HEMISKI Zbirka re{eni zada~i REAKTORI 3

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SODR@INA Prv del DEFINICII, KONCEPTI, STEHIOMETRISKI TABLICI, OSNOVNI RAVENKI OD HEMISKA RAMNOTE@A I KINETIKA, RAVENKI ZA DIZAJN, TOPLINSKI BILANSI I KORISNI PRILOZI ZA ANALIZA I DIZAJN NA HEMISKI REAKTORI 1. STEHIOMETRIJA .................................................................................... 3 1.1. Prost reakcionen sistem ....................................................................3 1.2. Stehiometriska tablica .....................................................................4 2. TOPLINA NA REAKCIJA I HEMISKA RAMNOTE@A .................................................................7 2.1. Toplina na reakcija ...............................................................................7 2.2. Uslov za ramnoteà vo hemiski reakcionen sistem ....................8 2.3. Relacii pome|u ramnote`nite konstanti ........................................9 3. IZRAZI ZA BRZINA NA HEMISKA REAKCIJA .....................11 3.1. Matemati~ka definicija za brzina na reakcija ..........................11 3.2. Izrazi za brzina na ireverzibilni reakcii .................................11 3.3. Izrazi za brzina na reverzibilni reakcii. Ramnoteà ...........12 3.4. Stehiometriska relacija na brzinite na reakcija vo odnos na poedine~en u~esnik vo reakcijata ............................14 3.5. Stehiometrija i stehiometriski relacii. Neto-brzina kaj multireakcioni sistemi ...................................14 4. RAVENKI ZA DIZAJN ..........................................................................17 4.1. Ravenki za dizajn na {arèn reaktor ...........................................17 4.2. Ravenki za dizajn na idealen ceven reaktor .................................19 4.3. Ravenki za dizajn na idealen ceven reaktor so recirkulacija ..................................................................................22 4.4. Ravenki za dizajn na idealen CSTR .................................................24 4.5. Ravenki za dizajn na polu{arèn reaktor ....................................27
5. TOPLINSKI BILANSI ......................................................................29 5.1. Toplinski bilansi na {arèn reaktor .........................................29 5.2. Toplinski bilansi na idealen ceven reaktor .............................32 5.3. Toplinski bilansi na CSTR .............................................................35 6. PRILOZI ....................................................................................................39 6.1. Stehiometriski tablici ...................................................................39 6.2. Korisni tabli~ni integrali ...........................................................47 6.3 Numeri~ka evaluacija na integrali ................................................48 6.4. Korisni softverski paketi .............................................................52 XII Vtor del [AR@EN REAKTOR Zada~a 1. [arèn reaktor so razmena na toplina ................................55 Zada~a 2. [arèn reaktor i CSTR so ista proizvodnost ...................64 Zada~a 3. [arèn reaktor so promenliv volumen .................................67 Zada~a 4. [arèn reaktor – presmetka na broj {arì .......................68 Zada~a 5. Adijabatski {arèn reaktor so prethodno zagrevawe na reaktantot ...............................................................................71 Zada~a 6. Esterifikacija na ocetna kiselina so etanol vo izotermen {arèn reaktor .................................................75 Zada~a 7. Polimerizacija na stiren vo izotermen {arèn reaktor ..................................................77 Zada~a 8. Reakcija vo gasna faza vo izotermen {arèn reaktor so promenliv volumen i pritisok ......................................................................................88 Zada~a 9. Reakcija vo gasna faza vo izobaren adijabatski {arèn reaktor so promenliv volumen ...................................91 Zada~a 10. Reakcija vo gasna faza vo izotermen {arèn reaktor so V=const. i promenliv pritisok ..........................................94 Zada~a 11. Hidroliza na acetanhidrid vo {arèn reaktor. Kinetika, izotermen i adijabatski proces .......................97 Zada~a 12. [arèn reaktor so egzotermna reverzibilna reakcija vo te~na faza. Reakcionen plan, izotermen i adijabatski proces ...............................................................101
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 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 32: Prv del. Definicii, koncepti, stehi
Page 35 and 36: Molskite koncentracii vklu~eni vo b
Page 37 and 38: kako ravenkata (52). Razlikata e vo
Page 39 and 40: Ravenkite za dizajn na cevniot reak
Page 41 and 42: Ravenkata za dizajn na ceven reakto
Page 43 and 44: Za presmetka na brojot na reaktorit
Page 45 and 46: 28 Po~eten uslov za re{avawe na sis
Page 47 and 48: Toplinski bilansi za adijabatska ra
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Prv del. Definicii, koncepti, stehi
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Vtor del [arèn reaktor
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Re{enie: a) Za izotermna rabota na
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POLYMATH Results Calculated values
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Explicit equations as entered by th
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Jasno e deka vremeto potrebno za re
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Zada~a 2 64 [arèn reaktor i CSTR s
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Rezultatot e deka so eden {arèn re
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Vo ravenkata za dizajn (48) gi zame
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a) Brojot na {arìte koj }e go obez
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Kone~nata forma na brzinskiot izraz
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76 Mi % (w/w) 1 3 Cio smesa kmol/m
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Re{enie: Samo so primena na ravenka
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data e so sè pomali temperaturni r
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) Za varijantata na razmena na topl
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( H r )( rA ) V TW , vlez T
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Vkupnata koli~ina toplina {to }e se
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) Za presmetka na vremeto na reakci
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( 1 X ) To C A C Ao ; (1) ( 1 0, 5
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11620 X T To . (6) 38, 73 12, 91X
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96 t r t r C P dP dP C Ao ; 0, 5(
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a) Od kineti~kite podatoci da se op
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100 C C W n C Wo / V Wo W rastvor
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A B ; ( rA) k1C A k2C B ; 7 1 k
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) Vremeto na reakcija za 80% konver
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presmetki za izotermna rabota na re
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Zada~a 1 Hidrogenacija na etilen vo
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Tret del. Proto~en reaktor od rezer
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1 Tret del. Proto~en reaktor od rez
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POLYMATH Results Tret del. Proto~en
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F F X X A1 B1 1 1 Tret del. Proto~e
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C B2 0, 1056 F F X 2 A2 B2 2 Tre
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Zada~a 8 Tret del. Proto~en reaktor
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Explicit equations [1] R = 0 [2] T
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X * XMB XEB X*; XMB; XEB 1 0.8 0.6
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XMB XEB 1 0.8 0.6 0.4 0.2 Zada~a 10
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( C C A1 ( C C A2 ( C C A3 A Tret d
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1 Tret del. Proto~en reaktor od rez
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Zada~a 15 Tret del. Proto~en reakto
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C C C C Bo Bo Wo Wo Tret del. Proto
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dT dt Tret del. Proto~en reaktor od
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Zada~a 1 Endotermna reakcija vo gas
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êtvrti del. Idealen ceven reaktor
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Re{enie: êtvrti del. Idealen ceven
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A (NO) B (O2) C (NO2) I (N2) êtvrt
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X 0 0, 2 êtvrti del. Idealen ceve
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Re{enie: a) Izotermna rabota: êtvr
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T (K) k (T) izraz (4) êtvrti del.
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( r êtvrti del. Idealen ceven reak
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0,22 êtvrti del. Idealen ceven rea
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Zada~a 16 êtvrti del. Idealen ceve
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V PFR k F Ao êtvrti del. Idealen c
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Ropt=1,5 Vmin=1884litri êtvrti del
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Petti del Kataliti~ki reaktor so fi
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ili 318 - diferencijalen oblik, kak
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Od izve{tajot i od rezultatite od p
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Grafi~ka prezentacija na site rezul
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Ponatamu podgotvuvame brzinski izra
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Zada~a 3 326 Reakcija vo gasna faza
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Iako brzinskiot izraz e prili~no go
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330 Fio Fi() Fi(X) pi = yiP = (Fi/F
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332 A FAo B Bo Fio Fi() Fi(X) F 2F
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Ako reakcijata se odviva vo pove}ec
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Isto taka, dobro e da znaeme kolku
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Prvo, brzinskiot izraz se pi{uva vo
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340 Yexp X Ycalc 6087E-12 0.105 8.0
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Re{enie: Rabota so razmena na topli
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344 dT dV dT dT dT FT CP 65, 9 6,
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Kako {to moè da se vidi od dobieni
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Komentari: 1) So adijabatska rabota
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za KC(T) se dobiva sledniov izraz:
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352 W (kg) W (kg) (-rA) = f(W) W (k
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354 - toplina na reakcijata: Hr = 1
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356 dT dV ( H r )( r C A ) smes
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358 Potrebniot broj reaktorski cevk
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360 C TS r a, T kT pT Cv K
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364 Za brzinski izraz preku konverz
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366 0, 2 0 h f ( X ) dX 3 0, 2 0
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368 Sega go pi{uvame bilansot na ak
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Re{avawe na ravenkata (8) zna~i pre
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Analizata za razli~ni vrednosti na
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Re{enie: 1) Ravenkata za dizajn na
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[8] Po = (1-X)*P/(2-X) [9] Ph = (1-
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1 ( rO ) f ( W ) ili D f ( X )
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380 f 9, 375 ( 1, 75 0, 0585 ?) 9
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Za da zaklu~ime dali ovoj volumen e
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pritisokot i konverzijata. Zavisnos
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k 3.194E-05 3.194E-05 3.194E-05 3.1
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[esti del Industriski reaktori
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392 - vlez vo reaktorot: T C o 650
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Izleznata konverzija normalno raste
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gramata se vnesuvaat ovie dve raven
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Toplinskiot bilans vo ovoj slu~aj }
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400 X 0.5 0.4 0.3 0.2 0.1 1 2 3 4 5
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402 1060 1032 T(K) X 1004 976 948 9
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Zada~a 2 404 Piroliza na etan do et
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406 C A C Ao ( 1 X ) ; ( 1 0, 6X )
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408 X 1 0.8 0.6 0.4 0.2 0 900 950 1
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T 1053 930.72495 1053 930.72495 FAo
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sokot, potoa podatokot za konstante
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Za vrednosti na Re-brojot pome|u 30
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416 V (m 3 ) P(V) V (m 3 ) X(T) T (
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eaktorot: dali toa }e bide izotermn
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2) Da se povtori re{enieto pod 1),
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e{avawe na zada~ata da se koristi p
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ni ravenki, (5), (6) i (7), zavisno
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Ramnoteà: Za da se kompletira slik
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Explicit equations [1] Feo = 0.0034
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432 T (K) Presek na ramnote`na i ad
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cionen mehanizam koj, pokraj glavna
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436 - vodorod, H: - benzen, B: - et
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Za da se re{i sistemot od 7+1 difer
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440 FE(V) Promena na molskite proto
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442 F F F F F F F E FEo 1) 1 ( 1
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enzen izvedena pod dadenite uslovi
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- toplinski kapaciteti na reaktanto
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dX (rA ) . (3) dW FAo Ravenkata (3
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FAo 20 20 20 20 T 527.23 527.23 812
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2) Novata varijanta na adijabatskat
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454 C P, A F C i H r C P, i P, B
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Zna~i, so ovaa varijanta razreduvaw
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segment }e treba da se presmetuva p
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dodeka izrazite za molskite koncent
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Toi 650.66442 650.66442 650.66442 6
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Sedmiot segment: POLYMATH Results C
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470 X 0.4 0.32 0.24 0.16 0.08 0 500
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Zada~a 5 472 Proizvodstvo na glukon
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30 24 / 144 5 . Zna~i, na po~etok
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T a b e l a 1 Po~etok na ciklus 10
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478 Vmax / K m 1 5 3 k 0, 016 h
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te~nata reakciona smesa se odrùva
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482 r r , r , 1 r , 2 r , 3 C
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azot za vkupno sozdadena kiselina (
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486 CB(t) CM(t) t (s) t (s) t (s) A
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Zada~a 7 488 Kataliti~ka oksidacija
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490 dX dW ( rA ) F1 ( X , T ) (2)
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Podolu se izve{taite i grafi~kite p
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K2 13.126279 5.2903007 13.126279 5.
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Reakcioniot plan pretstavuva grafik
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498 Podatoci potrebni za re{avawe n
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nosno ravenka za dizajn (preku konv
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0, 01094 kmol ( rA ) k 0, 425 P ; P
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- proizvod od koeficientot na preno
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506 - Drugite podatoci se: sloj 5
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508 X(W) W (kg) Zavisnost konverzij
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temperatura dava podobar efekt i vo
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Bidej}i reakcijata e egzotermna so
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514 - Kinetika r ( r k r k 1 1 2 2
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516 k k r k k 1 1 1 2 2 2 dF C dV d
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So solverot za diferencijalni raven
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na koncentracijata na kislorodot. T
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522 Varijanta 2. Proces so kislorod
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Ravenka za dizajn na PBR: Ravenkata
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Sistemot diferencijalni ravenki (11
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528 FA(W) FB(W) FC(W) W (kg) FD(W);
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Ravenkite {to treba da se kombinira
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vo 7648.55 7648.55 7648.55 7648.55
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536 r2(W) r1(W) Grafik na zavisnost
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Y = 1 7, 077 ( 1 0, 45) ( 1 0, 4
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540 r2(W) r1(W) W (kg) Grafik na za
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1 ( rA ) 1 r1 k1 p A pB kmol/(kg
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544 Za specifi~nata povr{ina se zam
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na toplina i za protokot na vodata
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Cpa 44.257982 44.257982 65.187219 5
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Na prviot grafik ne e pretstavena z
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552 Da se presmetaat i analiziraat
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FMo 9, 07 3 CMo 0, 169 kmol/m .
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povtorno treba da se re{at ravenkat
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da se odviva taka vleznata temperat
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560 ~ , i iC P 35 12, 518 0, 05
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Vremeto na nestacionarniot period n
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564 C C C Ao Bo Mo F F Ao o Bo
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Kako {to se gleda od dobienite rezu
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Zada~a 11 568 Proizvodstvo na akril
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na izreagiran propilen (AK/P 0,82-
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se dobivaat preku stehiometriskite
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Granicite za re{avawe na ravenkite
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578 T(V) Grafik 2. Promena na tempe
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turata e T 520 K. Vo ovaa presmetk
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smesa moè da se izrazi preku edins
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inerti i amonijak. Koga vtoroto e s
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586 k1 pC 2 R 0 K P ( atm ) ; (
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duvanata reakcija. Ovaa operacija t
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I dvata grafika, 2 i 3, pokaùvaat
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( r A 592 F C F F F F To T T F
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Sledniot ~ekor e da se sostavat mol
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na i specifi~nata povr{ina na topli
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[5] k1 = 1.79*(10^4)*exp(-20800/1.9
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Stepen na konverzija na azot Stepen
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602 1) UaV = 25000 kJ/(m 3 ·h·K)
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LITERATURA 1. Levenspiel, Octave, C
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ISBN 978-608-65044-3-4
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HEMISKI Zbirka re{eni zada~i REAKTORI 3

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