⇒ click vaìo parameter (chæî âoí vaì gaûch dæåïi âoí) trong muûc Specifications ⇒ xuáút hiãûn cæía säø Parameter ⇒ choün Stream åí muûc Stream/Unit vaì choün doìng S3 åí muûc Stream Name laì doìng saín pháøm âaïy cuía thaïp

- Click vaìo Parameter (chæî tràõng trãn nãön âoí) ⇒ xuáút hiãûn cæía säø Parameter selection ⇒ choün Composition åí muûc Parameter ⇒ choün PROPANE laì cáúu tæí âáöu vaì cáúu tæí cuäúi ⇒ OK âãø tråí vãö cæía säø Parameter ⇒ nhàõp choün vaìo Mole Fraction ⇒ click UOM ⇒ xuáút hiãûn baíng Convert Unit of Measure ⇒ choün Mass ⇒ Percent ⇒ nhàõp Change Units ⇒ OK : tråí vãö cæía säø Parameter ⇒ OK : hoaìn thaình cæía säø Parameter ⇒ tråí vãö cæía säø Column - Specifications and Variables ⇒ click vaìo Value ⇒ nháûp giaï trë 2

- Nhàõp choün Insert Specification/ Variable ⇒ xuáút hiãûn thãm mäüt Specification 2

- Tiãúp tuûc nhàõp choün Parameter maìu âoí cuîng åí muûc Specifications ⇒ xuáút hiãûn cæía säø Parameter ⇒ choün Stream åí muûc Stream/Unit vaì choün doìng S2 åí muûc Stream Name ⇒ Click vaìo Parameter (chæî tràõng trãn nãön âoí) ⇒ xuáút hiãûn cæía säø Parameter selection ⇒ choün Composition åí muûc Parameter ⇒ choün BUTANE laì cáúu tæí âáöu vaì cáúu tæí cuäúi ⇒ OK âãø tråí vãö cæía säø Parameter ⇒ nhàõp choün vaìo Mole Fraction ⇒ click UOM ⇒ xuáút hiãûn baíng Convert Unit of Measure ⇒ choün Mass ⇒ Percent ⇒ nhàõp Change Units ⇒ OK : tråí vãö cæía säø Parameter ⇒ OK : hoaìn thaình cæía säø Parameter ⇒ tråí vãö cæía säø Column - Specifications and Variables ⇒ click vaìo Value ⇒ nháûp giaï trë 1

- Click vaìo parameter (chæî âoí vaì gaûch dæåïi âoí) trong muûc Variables 1 ⇒ xuáút hiãûn cæía säø Parameter Selection ⇒ Choün Heat Duty (nàng suáút nhiãût) ⇒ ÅÍ muûc Heater choün REBOILER ⇒ OK : quay laûi cæía säø Variables ⇒ OK : quay laûi cæía säø Column - Specifications and Variables ⇒ Tiãúp tuûc Click vaìo parameter (chæî âoí vaì gaûch dæåïi âoí) trong muûc Variables 2 ⇒ xuáút hiãûn cæía säø Parameter Selection ⇒ Choün Heat Duty (nàng suáút nhiãût)



⇒ ÅÍ muûc Heater choün CONDENSER ⇒ OK : quay laûi cæía säø Variables ⇒ OK : quay laûi cæía säø Column - Specifications and Variables OK : hoaìn thaình viãûc nháûp dæî liãûu cho T1

8.4.3.6 Tiãún haình mä phoíng vaì xem kãút quaí $ Generated by PRO/II Keyword Generation System <version 7.0> $ Generated on: Tue Jul 26 15:12:44 2005 TITLE PRINT INPUT=REFP, ION=NONE DIMENSION METRIC, PRES=BAR, STDTEMP=0, STDPRES=1.01325 SEQUENCE SIMSCI CALCULATION RVPBASIS=APIN, TVP=37.778 COMPONENT DATA LIBID 1,PROPANE/2,BUTANE, BANK=PROCESS,SIMSCI THERMODYNAMIC DATA METHOD SYSTEM=GS, SET=GS01, DEFAULT STREAM DATA PROPERTY STREAM=S1, PRESSURE=18, PHASE=M, LFRACTION(WT)=0.6, & RATE(WT)=400000, COMPOSITION(M)=1,26/2,74 UNIT OPERATIONS COLUMN UID=T1 PARAMETER TRAY=22,IO FEED S1,11 PRODUCT OVHD(WT)=S2,100000, BTMS(M)=S3 CONDENSER TYPE=BUBB, PRESSURE=16.2 DUTY 1,1,,CONDENSER/2,22,,REBOILER PSPEC PTOP=16.5, DPTRAY=0.01 PRINT PROPTABLE=PART ESTIMATE MODEL=CONVENTIONAL, RRATIO=3 SPEC STREAM=S2,PCT(WT), COMP=2,WET, VALUE=1 SPEC STREAM=S3,PCT(WT), COMP=1,WET, VALUE=2 VARY DUTY=1,2 REBOILER TYPE=KETTLE END



SIMULATION SCIENCES INC. R PAGE H-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM CALCULATION HISTORY 07/26/05 ============================================================================== *** PROBLEM SOLUTION BEGINS FEED FLASH COMPLETE SCALING 0 FACTORS = 7.160E-01 ERROR = -6.778E-02 SCALING 1 FACTORS = 7.232E-01 ERROR = -6.464E-02 SCALING 2 FACTORS = 8.709E-01 ERROR = 4.160E-03 INNER 0 : E(ENTH+SPEC) = 4.100E-01 CALCULATING NEW MATRIX INNER 1 : E(ENTH+SPEC) = 2.017E-01 ALPHA = 1.0000 INNER 2 : E(ENTH+SPEC) = 7.976E-02 ALPHA = 1.0000 INNER 3 : E(ENTH+SPEC) = 2.838E-02 ALPHA = 1.0000 INNER 4 : E(ENTH+SPEC) = 6.419E-03 ALPHA = 1.0000 ITER 1 E(K) = 1.144E-02 E(ENTH+SPEC) = 6.419E-03 E(SUM) = 1.604E-01 DAMP = 1.000E+00 INNER 0 : E(ENTH+SPEC) = 1.660E-02 INNER 1 : E(ENTH+SPEC) = 6.574E-03 ALPHA = 1.0000 INNER 2 : E(ENTH+SPEC) = 1.651E-03 ALPHA = 1.0000 INNER 3 : E(ENTH+SPEC) = 6.993E-05 ALPHA = 1.0000 ITER 2 E(K) = 1.346E-03 E(ENTH+SPEC) = 6.993E-05 E(SUM) = 1.595E-02 DAMP = 1.000E+00 INNER 0 : E(ENTH+SPEC) = 2.911E-03 INNER 1 : E(ENTH+SPEC) = 1.527E-04 ALPHA = 1.0000 INNER 2 : E(ENTH+SPEC) = 2.738E-05 ALPHA = 1.0000 INNER 3 : E(ENTH+SPEC) = 2.525E-06 ALPHA = 1.0000 ITER 3 E(K) = 0.000E+00 E(ENTH+SPEC) = 2.525E-06 E(SUM) = 9.704E-04 UNIT 1 SOLVED - 'T1 ' *** PROBLEM SOLUTION REACHED *** THIS RUN USED 47.38 PRO/II SIMULATION UNITS *** RUN STATISTICS STARTED 15:11:49 07/26/05 NO ERRORS FINISHED 15:11:50 07/26/05 NO WARNINGS RUN TIMES NO MESSAGES INTERACTIVE 0 MIN, 0.00 SEC CALCULATIONS 0 MIN, 0.21 SEC TOTAL 0 MIN, 0.21 SEC



SIMULATION SCIENCES INC. R PAGE I-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT INDEX 07/26/05 ============================================================================== PAGE CONTENTS ------ ---------------------------------------------------------------- COLUMN SUMMARY 1 UNIT 1, 'T1' 3 TRAY RATES AND DENSITIES 5 STREAM MOLAR COMPONENT RATES 6 STREAM SUMMARY



SIMULATION SCIENCES INC. R PAGE P-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COLUMN SUMMARY 07/26/05 ============================================================================== UNIT 1, 'T1' TOTAL NUMBER OF ITERATIONS IN/OUT METHOD 3 COLUMN SUMMARY ---------- NET FLOW RATES ----------- HEATER TRAY TEMP PRESSURE LIQUID VAPOR FEED PRODUCT DUTIES DEG C BAR KG-MOL/HR M*KCAL/HR ------ ------- -------- -------- -------- --------- --------- ------------ 1C 47.6 16.20 10899.4 1776.8L -38.3190 2 48.8 16.50 10895.5 12676.2 3 49.8 16.51 10726.7 12672.3 4 51.7 16.52 10426.7 12503.5 5 55.3 16.53 9992.8 12203.5 6 61.1 16.54 9530.6 11769.6 7 68.4 16.55 9200.0 11307.4 8 75.6 16.56 9054.2 10976.7 9 81.4 16.57 9031.4 10831.0 10 85.4 16.58 9053.8 10808.2 11 87.8 16.59 13199.0 10830.6 7342.6M 12 88.6 16.60 13218.4 7633.2 13 89.6 16.61 13243.0 7652.6 14 90.8 16.62 13273.6 7677.2 15 92.0 16.63 13311.0 7707.8 16 93.4 16.64 13355.2 7745.2 17 94.8 16.65 13405.7 7789.4 18 96.2 16.66 13461.0 7839.9 19 97.6 16.67 13519.9 7895.2 20 99.0 16.68 13579.4 7954.1 21 100.2 16.69 13637.2 8013.7 22R 101.3 16.70 8071.4 5565.8L 28.1602 FEED AND PRODUCT STREAMS TYPE STREAM PHASE FROM TO LIQUID FLOW RATES HEAT RATES TRAY TRAY FRAC KG-MOL/HR M*KCAL/HR ----- ------------ ------ ---- ---- ------ ------------ ------------ FEED S1 MIXED 11 0.5620 7342.55 33.5075



PROD S2 LIQUID 1 1776.78 2.4950 PROD S3 LIQUID 22 5565.77 20.8536 OVERALL MOLE BALANCE, (FEEDS - PRODUCTS) -7.9936E-12 OVERALL HEAT BALANCE, (H(IN) - H(OUT) ) 8.9387E-05



SIMULATION SCIENCES INC. R PAGE P-2 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COLUMN SUMMARY 07/26/05 ============================================================================== UNIT 1, 'T1' (Cont) SPECIFICATIONS SPECIFICATION PARAMETER TRAY COMP SPECIFICATION SPECIFIED CALCULATED NUMBER TYPE NO NO TYPE VALUE VALUE ------------- --------- ---- ------ ------------- ---------- ---------- 1 (ACTIVE) STRM S2 1 2 WT PERCENT 1.000E+00 1.000E+00 2 (ACTIVE) STRM S3 22 1 WT PERCENT 2.000E+00 2.000E+00 REFLUX RATIOS -------- REFLUX RATIOS -------- MOLAR WEIGHT STD L VOL --------- --------- --------- REFLUX / FEED STREAM S1 1.4844 1.2045 1.3420 REFLUX / LIQUID DISTILLATE 6.1343 6.1343 6.1343



SIMULATION SCIENCES INC. R PAGE P-3 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COLUMN SUMMARY 07/26/05 ============================================================================== UNIT 1, 'T1' (Cont) TRAY NET VAPOR RATES AND DENSITIES --------------- RATES --------------- TRAY MW ACTUAL DENS Z FROM NORMAL ACTUAL KG/M3 DENSITY K*KG/HR K*M3/HR K*M3/HR ---- -------- ------------ -------- ----------- ----------- ----------- 2 44.204 36.45367 0.74741 560.333 284.124 15.371 3 44.345 36.44317 0.74822 561.952 284.037 15.420 4 44.642 36.41043 0.74985 558.177 280.253 15.330 5 45.228 36.38064 0.75244 551.942 273.529 15.171 6 46.258 36.45968 0.75520 544.442 263.804 14.933 7 47.758 36.80700 0.75623 540.014 253.443 14.671 8 49.470 37.44251 0.75444 543.015 246.032 14.503 9 51.000 38.17083 0.75094 552.382 242.766 14.471 10 52.126 38.79028 0.74745 563.394 242.256 14.524 11 52.855 39.23045 0.74481 572.454 242.757 14.592 12 53.111 39.40816 0.74375 405.407 171.090 10.287 13 53.416 39.61896 0.74246 408.777 171.526 10.318 14 53.773 39.86539 0.74093 412.823 172.076 10.355 15 54.178 40.14806 0.73914 417.591 172.763 10.401 16 54.624 40.46479 0.73709 423.075 173.600 10.455 17 55.101 40.81009 0.73483 429.207 174.591 10.517 18 55.594 41.17528 0.73241 435.853 175.723 10.585 19 56.086 41.54870 0.72991 442.811 176.963 10.658 20 56.560 41.91877 0.72740 449.885 178.284 10.732 21 57.002 42.27451 0.72498 456.795 179.618 10.805 22 57.403 42.60685 0.72270 463.322 180.913 10.874



SIMULATION SCIENCES INC. R PAGE P-4 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COLUMN SUMMARY 07/26/05 ============================================================================== UNIT 1, 'T1' (Cont) TRAY NET LIQUID RATES AND DENSITIES --------------- RATES --------------- TRAY MW ACTUAL DENS Z FROM STD LIQ ACTUAL KG/M3 DENSITY K*KG/HR M3/HR M3/HR ---- -------- ------------ -------- ----------- ----------- ----------- 1 44.204 454.920 0.05902 481.793 948.662 1059.073 2 44.368 453.949 0.06024 483.412 949.936 1064.902 3 44.714 454.767 0.06046 479.637 938.558 1054.687 4 45.403 456.349 0.06085 473.402 918.766 1037.368 5 46.624 458.882 0.06149 465.902 891.505 1015.297 6 48.420 461.858 0.06240 461.474 865.666 999.167 7 50.487 464.025 0.06341 464.475 852.732 1000.969 8 52.334 464.707 0.06431 473.841 854.266 1019.657 9 53.685 464.413 0.06497 484.854 863.093 1044.015 10 54.553 463.867 0.06541 493.914 872.299 1064.775 11 55.070 463.398 0.06570 726.866 1277.801 1568.556 12 55.244 463.188 0.06582 730.237 1281.752 1576.544 13 55.447 462.939 0.06596 734.283 1286.552 1586.133 14 55.678 462.647 0.06611 739.051 1292.289 1597.441 15 55.934 462.310 0.06627 744.534 1298.987 1610.466 16 56.208 461.932 0.06644 750.667 1306.592 1625.059 17 56.492 461.520 0.06662 757.313 1314.958 1640.912 18 56.777 461.086 0.06680 764.271 1323.830 1657.544 19 57.053 460.639 0.06697 771.345 1332.978 1674.509 20 57.311 460.204 0.06714 778.255 1342.007 1691.107 21 57.547 459.796 0.06729 784.782 1350.610 1706.805 22 57.757 459.422 0.06744 321.460 552.275 699.705



SIMULATION SCIENCES INC. R PAGE P-5 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM MOLAR COMPONENT RATES 07/26/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED LIQUID LIQUID FLUID RATES, KG-MOL/HR 1 PROPANE 1909.0633 1763.2672 145.7961 2 BUTANE 5433.4878 13.5127 5419.9751 TOTAL RATE, KG-MOL/HR 7342.5511 1776.7799 5565.7712 TEMPERATURE, C 92.8478 47.6030 101.2840 PRESSURE, BAR 18.0000 16.2000 16.7000 ENTHALPY, M*KCAL/HR 33.5075 2.4950 20.8536 MOLECULAR WEIGHT 54.4770 44.2037 57.7566 MOLE FRAC VAPOR 0.4089 0.0000 0.0000 MOLE FRAC LIQUID 0.5911 1.0000 1.0000



SIMULATION SCIENCES INC. R PAGE P-6 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 07/26/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED LIQUID LIQUID ----- TOTAL STREAM ----- RATE, KG-MOL/HR 7342.551 1776.780 5565.771 K*KG/HR 400.000 78.540 321.460 STD LIQ RATE, M3/HR 706.922 154.648 552.275 TEMPERATURE, C 92.848 47.603 101.284 PRESSURE, BAR 18.000 16.200 16.700 MOLECULAR WEIGHT 54.477 44.204 57.757 ENTHALPY, M*KCAL/HR 33.507 2.495 20.854 KCAL/KG 83.769 31.767 64.872 MOLE FRACTION LIQUID 0.5911 1.0000 1.0000 REDUCED TEMP (KAYS RULE) 0.8910 0.8663 0.8837 PRES (KAYS RULE) 0.4596 0.3815 0.4382 ACENTRIC FACTOR 0.1887 0.1533 0.2000 WATSON K (UOPK) 13.751 14.691 13.521 STD LIQ DENSITY, KG/M3 565.833 507.866 582.065 SPECIFIC GRAVITY 0.5664 0.5084 0.5826 API GRAVITY 118.327 146.842 111.360 -------- VAPOR --------- RATE, KG-MOL/HR 3002.482 N/A N/A K*KG/HR 160.002 N/A N/A K*M3/HR 3.683 N/A N/A NORM VAP RATE(1), K*M3/HR 67.298 N/A N/A SPECIFIC GRAVITY (AIR=1.0) 1.840 N/A N/A MOLECULAR WEIGHT 53.290 N/A N/A ENTHALPY, KCAL/KG 119.965 N/A N/A CP, KCAL/KG-C 0.605 N/A N/A DENSITY, KG/K*M3 43449.039 N/A N/A Z (FROM DENSITY) 0.7255 N/A N/A -------- LIQUID -------- RATE, KG-MOL/HR 4340.069 1776.780 5565.771 K*KG/HR 239.998 78.540 321.460 M3/HR 525.730 172.646 699.705 GAL/MIN 2314.717 760.138 3080.705 STD LIQ RATE, M3/HR 421.056 154.648 552.275 SPECIFIC GRAVITY (H2O=1.0) 0.5706 0.5084 0.5826 MOLECULAR WEIGHT 55.298 44.204 57.757 ENTHALPY, KCAL/KG 59.637 31.767 64.872 CP, KCAL/KG-C 0.712 0.715 0.715 DENSITY, KG/M3 456.504 454.920 459.422 Z (FROM DENSITY) 0.0717 0.0590 0.0674 (1) NORMAL VAPOR VOLUME IS 22.414 M3/KG-MOLE (0 C AND 1 ATM)



8.5 Baìi toaïn 5: Xaïc âënh âéa naûp liãûu täúi æu cho thaïp taïch propane bàòng cäng cuû Optimiser

8.5.1 Baìi toaïn




- P = 18 bar


• Thaïp :

- 22 âéa lyï thuyãút








- saín pháøm âènh : coï 0,5% khäúi læåüng C4

- saín pháøm âaïy : coï 0,5% khäúi læåüng C3

⇒ Haîy xaïc âënh âéa naûp liãûu täúi æu âãø nàng suáút cuía thiãút bë âun säi laûi laì beï nháút

8.5.2 Sæí duûng cäng cuû Optimiser

• Optimiser laì mäüt cäng cuû ráút tiãûn êch cuía PRO/II nhàòm cæûc âaûi hoàûc cæûc tiãøu hoïa mäüt haìm muûc tiãu naìo âoï bàòng caïch thay âäøi giaï trë cuía mäüt biãún naìo âoï trong säú caïc tiãu chuáøn âæa ra

• Haìm muûc tiãu coï thãø laì nàng suáút, cäng suáút hoàûc haìm kinh tãú nhæ haìm giaï caí hoàûc haìm chi phê. Vç váûy tuyì theo træåìng håüp maì seî täúi æu haìm muûc tiãu âãún giaï trë cæûc âaûi hoàûc cæûc tiãøu

• Biãún seî thay âäøi giaï trë trong mäüt khoaíng naìo âoï (giæîa Minimum Value vaì Maximum Value) âãø haìm muûc tiãu âaût âãún giaï trë cæûc âaûi hoàûc cæûc tiãøu



8.5.3 Giaíi quyãút baìi toaïn

• Chuïng ta seî tiãún haình mä phoíng baìi toaïn nhæ baìi toaïn træåïc, sau âoï seî caìi âàût thãm thiãút bë Optimiser OP1 cho thaïp ⇒ OP1 âæåüc viãön âoí

• Double-click vaìo OP1 ⇒ hiãøn thë cæía säø PRO/II - Optimiser

• ÅÍ muûc Description nháûp tãn OPTIMISER

• Goüi cäng cuû Optimiser våïi:

o Haìm muûc tiãu: Nàng suáút cuía thiãút bë âun säi laûi

o Loaûi baìi toaïn: Cæûc tiãøu (minimize)

o Biãún: Vë trê âéa naûp liãûu, biãún thiãn tæì âéa thæï 2 âãún âéa thæï 21

• ÅÍ muûc Objective ⇒ Choün Minimize

• ÅÍ muûc Objective Function ⇒ Nhàõp choün Parameter ⇒ hiãøn thë cæía säø Parameter ⇒ ÅÍ muûc Stream/Units ⇒ Choün Column ⇒ Nhàõp choün Parameter ⇒ hiãøn thë cæía säø Parameter Selection ⇒ ÅÍ muûc Parameter choün Heat Duty ⇒ ÅÍ muûc Heater choün Reboiler ⇒ OK : tråí vãö cæía säø Parameter ⇒ OK : tråí vãö cæía säø PRO/II - Optimiser

• ÅÍ muûc Variables ⇒ Nhàõp choün Parameter ⇒ hiãøn thë cæía säø Parameter ⇒ ÅÍ muûc Stream/Units ⇒ Choün Column ⇒ Nhàõp choün Parameter ⇒ hiãøn thë cæía säø Parameter Selection ⇒ ÅÍ muûc Parameter choün Tray Location ⇒ ÅÍ muûc Tray Location choün Feed ⇒ ÅÍ muûc Feed Stream choün S1 ⇒ OK : tråí vãö cæía säø Parameter ⇒ OK : tråí vãö cæía säø PRO/II - Optimiser

• Tiãúp tuûc åí muûc Variables ⇒ nháûp giaï trë 2 cho muûc Minimum Value vaì giaï trë 22 cho muûc Maximum Value ⇒ nhàõp OK : hoaìn thaình viãûc nháûp dæî liãûu cho OP1



8.5.4 Tiãún haình mä phoíng vaì xem kãút quaí

8.6 Baìi toaïn 6: Xaïc âënh säú âéa lyï thuyãút täúi thiãøu vaì chè säú häöi læu täúi thiãøu cho thaïp taïch propane bàòng phæång phaïp shortcut

8.6.1 Baìi toaïn




- P = 18 bar


• Thaïp :








- saín pháøm âènh : coï 0,5% khäúi læåüng C4

- saín pháøm âaïy : coï 0,5% khäúi læåüng C3

⇒ Haîy xaïc âënh :

- Säú âéa lyï thuyãút täúi thiãøu?

- Chè säú häöi læu täúi thiãøu?



8.6.2 Tiãún haình mä phoíng vaì xem kãút quaí $ Generated by PRO/II Keyword Generation System <version 7.0> $ Generated on: Mon Aug 15 18:33:48 2005 TITLE DIMENSION METRIC, PRES=BAR, TIME=DAY, STDTEMP=0, STDPRES=1.01325 SEQUENCE SIMSCI CALCULATION RVPBASIS=APIN, TVP=37.778 COMPONENT DATA LIBID 1,PROPANE/2,BUTANE, BANK=PROCESS,SIMSCI THERMODYNAMIC DATA METHOD SYSTEM=GS, SET=GS01, DEFAULT STREAM DATA PROPERTY STREAM=S1, PRESSURE=18, PHASE=M, LFRACTION(WT)=0.6, & RATE(WT)=400000, COMPOSITION(M)=1,26/2,74 UNIT OPERATIONS SHORTCUT UID=SCD1 FEED S1 PRODUCT STREAM=S2, RATE(WT)=1E5, PHASE=L, PRESSURE=16.2 PRODUCT STREAM=S3, PHASE=L, DP=0 CONDENSER TYPE=BUBB EVALUATE MODEL=CONV, TRIAL=50, KEYLIGHT=1, KEYHEAVY=2, RRMIN=2 FINDEX 2 SPEC STREAM=S2,PCT(WT), COMP=2,WET, VALUE=0.5 SPEC STREAM=S3,PCT(WT), COMP=1,WET, VALUE=0.5 END



SIMULATION SCIENCES INC. R PAGE H-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM CALCULATION HISTORY 08/15/05 ============================================================================== *** PROBLEM SOLUTION BEGINS FEED FLASH COMPLETE UNIT 1 SOLVED - 'SCD1 ' *** PROBLEM SOLUTION REACHED *** THIS RUN USED 20.71 PRO/II SIMULATION UNITS *** RUN STATISTICS STARTED 18:33:32 08/15/05 NO ERRORS FINISHED 18:33:33 08/15/05 NO WARNINGS RUN TIMES NO MESSAGES INTERACTIVE 0 MIN, 0.00 SEC CALCULATIONS 0 MIN, 0.12 SEC TOTAL 0 MIN, 0.12 SEC



SIMULATION SCIENCES INC. R PAGE I-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT INDEX 08/15/05 ============================================================================== PAGE CONTENTS ------ ---------------------------------------------------------------- 1 COMPONENT DATA 2 CALCULATION SEQUENCE AND RECYCLES SHORTCUT COLUMN SUMMARY 3 UNIT 1, 'SCD1' 4 STREAM MOLAR COMPONENT RATES 5 STREAM SUMMARY



SIMULATION SCIENCES INC. R PAGE P-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COMPONENT DATA 08/15/05 ============================================================================== COMPONENT COMP. TYPE PHASE MOL. WEIGHT DENSITY KG/M3 --------------------- ----------- ----------- ----------- ----------- 1 PROPANE LIBRARY VAP/LIQ 44.097 507.199 2 BUTANE LIBRARY VAP/LIQ 58.124 583.824 COMPONENT NBP CRIT. TEMP. CRIT. PRES. CRIT. VOLM. C C BAR M3/KG-MOL --------------------- ----------- ----------- ----------- ----------- 1 PROPANE -42.070 96.670 42.496 0.2030 2 BUTANE -0.500 152.000 37.997 0.2550 COMPONENT ACEN. FACT. HEAT FORM. G FORM. KCAL/KG-MOL KCAL/KG-MOL --------------------- ----------- ----------- ----------- 1 PROPANE 0.15290 -24805.58 -5633.13 2 BUTANE 0.20130 -30040.13 -3982.90



SIMULATION SCIENCES INC. R PAGE P-2 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT CALCULATION SEQUENCE AND RECYCLES 08/15/05 ============================================================================== CALCULATION SEQUENCE SEQ UNIT ID UNIT TYPE --- ------------ ---------- 1 SCD1 SHORTCUT



SIMULATION SCIENCES INC. R PAGE P-3 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT SHORTCUT COLUMN SUMMARY 08/15/05 ============================================================================== UNIT 1, 'SCD1' FEEDS STREAM PHASE ------------ ------ S1 MIXED PRODUCTS ------------- TOTAL STREAM RATES ------------- MOLES WEIGHT LIQUID VOL NORM VAPOR(1) NUM STREAM + PHASE KG-MOL/DAY KG/DAY M3/DAY M3/DAY SECTION TRAYS ------ ------ - ---------- ---------- ---------- ---------- ------- ----- S2 L 1880.26 83014.05 163.56 42144.15 1 13.60 S3 L 5462.28 316985.62 543.36 122431.59 TOTALS 7342.54 399999.66 706.92 164575.74 13.60 SPECIFICATIONS PARAMETER COMP. SPECIFICATION SPECIFIED CALCULATED TYPE NUM TYPE VALUE VALUE ----------------- ------- ------------- ---------- ---------- STRM S2 2 WT PERCENT 5.000E-01 5.001E-01 STRM S3 1 WT PERCENT 5.000E-01 5.000E-01 SUMMARY OF UNDERWOOD CALCULATIONS MINIMUM REFLUX RATIO 3.95841 FEED CONDITION Q 0.59108 FENSKE MINIMUM TRAYS 13.60067 OPERATING REFLUX RATIO 2.00 * R-MINIMUM TOTAL FEED R/R-MIN M/M-MIN REFLUX DUTY, M*KCAL/DAY TRAYS TRAY RATIO CONDENSER REBOILER ----- ---- ------- ------- ------ ---------- ---------- 23 15 1.500 1.657 5.938 -3.924E+01 2.891E+01 21 14 1.750 1.526 6.927 -4.484E+01 3.450E+01 20 13 2.000 1.437 7.917 -5.044E+01 4.010E+01 19 12 2.250 1.372 8.906 -5.604E+01 4.570E+01 18 12 2.500 1.323 9.896 -6.164E+01 5.130E+01 (1) NORMAL VAPOR VOLUME IS 22.414 M3/KG-MOLE (0 C AND 1 ATM)



SIMULATION SCIENCES INC. R PAGE P-4 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM MOLAR COMPONENT RATES 08/15/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED LIQUID LIQUID FLUID RATES, KG-MOL/DAY 1 PROPANE 1909.0616 1873.1184 35.9433 2 BUTANE 5433.4831 7.1424 5426.3407 TOTAL RATE, KG-MOL/DAY 7342.5447 1880.2608 5462.2839 TEMPERATURE, C 92.8478 47.4612 101.2441 PRESSURE, BAR 18.0000 16.2000 16.2000 ENTHALPY, M*KCAL/DAY 33.5076 2.6303 20.5389 MOLECULAR WEIGHT 54.4770 44.1503 58.0317 MOLE FRAC VAPOR 0.4089 0.0000 0.0000 MOLE FRAC LIQUID 0.5911 1.0000 1.0000



SIMULATION SCIENCES INC. R PAGE P-5 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 08/15/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED LIQUID LIQUID ----- TOTAL STREAM ----- RATE, KG-MOL/DAY 7342.545 1880.261 5462.284 K*KG/DAY 400.000 83.014 316.986 STD LIQ RATE, M3/DAY 706.922 163.564 543.358 TEMPERATURE, C 92.848 47.461 101.244 PRESSURE, BAR 18.000 16.200 16.200 MOLECULAR WEIGHT 54.477 44.150 58.032 ENTHALPY, M*KCAL/DAY 33.508 2.630 20.539 KCAL/KG 83.768 31.685 64.794 MOLE FRACTION LIQUID 0.5911 1.0000 1.0000 REDUCED TEMP (KAYS RULE) 0.8910 0.8664 0.8814 PRES (KAYS RULE) 0.4596 0.3814 0.4260 ACENTRIC FACTOR 0.1887 0.1531 0.2010 WATSON K (UOPK) 13.751 14.697 13.503 STD LIQ DENSITY, KG/M3 565.833 507.533 583.383 SPECIFIC GRAVITY 0.5664 0.5080 0.5840 API GRAVITY 118.327 147.025 110.812 -------- VAPOR --------- RATE, KG-MOL/DAY 3002.440 N/A N/A K*KG/DAY 160.000 N/A N/A K*M3/DAY 3.682 N/A N/A NORM VAP RATE(1), K*M3/DAY 67.297 N/A N/A SPECIFIC GRAVITY (AIR=1.0) 1.840 N/A N/A MOLECULAR WEIGHT 53.290 N/A N/A ENTHALPY, KCAL/KG 119.965 N/A N/A CP, KCAL/KG-C 0.605 N/A N/A DENSITY, KG/K*M3 43449.017 N/A N/A Z (FROM DENSITY) 0.7255 N/A N/A -------- LIQUID -------- RATE, KG-MOL/DAY 4340.105 1880.261 5462.284 K*KG/DAY 240.000 83.014 316.986 M3/DAY 525.734 182.536 687.057 GAL/MIN 96.447 33.487 126.042 STD LIQ RATE, M3/DAY 421.060 163.564 543.358 SPECIFIC GRAVITY (H2O=1.0) 0.5706 0.5080 0.5840 MOLECULAR WEIGHT 55.298 44.150 58.032 ENTHALPY, KCAL/KG 59.637 31.685 64.794 CP, KCAL/KG-C 0.712 0.715 0.715 DENSITY, KG/M3 456.504 454.782 461.367 Z (FROM DENSITY) 0.0717 0.0590 0.0655 (1) NORMAL VAPOR VOLUME IS 22.414 M3/KG-MOLE (0 C AND 1 ATM)

Tæì kãút quaí P-3 cuía Programme file: MINIMUM REFLUX RATIO 3.95841

FENSKE MINIMUM TRAYS 13.60067

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