Dimensionarea Serpentinei Unui Cuptor de Piroliza a Benzinei

5/25/2018 Dimensionarea Serpentinei Unui Cuptor de Piroliza a Benzinei

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Tema proiectului:

Dimensionarea serpentineunui cuptor de piroliz a

benzinei.



2

CUPRINS

1.Obiectivul proiectului.Date iniiale de proiectare42. Consideraiigenerale privind procesul de piroliz83. Calculul proprietilormateriei prime.....103.1. Densiti.10

3.2. Temperaturi medii de fierbere funcie de temperatura de fierbere(ASTM) medie volumetric ...113.3. Factor de caracterizare (Watson) ...123

.4. Masmolarmedie.

.

..

12

3.5. Raport....133.6. Curba VE (vaporizare la echilibru)....133.7. Curba VE la presiune diferit de ceaatmosferic..153.8. Vscoziti... .....................17

4. Calculul de dimensionare al cuptorului de piroliz .......194.1.Zona de convecieZC..........194.1.1.Calculul serpentine n sectorul 1 din zona de convecie ZC194.1.2. Calculul serpentine n sectorul 2 din zona de convecie ZC......214.1.3. Calculul serpentine n sectorul 3 din zona de convecie ZC..24

4.2.

Zona de radiaie ZR.28

4.2.1.Entalpia de reacie. Entalpiaamestecului de reacie..284.2. 2Calculul serpentine n sectorul 1 din zona de radiaie ZR...334.2.3.Calculul serpentine n sectorul 2 din zona de radiaie ZR...364.2.4.Calculul serpentine n sectorul3 din zona de radiaie ZR....39

5. Breviar de rezultat...406.Bibliografie



3

1 OBIECTIVE: Stabilirea numrului de serpentine nparalel; Dimensionarea serpentinei: determinarea lunigimii acesteia n ZC, ZR;numrcoturi; bilanurimasice, termice pe serpentin; determinarea parametrilor de funcionare presiune, temperatur de-a

lungul serpentinei;

estimare VV (LHSV, h-1 i a timpului total de staionaren zona dereacie.

D TE INII LE DE PROIECT RE:1) Caracteristici ale materiei prime (benzin)

- curba de distilare ASTM (STAS):Nr.Crt. %Vol. distilat Temperatura, 1 0 602 5 693 10 754 20 855 30 926 40 1007 50 1088 60 116

9 70 12410 80 13411 90 14412 95 15113 100 160



4

Fig1.Curba de distilare ASTM (STAS)

- Densitate (relativ): d ,74

2) Parametri de funcionare a cuptorului

Capacitate de prelucrare: 120 000 t/an; Duratanual de funcionare: 8 000 h/an; Temperatura n alimentarea cuptorului: tiC= 100; Presiunea n alimentarea cuptorului: piC= 5,5bar a; Temperatura la care ncep reaciile (temperatura la intrare n zona de reacie): tiR= 650; Raport (la intrarea n ZR): ra = 0,6 kg/kg; Tensiuni termice n zona de convecie (ZC): 79 62 ; Tensiuni termice n zona de radiaie (ZR): 318 47 ; Sarcinmaximpentru o serpentin: Smax= 2 500 kg/h; Conversie final (la ieire din ZR): xcf= 0,84; Se admite o distribuie a produilor de reacieconstant de-a lungul serpentine n ZR

(deci dependent de conversiaxc) iidentic cu cea de la ieirea din ZR.

0

20

40

60

80

100

120

140

160

180

0 20 40 60 80 100

Temperatura,

%Vol. distilat



5

Tabel.Compoziieeflunet (gaz cracat uscat) ZR.

Nr. Component Compoziie,%mas

Masmolar

1 Hidrogen H2 0,50 2,0162 Metan CH4 5,20 16,0433 Acetilen C2H2 0,40 26,0384 Eten C2H4 25,00 28,0545 Etan C2H6 4,10 30,0706 Propen C3H6 18,40 42,0817 Propan C3H8 2,60 44,0978 C4

(C3H4; C4H4; 1-C4H6; 1,2-, 1,3-C4H6)C4H5 7,70 53,084

9 Butene(1-C4; cis-, trans-2-C4; i-C4)

C4H8 7,40 56,108

10 Butan (n+i) C4H10 4,70 58,12311 Benzin - 16,00 (xcf) (MP)12 Combustibil lichid greu - 8,00 250

Pentru fracia combustibillichid rezultat din reacie se cunosc:d ,9153 i 11,17 11,1685.3) Caracterisitici constructive

Dimensiuni tuburi: Diametru interior di = 80 mmDiametru exterior de= 100 mmLungime Lu = 8 m

4) Cinetic

Se admite o cineticaparent (global) de ordin I pentrupiroliza benzinei: k C

Unde: Rviteza de reacie, ;

Cbzcencentraiematerieprim (benzin),

.

Ecuaiacinetic se poatescrie sub formintegrat:ln k , sau x c 1 eUnde: xcconversia benzinei;

timp, s;kconstanta de vitez, s-1;

Respect o dependen Arrhenius detemperatura, cu:



6

A 1 , 7 7 8 1 s; Ea21,3 ;Dependencepoate fi redati sub forma din relaiaurmtoare:

lgk 11,25197

T

5) Proceduri de calcul. Prezentarea proiectului.

Se folosesc proceduri de calcul simplificate, de exemplu cea pentru serpentine n zona deradiaie.Pentrumaterii prime hidrocarburi inferioare sau fraciiuoare, la calculul ZRse pot folosii modele mai simple sau modele cinetice detaliate i procedurile avansate de calcul oferite deprograme specializate precum ChemKin.



7

2 Consideraiigenerale privind procesul de piroliz

Piroliza,cunoscuti sub denumirea de cracare termic la presiunijoase,este procesul dedescompunere termic a hidrocarburilor,care se desfoarn fazvapori la temperaturimai maride 800C,la presiunijoase,sub 5atm,n scopul obineriiolefinelor inferioare folosite ca materiiprime n petrochimie.

Materiile prime constau din etan,propan,n-butan i amestecuri ale acestora;bezineprimare(nafta);rafinatul liber de aromatice al benzinelor din RC;benzene hidrogenate proveninddin procesele de cracare termic(reducerea de vscozitate,cocsare),motorine DA imotorineDV,ca atare sau dezamortizate i desulfurizateparialprin hidratare.n unele dinprocesele de pirolizneconvenionale se urmretepiroliza ieiuluii a produselor rezidualerezultate din prelucrarea acestuia.

Materia prima se caracterizeazprin coninutul de componenipuri,n cazul alimentriicu C2,C3,C4 sau cu amestecuri ale acestora.

INST L I DE PIROLIZSchema unei instalaii de piroliz a benzinei,redus la parile component eseniale,este

redat in figuraurmtoare ,distingndu-se seciacaldi seciarece a instalaiei.

Fig. Schema de principiu,redus a uneiinstalaiitipice de piroliz,cuindicarea secieicalde

i reci.

1-cuptor2-generator de abur3-coloan de fracionare4-compresor5-secie de fracionare



8

Instalaiacuprinde urmtoareleseciiprincipale: -secia de pirolizpropriu-zis; -secia de pretratarei comprimare a gazelor de piroliz; -secia de recuperare a produselor utile din gazele de piroliz.

Dupmpdul n care se asigurclduranecesarreaciilor de piroliz,instalaiile industrial pot fi:

-instalaii cu cuptor tubular; -instalaii cu purttor de cldurn strat mobil; -instalaii cu purttor de cldurn strat fluidizat.

n prezent cele mai rspnditesunt instalaiile cu reactor de tip tubular care permit utilizareauneigame largi de materii prime(gazoase i lichide) i o variaielarg a parametrilor de funcionare.

Seciunetipicunui cuptor de piroliz1-serpentin de reacie

2-serpentin de prenclzire3-arztoare laterale4-arztoare de podea5-zidrie refractar6-schelet de rezisten7-pode de deservire8-scar de accesarztoare9-suspensie eviradiaie10-gur de acces11-clanpet de observaie12-evi prnclzireapdemineralizat

13-evi prenclzireaburi14-rcitor de gazcracat15-colector de abur16-ghidaj



9

3.Calculul proprietilormateriei prime3.1 Densiti

Convertirea unei densiti relative naltapoate fi fcut cu una din ecuaiile:d ,74d,, ,9952d ,86d,, ,745d,, 1,1d, d, ,744d,, ,9915 ,86 ,742 gml 20 este densitatea produsului petrolier n stare lichid, g/ml, la 20.Densitatea API se determinn funcie de densitatearelativd,,cu relaia:API 141,5

d,, 131,5API58,558

Variaiadensitii, L, kg/m3, a unei fraciunipetroliere sau a unui iein fazlichid cutemperatura poate fi estimat cu funcia:

d, t d 1 t 2 2,296,34d 5,965 dNr. Crt %Vol.distilat Temperatura, Temperatura, K1 0 60 333,152 10 75 348,153 30 92 365,154 50 108 381,15

5 70 124 397,156 90 144 417,157 100 160 433,15

d, t ,741 6 2 2,296,34,745,965,74 75,774 kgmd, t ,741 7 5 2 2,296,34,745,965,74692,939kgmd, t ,741 9 2 2

2,296,34,745,965,74 678,393 km

d, t ,741 1822,296,34,745,965,74 664,72 kmd, t ,741 12422,296,34,745,965,74 651,12 kmd, t ,741 14422,296,34,745,965,74 633,899 kmd, t ,741 1622,296,34,745,965,74 62,28 km



10

Fig.Variaiadensitiiunei fraciunipetroliere n fazlichid cu temperatura.

3.2.Temperaturi medii de fierbere funcie de temperatura de fierbere(ASTM) medie volumetric

Panta: pa pa,8625 tmVf 7 5 9 2 1 8 1 2 4 1 4 45 18,6tmMftmVf,3161379e,,

18,6,3161379e,,,, 1,367

tmftmVf2,5993481

e,,

18,62,5993481 e,,,,11,635

600

620

640

660

680

700

720

50 70 90 110 130 150 170

L,

kg/m3

Temperatura,



11

tmCftmVf,4388152e,, 18,6,4388152e,, ,,

16,518

tmMeftmVf,2161448e,,18,6,2161448e,,,,13,43tmMef tmMftmCf2 1,36716,5182 13,443tmVf este temperature medie volumetric (ASTM);tmMf este temperature medie molar;

tmWf este temperature medie greutate (mas, ponderat);tmCf este temperature medie cubic;tmMef este temperatura de fierbere medie a mediilor.

3.3.Factor de caracterizare (Watson)

Relaiarecomandatn prezent pentru stabilirea factorului de caracterizare este:

1,8 tmMef273,15

d,, 1,813,443273,15

,74511,791

3.4.Masmolarmedie

Masa molarmedie a unei fraciunipetroliere se poate determina cu relaia:

Mm(d,,,TmMef)42,9654TmMef, (d,,), e(,,,,,,,)42,9654376,593

, ,745

, e(,,,,,,,) 12,481TmMef tmMef 273,15 13,443 273,15 376,593

Astfel, relaia se poateutilize pentru TmMef cuprinsntre 305 K i 838 K (32-565 ),d,,ntre 0,63i 0,97i Mm = 70 700, cu o eroare de max. cca 7%.



12

3.5.Raport

Raportul masicdin molecula medie de hidrocarbur se poate determina cu relaia:

Rw 8,77431 e(,,,,,,,) Tb, (d,,),8,77431 e(,,,,,,,)381,15, ,745, 5,581T b t 273,1518273,15381,15 Cunoscnd raportul masic

, raportul dintre numrulde atomi de H icel de C poate fi calculat curelaia:

Ra AA 1Rw 12,111,8 15,581 2,135Unde Aci AH sunt masele atomice ale carbonului, respective hidrogenului.A 12,11 i A 1,83.6.Curba VE (vaporizare la echilibru)

Curba VE a fraciuniipetroliere se poate determina prin calcul, pe baza curbei de distilareASTM, cu ajutorul metodei Riazi-Daubert. Aceasta foloseteurmtoarelerelaiipentru gsireatemperaturilor, TiVE, K, de pe curba VE, plecnd de la temperaturile TiASTM, K, de pe curbaASTM.

T A T (d,,)Coeficienii Ai, BiiCisunt dain urmtorultabel.

Tabel.Coeficieni din relaiepentru convertirea curbei de distilare ASTM la curba VE.

I %Vol.distilat

Ai Bi Ci Domeniu de temperatur(ASTM),

1 0 2,9747 0,8466 0,4209 102652 10 1,4459 0,9511 0,1287 603203 30 0,8506 1,0315 0,0817 903404 50 3,2680 0,8274 0,6214 1103555 70 8,2873 0,6871 0,9340 1304006 90 10,6266 0,6529 1,1025 160520

7 100 7,9952 0,6949 1,0737 190430



13

T 2,9747 6273,15, ,745, 359,17 T 1,4459 75273,15, ,745, 364,955 T ,856 92273,15, ,745, 365,149 T 3,268 18273,15, ,745, 371,911 T 8,2873 124273,15

,

,745,

384,369

T 1,6266 144273,15, ,745, 394,671 T 7,9952 16273,15, ,745, 396,62

%Vol.distilat

Temperatura pe curba VE lapresiunea atmosferic, K

Temperatura pe curba VE lapresiunea atmosferic,

0 359,170 86,0210 364,955 91,80530 365,149 91,999

50 371,911 98,76170 384,369 111,21990 394,671 121,521100 396,062 122,912

Fig.Curba VE la presiune atmosferic.

0

20

40

60

80

100

120

140

0 10 20 30 40 50 60 70 80 90 100

Temperautra,

%Volum



14

3.7.Curba VE la presiunediferitde cea atmosferic

Relaiaurmtoarepoate fi utilizatpentru determinarea curbei VE la diferite presiuni p,bar, pe baza curbei VE la presiune atmosferic.

Logp 3,2411,998 Tnf41Tf 4 1 1393Tf1393TnfTf 1393 , , 1 1 , , 1 Presiunea: p 5,3 bar

Tf 1393

, ,

, 1 ,

,1 , ,, 1 ,, 425,18 Tf 1393 , ,, 1 ,,1 , ,, 1 ,, 431,638

Tf 1393, ,, 1 ,,

1

, ,

, 1 ,

,

431,857

Tf 1393 , ,, 1 ,,1 , ,, 1 ,, 439,471

Tf 1393, ,, 1 ,,1 , ,, 1 ,, 453,445

Tf 1393

, ,

, 1 ,

,1 , ,, 1 ,, 464,949 Tf 1393

, ,, 1 ,,1 , ,, 1 ,, 466,498



15

%Volum Temperatura pe curba VE lapresiunea de 5,3 bar, K

Temperatura pe curba VE lapresiunea de 5,3 bar,

0 425,108 151,95810 431,638 158,48830 431,857 158,707

50 439,471 166,32170 453,445 180,29590 464,949 191,799100 466,498 193,348

Fig.Curba VE la presiunea de 5,3 bar

3.8.Vscoziti

Vscozitatea cinematic, L, m2/s, a unei fraciunipetroliere lichide la diferite temperaturi

t, , se poate exprima cu relaia:(d,,, , t ) 11,766(d,, ), 29,263 1 xv(d,,, ) e,

,,

Unde:xv(d,,, ) e*,,(,,)+ xv(d,,, )812,344Relaievalabilpentru:( d,,) 1 , 7 4 11,791,745 1,748,7841,74

0

20

40

60

80

100

120

140

160

180

200

0 10 20 30 40 50 60 70 80 90 100

Temperatura,

%Volum



16

(d,,, , t) 11,766,74511,791, 29,263 1 11,791812,344 e ,,3,1981 m s

(d,,

, , t) 11,766

,74511,791, 29,2631 11,791

812,344 e,,

3,161 m s (d,,, , t) 11,766,74511,791, 29,263 1 11,791812,344 e ,,3,131 m s (d,,, , t) 11,766,74511,791, 29,263 1 11,791812,344 e ,,3,41 m s (d,,, , t) 11,766,74511,791, 29,263 1 11,791812,344 e ,,

2,8371

m

s

(d,,, , t) 11,766,74511,791, 29,263 1 11,791812,344 e ,,2,7141 m s (d,,, , t) 11,766,74511,791, 29,263 1 11,791812,344 e ,,2,6981 m s Metoda permite determinarea vscozitiicinematice, cSt, a unei fraciunipetroliere lichide pebaza t50%vol. distilate:

A eUnde: A 91,83Tb, 29,263 e,,Tb este temperatura, K, la 50% vol. distilate.Tb 439,471 e,,, 1128,47

A

91,83439,471

,

29,263

11,791

1128,47 A

,25

A e ,25e,, ,325 cSt



17

4.Calculul de dimensionare al cuptorului de piroliz

4.1. Zona de convecie

10 serpentine n paralel 1 15 kgh ra 1 5 kgh ,6 kg aburkg mp 9 kgh mprimserpentina n trei zone:

Zona n care au loc fenomenef izicenclzireabenzinei n stare lichidpn la t0%VElap=5,3 bar;

Zona de vaporizare i nclzire a benzineipn la t100%VEla p=5,3 bar; Zona de serpentinn care are loc nclzireabenzinei n stare vapori.

4.1.1.Calculul serpentinensectorul 1 din zona de convecie (ZC)

tic=100Cpic=5,5 barti2c=t0%VE(5.3)=151.958C

p p

p

p

p

Ecuaia de bilantermic pe sectorul 1: h Q hQ d LEntalpia amestecurilor complexe de hidrocarburi (fraciunilorpetroliere) n stare lichid, kJ/kg, lao temperatur t, , se poate stabili cu ecuaiasimpl:I(d,,, , t)[(2,9641,332d,,)t(,374,1154d,,) t]

,538 ,3544

Cu originea IL=0 pentru lichid la 0I(d,,, , t) 2,9641,332,745 1 ,374,1154,745 1 ,53811,791,3544 216,842kjkg



18

I(d,,, , t) 2,9641,332,745 151,958 ,374,1154,745151,958 ,53811,791,3544 346,795 k kg

L (h

h

) d 15346,795216,842 ,17962 7,793 mCderea de presiune, p, pentrucurgerea la interiorul conducteipoate fi determinat cu ajutorulecuaiei:

p Ld w2

Coeficientul k de rugozitate pentru conductele de oeln exploatare are valoarea: k=5 m

, 1 kd,

, 1 5,8,

,366

Variaiadensitii, L, kg/m3, a unei fraciunipetroliere se calculeaz cu relaia:

d, t d 1 t 2 2,296,34d 5,965 dd, t ,741 122,296,34,745,965 ,74671,547 kgm

d

, t ,741151,9582

2,296,34,745,965 ,74627,89 kgm 2 671,547627,892 649,318kgm w

36

4 36 d 41536 ,8 671,547 , 1 2 3 m s

w 4 36 d 41536 ,8 627,89 , 1 3 2 m s w w w2 ,123,1322 ,1275 ms p Ld w

2 ,366 7,793,8 649,318,12752 18,816 Pa



19

Re d w

Re d w

t 1t 151,958t t t2 1151,9582 125,979(d,,, , t) 11,766,74511,791, 29,263 1 11,791812,344 e ,,3,6211 m s

Re d w ,8,12753,6211 28169,14 23 Regim turbulent, chiar rugozQ d L 7962 ,17,7931,9491 k h 4.1.2. Calculul serpentine n sectorul 2 din zona de convecie (ZC)

ti2c=151.958Cpi2c=5.499 barti3c=t100%VE=193.34 barpi3c=5.3 bar

p 18,816 Pa 1,882 1barp p p 5,51,8821 5,499 bar d L ( h)

I(d,,, , t) 2,9641,332,745 151,958 ,374,1154,745151,958 ,53811,791,3544 346,795 k kg Pentru fraciunipetroliere vapori, entalpia specific, kJ/kg, se poatecalcula cu relaia:

I(d,,, , t)532,1721,61d,, (1,8213,45638d,,) t(,23447,5937d,,) t 4,187t837 ,7 ,84



20

I(d,,, , t)532,1721,61,745 1,8213,45638,745 193,348 ,23447,5937,745 193,348 4,187193,348837 ,711,791,84 733,283 k kg d L ( h) 7 9 6 2 , 1 L15 733,283346,795 L 23,176 mNumr de coturi: n1C=0

n2C=3

L 7 5 dL L n 7 5 d 23,176 3 75 ,8 41,176 m

p

Ld

w

2

627,89 kgm p MR T p p MR T 2 w w w2

p L 36

d

1 M p 1 p

R T 1 R T1 M p 1 p ,36641,1761536 ,8627,89 112,481 5,4991 p8,314466,498 1627,89 8,314466,498112,481 5,4991 p

p 28532,5 Pa ,285 barw 4 d 36 4 M d 36 415,,, 12,481 ,8 36 6 , 6 m s



21

w w w2 ,1326,62 3 , 6 9 m s

p

p MR T 5,499,285 12,481,83466,498 13,8 kg m

2 627,8913,82 32,444 kg m t 151,958t 193,348t t t2 151,958193,3482 172,653

(d,,, , t) 11,766,74511,791, 29,263 1

11,791812,344 e,

,2,9261 m s Re d w ,83,692,9261 83997,7423Regim turbulentQ d L 7962 ,123,1765,7971 k h

4.1.3. Calculul serpentine n sectorul 3 din zona de convecie (ZC)ti3c=193.348Cpi3c=5.214 bartiR=650C

p p p 5,499 ,285 5,214 bar d L ( )I(d,,, , t)532,1721,61,745 1,8213,45638,745 193,348

,23447,5937,745 193,348 4,187193,348837 ,711,791,84 733,283 k kg I(d,,, , t)532,1721,61,745 1,8213,45638,745 65 ,23447,5937,74 65 4,18765837 ,711,791,84 2116,594 k kg



22

d L ( ) 7 9 6 2 , 1 L15 2116,594733,283 L 82,954 mn 11 coturiL 7 5 d

L L n 7 5 d 82,9541175,8148,954 mp R L 136 d M pT p 1

pT Tp Tp 1 p

,3668,31415 148,954136 ,8 12,481 5,214466,498 5,2141 p923,15

466,498

5,214 923,15

5,2141 p

p 3139,5 Pa ,31 barw 4 d 36 4 M d 36 415,,, 12,481 ,8 36 6 , 6 m s

pR T M 5,214,83466,498 12,481 13,8 kg m

t 193,348t 65t t t2 193,348652 421,674T 694,824 Pentru determinarea vscozitiidinamice a unei fraciunipetroliere vapori, V, la presiuni joase(sub 5-10 bar) se poate utilize relaia:

M

, T ,92696,13835,97121

M

T

1,12491

MM, T,92696,13835,97121 12,481694,8241,12491 12,481 ,124 cP 1,24 1 k g m s



23

M, T ,92696,13835,97121 12,481923,15 1,1249 1 12,481 ,155 cP 1,55 1 k g m s

M

, T

M

, T

2 1,241

1,551

21,3951 k g m s p p p 5,214 ,31 4,913 barw 4 d 36 4 M d 36 415,,, 12,481 ,8 36 1 2 , 6 1 4 m s

w w w2 12,6146,62 9 , 3 1 m s p p MR T 5,214,31 12,481,83923,15 6,571 kgm 2 13,86,5712 1,185 kg m

Re

d

w

,89,311,1851,3951 543784,8

i: Q d LQ e: Q

d L Q d L 7962 ,182,9542,741 k h I(d,,, , t)

532,1721,61,745 1,8213,45638,745 193,348 ,23447,5937,745 193,348 4,187193,348837 ,711,791,84 733,283 k kg Q 15733,2831,991 k k g



24

I(d,,, , t)532,1721,61,745 1,8213,45638,745 65 ,23447,5937,745 65 4,18765837 ,711,791,84 2115,346 k kg Q 15 2115,346 317319 k kg

4.2. Zona de radiaie (ZR)MP,84g ,5g C,52g C,4g C,25g C,41g C,184g C,26g C,77g C,74g C,47g comb,8g

C,,

Compoziie, entalpieamestec de reaciefuncie de conversiacurent.I ig Comp Mi

g/molgfi(xcf=0,84)g/g MP alim

n gM10-3mol/gMP alim

gx gx x g/g MP alim

nx gxM1 0 H2 2,016 0,005 2,480 ,5,84 x ,5,84 x2,162 1 CH4 16,043 0,052 3,241

,52,84 x

,52,84 x

16,43 2 C2H2 26,038 0,004 0,153 ,4,84 x ,4,84 x26,34 3 C2H4 28,054 0,250 8,911 ,25,84 x ,25,84 x28,55 4 C2H6 30,070 0,041 1,363 ,41,84 x ,41,84 x3,76 5 C3H6 42,081 0,184 4,372 ,184,84 x ,184,84 x42,87 6 C3H8 44,097 0,026 0,589 ,26

,84 x

,26,84

x44,98 7 C4H5 53,084 0,077 1,450 ,77,84 x ,77,84 x53,8

9 8 C4H8 56,108 0,074 1,318 ,74,84 x ,74,84 x56,110 9 C4H10 58,123 0,047 0,808 ,47,84 x ,47,84 x58,12



25

11 MPbenzin

102,481 0,160(1-xcf)

1,561 1 x 1 x12,48112 Comb 250 0,080 0,320 ,8,84 x ,8,84 x2513 H2O 18,015 0,600

(ra)

33,305 ra

ra18,15

1,600(1+ra)

59,871 1,600(1+ra) ,216x,43635

nxc ,216x ,43635 mol g MP alim M y M nxcnxc M

Mxc 1 r anxc 1 , 6,216x ,43635 1,6,216x ,43635

4.2.1.Entalpia de reacie. Entalpiaamestecului de reacie

T

C p

TdT

1

1

CpT a b T c T 11,1685d ,9153d, , ,9189CpT 27,7473,389851 T T 27,7473,389851 T

dT 111,694931 T ,27747 T 8,4652 k mol CpT 22,347948,12751

T

T 7 4 , 5 2 22,347948,12751 T dT 11,24637T ,223479 T 83,3166 k mol CpT 27,9696,23621 T19,467621 T



26

T 2 2 8 , 2 27,9696,23621T19,467621 T

dT 116,489211T ,31181T ,27969T

217,365 k mol

CpT 1,8667121,6881 T37,565251 T T 5 2 , 5 1 1,8667121,6881T37,565251T dT

111,252171T ,6844T ,18667T 44,22 k mol CpT 1,2338158,1231 T45,56651 T T 8 3 , 8 2 1,2338158,1231T45,56651T

dT 111,518691T ,79615T ,12338T 93,4888 k mol CpT 13,492519,97261 T59,163551 T

T 1 9 , 7 1 13,492519,97261T59,163551T

dT 111,972121T ,954863T ,134925T 7,73156 k mol CpT 1,8549237,63171 T72,911231 T

T 14,68 1,8549237,63171

T72,911231

T

dT 1

12,43371T ,118816T ,18549 T 117,823 k mol CpT 24,6162185,6851 T6,875261 T T 186,11 24,6162185,6851T6,875261T

dT 112,29181T ,92843T ,246162T 171,67 k mol CpT 16,9533258,81191 T79,779591 T

T 9 , 1 16,9533258,81191T79,779591T

dT 112,659321T ,12946T ,169533 T 24,851 k mol CpT 15,579312,3731 T98,17211 T



27

T 129,985 15,579312,3731T98,17211T

dT 113,27241 T ,15619T ,15579T

147,617 k mol

T T 1 M1 Ct dT1 M1 (1,69578,2939 ,45638d,,) dT M1

1 (4,68941,1874d,,)T 2 7 3dT

1 12,4811 1,69578,293911,791,45638,745 dT 12,4811 1 4,68941,1874,745T 2 7 3dT

,195213T ,38947 T 128,94 k mol

T T

1 M1 (1,69578,2939 ,45638d,

,

) dT

M1 1 (4,68941,1874d, , )T 2 7 3dT

1 251 1,69578,293911,1685,45638,9189dT

251 1 4,68941,1874,9189T 2 7 3dT

,45552T ,435555 T 47,96 k mol

Cp T 34,4,627751 T5,6791 T



28

Q 1M CTdT

118,15 34,4,627751 T5,6791 TdT

1,37641 T ,17423T 1,9952T 1,3764 1 T ,17423T 1,9952T k k g i Comp k m o l Tk m o l

1 H2 0 1,694931 T ,27747T8,46522 CH4 -74,52 ,24637T ,223479T83,31663 C2H2 228,2

6,489211

T

,31181T

,27969T217,3654 C2H4 52,51 1,252171T ,6844T ,18667T44,225 C2H6 -83,82 1,518691T ,79615T ,12338T93,48886 C3H6 19,71 1,972121T ,954863T ,134925T7,731567 C3H8 -104,68 2,43371T ,118816T ,18549T117,8238 C4H5 186,11 2,29181T ,92843T ,246162T

171,67

9 C4H8 -9,01 2,659321T ,12946T ,169533T24,85110 C4H10 -129,985 3,27241 T ,15619T ,15579T147,61711 MP

benzin-100 ,195213T ,38947T128,94

12 Comb 100 ,45552T ,435555T47,9613 H2O -241,814

i Comp

1 nxx

k kg MP reacionat 1 H2 5,842,16 1,694931 T ,27747T8,46522 CH4 52,8416,43 ,24637T ,223479T83,3166



29

3 C2H2 4,8426,38 6,489211T ,31181T ,27969T217,3654 C2H4 25

,8428,54 1,252171

T

,6844T

,18667T44,225 C2H6 41,843,7 1,518691T ,79615T ,12338T93,48886 C3H6 184,8442,81 1,972121T ,954863T ,134925T7,731567 C3H8 26,8444,97 2,43371T ,118816T ,18549T117,8238 C4H5

77,8453,84 2,29181T ,92843T ,246162T171,679 C4H8 74,8456,18 2,659321T ,12946T ,169533T24,85110 C4H10 47,8458,123 3,27241 T ,15619T ,15579T147,61711 MP

benzin 112,481

,195213T ,38947T128,9412 Comb 8,8425 ,45552T ,435555T47,9613 H2O 3,866911 T ,23842T ,1363T1358,52 T 3,866911T ,23842T ,1363T1358,52

i Comp x, T 1 nx k kg MP alim sau k kg prod de reac

ie

1 H2 5 x,842,16 1,694931 T ,27747T8,46522 CH4 5 2 x,8416,43 ,24637T ,223479T83,31663 C2H2 4 x,8426,38 6,489211T ,31181T ,27969T217,365



30

4 C2H4 2 5 x,8428,54 1,252171T ,6844T ,18667T44,225 C2H6 4 1 x

,843,7 1,518691

T

,79615T

,12338T93,48886 C3H6 1 8 4 x,8442,81 1,972121T ,954863T ,134925T7,731567 C3H8 2 6 x,8444,97 2,43371T ,118816T ,18549T117,8238 C4H5 7 7 x,8453,84 2,29181T ,92843T ,246162T171,679 C4H8

7 4 x,8456,18 2,659321T ,12946T ,169533T24,85110 C4H10 47 xc

0,84 58,123 3,2724 108 T3 0,000156019 T2 0,015579 T 147,61711 MP

benzin1000 1 xc

102,481 0,000195213 T2 0,0389407 T 128,9412 Comb 80 xc

0,84 250 0,000450552 T2 0,0435555 T 47,009613 H2O

3,86691 107

T3

xc 0,00023804 T2

xc 0,00190487 T2

0,10363 T xc 0,37998 T 1358,52 xc 1258,18Entalpia amestecului la o anumittemperatur:Hhspxc, T 3,86691 107 T3 xc 0,00023804 T2 xc 0,00190487 T2 0,10363 T xc 0,37998 T 1358,52 xc 1258,18 kJ kg MPalimsau kJ kg proddereacie

4.2.2.Calculul sperpentinei n sectorul 1 din zona de reacie (ZR)

t 65 923,15 p 4,913 bar 1 5 k g h ra , 6Bilantermic pe sector: x, T



31

(x , T)15 3,866911 923,15 ,2384923,15 ,19487923,15 ,1363923,15,37998923,151358,521258,18 1,739141

k h

Presupunem: t 725xc ,16382

xc xc xc ,16382 xc, T15 3,866911 998,15 ,16382,2384998,15,16382,19487998,15 ,1363998,15,16382 ,37998 998,15 1358,52 ,16382 1258,181,7381581 k h

Q ra C TdT,,15,6 1,37641 T ,17423T 1,9952T 1,3764 1 T ,17423T 1,9952T15,6 1,37641 923,15 ,17423923,15 1,9952923,151,37641 998,15 ,17423998,15 1,9952998,15 15553,8 k h

Q xc 657252 273,1515,16382 3,866911 96,65 ,2384296,65 ,136396,651358,52 21319,42 k h Calculmlungimea sectorului pe baza ecuaiei de bilantermic:

Q Q Q1,739141 Q 1,7381581 15553,821319,42Q 1,27821 k h Q d L



32

L Q Q d 1,7381581 15553,821319,421,739141 ,131847

1,273 m

n 1L L n 7 5 d 1,273 1 75 ,8 16,273 mMxc 1,6,216,43635 37,154Mxc 1,6,216,16382,43635 35,43p R L 1 r a

d

36

p 1 MxcT 1 p p Mxc1T Tp 1 Mxc 1T1 p p Mxc

,366 8,31416,27315 1 , 636 ,8 4,913137,154923,15 1 4,913 p 35,431998,15

923,15

4,913137,154 1998,15

1 4,913

p 35,43

p 376 Pa ,37 bar p MR T 4,91337,154,83923,15 2,382 kgm p p MxcR T 4,913,37 35,43,83998,15 1 , 9 6 8 k g m

2 2,3821,9682 2 , 1 7 5 k g m

w 4 1 r a36 d 4151,6362,382 ,8 5 5 , 6 7 9 m s w 4 1 r a36 d 4151,6361,968 ,8 6 7 , 3 9 2 m s w w w2 55,67967,3922 6 1 , 5 3 5 m s



33

Lw 1,27361,535 ,166 s

Verificarea presupunerii fcute:lg 11,25 197T T 657252 273,15 96,65 lg 11,25 197T T,677

xc 1 e

1 e,,

,16297

Presupus: xc ,163824.2.3.Calculul serpentine n sectorul 2 din zona de radiaie (ZR)

1 5 k g h T 998,15 1,7381581 k h p p p 4,913 ,37 4,66 barxc xc ,16382,16382Presupunem:

t 761

xc ,4383xc xc xc ,16382,4383,536465 Bilantermic pe sector:i: xc, T xc, T15 3,866911 998,15 ,16382,2384998,15,16382,19487998,15 ,1363998,15,16382 ,37998 998,15 1358,52 ,16382 1258,18

1,7381581

k h

xc, T15 3,866911 134,15 ,536465,2384134,15,536465,19487134,15 ,1363134,15,536465,37998134,151358,52,5364651258,18 2,798981 k h



34

Q ra C TdT,

,15,6 1,37641

T

,17423T

1,9952T 1,3764 1 T ,17423T 1,9952T15,6 1,37641 998,15 ,17423998,15 1,9952998,151,37641 134,15 ,17423134,15 1,9952134,15 73431,4 k h

Q xc 7257612 273,1515,4383 3,866911 116,15 ,23842116,15 ,1363116,151358,52 841168,85 k h

Calculmlungimea sectorului pe baza ecuaiei de bilantermic Q Q QL Q Q d 2,798981 73431,4841168,851,7381581

,131847 19,73 m

n 2L L n 7 5 d 19,73 2 75 ,8 31,73 mMxc 1,6,216,16382,43635 35,43Mxc 1,6,216,536465,43635 29,739



35

p R L 1 r a d 36 p 1 MxcT p 1 p MxcT 1

Tp 1 Mxc Tp 1 p Mxc,366 8,31431,7315 1 , 636 ,8 4,66135,43998,15 1 4,66 p 29,7391134,15 998,154,66135,43 1134,151 4,66 p 29,739

p 8528,2 Pa ,852 bar

p p MxcR T 4,913,37 35,43,83998,15 1 , 9 6 8 k g m p p MxcR T 4,66,852 29,739,83134,15 1 , 3 6 kgm 2 1,9681,362 1 , 6 3 4 3 kgm

w 4 1 r a36 d 4151,6361,968 ,8 6 7 , 3 9 2 m s w 4 1 r a36 d 4151,6361,36 ,8 1 1 , 9 7 5 m s w w w2 67,39211,9752 8 4 , 6 8 3 5 m s L

w 19,73

84,6835 ,232 s

Verificarea presupunerii fcute:lg 11,25 197T T 7257612 273,15 116,15



36

lg 11,25 197T T2,846xc 1 x c ( 1 e) 1,16382 1 e,, ,431876Presupus:

xc ,4383

4.2.4.Calculul serpentine nsectorul 3 din zona de radiaie (ZR)

1 5 k g h T 134,15 2,798981 k h p p p 4,66 ,852 3,754 barxc xc xc ,16382,4383,536465 Presupunem: t 828,622

xc xc xc ,84,536465,33535

t 828,622T 828,622 273,15 111,772 Bilantermic pe sector: xc, T xc, T15 3,866911 134,15 ,536465,2384134,15 ,536465,19487134,15 ,1363

134,15,536465,37998134,151358,52,5364651258,18 2,798981 k h xc, T15 3,866911 111,772 ,84,2384111,772 ,84,19487111,772 ,1363111,772,84,37998111,7721358,52,841258,18 3,7772341 k h Q ra C TdT

,,

,15,6 1,37641 T ,17423T 1,9952T 1,3764 1 T ,17423T 1,9952T15,6 1,37641 134,15 ,17423134,15 1,9952134,151,37641 111,772 ,17423111,7721,9952111,772 1492,8 k h



37

Q xc 761828,6222 273,1515,33535 3,866911 167,961 ,23842167,961 ,1363167,9611358,52 57888,14 k h

Calculmlungimea sectorului pe baza ecuaiei de bilantermic Q Q QL Q Q d 3,7772341 1492,857888,142,798981

,131847 16,964 mn 2L L n 7 5 d 16,964 2 75 ,8 28,964 m

Mxc 1,6,216,536465,43635 29,739Mxc 1,6,216,84,43635 26,721p R L 1 r a d 36 p 1 MxcT p 1

p MxcT 1

Tp 1 Mxc Tp 1 p Mxc

,366 8,31428,964 15 1 , 636 ,8 3,754129,739134,15 1 3,754 p 26,7211111,772 134,153,754129,739 1111,7721 3,754 p 26,721

p 148746 Pa1,487 bar p p MxcR T 4,66,852 29,739,83134,15 1 , 3 6 kgm p p MxcR T 3,7541,487 26,721,83111,772 , 6 6 2 4 kgm 2 1,36,66242 , 9 8 1 5 kgm



38

w 4 1 r a36 d 4151,6361,36 ,8 1 1 , 9 7 5 m s

w 4 1 r a36

d 4151,6

36,6624

,8 2 , 2 2 5 m s

w w w2 11,9752,2252 1 5 1 , 1 m s Lw 16,964151,1 ,112 sVerificarea presupunerii fcute:lg 11,25 197

T

T 761828,6222 273,15167,961 lg 11,25 197T T9,58xc 1 x c ( 1 e) 1,536465 1 e,, ,33725Presupus: xc ,33535



39

5.Breviar de rezultate

Proprietilezonei de convecie:Sector

Parametru1 2 3

ti, 100 151,958 193,348pi, bar 5,5 5,499 5,214p, bar 1,882*10- 0,285 0,301L, m 7,793 23,176 82,954nc, coturi 0 3 11Lech, m 41,176 148,954Rem 28169,014 839097,74 543784,08Qf, kJ/h 1,949*10 5,797*10 2,074*10

Proprietilezonei de radiaie:Sector

Parametru1 2 3

ti, 650 725 761pi, bar 4,913 4,606 3,754p, bar 0,307 0,852 1,487L, m 10,273 19,73 16,964nc, coturi 1 2 2

Lech, m 16,273 31,73 28,964, s 0,166 0,232 0,112xc 0,106382 0,430083 0,303535xcv 0,106297 0,431876 0,303725

Dimensionarea Serpentinei Unui Cuptor de Piroliza a Benzinei

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