HEMISKI Zbirka re{eni zada~i REAKTORI 3

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Prv del. Definicii, koncepti, stehiometriski tablici, osnovni ravenki od hemiska ramnoteà i kinetika, ravenki za dizajn, toplinski bilansi i korisni prilozi za analiza i dizajn na hemiski reaktori Op{tata, odnosno osnovnata stehiometriska korelacija za multireakcioni proto~ni sistemi e : odnosno dF i, j d j i, j R j R j1 j1 ( F ) , (36F) i j i, j Fi i, j j Fi Fio j , (37F) kade {to dosegot na reakcijata j e vo edinici na molski protok. Neto-brzinata na reakcija za sekoj u~esnik vo multireakcionen sistem pretstavuva zbir na brzinite vo odnos na toj u~esnik vo site reakcii vo koi toj u~estvuva: r i R ri j j1 , . (38) Vo ravenkata (38) ri e neto-brzina na u~esnikot i, dodeka ri,j e brzina vo odnos na toj u~esnik vo reakcijata j. Relacijata pome|u brzinite na poedine~en u~esnik vo multireakcionen sistem vo reakcijata j e slednata: ili r i, j i, j r1, j r2, j rN , j R j ; . . . . (39) r i, j i, j 1, j 2, j k, j N , j rk , j . (40) Vo relacijata (39) Rj e brzina na promena na dosegot na reakcijata j po edinica reakcionen prostor. Relacijata (40) e kompaktna forma na relativnite brzini na formirawe na u~esncite vo reakcijata j i vo koja bilo druga reakcija vo kompleksnata {ema od 1, 2, 3 . . . . do R reakcii. Oznakata k se odnesuva na klu~niot u~esnik vo reakcijata j, vo odnos na koj e daden brzinskiot izraz za taa reakcija. 15
Page 1 and 2: HEMISKI REAKTORI 3 Zbirka re{eni za
Page 3 and 4: Skopje, 2010
Page 6 and 7: Predgovor . . . Hemiskiot reaktor e
Page 8 and 9: lot da se stekne so ve{tina da gi k
Page 10: ~ite }e mu ovozmoì preku niv da go
Page 13 and 14: 5. TOPLINSKI BILANSI ..............
Page 15 and 16: XIV êtvrti del IDEALEN CEVEN REAKT
Page 17 and 18: Zada~a 4. Adijabatski PBR so pretho
Page 20 and 21: 1. STEHIOMETRIJA 1.1. Prost reakcio
Page 22 and 23: Prv del. Definicii, koncepti, stehi
Page 24 and 25: 2. TOPLINA NA REAKCIJA I HEMISKA RA
Page 28 and 29: 3. IZRAZI ZA BRZINA NA REAKCIJA 3.1
Page 34 and 35: 4. RAVENKI ZA DIZAJN 4.1. Ravenki z
Page 46 and 47: 5. TOPLINSKI BILANSI 5.1. Toplinski
Page 56: 6. PRILOZI 6.1. Stehiometriski tabl
Page 59 and 60: 42 T a b e l a 2 Op{ta stehiometris
Page 61 and 62: 44 T a b e l a 4 Op{ta stehiometris
Page 63 and 64: 46 {arèn aA bB cC dD te~na faza g
Page 65 and 66: kade {to p i q se koreni na ravenka
Page 67 and 68: moè da se re{i analiti~ki, odnosno
Page 69 and 70: Koga rabotata na reaktorot e neizot
Page 72 and 73: Zada~a 1 [arèn reaktor so razmena
Page 74 and 75: Vtor del. [arèn reaktor b) Za pres
Page 76 and 77: dT m dT Vtor del. [arèn reaktor s
Page 78 and 79: X X 1 0.8 0.6 0.4 0.2 Vtor del. [ar
Page 80 and 81: Vtor del. [arèn reaktor Re{enieto
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Vtor del. [arèn reaktor C A Ao C
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Zada~a 3 Vtor del. [arèn reaktor [
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Vtor del. [arèn reaktor Re{enie: P
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Zada~a 5 Vtor del. [arèn reaktor A
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t C r Ao Vtor del. [arèn reaktor 1
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Zada~a 6 Vtor del. [arèn reaktor E
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Zada~a 7 Vtor del. [arèn reaktor P
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Vtor del. [arèn reaktor Za da se o
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Vtor del. [arèn reaktor od {to sle
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Vtor del. [arèn reaktor Vremenska
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Vtor del. [arèn reaktor Ako sakame
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TW,vlez Vtor del. [arèn reaktor TW
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Vtor del. [arèn reaktor b) Ako se
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Zada~a 9 Vtor del. [arèn reaktor R
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Vtor del. [arèn reaktor Za vreme o
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Vtor del. [arèn reaktor presmeta d
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Vtor del. [arèn reaktor Brzinskiot
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Vtor del. [arèn reaktor Pred da ja
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Vtor del. [arèn reaktor Ako se opr
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Vtor del. [arèn reaktor Ravenkata
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Vtor del. [arèn reaktor // X'=R/Ca
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Tret del Proto~en reaktor od rezerv
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110 Sostavuvame stehiometriska tabl
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Zamenuvame vo ravenkata za dizajn (
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Vo ravenkata (2) se zamenuvaat nume
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Kako {to se gleda od tabelata, ized
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118 ~ UA( T Ta ) FAoC P, A( T To
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peraturata vrz molskata koncentraci
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a) Da se opredeli izlezniot efekt o
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i ja kombinirame so brzinskiot izra
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126 T T o 70000 ~ ~ ) ( H r X X
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dopolnitelni podatoci: CP,smesa = 3
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Kako {to se gleda od grafikot, so v
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Zada~a 5 132 Serija od izotermni CS
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nost: ( r 134 A ) Brzinata na reakc
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6) Znaeme deka kineti~kata kriva i
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138 C C C C A, 1 A, 2 A, 3 A, 4 15,
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za izleznata koncentracija od ovoj
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142 Drugite podatoci na izlezot od
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Volumenskiot protok na vlezot i izl
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146 - toplina na reakcijata, H r 1
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) Za adijabatska rabota na serijata
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150 T T T izlez o izlez 95 T o
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152 a-1) Ramnote`na linija X * (T):
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Kako {to se gleda od reakcioniot pl
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POLYMATH Results Calculated values
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cijata na 25 o C e Hr = -131000 cal
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koncentracija na natriumtiosulfat,
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a) Da se opredeli potrebniot volume
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Se izramnuvaat izrazite (6) i (7) i
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166 - Volumenot na vtoriot reaktor:
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eakcijata nema da se menuva, no vol
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Izleznata konverzija od prviot reak
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172 ; (mol/l)/h 373 , 0 095 , 5 685
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Zada~a 12 Vlijanieto na vremeto na
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176 V F Ao X 3 ; FAo C Ao o 0, 5
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* ( 0, 1 K) ( 0, 1 K) 4( 1 0, 4
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simumot na krivata XMB(T) za a = 3,
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182 2FAo FA FA 2 oC A o ; FA
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na reakcijata i koncentracijata na
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Zada~a 14 Osetlivost na po~etnata t
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Vo ravenkata na toplinskiot bilans
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d( C AV ) FAo FA rA V , (85) dt
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192 Spored pokaàniot rezultat, Ti
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Prisposobeni za razgleduvanata este
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[7] k1 = 4.76*(10^(-4)) [8] R = (k1
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2) Da se presmeta dolìnata na cevk
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200 Vrednostite za Vo, o, CFi i CA
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Dolìnata na cevkata od koja e napr
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êtvrti del Idealen ceven reaktor (
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treba cela stehiometriska tablica.
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Ako ovoj proces se izveduva vo indu
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Zada~a 3 212 Sogoruvawe na motorno
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potoa numeri~kite vrednosti na brzi
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) Ako se zeme predvid promenata na
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218 k( T ) ( rA ) k( T ) C ACB 5
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220 F Ao 5 k( 293) 1, 287 10 exp(
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222 0, 8333 3 T ( 1 0, 05X ) V 0,
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Re{enie: a) Vo ovaa zada~a volumeno
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Kako {to se gleda od tabelata, re{e
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Zada~a 6 Reverzibilna reakcija vo g
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230 ( r A ( r A ) 0 ( 1 X ) 0 10
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zibilnite reakcii bi trebalo da se
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234 Brzinskiot izraz preku konverzi
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236 ( 11 0) f ( X o , To ) 1; 11(
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238 Fio Fi() Fi(X) pi = (Fi/FAo)P A
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Izborot na goleminata na reaktorot
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Od ovoj rezultat se gleda deka reak
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v) Potrebniot protok na vodata za l
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246 2 2 2 ( 1 X ) To ( r ) k( T
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Re{enie: Reaktorot e so daden volum
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Toplinskiot bilans za adijabatska r
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Kako {to se gleda od dobienite rezu
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( 1 X ) C A C Ao ; ( 1 0, 6X ) ( 1
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256 ( H r ) ( T T o) X ( iC P, i
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Zada~a 13 258 3 V 0, 87 m ; To 10
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260 Podatocite se kombiniraat so ra
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52, 6( To 406 X ) To 406X T . (
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Zada~a 14 264 Zavisnosta X izlez (T
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266 X X izlez izlez V dX dX F
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To 273 273 273 273 B 0.1359551 0.13
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Re{enie: Zaedni~ki za dvata tipa re
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272 Adijabatska operaciona linija i
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Za volumenot na reaktorot za X izle
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X Kako {to se gleda od grafikot, bi
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278 X 2 k 0, 9 VCSTR ( 90 100X 1
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280 1) Serija PFR-CSTR - V PFR F k
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282 V C Ao CSTR o C C C Bo A B 1,
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dC A 1 k C A[ CBo ( C Ao C A)]
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Na primer, za R = 1,0 koncentracija
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288 R CAo CA,izlez= CA2 CA1 V (litr
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290 - Konverzijata vo PFR: FAo FA
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ODE Report (RKF45) Differential equ
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294 Brzinata na reakcijata za X = 0
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Pred da se re{ava ravenkata (8) prv
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cija. Reakcijata e silno egzotermna
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300 T T T I II III 304K ; 323K ;
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Kako {to se gleda od rezultatite i
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Vo ravenkata (10) se zamenuvaat num
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za obi~ni diferencijalni ravenki od
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so takva promena na koncentracijata
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PFR so recirkulacija: Povtorno bara
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Presmetani se volumeni na PFR so re
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314 Trite povr{ini obeleèni na gra
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Zada~a 1 Kataliti~ka hidratacija na
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Petti del. Kataliti~ki reaktor so f
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Zada~a 1 Krekuvawe na aceton vo PFR
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[esti del. Industriski reaktori ( 1
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[esti del. Industriski reaktori Za
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0.25 0.2 X 7 0.15 6 5 4 3 0.1 0.05
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Explicit equations as entered by th
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[esti del. Industriski reaktori Spo
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[esti del. Industriski reaktori O~i
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[esti del. Industriski reaktori v)
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[esti del. Industriski reaktori Top
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[esti del. Industriski reaktori na
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C C C i C P P, i C P, B P, A C
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[esti del. Industriski reaktori ‡
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[esti del. Industriski reaktori Bar
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[esti del. Industriski reaktori C6H
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[esti del. Industriski reaktori ba
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[esti del. Industriski reaktori K P
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[esti del. Industriski reaktori Kak
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[14] B2 = -13020/T [15] B3 = 5.051*
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[esti del. Industriski reaktori Ana
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B 4 [esti del. Industriski reaktori
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[esti del. Industriski reaktori dF
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[esti del. Industriski reaktori r1
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[esti del. Industriski reaktori To
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Y Y Y S / E B / E T / E j j
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[esti del. Industriski reaktori Adi
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( r A ) k ( T ) C [esti del. Indus
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[esti del. Industriski reaktori rat
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X * ad.=0,404 X izlez=0,274 [esti d
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[esti del. Industriski reaktori Vle
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[esti del. Industriski reaktori se
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[esti del. Industriski reaktori FB
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[esti del. Industriski reaktori vre
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Tretiot segment: POLYMATH Results C
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[esti del. Industriski reaktori Exp
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[esti del. Industriski reaktori Toi
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[esti del. Industriski reaktori Ako
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X 0.4 0.32 0.24 0.16 0.08 [esti del
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[esti del. Industriski reaktori pri
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C C C G, 2 P, 2 P, 2 C P, 1 [esti
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[esti del. Industriski reaktori Pri
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Zada~a 6 [esti del. Industriski rea
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[esti del. Industriski reaktori Ste
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[esti del. Industriski reaktori [4]
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[esti del. Industriski reaktori Kon
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[esti del. Industriski reaktori Kin
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p p B C [esti del. Industriski reak
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[esti del. Industriski reaktori ‡
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[esti del. Industriski reaktori Od
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X 1 0.8 0.6 0.4 0.2 [esti del. Indu
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C C P, SO3 P, N2 35, 64 26, 167 [
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F Bo I y 1; A I Bo F y F To B
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[esti del. Industriski reaktori So
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[esti del. Industriski reaktori T (
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X 1 0.8 0.6 0.4 0.2 [esti del. Indu
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2) Toplina na reakcija [esti del. I
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[esti del. Industriski reaktori (to
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ODE Report (RKF45) [esti del. Indus
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FB(V) r2(V) [esti del. Industriski
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[esti del. Industriski reaktori Zab
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[esti del. Industriski reaktori umo
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[esti del. Industriski reaktori Cpa
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[esti del. Industriski reaktori So
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[esti del. Industriski reaktori [3]
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[esti del. Industriski reaktori Y =
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[esti del. Industriski reaktori FC(
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W W kat kat V 1000 [esti del. In
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FB(W) FC(W) [esti del. Industriski
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[esti del. Industriski reaktori Ne
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[esti del. Industriski reaktori - R
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[esti del. Industriski reaktori Sog
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[esti del. Industriski reaktori - i
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[esti del. Industriski reaktori Gra
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[esti del. Industriski reaktori [to
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Toplinskiot bilans: [esti del. Indu
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ODE Report (RKF45) Differential equ
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[esti del. Industriski reaktori dC
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[esti del. Industriski reaktori 4-2
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[esti del. Industriski reaktori ODE
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[esti del. Industriski reaktori 4-3
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[esti del. Industriski reaktori Izr
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[esti del. Industriski reaktori Rav
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[esti del. Industriski reaktori Exp
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[esti del. Industriski reaktori pro
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Zada~a 12 [esti del. Industriski re
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A (N2) B (H2) p p A C [( 4 [( 4 C
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[esti del. Industriski reaktori gra
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Stepen na konverzija na N2 Stepen n
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[esti del. Industriski reaktori - d
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[esti del. Industriski reaktori 12)
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[esti del. Industriski reaktori H r
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Temperatura (K) Stepen na konverzij
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[esti del. Industriski reaktori Ana
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HEMISKI Zbirka re{eni zada~i REAKTORI 3

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