Giao-Trinh Thiet Ke Mo Phong

Thit k m phong 1/1

MUC LUC 1 Gii thiu tng quan ................................................................................................3

1.1 Muc ch, vai tro cua thit k m phong.........................................................3 1.2 Cac phn mm m phong trong cng ngh hoa hoc .......................................4

2 Phn mm PRO/II....................................................................................................4 2.1 Lnh vc s dung .............................................................................................4 2.2 Qua trnh m phong bng phn mm PRO/II..................................................5

3 Cac khai nim c ban v chng ct .........................................................................5 3.1 Thit b ngng tu nh thap .............................................................................5 3.2 Thit b un si ay thap .................................................................................6

4 Ly thuyt nhit ng hoc .........................................................................................8 4.1 Phng phap phng trnh trang thai ..............................................................8

4.1.1 Phng trnh bc ba tng quat .....................................................................9 4.1.2 Phng trnh Soave-Redlich-Kwong...........................................................9

5 La chon m hnh nhit ng................................................................................10 5.1 C s la chon ...............................................................................................10 5.2 Cac ng dung cu th ......................................................................................13

5.2.1 Cac qua trnh loc du va ch bin kh .......................................................13 5.2.2 Cac qua trnh hoa du ................................................................................13

6 Cac phn c ban cua PROII...................................................................................14 6.1 Giao din cua PROII .....................................................................................14

6.1.1 Qui c ban u.........................................................................................14 6.1.2 Ca s PRO/II............................................................................................15

7 Cac thao tac thng dung trong m phong bng PRO/II ......................................16 7.1 M mt chng trnh m phong mi (Opening a New Simulation) .............16 7.2 M mt chng trnh m phong a co (Opening an Existing Simulation) ...16 7.3 Ghi mt file m phong ang hin hanh (Saving the Current Simulation) ....16

7.3.1 Ghi mt file m phong ang hin hanh.....................................................16 7.3.2 Ghi mt file m phong vi mt tn khac...................................................17

7.4 Xoa mt chng trnh m phong (Deleting a Simulation)............................17 7.5 Sao chep mt chng trnh m phong (Copy a Simulation) .........................17 7.6 Thay i dang ng vin cac dong (Modifying the Flowsheet Stream Border Style)..............................................................................................................17 7.7 Hin th tnh cht cua dong trn s m phong..........................................18 7.8 S dung Flash Hot-Key Tool.........................................................................19 7.9 Xut mt s m phong ra ca s lu tr tam (Exporting the PFD to the Windows Clipboard) .................................................................................................19

ThS. L Th Nh Y ai Hoc Bach Khoa

Thit k m phong 2/2

7.10 Nhp mt file PRO/II co sn (Importing a PRO/II Keyword Input File) .....20 7.11 Xac nh cac tnh cht v cn bng long - hi cua cac h 2 cu t (Display BVLE) 20

8 BAI TP AP DUNG.............................................................................................22 8.1 Bai toan 1: M phong s cng ngh cua phn xng tach Methane........22

8.1.1 Phng phap tin hanh ..............................................................................23 8.1.2 M phong vung 1.......................................................................................23

8.2 Bai toan 2: M phong thit b tach kh - long ...............................................61 8.2.1 Bai toan......................................................................................................61 8.2.2 Kt qua: .....................................................................................................62

8.3 Bai toan 3: Tnh nhit si cua mt hn hp hai pha mt ap sut nht nh 70

8.3.1 Bai toan......................................................................................................70 8.3.2 Giai quyt bai toan.....................................................................................70 8.3.3 S bai toan ............................................................................................70 8.3.4 Kt qua: .....................................................................................................71

8.4 Bai toan 4: M phong thap tach propane ......................................................78 8.4.1 Bai toan......................................................................................................78 8.4.2 S bai toan ............................................................................................79 8.4.3 Cac bc m phong ...................................................................................79

8.5 Bai toan 5: Xac nh a nap liu ti u cho thap tach propane bng cng cu Optimiser ...................................................................................................................92

8.5.1 Bai toan......................................................................................................92 8.5.2 S dung cng cu Optimiser .......................................................................93 8.5.3 Giai quyt bai toan.....................................................................................94 8.5.4 Tin hanh m phong va xem kt qua ........................................................95

8.6 Bai toan 6: Xac nh s a ly thuyt ti thiu va ch s hi lu ti thiu cho thap tach propane bng phng phap shortcut ..........................................................95

8.6.1 Bai toan......................................................................................................95 8.6.2 Tin hanh m phong va xem kt qua ........................................................97


Thit k m phong 3/3

1 Gii thiu tng quan 1.1 Muc ch, vai tro cua thit k m phong Thit k m phong la qua trnh thit k vi s tr giup cua may tnh vi cac phn

mm chuyn nghip

Cac t khoa thng c s dung trong thit k m phong la : - Simulation, process simulation : m phong, qua trnh m phong

- Dynamic simulation : m phong ng

- Simulator : thit b m phong

- Equation of state (EOS) : phng trnh trang thai

- Steady-state simulation : m phong trang thai bn vng

- To proceed by trial and error : Tin hanh bng cach mo mm

- Model : m hnh

- Modelling : m hnh hoa

M phong la mt cng cu cho phep ngi ky s tin hanh cng vic mt cach hiu qua hn khi thit k mt qua trnh mi hoc phn tch, nghin cu cac yu t anh hng dn mt qua trnh ang hoat ng trong thc t.

Tc cua cng cu m phong cho phep khao sat nhiu trng hp hn trong cung thi gian vi chnh xac cao hn nu so vi tnh toan bng tay. Hn na, chung ta co th t ng hoa qua trnh tnh toan cac s cng ngh tranh vic phai thc hin cac phep tnh lp khng co c s hoc mo mm. V du, chung ta co th s dung mt m hnh mu nghin cu s vn hanh cua mt phn xng khi thay i ngun nguyn liu hoc cac iu kin vn hanh cua cac thit b anh hng n hiu sut thu va cht lng san phm nh th nao ? iu nay se n gian, nhanh chong va tit kim hn nhiu so vi th trn phn xng thc t. V rng c s tnh toan cac cng cu m phong thng da trn cac b c s d liu chun hoa, nn mt khi a xy dng mt m hnh hp ly th bt ky mt ky s nao cung co th s dung no tnh toan va cho cac kt qua chnh xac.

Thit k m phong thng c s dung : - Thit k (Designing) mt qua trnh mi

- Th lai, kim tra lai (Retrofitting) cac qua trnh ang tn tai

- Hiu chnh (Troubleshooting) cac qua trnh ang vn hanh

- Ti u hoa (Optimizing) cac qua trnh vn hanh


Thit k m phong 4/4

xy dng mt m hnh m phong hiu qua, chung ta phai xac nh ung muc tiu. Bc u tin trong bt c mt qua trnh m phong nao la lng hoa cac muc tiu cang nhiu cang tt. Cac kt qua at c thng phu thuc vao cac yu cu t ra. Nh vy, trc khi m phong mt qua trnh nn t ra cac cu hoi sau :

- Muc ch s dung cng cu m phong trong trng hp nay lam g ?

- Qua trnh m phong se thc hin nhng vic g ?

- S phc tap co cn thit khng ?

- Cn thit phai tm ra cac kt qua nao t qua trnh m phong ?

Cn nh rng cac gia tr thu c t kt qua m phong phu thuc rt nhiu vao nhng la chon ban u ma chung ta a nhp vao.

1.2 Cac phn mm m phong trong cng ngh hoa hoc Trong cng ngh hoa hoc, ngi ta s dung rt nhiu cac phn mm m phong :

- DESIGN II (WINSIM) : s dung trong cng nghip hoa hoc noi chung

- PRO/II (SIMSCI) : s dung trong cng nghip hoa hoc, cng nghip loc - hoa du

- PROSIM : s dung trong cng nghip hoa hoc

- HYSIM (HYSYS) : s dung trong cng nghip ch bin kh

Trong cac phn mm k trn, phn mm PRO/II la phn mm ni ting nht, c s dung rng rai nht trong nhiu lnh vc cng nghip.

2 Phn mm PRO/II 2.1 Lnh vc s dung Phn mm PRO/II la phn mm tnh toan chuyn dung trong cac lnh vc cng

ngh hoa hoc noi chung, c bit trong lnh vc loc du, hoa du, polymer, hoa dc, ... y la phn mm tnh toan rt chnh xac cac qua trnh chng ct. La san phm cua SIMSCI, hnh thanh t nm 1967 va c chnh thc s dung vao nm 1988 sau nhiu ln c cai tin. Hin nay, chung ta ang s dung phin ban PRO/II 7.0

PRO/II vn hanh theo cac modul lin tip, mi thit b c tnh ring le va ln lt tnh cho tng thit b.

PRO/II bao gm cac ngun d liu phong phu : th vin cac cu t hoa hoc, cac phng phap xac nh cac tnh cht nhit ng, cac ky xao vn hanh cac thit b hin ai cung cp cho cac ky s cng ngh cac ky nng biu din tt ca cac


Thit k m phong 5/5

tnh toan cn bng vt cht va nng lng cn thit khi m phong cac trang thai dng cua cac s cng ngh.

Phn mm PRO/II c s dung theo nhm 2 muc ch : - Thit k mt phn xng mi (Sizing)

- M phong mt phn xng a c xy dng trong thc t nghin cu cac yu t anh hng n s vn hanh cua no (Rating) nh : thay i ngun nguyn liu, iu kin vn hanh hoc tiu chun ky thut cua san phm, ...

2.2 Qua trnh m phong bng phn mm PRO/II Trc khi tin hanh m phong, chung ta phai din at cac d liu t s thc t

thanh m hnh m phong. Qua trnh nay bao gm cac bc sau :

- Xac nh h n v o : co 3 h n v o : h Anh, h Met va h SI. Tuy trng hp, chung ta chon h n v o cho thch hp, thng thng chon h Met;

- Xac nh thanh phn cu t co trong h : c chon t ngun d liu phong phu cac cu t cua PROII;

- La chon cac phng trnh nhit ng thch hp : trn c s thanh phn hoa hoc cua nguyn liu va iu kin vn hanh cua thit b ;

- La chon cac dong nguyn liu va san phm : xac nh thanh phn, trang thai nhit cua cac dong;

- Xac nh cac d liu v thit b va iu kin vn hanh cho cac thit b.

Hn na, trong nhiu trng hp chung ta phai thay i s cng ngh thc t sang muc ch m phong. Mc du co s tng ng gia s cng ngh thc t va s m phong nhng vn co nhng s khac bit cn chu y.

V cng cu m phong ch m ta trang thai dng nn trong s m phong khng nn b tr cac thit b iu khin, kim tra

3 Cac khai nim c ban v chng ct 3.1 Thit b ngng tu nh thap PRO/II mc nh Condenser c xem la mt bc thay i nng (mt a ly thuyt) va co 4 dang Condenser :

Partial : Long a 2 c lam lanh va ch ngng tu mt phn. Loai Condenser nay thc s la mt bc thay i nng . Nhit trong Condenser chnh la nhit im sng cua hn hp hi cn bng Gm 2 loai :


Thit k m phong 6/6

- loai Distillat vapor : long ngng tu ch hi lu v nh thap, con san phm ly ra th hi c goi la Overhead.

- Loai Distillat mixe : long ngng tu mt phn hi lu v nh thap, con lai ly ra lam san phm san phm nh gm 2 loai la san phm hi va san phm long.

Bubble Temperature : Long a 2 c c lam lanh n nhit im si cua hn hp va ngng tu hoan toan, mt phn cho hi lu v a 2 nh thap, phn con lai ly ra dang san phm long, c goi la Fixe Rate Draw. Nhit trong Condenser chnh la nhit im si cua hn hp long cn bng

- Subcooled, Fixe Temperature : Long a 2 c c lam lanh di nhit im si cua hn hp long. Long nay goi la long qua lanh.

- Subcooled, Fixe Temperature Drop : Loai Condenser nay cung ging nh loai trn nhng qua lanh cua hn hp long c xac nh bi mt gia tr nao o.

LongLong

HiHi

a- Dang Partial

Distillate vapor Distillate mixe

b- Dang Bubble

3.2 Thit b un si ay thap PRO/II mc nh Reboiler c xem la mt bc thay i nng va co 3 dang Reboiler :

- Dang Kettle : c mc nh (qui chun)

- Thermosiphon without baffles

- Thermosiphon with baffles


Thit k m phong 7/7


Thit k m phong 8/8

210

300

?

?

?

?

50

4 Ly thuyt nhit ng hoc Cac tnh cht nhit ng la c s d liu quan trong nht cho vic tnh toan qua

trnh phn tach toan h thng.

Co nhiu phng phap tnh toan cac tnh cht nay, trong o, quan trong nht la 2 phng phap :

- Phng phap tng quan : API va Rackett

- Phng phap phng trnh trang thai : phng trnh bc ba tng quat, cng thc Alpha, cac qui lut hn hp, phng trnh SRK, phng trnh PR, phng trnh SRKP, SRKM, SRKS, ...

Phng phap API va Rackett tnh toan kha chnh xac t trong cua pha long, con cac tnh cht nhit ng khac nh : enthalpie, entropie long va hi, t trong pha hi, ... th c tnh toan rt chnh xac bng cac phng trnh trang thai nh : SRK, SRKM, ...

4.1 Phng phap phng trnh trang thai Phng phap tnh cn bng pha nay co th ap dung trong mt khoang rng nhit

va ap sut. Ngoai ra, con tnh toan cac tnh cht nhit ng nh Enthalpie va Entropie. Trang thai tham khao cho ca hai pha long-hi la kh ly tng, cac chnh lch


Thit k m phong 9/9

cua h thc so vi h ly tng c xac nh bng cach tnh h s hoat ap cho ca hai pha.

Cu th i vi cac phng trnh trang thai bc ba, cac iu kin ti han va qua ti han c tnh toan kha chnh xac. Bng cach s dung mt ham theo nhit biu din lc hp dn gia cac phn t, ham th tch, quy lut hn hp, cac phng trnh trang thai bc ba a c vn dung kha thanh cng tnh cn bng long - hi cac h phi ly tng ln.

4.1.1 Phng trnh bc ba tng quat Phng trnh gm 2 tham s a va b c biu din di dang sau :

( ) 22 wbubvvTa

bvRTP ++=

Trong o : P : ap sut

T : nhit tuyt i

v : th tch mol

u, w : hng s, dang s nguyn

Cac gia tr cua u va w se xac nh dang cua phng trnh trang thai bc ba nh bang di y :

u w Phng trnh trang thai

0

1

2

0

0

-1

Van der Waals (vdW)

Redlich-Kwrong (RK)

Peng-Robinson (PR)

4.1.2 Phng trnh Soave-Redlich-Kwong n nm 1972, cai thin tnh chnh xac khi tnh ap sut hi cua cu t tinh khit va tnh cn bng long - hi cua h a cu t, Soave a xac nh : ( ) ( ) ( )cTaTTa .= ( ) ( )[ ]221rT1M1T /+= 217605741480M += ,,,Trong o :

a (T) : h s phu thuc vao nhit


Thit k m phong 10/10

(T) : ham phu thuc vao nhit , c trng cho lc hp dn gia cac phn t Tc : nhit ti han

Acentrics hng:

gon rut nhit :

=

cr T

TT

5 La chon m hnh nhit ng 5.1 C s la chon La chon m hnh nhit ng thch hp cho mt ng dung cu th ong mt vai tro

rt quan trong, anh hng ln n chnh xac cua kt qua m phong

Mi phng phap nhit ng cho phep tnh cac thng s sau : - Hng s cn bng pha K : th hin s phn b cu t gia cac pha iu kin

cn bng

- Enthapie cua cac pha long va pha hi : xac nh nng lng cn thit chuyn mt h t trang thai nhit ng nay sang trang thai khac

- Enthapie cua cac pha long va pha hi : nhm phuc vu vic tnh toan cac may nen, thit b gian n va nng lng t do ti thiu cac thit b phan ng

- T trong cua pha long va pha hi : tnh toan qua trnh truyn nhit, tr lc va xac nh kch thc thap chng ct

la chon m hnh nhit ng thch hp, nn da vao cac yu t sau : - Ban cht cua cac c trng nhit ng cua h nh : Hng s cn bng long-

hi (VLE : Vapor Liquid Equilibrium) cua cac qua trnh chng ct, c c hoc bc hi, qua trnh trch ly, ...

- Thanh phn cua hn hp

- Pham vi nhit va ap sut

- Tnh sn co cua cac thng s hoat ng cua cac thit b

Cu th, ta co th da vao s sau :



5.2 Cac ng dung cu th

5.2.1 Cac qua trnh loc du va ch bin kh H thng ap sut thp (thap chng ct ap sut kh quyn va chn khng) : Trong

nguyn liu cua cac h thng nay noi chung co khoang 3 % th tch phn nhe co th chon m hnh BK10 hoc GS va cac bin th cua no. Khi ham lng phn nhe ln (nht la thanh phn C1) nn chon EOS: SRK, PR

H thng ap sut cao (thap chng phn oan san phm cua phn xng cracking, cc hoa, ...) Trong h thng nay, ham lng phn nhe noi chung ln hn Cac m hnh nn chon : GS, SRK, PR

Cac qua trnh ch bin kh thin nhin : trong thanh phn thng co cha N2, kh acide (CO2, H2S) va cac hydrocarbon nhe :

- Vi loai kh cha t hn 5% N2, CO2, H2S va khng co cu t phn cc nao khac nn chon SRK, PR hoc Benedict - Webb - Rubin - Starling (BWRS)

- Vi loai kh cha nhiu hn 5% N2, CO2, H2S nhng khng co cu t phn cc nao khac nn chon SRK, PR va ngi s dung nn a vao cac thng s tng tac thu c kt qua tt hn

- Vi h thng x ly kh thin nhin co ln nc lam vic ap sut cao (trong trng hp nay hoa tan cua hydrocarbon trong ncse tng ln) nn chon cac bin th cua cac phng trnh trang thai nh : SRKM, PRM hay SRKS, SRKKD (Kabadi - Danner Modification to SRK)

- Khi kh thin nhin cha cac cu t phn cc nh methanol SRKM, PRM hay SRKS

5.2.2 Cac qua trnh hoa du Qua trnh x ly hydrocarbon nhe :

- ap sut thp : SRK, PR

- ap sut cao : SRKKD

x ly hydrocarbon thm : - P < 2 bars : IDEAL

- P > 2 bars : GS, SRK, PR

X ly hn hp hydrocarbon thm va hydrocarbon khac : NRTL, UNIQUAC, UNIFAC



6 Cac phn c ban cua PROII 6.1 Giao din cua PROII

6.1.1 Qui c ban u Khi khi ng PROII, u tin se xut hin mt ca s giao din qui c ban u nh sau:

Cac nut hoc cac biu tng trong mt vai trng hp c vin quanh bi 1 trong 6 mau sau : o, xanh luc, xanh dng, vang, nu va en. Y ngha cua mi mau nh sau :

o : d liu yu cu cn phai nhp Xanh luc : d liu mc nh hoc la chon Xanh dng : d liu ban va cung cp thoa man yu cu Vang : bao rng s liu ban va nhp ngoai khoang cho phep Nu : d liu khng co gia tr en : d liu khng yu cu nhp vao ThS. L Th Nh Y ai Hoc Bach Khoa


6.1.2 Ca s PRO/II

T File menu Chon New : mt ca s View1 se xut hin cho chung ta mt flowsheet mi nh sau:

Man hnh bao gm :

Dong trn cung goi la Application Title Bar (Thanh tiu ng dung), o co tn cua ng dung la PRO/II with PROVISION, kem theo la Document Title Bar (Thanh tiu tai liu) o co tn cua chng trnh m phong ang thc hin (chng han la View 1 - la tn nguyn cua tai liu khi mi khi ng PRO/II)

Dong th hai goi la Menu Bar (Thanh trnh n) gm 10 muc t File n Help ; Dong th ba goi la Standard Tool Bar (Thanh cng cu chun) cha biu tng

cua cac lnh thng dung

Bn phai va pha di man hnh la thanh trt doc va thanh trt ngang Bn phai man hnh, bn ngoai thanh trt doc la thanh cng cu floating PFD (Pipe

Flow Diagram). Nu thanh cng cu PFD khng hin th th ta co th goi no nh sau :

- click vao biu tng Show or Hide PFD Palette trn Standard Tool Bar

- hoc t View Palettes nhp chon (hoc khng) PFD Ngoai ra con co thanh cng cu Run. lam xut hin hoc bin mt thanh cng cu

nay cung t View Palettes nhp chon (hoc khng) Run



7 Cac thao tac thng dung trong m phong bng PRO/II

7.1 M mt chng trnh m phong mi (Opening a New Simulation)

T File Menu New Nu ban mun PRO/II lun lun c m vi mt chng trnh m phong mi

Options Menu New File on Startup 7.2 M mt chng trnh m phong a co (Opening an

Existing Simulation) Ban co th m bt ky mt chng trnh m phong nao a c ghi trc o chnh sa, xem hoc in. Qui trnh :

T File Menu Open hin th ca s Open Simulation . anh tn chng trnh vao hoc chon tn file m phong OK hoc Enter hin th file Simulation cn thit 7.3 Ghi mt file m phong ang hin hanh (Saving the

Current Simulation)

7.3.1 Ghi mt file m phong ang hin hanh

T File Menu Save nu ban cha ghi chng trnh m phong nay ln nao th se hin th ca s Save as nhp tn Chon OK hoc nhp Enter. Con sau ln ghi u tin, mun ghi lai file ang hin hanh nhp vao biu tng Save

Chng trnh PRO/II se t ng nen 3 file d liu (*.pr1, .pr2, .pr3) va 1 file flowsheet biu cac dong (*.sfd) thanh mt file n *.prz. V vy, bn canh vic giam kch thc cua cac file lu tr con am bao rng vic cai t file a hoan thanh mi khi chung ta ghi cac chng trnh m phong

Chc nng Autosave cua PRO/II se t ng tao mt file sao chep d phong (backup file). Nu ban ong hoc thoat ra chng trnh m phong ma khng ghi th file nay se b xoa. Hay chon Options / simulation Defaults / Autosave t menu bar hin th ca s Autosave Options nhp chon Automatic Save File every nhp chu ky save (phut) OK



7.3.2 Ghi mt file m phong vi mt tn khac

T File Menu chon Save as hin th ca s Save as Nhp tn mi cho chng trnh m phong Chon OK hoc nhp Enter 7.4 Xoa mt chng trnh m phong (Deleting a

Simulation) T File Menu chon Delete PRO/II se hin th mt danh sach cac file m

phong a co

Nhp hoc chon tn cua flie mun xoa (Ban khng th xoa mt chng trnh m phong ang hin hanh)

Chon OK hoc nhp Enter PRO/II se xoa tt ca cac file lin kt vi chng trnh m phong nay

7.5 Sao chep mt chng trnh m phong (Copy a Simulation)

PRO/II co th copy tt ca cac file lin kt vi chng trnh m phong (3 file d liu va 1 flowsheet) vao mt file m phong mi hoc ang hin hanh. Nu ban mun copy vao mt file m phong ang hin hanh PRO/II se hoi ban co mun vit e ln file hin hanh nay khng ?

T File Menu chon Copy PRO/II se hin th ca s Select File to Copy Hay chon tn file cn copy (Ban khng th copy mt chng trnh m phong ang hin hanh) Nhp tn file ch (target) OK

7.6 Thay i dang ng vin cac dong (Modifying the Flowsheet Stream Border Style)

Thng thng ng vin cac dong thng co dang hnh ch nht Chung ta co th thay i thanh ng vin dang tron. Qui trnh nh sau :

- Right-click vao dong c chon hin th ca s la chon - Chon Display xut hin ca s Stream Style - Chon Circle t drop-down list box cua Stream Label Border

- click OK ng vin dong c chon t dang hnh ch nht chuyn thanh ng vin dang tron

Vi cach nh trn, ban co th thay i dang ng vin cho tng dong ring le. Con nu mun, ban co th click chut trai va quet chon mt hnh ch nht bao



xung quanh cac dong mun thay i dang ng vin ri tin hanh qui trnh nh trn. Hoc ban co th mc nh dang ng vin cho tt ca cac dong ngay t u theo qui trnh sau :

- T Options Menu Drawing Defauts Stream Display hin th ca s Stream Style

- Chon Circle t drop-down list box cua Stream Label Border. Va la chon nay ch co gia tr khi chung ta chon Name muc Stream Label Type OK

7.7 Hin th tnh cht cua dong trn s m phong Qui trnh nh sau :

- Right-click vao dong c chon hin th ca s la chon - Chon Display xut hin ca s Stream Style - Chon Properties t drop-down list box muc Stream Label Type

- Mc nh muc Property List la Property Label List se hin th tn, nhit , ap sut va lu lng dong OK



7.8 S dung Flash Hot-Key Tool PRO/II co mt cng cu hu ch cho phep hin th nhanh chong cac tnh toan flash

cua bt ky dong nao c chon o la cng cu Flash Hot-Key, cung cp mt phng tin nhanh chong, d dang xac nh ham lng va thanh phn cua pha long va pha hi cua bt ky dong nao

Hay th vi dong S1 : - click chon dong S1

- click vao biu tng Do flash se xut hin trn Programmers File Editor : file [S1.000]

7.9 Xut mt s m phong ra ca s lu tr tam (Exporting the PFD to the Windows Clipboard)

T Clipboard, ban co th dan mt cach n gian hnh ve ln bt ky mt chng trnh soan thao nao nh trong Microsoft Word. Qui trnh nh sau :

T Menu File Export Chon Flowsheet Drawing



Click OK PRO/II se hin th mt hp hi thoai khng nh rng flowsheet a c xut ra ca s lu tr tam

7.10 Nhp mt file PRO/II co sn (Importing a PRO/II Keyword Input File)

Ban co th nhp mt file keyword Input cua PRO/II dang *.inp co sn vao giao din PRO/II ang hin hanh. PRO/II se t ng chuyn i file nay thanh mt s tnh toan va chung ta co th tin hanh m phong nh m phong trn mt s PFD, t o chung ta co th chnh sa theo y mnh

T Menu File Import Nhp hoc chon tn cua flie mun nhp Chon OK hoc nhp Enter 7.11 Xac nh cac tnh cht v cn bng long - hi cua cac

h 2 cu t (Display BVLE) Gia s ta co h 2 cu t: propane va butane. xac nh cac tnh cht v bng long - hi cua cac h 2 cu t nay ap sut thng (1 atm) hay mt ap sut bt ky nao o, ta s dung cng cu Display BVLE.

Qui trnh nh sau :

Chon h n v Chon cu t Chon m hnh nhit ng thch hp Nhp chon biu tng Display BVLE Chon cac cu t, chon ap sut va nhp

chon Calculate Ta se c 5 loai biu : Biu X - Y Biu T - X - Y Biu h s Fugacity Biu hng s cn bng K thay i theo thanh phn mol Biu hng s cn bng K thay i theo



8 BAI TP AP DUNG 8.1 Bai toan 1: M phong s cng ngh cua phn xng

tach Methane Thap Demethanizer tach methane ra khoi hn hp kh trong s s dung turbo-expander.

Lu lng dong kh nguyn liu : 8 m3/s

Nhit : 120 oF

Ap sut : 602,7 psia (pound per square inch absolute

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

Thanh phn cua hn hp kh ban u nh sau :

Cu t % mol Cu t % mol

N2CH4C2H6C3H8

i-C4H10

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

n-C4H10i-C5H12n-C5H12C6H14C7H16

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

S nh sau : (Hnh I-1)

ThS. L Th Nh Y ai H)

125 psia

oc Bach Khoa


Hay xac nh: 1. Cng sut thc cua may nen C1? 2. Thanh phn, nhit va ap sut cua cac dong san phm kh va long?

8.1.1 Phng phap tin hanh Chung ta se chia s trn thanh 2 vung :

Vung 1 : Chung ta se m phong 3 thit b (Hnh 1-1) lam quen vi phn mm PROII

Vung 2 : Chung ta se m phong toan b qua trnh tm hiu nhng im u vit cua phn mm PROII

8.1.2 M phong vung 1 Vung 1 bao gm 3 thit b : thit b tach, van giam ap long va turbo-expander S nh sau (Hnh 1-1) Cac bc tin hanh m phong : 8.1.2.1 M mt flowsheet mi :

T File menu Chon New : mt ca s View1 se xut hin cho chung ta mt flowsheet mi, trn o, chung ta se tin hanh xy dng cac s bng cng cu floating PFD

8.1.2.2 Xac nh h n v o cho qua trnh m phong :

Nhp vao biu tng cai thc o (Input UOM) trn dong Standard Tool Bar (hoc t Menu Input Input of Measure)

Xut hin bang Defaut Units of Measure for Problem Data Input Chon Initialize from UOM library Chon h ENGLISH-SET1 hoc METRIC-SET1. Gia thit chon h ENGLISH-

SET1. Tuy nhin, chung ta co th thay i n v o cho tng ai lng bng cach nhp vao cac drop-down list va chon

Nu nhp vao Standard Vapor Conditions... (iu kin tiu chun cua pha hi) hin th ca s Problem Standard Vapor Conditions. Tuy theo h n v ma iu kin nay se khac nhau. Cac gia tr tiu chun c mc nh trong PRO/II la :

H n v Nhit Ap sut Th tch kh

English

Metric

60oF

0oC

14.696 psia

1.0332 kg/cm2379.48 ft3/lbmol

22.414 m3/kgmol



SI 273.15 K 101.32 kPa 22.414 m3/kgmol

Nu nhp vao TVP and RVP Conditions... (iu kin xac nh ap sut hi bao hoa thc va ap sut hi bao hoa Reid ) hin th ca s Problem TVP and RVP Conditions, trong o PRO/II mc nh : TVP c xac nh 100oF va RVP c xac nh theo cac phng phap API Naphta, API Crude, ... OK

hin th th vin cac n v o T Options / Units of Measure List xut hin ca s Units of Measure Library cung cp 3 h n v o chnh : English, Metric va SI ta co th tao mi, copy, xoa, ... cac loai n v

8.1.2.3 Thit lp cac thit b co trong s :

Cng cu floating PFD co th dch chuyn n bt ky ni nao trn giao din PROII Click vao biu tng thit b cn thit trn cng cu floating PFD ri click lai mt

ln na vao v tr mun t thit b trn s

Sau khi a click vao biu tng 1 thit b nao o ma cha t no vao trong s , nu khng mun chon thit b nay na right-click

Mun xoa bo mt thit b co trong s click vao thit b mun xoa xung quanh thit b o se co mt ng vin t bm Delete hoc right-click nhp chon Delete

Vi vung 1, ta click chon 3 thit b : thit b tach F1, van giam ap long V1 va turbo-expander EX1

8.1.2.4 Thit lp cac dong lu th chuyn ng ra vao cac thit b :

Click vao nut Streams trn cng cu floating PFD ; Khi o, trn cac thit b se xut hin cac ca vao va ra cua cac dong lu th. Cac

ca vao va ra yu cu cn phai co (required) se co mau o, nu khng se co mau xanh ;

Ve cac dong lu th cn thit S1, S2, S3, S4, S5 Xong, click lai vao nut Streams hoc nhp Esc thoat khoi vic thit lp cac

dong lu th

8.1.2.5 Xac nh thanh phn cu t co trong h :

Nguyn liu bao gm cac paraffine t methane n heptane va nitrogen. Tt ca cac cu t nay u c tm thy t ngn hang d liu (databanks) phong phu cac cu t cua PROII



Click vao biu tng phn t benzene c vin o (d liu yu cu phai nhp vao) trn thanh cng cu chon cac cu t (hoc click vao Input (Menu) chon Component Selection)

Co th nhp trc tip vao Component, hoc co th nhp chon Select from list Hydrocarbon lightents Chon cu t cn thit : N2 Add component Chon CH4 Add component C2H6, C3H8, i-C4H10, ... n C7H16 Sau khi a chon xong OK

8.1.2.6 La chon cac phng trnh nhit ng thch hp :

Click vao biu tng biu pha c vin o (d liu yu cu phai nhp vao) trn thanh cng cu chon cac m hnh nhit ng thch hp (hoc click vao Input (Menu) chon Thermodynamic Data) Chon Most Commonly Used t Category Chon Peng-Robinson t Primary Method tnh gia tr K va chon API tnh t trong long

Click Add xac nh phng phap tnh nhit ng PR01 cho h OK 8.1.2.7 Xac nh thanh phn, trang thai cua cac dong, xac nh cac d liu v

thit b

Dong S1, thit b F1, V1 va EX1 c vin o (d liu yu cu phai nhp vao) Chon thit b hoc dong bng cach click chon no (hoc click vao Input (Menu)

chon Data Entry)

a- Dong S1

Double click dong S1 hin th bang Stream Data muc Description ban co th nhp tn FEED (nguyn liu) cho dong nay click chon Flowrate and Composition chon Total Fluid Flowrate nhp vao gia tr 8. Chu y, lu lng nguyn liu c tnh bng m3/s, ma y n v la LB-MOL/HR click UOM xut hin bang Convert Unit of Measure chon Vap. Vol M3 SEC nhp Change Units

Nhp thanh phn cac cu t cua dong S1 : Nhp gia tr 7.91 cho cu t 1 nhp nut TAB nhp 73.05 cho cu t 2, ... n 0.69 cho cu t cui cung nhp OK quay lai ca s chnh Stream Data

xac nh nhit va ap sut cua dong S1 muc Thermal Condition : dong First Specification chon Temperature nhp gia tr -84. Xong nhp chon Pressure muc Second Specification nhp gia tr 587.7 psia (= 602.7 - 10 - 5) OK

b- Thit b F1



Double click vao thit b F1 nhp tn SEPARATOR Lu y : d liu Pressure Drop (tr lc) c vin xanh khng yu cu nhp,

nu chung ta khng nhp s liu vao nay, PROII se mc nh nhp gia tr 0

Click vao Unit Specification chon Duty (nhit lng). y, gia tr nay c mc nh bng 0

Quan sat thy khng con vung nao c vin o vic nhp d liu cho thit b an thanh OK

ghi lai cac s liu va nhp vao flowsheet ang lam vic T File menu chon Save As nhp tn SESSION1 cho chng trnh m phong vung 1 OK

c- Thit b V1

Double click vao thit b F1 nhp tn VALVE Chon Outlet Pressure t muc Operating Parameter nhp gia tr 125 OK d- Thit b EX1

Double click vao thit b F1 nhp tn EXPANDER Chon Outlet Pressure t muc Pressure and Work Specifications nhp gia tr

125

Thay gia tr mc nh 100% cua Adiabatic Efficiency (hiu sut oan nhit) thanh 80% OK

By gi, khng co mt biu tng nao trn dong Toolbar, mt thit b hoc mt dong nao c vin o iu o co ngha la tt ca cac s liu yu cu nhp vao flowsheet u hoan toan thoa man Hay ghi lai file bng cach nhp vao biu tng Save

8.1.2.8 Chay phn mm m phong

Click vao biu tng Run trn Toolbar Sau vai giy, hay sn sang nhn kt qua :

- Nu thanh cng, toan b dy chuyn se chuyn t mau xanh luc nhat sang mau xanh dng m OK

- Nu khng toan b se chuyn thanh mau o 8.1.2.9 Xem kt qua m phong

Click vao biu tng Generate Report trn Toolbar Kt qua cua qua trnh m phong se t ng xut hin trong ca s Programmers

File Editor nh sau:



$ Generated by PRO/II Keyword Generation System $ 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)M phong vung 2

8.1.2.10 Xy dng flowsheet cho toan b qua trnh (required)

Chung ta se xy dng mt flowsheet cho toan b qua trnh trn c s flowsheet cua vung 1 theo cac bc sau :

T File menu Open Chon file SESSION1.PRZ PRO/II se ghi tip tuc cac d liu mi vao file nay ngha la trong

SESSION1.PRZ chung ta se dung cng cu floating PFD lp t thm 2 thit b trao i nhit E1 va E2, 1 may nen C1 va 1 thap chng ct T1 vao s

Chu y : Khi mun lp t nhiu thit b cung loai vao s (V du 2 thit b trao i nhit) click vao thit b mong mun trn thanh cng cu PFD nhn gi nut Shift click vao cac v tr mun t thit b trong s

Khi chon biu tng thap chng ct trn cng cu PFD se xut hin mt ca s yu cu nhp s a (ly thuyt) Hay chon mt thap 10 a k ca thit b un si lai (la mt a) va khng co thit b ngng tu nh thap

Chu y : PRO/II co th m nhiu viewport cho cung mt bai toan m phong, cho phep chung ta quan sat s nhiu goc khac nhau. Mun vy, co nhiu cach :

- T Window menu chon New View tao View 2 - Click vao biu tng New View trn Standard Tool Bar tao View 2 - T Window menu chon Tile Horizontally tao 2 Viewport theo chiu

ngang

- T Window menu chon Tile Vertically tao 2 Viewport theo chiu doc Biu tng Zoom Full : cho phep quan sat toan b s trn toan man hnh Biu tng Zoom In : cho phep quan sat mt phn s c chon trn toan man

hnh

Click vao biu tng Streams trn thanh cng cu PFD va xy dng cac dong sau : - Dong (hi) i ra t nh cua thap Demethaniser va vao thit b trao i nhit

E1

- Dong i ra t thit b trao i nhit E1 vao may nen C1

- Dong san phm i ra khoi may nen C1

- Dong i ra t thit b trao i nhit E1 vao thit b trao i nhit E2

- Dong san phm i ra khoi thit b trao i nhit E2



- Dong san phm ra t thit b un si lai cua thap

Chung ta nhn thy rng : thanh phn cua dong nguyn liu vao thit b trao i nhit kh - kh E1 (gas-gas heat exchanger) chnh la thanh phn cua dong kh nguyn liu vao thit b tach F1. tranh vic nhp d liu lp lai vao cac dong, ta se tin hanh ni lai cac dong theo ung s (I-1) nh sau :

- R chut n u mui tn cua dong S1 Nhp chut trai va gi nguyn, r n u vao cua thit b E1 Bung chut ra By gi dong nguyn liu S1 se i vao thit b E1

- Tin hanh tng t a dong S10 i ra t E2 n vao thit b F1 - Dong S4 vao a 1 cua thap Demethaniser, dong S5 vao a 3 cua thap

Demethaniser. Chung ta a hoan thanh vic thit lp toan b s nh sau:

Chu y : Trn s , khng co dong nao c vin o Trc khi tin hanh m phong, ch con vic thay i nhit va ap sut cua dong S1 va nhp d liu cho cac thit b c vin o : E1, E2, C1 va T1



8.1.2.11 Thay i nhit va ap sut cua dong S1 (required)

Tin hanh thay i nhit cua dong S1 t -84oF n 120oF va ap sut t 587.7 psia thanh 602.7 psia nh sau :

Double-click dong S1 xut hin ca s Stream Data Thay i nhit t -84oF thanh 120oF Thay i ap sut t 587.7 psia thanh 602.7 psia 8.1.2.12 Nhp d liu cho E1 (required)

Thit b nay yu cu chnh nhit gia lu th nong vao va lu th lanh ra la 10 oF va tr lc pha lu th nong la 10 psi va tr lc pha lu th lanh la 5 psi

Double-click E1 xut hin ca s Heat Exchanger muc Description nhp tn GAS-GASS HX Click vao muc Process Stream xac nh dong nong va dong lanh cho thit b

xut hin ca s Heat Exchanger- Process Stream click vao muc Hot hoc Cold tng ng vi cac dong OK v lai ca s Heat Exchanger

Chon Specification xut hin ca s Heat Exchanger-Specifications chon Hot Inlet-Cold Outlet Temperature Approach va nhp gia tr 10oF OK v lai ca s Heat Exchanger

muc Pressure Drop (tr lc) : nhp gia tr 10 psi cho Hot Side va 5 psi cho Cold Side OK hoan thanh vic nhp d liu cho E1

8.1.2.13 Nhp d liu cho E2 (required)

Thit b nay yu cu lam lanh dong S9 xung nhit la -84oF va tr lc pha lu th nong la 5 psi

Double-click E2 xut hin ca s Heat Exchanger muc Description nhp tn CHILLER Chon Specification xut hin ca s Heat Exchanger-Specifications chon

Hot Product Temperature va nhp gia tr -84oF OK v lai ca s Heat Exchanger

muc Pressure Drop (tr lc) : nhp gia tr 5 psi cho Hot Side OK hoan thanh vic nhp d liu cho E2

8.1.2.14 Nhp d liu cho C1 (required)

Double-click vao C1 xut hin ca s Compressor muc Description nhp tn COMPRESSOR ThS. L Th Nh Y ai Hoc Bach Khoa


Nhp gia tr 75% cho muc Efficiency or Temperature Specification Chu y rng cng sut cua may nen C1 se c cung cp bi cng sut thu c t

expander EX1 nn se chnh bng cng sut cua EX1

Chon Work t muc Pressure, Work or Head Specification Click chon muc Define dong Toolbar xut hin ca s Definition click

chon muc Set Up Definition for Compressor Work click chon thng s Parameter c vin o xut hin ca s Parameter

Click chon thit b Expander EX1 t muc Constant/Stream/Unit click chon Parameter c vin o xut hin ca s Parameter Selection

chon Actual Work OK tr v ca s Parameter OK tr v ca s Definition OK tr v ca s Compressor OK nhp

xong d liu cho C1

8.1.2.15 Nhp d liu cho T1

Double-click vao C1 xut hin ca s Column muc Description nhp tn TOWER Nhp chon vao th hai c vin o Feeds and Products xut hin ca s

Column - Feeds and Products bang trn, xac nh dong S4 c nap vao a 1 va S5 c nap vao a 3 : nhp gia tr 1 tng ng vi dong S4 Tab nhp gia tr 3 tng ng vi dong S5 bang di, nhp gia tr lu lng 500 lbmol/hr cho dong hi san phm nh S6 ra t a 1 (1 libra = 1 pound = 453,6 g)

muc Feed Flash Convention : co 2 la chon : - Vapor and liquid to be the feed tray : c mc nh

- Flash the feed adiabatically, vapor onto the tray above and liquid onto the feed tray : la chon nay ch c chon khi nap liu a cui cung ay thap

Nhp chon vao th nht c vin o Pressure Profile xut hin ca s Column - Pressure Profile Nhp gia tr 125 psia la ap sut a trn cung cua thap muc Overall Specification OK tr v ca s Column

Chu y rng : yu cu cht lng cua san phm ay la t l C1/C2 = 0.015 muc Performance Specification

- Nhp chon xut hin ca s Column - Specifications and Variables click vao chon Add Specifications and Variables click vao parameter (ch o va gach di o) trong muc Specifications xut hin ca s



Parameter chon Stream muc Stream/Unit va chon dong S11 muc Stream Name la dong san phm ay cua thap

- Click vao Parameter (ch trng trn nn o) xut hin ca s Parameter selection chon Flowrate muc Parameter chon Selected Components muc Flowrate chon METHANE la cu t u va cu t cui OK tr v ca s Parameter OK : hoan thanh ca s Parameter tr v ca s Column - Specifications and Variables

- muc Specifications nhp vao du = trc ch Value mau o xut hin cac la chon +, -, /, * Parameter chon /

- Tip tuc nhp chon Parameter mau o cung muc Specifications xut hin ca s Parameter chon Stream muc Stream/Unit va chon dong S11 muc Stream Name Click vao Parameter (ch trng trn nn o) xut hin ca s Parameter selection chon Flowrate muc Parameter chon Selected Components muc Flowrate chon ETHANE la cu t u va cu t cui OK tr v ca s Parameter OK : hoan thanh ca s Parameter tr v ca s Column - Specifications and Variables

- click vao Value nhp gia tr 0.015 - click vao parameter (ch o va gach di o) trong muc Variables xut

hin ca s Parameter Selection Chon Heat Duty (nng sut nhit) muc Heater se xut hin REBOILER OK : quay lai ca s Variables OK : quay lai ca s Column - Specifications and Variables OK : hoan thanh vic nhp d liu cho T1

muc Condenser : chon dang Bubble muc Reboiler : Chon dang Kettle : c mc nh (qui chun) 8.1.2.16 Tin hanh m phong (required) va xem kt qua m phong

Click vao biu tng Run trn Toolbar. Sau vai giy, toan b dy chuyn se chuyn t mau xanh luc nhat sang mau xanh dng m OK

Click vao biu tng Generate Report trn Toolbar Kt qua cua qua trnh m phong se t ng xut hin trong ca s Programmers

File Editor vi tn file la SESSION2.OUT nh sau:



$ Generated by PRO/II Keyword Generation System $ 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 =============

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