Laurito-STOICHIOMETRY of Fuel Combustion Etc. (1)

ffiYffitrffiffififfifu?ffiTffiY OF FUEL CCI\4tsUSTION AND RELATED PFIOCESS INDUSTRIES

Evelyrn Fl. Laurito Chernicai Ingineerlng Department Universify of Santo Tomas

f{#,"-l Book Store

ouAD ALpHA cEtur RuNl' ei"DG. 125 Pioneer St., [4andali.rvor]q City

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-

CCNTENTS

leol 3torc

ftilt

lt't'tNtl coPYRlcHT. 1994 bt F velvrr lt I aurito

Freface of Publicatioirr, i991 PA6F-

CHAPTER

ill r lElrlc rcserved. f{l

t Fpt

I

lrar I rrl this book may be

rNr*o,ucrtoN

lrlur.rr l in aly fbrm or by

i

1.1 1r)

Errr nlr,ril:;, r:xcept brief quotations l,rr,r I r'r,rrr!, without permission Irr r+r lltrrE lr.orn the Author.

COMPLE]E COMBUSTION THEOREnCAL OXTGEN . ."... ".".."..... THEORETIC-qL A]R FOl1 COMBUSTTON 1.5 PERCENT EXCESS AiR l.\.,

1

) 4 5

1.6 INCOMPTETE COidBUSTION

2 Ft l'li't ( r,r lilicate of HeEli-lrrrlr,rr No. SP 594

I ttnt, ,l l,t' !,;,r I .,,/,r rt', f ,i11111.1,;17phic ArLt & /)rittii;;g +'i 16,t1,i1,11t,',1 , lrrr1.t,. ,\on .IO.Se, l.{.'-. ' t I ',r'

GASEOUS FUEIJ 2.1 CLASSIFICATTON a) Nai.unl Gas". b) Manufactured

Gases

2.2 \TOLIJMR MEASUREMENI 2.3 CAII)RIFIC VALUES OF GASEOUS FUEIS ... ". 2.4 CArcUIA IONS BA.SEE ON FLJEL ANALYS;S ., 2.5 CAI-ORJFIC VALUE LOSSES a) Dr:e to Incomplete Coinbustjon... b) Due to Sensible Fleat;".":. c) Due to t-lnccndensed WaLer \/apor ):'rc,s.s

isBN 971-0&5782.7

6 6 6 7

I Ii

t5 i5 r6 t6

+.5 COAL COMBUSTION

CAiCULIiTIONS BI.SED Cl{ FLIJE GAS A}IAJJSIS ....

""""""'

COMBUSNBIES I,OST IN THE FEFUSE al Uncoked Cod I-ost i:: the $efuse,'",..":l,'."""""" b) Coked Coal lnst in the Refuse""..-""".'..;"..'."""" c) Combination of Coked and Uncoked Co-al "''""

29

LIOUID FUEI.S

5

3.1

3.4

3.5 CArcUIATIONS

BASED ON PARNAL ANALYSIS OF THE FLUE GAS..". 43 PROBWMS..........'. -...'-,. :...' i.'.'.. "' ""'' " ": :". "', " "' 47

60 62 62 62

62 78

Raw Sulfur Anatlsis' ".-.. ;...;-.. " " "'' " " " "' " "'' " " "' b)t Catculations Based on Andsis "'"""""""" of Bunrer G'as HfzuTES":"""""."""",;'r"' IRON 5.3 ROASTING OF 5.4 PRODUCTIGN OF H2S-O4 AND OLEI-llvl ' .' ,) Co.rt ct Process."...."-......'"" """"'.""'

81 81

82

84 86 90 90

' s.6 glsut,rrrr LIguoR

PRoDUCTIoIq " ............'.',.. 98 ...,..,-.-.-..r........ I01 QR]BLEMS "....."..""......

SOLTD FIJEI-s

4.2

tra

SIJLFUR AT{E' TTS COMPOUNDS

5.1 SULFIJR- COMPOUNDS ,."..'."......'"..'."'"'':" 5.2 BURNiNG OF nXW SUFUR ""....."-,".'.....'...'-:... a) Calculations Baslt' on

oa

t) ,,1, Qr)

r

.....1..-."

4.6 COAL COMBUSRON WITH

PROBIf,MS

4.

NO

PR.OBTEMS

ANALYSIS OF FLUE GAS...'".,,....

rt

}l/iTH

CON,IBUSTIBLES LOSI' IN LHE RI;FUSE

49 CLASSIFICATION OF SOLID FUEIS 49 ....,'..'. " "' " " Fuels " " " " " " " :" " a) Natural So1id j"""""' 49 Fuels """" b).arUficia.l Solid 50 FUEI,S".J............. ANALYSIS OF SOLID 50 a)' Proximate AnalYsis 50 """'"."""""',:' b) UlUmate AnaJysis 50

4.3 EMPIRICAL pguATioNS Oi{ coAL AI{ALYSIS AND CAI'ruFIC VALUES "...". ' a) Dulong's Ponnula

ui caa.riood

Equauon '.......-... COMBUSTION CAI'I,II.ATIONS .. "..

rrl

"'

PRODUCNON OF UME 6.1 LIME PRODUCilON .' "... :...;.,.....

6.2 O{-CL.IIATIONS BASED ON 6.3

"".... 51

51

5I (e

\rii

r04

PREFACE Dedicoted lo the Memory of nny Mentor: Prof,'sduardo M. Igqacio Jr. Fuel combusUon consututes an tmportant step in iilmosI aJry t is desired. Thus tlre study of combusrion ls mosr impoi.*i;;;;;hivl, "di-g.rreration ,t. r,.ra of Chenri cal Engin eSring which ..,"o*p^"es the Cn.rir.", i".# It is for tliis ieason that this -o-ook has r..u pr*p*.il lndultry js the autlior:s objeclive rhat"rhror.rgh It t.h,; bil{irr. "Cir*,rr.or Engir:eering student is provideci *"r"t ,.o , .'o*,. concepts encountered rn fuer combustion"J""1"? and r.e,ateJ- fro".." indusbies' It is afso trre book wilr'expose {1thor's hope that this .of tle student to a meth.odbJory for the sojution Stoichiometry proble*rs that wiII developl6ls:6aiy,cal minA anJ ir.fp f.,,1iu"f,l. other related engineering problerns. Fuel combuslion js such a vast and compiicated topic that Lhr's book can only cover thaf part whjch oeas"m$: L"J., *or. and volume reliaUons among fhe fuel, a:r inA pioJu.tu of combusLio," calcuration of heat ]osses are a-lso ir"r.,Ju,l to de[ermine ti:e arnount of heat avaj]able for power -"ul,Ol g.n._*trorr. Di{ferent g,pes of fuelsUq"tri 6ar. are described u,jthin problem statements to famiiiarize the stude,t n"ith l}eir srr;;; and u-ses. ot,er proces.s indus.rres ;;;;;;;:;:,; U,:"_, Bisulfite and Lime production ha,e been "r; incrudecr because of iheir similan ty in stoi chi om etri c ca] c-ulai on. *,i, ."",;;;;;' Ttre approach of th-is book is rnturr);, .o,r,pr,u.o;;.;;;.roru problems" irodr sample caicutatior* Ld pir"r,".- rorri.il"-u rr, ansl/ers have been lncruded to aid the studentf in his c-hemical process industry-wh*r*

O ur

Qre.at 1)esire is tfiat Eatfr One of /ou 'lt'ttp tts 5{ts Eagerness to En{, so tfie ifrit tfie Ifirryt you g{ope for Witt Comz True. .

9{e6. 6:17

r

-qrudy.

Although cornputauons are basicaly Materiai Balance calculauons, tlle solution of problems have been further simpli-fied by diyiding t /rern into cAsES or TypES each with u up..ifi" irt)proach. The Systemi International (SI) ii appiied "o*iotationai rir";gh;; Itt rlccordar:ce with the shjft from English Cusio-mary units to SI rrrrits worldu.ide. It is the author s hope that this book lr.lil help not only the (lhernical Engineerirrg student but also students of ,trr**

Iirrflineering disciplinel as well as those pr.p*irrg

l,l r:enSure

i;, il;;

Exarninations. tastly, acknowredgments have to be gpen to those wh. have -lree, of great ngr, i:: the_prepaiation of rhls book- To rry h";sband; I)ean Alberto-laurito,,for providing arl the material a,d moral trrrpport and for pauently teaghing me all the ireeded computer s'{tware that have facilitated the p}epar:auo" *a-""*p"t.uon of grroblems; to the Iate prof. Bduaido ro, rr.rra6;; vrrlurninous notes in stpichionlebDr, ;"roy of which have!.o*a*a llre hasis foy the computational upprou."li pr.".oted in uirJ"lx, rrls. to both these people ror'taung-time to^review this manuscript rrrrl'.qrorriding usefuf suggesu"rr"" n',ully, above ax, 1;t wl,lehe?t.d grytttude to the Lard arrrgnty, and whose Light, Guid,r(:e and lr:sp lauon helped me to pu*I,,r.le all trrr:oJgnout the 1rt elraration of this book. I feel wtthout Hirn, this bborr iouta- not ^-": Irirvt: treen

ig';".,

a

CHAPTER

ilil

realit5r.

t)velyn R. Laurito

f,

INTRODUCTION 'fr

,

.

I

DEFINITION

'COIv{tsUSTIONis a unit pro.*ui in which oxidalion reaction takes place. However not ait oxidation reactjons ar:e terrrjed as c.qmblstion, e.g., oxidation of toluene tt: benzaldehyde, oxlclatiorr of h;rdrogen chloride to chlonne, etc are not normally ternred processeq, Qqqlbustioq ]s a chbmical reiction in ": :u.rybustion whigh gne- of t}e rg"q,c(ants ii o"yg*r, f.om tt e ait and the other an:e] {gaseous, iiq.ria, soiiffi_g,pusuqn-1s,1g,gomp_q4ied by 13 the evolution of ligh.t ana neat,6-d thus}und[smAa is g;";ra]Iy :s:d in the generalion of heat to suppiy energltbtir-e"proeess-

:

industries.

I,2

COMPLETE COMBUSTION

The complete combustion of a fuel mezrns that a]l of its combusubie components are gasified: all of the carbon 1',1,putever forrn it may exjst in the fuel) jsbr:rned to carbor-i dioxjde: aJi of llie hvdrogen js converted to water anei all sulfur to sulfur dioxide.

h.-

j

2,,

s-r-urr.ti i;CI\40.t.ii.,.

.

und ernorma-r oxidizing conditJo:rs, furnace combi.rstion rrrg pjace co:'r.sist o^f tak_ gomprix ,;;J;r. ..o.i,o;;:;;, ;omputa_ riona-l puryoge_s of this f,ooi. v+L r.rL.,wEVCr, rror."er, Lne f.he IOilOwin$ fo,owing freacuons .sl,ral] be conSjdeied.

HZS + 3/2:.fu,=,S02 + HZO tu

(0.06)

t,,,,.

f.t

H2+1/2,Or= S +Or = SO, -l

n IJ

'r,4.t

Y"5

-ts',

complete combustio]r of any organic fueJ is represented

'''ll*(')vs,

* r/2

[2w +x/2 +zz-;v] 02 =

(0.3) s7

coz + x/2Hro + z So,

*:o

T.3 THEORETICAL OXYGEN 'l'rreoreticai lrr r:'r ll[Yl:('ll:

Met'rrod

l''r,l

o:rygen is the

o.lygen r,rr' The.. *1il;,;;irr"o"ir Yv

tt1ilt,

vr

l:

requirecr for compiete corn_ \r('Lcrirli rhe rheorerica,r

Method

d.;;;i"ing

The indivirruaJ^!aranced tion of eac. comb,rsuul. equation for the oxidarlllntten. The rhdorericar grygen is the sum ririi"the oxl,ger: used jn each complete combur;;;:

De-termine the theoretjcal moles of dry a:r re_ qulred for the cornbusrl"".i"ne more of refinery gases contajnj:rg 6g6 ff"S, iqa l1r' 57o/o C"LJ., 2;/a cor. ";;'*t% cuH,,,.

,

/2 o,= H,o I,:l (0.05)

HrO

p^o|.ro (

i

Solutioru Basis I mole of gaseous fuel

C+or=Co,

.

IrvTt?onueroN

'

:do= 3 eO, + 4 HrO

+ t3/2 3, = 4 COz + 5 I{rO

",'',: ?.Y#}fff":

/2rc.05) + 5(0"5a

n

ru,,r(Q"so)

2:

of the fuel are broken down Tg compo-nentsuto*" rnro : "llonorrairrg_ of carb,o;:";"r#;;["-

gen and moles of o4ygen present. For .odpi*t. combustion, each c- i[uro** t more or; "io-*- r each atom sutfur requlres mli. a",;;;.I,i* H requires r /4 mole 0* Th; the fuer is subtracted frn* ur..o, *?i1., ,r A: ,; .."q"".LILq" to give the theoretica-r o, from air" The ralionare behhd this is ti:at !e{o!; ;, amount of O- is tafren from the air, the fuel frr_, ,n."/r*, together wlth it. Thus: "Oir?.,

l;il

3

cHAprE

-

(4) From Petroleum and oji shale n By crachng (.Reflnerrr, Gas) . By hydi:ogenaUon (Ort Cqs) o By u'ater gas reacUon (Orl Go51 ,r ai nxjdauon tCrit Cas)

2

.

GASEOUS FUELS

:

(5) From Carl:ides wirh water (Aee{risn.1 (6) By Electrollzsjs wjttr eiectncity (FJr1

2.2 7. T CLASSIFiCATION GF GASEOUS FUELS

fuels of value in Commerce inciude ,atural ';i:rr:ous gases, gases Irvrl,',,,,,nrbon

manufactured solely for.use as fuels, 'rrrrl ;lirses obtajned as by-prod""i"^ or sr;me jndushes. The lrrll,rrri'{ classificatiorr .of giseous r,-,ers ,"J"a"" o, r oI nt I rf ,r-(,ia_l importance.

"r",_[."

a,r

d

VOLIJME MEASURENfiENT temp erature, these coi

dtions'"i.""

when ttte volume of a gas js given.

t

Cas)

(2) Frorn peal_By CjstjllaLjo:r or carbor:izaUon (iJ) From CoaJ_By carbonizaUon {Coal Cas) " By gasificaUon (j) in atr (Froducer Gas) {iiJ in ajr arrd steam {Water (::1 ,, O, a::ld stearr: (Lttrgi Gas) Gas) ' By h-v*drogenation

.(peot Ga-s)

As a b1',-product of rhe redu cuo,. of ores (Blasr p.tmace Gas)

b<

-J-"yj'

fJ rl::",ilt;

Cornrnon Conditions for Gas Vohrme Measurerqents

are:

I tan d :rd te,m p erature anci pre-ss r*re(s. t. p ) which is 0"C and 760 mnr FIg Norrna.l Temperaturg and press-ti.rl (]rJ"fp) , which is 3l|[a.:fig_g*g]trg. or Q"c sla ?60 aAXt Qlagdard Tgrlperature and kessure{STp) which ts OO"F and S0' Hg or 15.56"C arrd 760 mm Hg -,

,r) Natura.l u,ith petroleum oi) deposils, wjth ^_*::"j:ited "u. or wirh the decay of o4ganic ;i;..-* ,.\ ::1itrlulac[ure ":r-" gases t) rvr (r ) From Woo_By disLillaUon or carborrizatiou (Wood

ia

.

*

Drgcpldtrons mears no water vapor js presenl i,,r+,- !L ![-u't e!.n-dE-ons ireans r}re gas is sati:ratlo *ii-*r l]Y *t at

.\t

STP

ScLturaiort Partial Piessurq of w.arer ji.l gas D ,qyur. rres_S..ur:€ = At padja.l Sa,iur:aUoq" - \/rnn,pressurr \/apor = r: (%Rll/ jO0)'

g*

water vapor

IN'lR(ji-rl.jCil0N z 5

I'

| ,\,unpie I by Method 2: I rrrole of glseous fuel

tn1,

I "5 FERCENT EXCESS AIR

t1.r'.1,,

Llt tl .ta

A?S

!i

ATC

ATH

0.06

)

4.12

i!

:ry

0.1

r.71

In actual practice, theo::etical. ajr is not sufficjenl, to get compl ete. combu sli on. Tw o_ob*iou s phen 0menon 0f in c'mplete or parUal combustion a-re CO and H2 formation jn fire flue gas

and the presence of uhburrred eombustibles in the refuse fcrr solid fuels. Excess air suppiy or eacess o2 supply is a r,ust ior complete comblrstion" It js defined as follows:'- " Excess Oz = Actual O, $ufnly - Theo O-

4.56 %

0.02

I ()o ',,

o.06

!l.J I

O

r.2a

9.00

oo, L,JO

'7.78

06 + 7.78/4

_

4.02

0.0? = 4.gI S Ansu;er

assumed to be i. r'r | -' ttrtl i' l'l'i, NZbyvolume. IV2in airlsnon-combustible a::d -, r ..r, .r ,lllrrr,rrl lo the O2in thJa:r. 1

llrrnace js fir-ed with petroleurn oil containing lA%H,30lo S, t% N and 3o/o rirc rnoles theoretjcd_] air requiieJ O. Deterrnlne ior tHe com_ lrusLion of one kg of oi1: ,A

,'ioolr C,

'11i1,

iir',r t i ,,i,r,,ll

,11

r

lt,i:;is: ;,,tt

Excess Ai-r

E-rcess O^

. -#-ua x l0ti = ;-.:rneoreucal !y_p1,:9 9z_ I:l_gz_ y

I I II II ()I\'I IICAL AIR FOR COMBUSTION irrr r'1r'(ir ;rrr" is air.that ri" "* rr' r| ( l')'rlAir fr-rrcombustio.,contains the exact aniount of alarroqi.nsis

1,ty1,1,

7,0

- -7.

():t0

ilr-r !r,

0.02

I lg'of fuel

/ )') +

ojl

3/3; + t3/4' , rr, = 0.0991 7 ,.1

ri.:;

r.i:ci.

Theo

0,

, orr

x5t (,z--

*. ,^n ----Supplied 0, - Excess O, ^ '" The act,a-l Percentage Excess fur depe,crs on t.he fuer ,serr for combustion. NormaJtygaseous fuels re qurre very rrt[le excess or; liquid fuels require s'rlewhatmore vo excess o, depending o. their characteristics; solid fi:els requrle maxirnum excess o...

i .6 INCOMPLETE COMEUSTION Incon:plete combustion cf f'uel repr,eser:Ls a loss of heat sincb thls should have Lieen given off foi ,ddruonal power use had the fuel been complete.ry brur::t. IrrdicaLars of incomplete ccimbustion are the presence of ccr, H" a-riri sool in the exhar:st gas as well as urrburned combustjbl6s nr Lhe relusr.

t

r-r'l"r.rlr.:;iO;riEi-li)'

T]-ie Vann- D.-^^.---Dquerion il6ffi:::.:t

bl

usins Anroine,s

""'*ruted

I

Total B

lqgVp=A* u,ll(jre \,? is

l,irr.rvarcr

in mm Hg: T js jn

"C A= 7.9668f B =-iois.z,

Ca-ionfic Value

_

ci22g

CALORI'r]C..V4IU-ES

ir) 'lhe balorific

i,r Si a,-e exf.1e;sed 9l u ,JCr (MJi dry basis"Tjf.. rku75-sMl']r Gooc-ieq=d [g',,0

t

roeB '-::-t Lruiu

_O.E

G4SEOUS FUETS

v;alue) o1'a rirer is rhe given off bv the compJete hear 'j].'- "."t oirnousii.;; ;;'::-',] a unjl quanUry ,rf the fuei &t sonre rcfa-o^^^ -rsUorr of t.", p.r" r,l *" tclnperature * Ill.I."as". 2s"c ^ ":: ;";;.;:::[T ;rrrrbient air lemperati.rre ffiI.:,.,,:*en may be used).

;*:S:::rT

ff

_

;l;;

tC i,a_lue jS ^al^.+tri^ ,, u,hether ir js rhe GCV or Hivg, a OrOblern WjthOUt SpeCrfung ti-ri XCri"lr ff"y n. assumed to be rhe Valut ,t-,"'in,.'r*rue which is usua,rr 3;'"":,.t"orific "irr..

Exaryle /: Calculate the gross and net value of a natural gas at- 25"C which calorific has the foiloio:ns composition:

h#f#.?

89.40/o

"'

of Calorjfic Values calo^fic tGc\'1 or Higher r{calins-va,ue ,?l;?il

v;;;

falo,nfic Va.lue measurecl when rvater formerl by r'rrrbustion is,.r t1;jr#;tilnen ,,., Nct (',') Nt't C;rln;t';^ caloririe \r-r..- -. ri?^i n

Y;*:*:::..:;#:::L" *

(

a)

MJllorol

b)

kcal/gmol

n'l

d)

MJ/ks MJrdry

e)

MJ/SCM

tins varue (LFrvl

;" x:I;,.?tr .,rnbustjon ;I.T# l'lis in. r,r: tle *"lliq" g.;.;;; ;;;.,

J:iY

Solulion Basis:

I

SCM

igmoi of natur-al

|t:;(,ol:S Mt_XtUfeS Hc,MJ/ kmol

u

lrllr. ll(,j = Heat of CombusLjon cf qornp6nent r rrj

L

CH., S% C.,H^" ,.gri;;';'* Zrt io, .,0 Jdi,ii.

0.40/a i-CoHio, 0.60;6 n.C.,H ,a" a llf :

'l'y1.rcs

l,i

I

i-atent Heat of Cr.:ndensaUon 44.04 M.l/lqmot of flp**-.,

\.f,,ffient .i7

r..I

r

Ir = =

rvhere

C+T

=

{Refer to ,Appendix l) mole fracli ii ofgaseolts con-ljlollerrt

, , ,,* *-*

i

CH,

0.894

u^I-t^ '*:l'

'8

j-a ri

inxr{c

o<

796.5I

0.05

l 560.92

78.05

0.019

)ni1 i.

tt r)

0.0c).{

.ROn

gas

GASiOI rS Ftiir_-.I.S I I I

-)

I

ji rl

rr-C 4H l0

0.006

( l()z

0.007

I!,,

r ------T! n x. H" I .,rr-r I Hc,MJi

I

ss

I I

ni *',*

0.06

0.02

'2j l,ie(

I

ToLal rnoles wat"er formed

NC\'= GCV -

t28 945.52

4.12s1

Cairirjfrc: Vialue

- atli/2 = 4:l2B12

Moles Water frorn Fuel Combustion Total Moles of Frrel

wtrere

x Lc c,f Warr:r

k = Latent Heat of Condensatinn =

I8.088

= L.A64 kg rno)

44.04 MJ/i(,gmol af HZO

a) MJllginol = 945.52 - (2.064/t) (44041 = 854.62 nvcrage molecular weisht of the €as = 18.088 kglksmot l/ Gross Calorific Value a) MJllgrnot = 945.5?

b) kcal/gmol = c)"

LLUIL'L

(i)

52::

MJ i dSClv{=94_5-i2

(1/1B.0BB)

MJ

:kgmol.

:945_i2 [0+]21

= i9 9i

224m3 "

.A.ns

b) =

n{' ,. ks moi I\4, r/ scM =, -. 273 kg.mol " 224m{ '- ;73;1556 . , .= 9qSS2 x i,O4t4V, =

3C2t .{\,S

36"06

13.i mm

Hg

zb0 - 131 760

If data,n air (0/o exccss air or arnoJ,t o[ air supp]jerl) is gi\/en togelhtr r.rrith lhe degree of cr_rrn;rletiorr of {.he reaction, the follovr.i;tg can be ca_lcr_riated: (l) Analysis iOr-_qat or CompleteJ of i_he prociur:ts r:l corntrustjorr ca_lled [he flue gases or {lre stack gases. These-$!.ses are rronr:ally CL)r, CO. SO" l_{, frce 02, li, zLnd i-1,O. Orsat aralvsis of tie gas ir j_,ll u,-il Coe*= noi. ili,c;1ude r,,'ater. 1:r

* Q,

't...,

-

'r

r1r;; ;1r<1j'I iq

?,: i'i ,',ii l" ';71 it fr,lrrr ,i,r' + N. Ir-,,r1 l,,i.l rrtoist.Ll.c frOl: i'ucl ; irriJt\[urr-. llOrlr ;t i.

= :i::::

Ij^() =

b-

47"28

CAI-CIJLATIONS BAsED Or.J FUEI ANALYSIS {CASE U a) Fronr the cornplete anirlysrs ol the rLietr. ihr rhcr:rerical o,a:!'gfn and Lj'le calorific va_lue ca;r he rjelerrrrined.

273+ l-i.56

\lP = 7.96683 - 1668.2 l/{228+l r.56)

MJ/kg = 854.62/t8.0BB =

2.4

213

(') Al_ l5.S6"C using Altoine Equalion: lrr;f

/4.18? = 204 tl

e) MJTSCM = 854.62 lO.O4I4Tl = 35.44

q1 17 =

o*o,.

62

d) MJIdSCM = 854.62 10.04221=

li) kcd/gmot = g45.5, x (t/A.lB7) )nR aa = r:) [4r r}u = 945

S54

. ii,O ionned

6

/l-orrr r:ornburslroLr

ol

l't.r e

i

..,s;ij()lis

Air-fuel Ratio

at Ca-rton = 2 at Hydrogen = 6

Stack gas-Fuel ralio ,,11."*1, effictencl, of combustion ca_n be ca-lculated of rhe rr-r er ald t_rr. y 1,,,i:: f:".-"- :*: : :_T ". l.:;.ses, -neglecling heat input from the il;; tlrr:nnal .. ..,.* urrrLrcrrLy elficiency {.rr of uornouslron combuslion rneasu: "?, measures % of the .Itrirt from the fuel that can ta rsJ to por,..rt" -, .

;";;;;

CO, formed = lotal a[ C = 2 I{rO fornled = at H/2 = 612 = Free O, = e-xcess A, = 0.7

al

i"; ;;;

Moles 2 0"7 15,8

GA.S

CO, o2 N2'

b)

10.81

3.78 85.41

kg dry ak/kgfuel =

il11i*8)A!l = 1e.33 ANS t) :3

c) ei9sry = !1?--'ljjl??9:#r 1#fkg

ettrane

-10

= 1671 ANS

r: Hasis: I kgnrole stia:ie or 30 kg ethane

d)

ToLa-l

rnol:s of comhusUon products = 18"5 + 3 = 101325 273+404

AIR

Stack tnno

m3 stackgas

kg etlnne

100 KPa

RIlilFqiFF

'Pt

EVtiitd_:\

P*,

:i0

moles *'aler tota.l moles

--r, qr.

,

i't,re !-

tl,,

-ll' .j,i..

:i.. +6.

# {

-yt.

&i.

h-

,AJ\JS

Vo

18"5

substantiall), ciry. Calculate; a) Orsat analysis of tl-re products ,rf cornbu bl F.dl, li, :,-:pp1ierJ,/kg of luel.gas c) Cnbic r::il.*;-s c{ ur/kg ethane d) .Cr-rbic rr)rll,ir-s of tiie prodrrcts of ilreasr_ri-cd i,rl, 400,,C, 100 kpa/kg cl P;ritial prcs.suIL: oi wa(er in fh.:= cofitbu stj,:n

ttrr,r

3

Orsat ,AnalSzsis of Cornbustjon Prociucts

L,rtrtltl(' 2: pure etha:lje is burned completely in 20o/o ajr. Air ts sr-roplied at 25"C, V4O lorrs arrd

tlt

2-614=3.5

Theo C), = at C + aL H/4 - moies )Css O, = 3.5(.2) = 0.7 O, f.rom air = q"5 + O.7 = Art \ frorn alr = 4.2 179121) = 15"8

r';rlcrrlatiorrs is rj:e DEW pAINTof tlte flue gas. *I!r."ti I I u r-moistr:-re present jn tJ.e gas, the nilne. is lts dew poJni ll tlre flue gases are cooled below fie Oew point. H, ,,1,1]:].:':1..:1d rnav ciissorve Co, a.nd So, Lo l'lr.se acids *. .o..o=ir,* uoJ r?;; ;;r;O*

,

r

ft

e)

Ptv .,

I

00 x (3/21.51

13 953 k-Pa ANS

2.i".5

l4

I

ltr )tctitoMETi
ilAstr()L;S i''i.;h.if,

l'lrrrnple 3; Pure met-hane is bur:ie,J with 40% excess ajr al,rj 25o/o of its carton conlent is converted to CO the rest to COr. 9Or/o of ils hydrogen bums to rvater, the rest remains as unbumed Hr. Air supplied is at 23oC; 758 mm Hg urith 800/o RH, Calculate: a) Orsat analysis of the combustion products b) m' of air suppited per kg.methane c) ms of combustion products at 35OoC ald riormal barometric prEssure per kg metftane. .$olutton.' Basis:

aJ

Orsat Analvsis

ANS o/a

moles 0.75 0.25 0.20 i.0?5 to5_t8 12.758

GAS

CO, CO H2

o2 N2

I Ig mole metharie

at 23"C, log \rF = 7.9668i -

5"88 1.96 1.57 8"03

82.56

1668 2lll228+23): VP = 20'82

' moles water from air

AIR

1 atm b)

A

a

x'ss O, = 0.4(2) = 0.8 (), frorn anr = 2 + 0.8 = ?.8 '. '' N., from ur = 2"8 x (79121) = 10.533 ()t.) icL;neC = 0.25 x I + rJ.25 ion,-red = I - 0.25 = C 7i Ilnbumed H, = ().1 x (4/2) = 0.2 ,l IrC fc:'inei = 0.! .t i'i,i2) = l.E lit'c r), = 0.3 t" '\ii.2':i)-i +-{,lt:i2)

,r' ait

(z a*tos::+0.30i)x 22

4Y9,31lI

l6

kg methane

' \ ?^ ''^ Gas 112758+210),)x224x m'Comb 16 kg metha-ne

'l'lreoOr=l+1/4=2

(l(t

u.

- = 0'30I --"''-:"'"' 758 - 20.92(.8)

moles waler jn cotlbustioir produe:ts = C'301 + i "B = 2.101

;rtC=l --

)n or{n s)

=20.75 ANS

Fuel cH+

Iil l1

(2,8+10.533) *

3500C Bt.iRNER

,.+ .lt

=

Stack Gas

230C 758 mm t-{g 40 o,/o x'ss

/ l5

=

l.C)25

273-35(r

-27J__

= 47 47 ANS

2.5 CALORIFIC VALUE LOSSE5 al CaJori{lc Va-iue loss due to irlcomplelr combr-rst-ion Th'epresenceofUnbumedComlrL:srib]esco]lsliLtltea calonfic \/a,lue l,oss: had iJ.]ese sui:slalces bee;r comlllg't-e,iv br:rned, t,irev would have ,{iven olf addiUonal heirt(1) due to CO = mr:lqs CO lr:rmed x 283 18 MJ/kgino)e izj dr-re. lo Hu = rnoles H" forned x 286'03 M'likgmoi

ll lrt

z:;'rc_rrcntoMETRr,

Crrjoriflc Va-iue loss dr_re to sensible heat part of the generateJ uy fuer conrbusuon

ll,f#::€ases *hi"h r.u*-i'," ^heat

CV ]oss due to Sensible Heat =

r:

;h;;;;;

rx

(Cpl1000)

GA-sEous

is absorbed n,gn

"i,.,1.,

x (le_To)

where T^- = of stack gas, .C TX = femp€rafrrre assumed +!vs ur as au 2S,c cp = specific heJt, rollrgmolK

6affi-[*#,"re,

Refer to Appendix

2

for

_ -rtT2 + D

A, B, C and

/(TiTr)

.D

T, = & +273 : = to *zzi':L f (ir+7,)/2 1 (';rlorific ll Value lost due to Uncondensed Wrrter Vapor (:V I,,ss due to Uncondens;J;;; rrroles water from cornbusuon i-n+.On MJllanoj l"rrrtrtple 4: A blast gas analyz ing 2Tok CO, t2o/o lyi"l.-. CO, ,oro ,r^:,.y. CfJ*,-and S+ilo N, at 2S"C alrd gg kpa and situratea .Lth ,rt.r rrupor is burned in l$a/o excess air. Ai1 is supplied a[ 30"C,.ZOZ to_" ,ra a_lso saturated wjih *rt... g0% of tfiei"t.J jn t1.e fuel js converted to CO, tir. ,;; "iU", JJCO. Moiar ratjo js t:4 jn t6e ,*.i.i.i, :iil to COZSb leaves at 200"dana "a.L!* ,oI;.s. Calculaie:

a) Orsat ,r-,aylis of tht slack b) air-fuel raUo by vclume c) moles stack gasrzmole fuel

gr.s

dJ Gross Calonfic Value of the fuei jn KJISCM e) 9,6 of Lhe calor]fic valrie losi jl r,rnbumi combustibles due lo jj) uncondensed u,ater vapor

:l

:iri se;ts;irll hc,;,i .,::;l.j ,.tl.:i:jer,ci.

-,1

I

kg mole dr-y Blast Furnace

AIR 300c 762 mm Hg sat'd

750 mm Hg

BURNER Riast Furnace Gas (25"C, 98'trpa, srltd) 27o/o CA

I2o/o CO, 2o/o

H,

570 CHo 54o/o N,

Gas mole

co 0.27 co, 0.12

P,2 c[{{

at e 0"27

1t"

,nole O,

0"04

i.,,

0:1 35

a.tz

0.02

0.05

.0.05

\, 0.24

0.44

R eEq

Tt1 o, 10aa+{0"24/4) 0.15 x 0.245

-0.2sb- =a"24s. = 0.03675 from air = 0.245 + 0,03575 O.:AiZS N, from air = 0.28t Zb :, ,.Tg/it)= = l G' = Il"1o, O,

C ccr:r,erted to CO, = 0.g x A.44 : - = 0 396 C conveded !o CO = {J.044

, Hr_unburned = 0.044 x (ti4) = .011 HrCJ formed = (0.24/2), 0li = "109 + (.aaa/2) i f". N, =?"=-.03675 N, Irom fuel * N., cl -=.:r.i+l.Ub=1fi

Ga-s

Stack Gas 2000c

Fuel

Cp

T.1y be esiimared by: cp /g.sl4 = A * BL * i/ s(sr^_T2

Soh:fu:ru Basis:

ruals

(,0r--'-' 1/2)

frorn.ai:.

=

06425

/

l7

l6

i9 Analysis AN*s Gas

e)

moLe

CO, CO

o?. N,

i)

o/a

0.396 4.a44 0.o11 0.06425 t.r)

H2

18.72

0.52 3.04 75.64

% CV iost due to H,

iJ)

fuei

=

23"6

98 x 760

GAS CO, CO

mole

Cp

41.89 29.6V

o2

4.a44 0.01I 0.06425

28.85 30.54

N2

1.6

20

-nn?a

HrO

0"2002

34.21

23.61 o/o

air = (1.06 + .28175) * -*:l',687-=

(toe + 28)15 +0.-s82]\ x

1

ilt illr

rrr' firel

(r + o::) *

760 213 + :O -- - -, 126 2i3_*

i01.325

273 + 25

98

273

iji)

,l)

(;('\./ =

-

+ 0.C2(286.C3i - 0UJi5l0.g5) 726.23 |IJlkgmol c:t' )26.7?,{C.O414Zl = 5.2S ivI._r/S{t}4

"14"U4

x

2.Z4ls

x

100 = 2.48% "ANS

16.59 1.3

ne, 1"

+/

2,1

96 u5

.6.86 74.A8 kJlK,

-

2:)

x

100 =

Thermai Elficiency

= =

Exctmple 5:-cozil Gas

i00 = 3 79

7A.23o/o

10Cl - tg.g3 + 73.670,/o ,sJ{S

A-NS

2.48

+

10.28 + S.79)

ai .r5"c, 760 rr:rzs a-nr-J sa(uraled

r,vrrr]-r

u'al_er vap,or is

buri:ed l:r a fui-rrace. Alr wjlh 6002i RH js supplidel at iie lale of S.l rn2/ m,,coal gas aild eniers at the sixnf Leil.tljcr.3ture ;l-nd ;trrssure as lhe coal ga.s. I*he r:r;al .q;r.; ;rn;-il-\.zcs ) 4, a()

2.7a/o C",11.., 0.79/aA-. S Sq4,'

h.

ANS

CY loss due lo Uncondensed Water Vapor 126 13

fJ

+ A.2AO2)l }.033 =

o/o

0 109 x

l(,lirl waler in stack Eas = 0.1C9+O.tr33+0.05g2 0.2OC2 =

rl Mrrlt:slackgas/rno1e fuel = {2.JtSZb

iooo)(2oo

1261'l

= LJ./.y

(-'.)7t233.181

9.811%

CV loss dr"re to ser:sible heat

_!+.osl

(].05g2

7b2* 3t.68i

. l,)

g?]Ii8lryl

0.396

H,

i

101325 -

Mtrlc:s water from

=

l./.O. I )

25,C logVP = 7.96683 - 1668.21iQ28+2$1 , VP 23.61 ll0"c log"v? = 7.96681 - 1668.21/(228+30) ; VP = =31.687

Mrrles water from

% cv josr dr,re Lo co *0'044(283 l8) x 100 = 1.2613

2.CB

21 15%

nt

Ca-ior-iiic Value l.osses

CrJ

53 2()/,,H". 2g 6jt,

i

,lllMl:.lJ'R'iJ

clAst<.rrisl

arld 6.670 Nr. ratro of CO, to CO jn thegtack gasj: ]e.mofar iO:i. Ail ttre H, jn the fuet is

t'urus /

21

CHo,

bumed to water. The stackgas tea.res at 4O0"C and a) %o

Moles of Dr1

1

Coa.l

- 12/a4

224

=

excess air

Olsat Analysis of the stack gas ms qtack gat/m3 of coal gasd) Dew Point of the stack gL

'160

2'73

213

+

15

416.14

b) c)

Moles water frorn coal Eas 416.14 x (12"64/76A) = 7.A4 =

10000 m3 of coal gas r'rt"ri'/1f coal gas

Stack Gas 4000c

soc

/(i0 torrs fio % RH

17"24

o2 CO

2.91

atH

mole 0, C.O*)

22.48 24"74

CHn

24.14 221.39 123.18

N,

zt.+t

-:,-_,

2.9r ]2"07 442.78

Moles dry air = 2412.1I

]OAL GAS

(t s.c, 760 l.4o/o CO.

torrs, satd)

123.18

492"72

I75.63

957"98

20.81

x [760 t2

G4("6)ll16CI = 2388.04

Moies O, from air = 0.21 -x 2388.04 = 501.4g Moies \ from air = 0.79 x 2388.04 = 1886.55 Moles water from air = 2412"11 - 2388.04 = 24"A2

2.7o/o crH, O.7o/o O,

l;.8% co

I\

29.60/o CHo ti.6olo \

7o excess O,

Al lir'C- logl? = 7.g66g3 VP

=

=

-s0t.49

*

394.32

--JX;;-*-

*

I00 = 27.19

ANS

CO, formed = il0/11) x 175.63 = I59.66 CO formed = {7/11j x 175.63 = f1EJ.-1lF I

\/olrrrrrc of air = 87000 mj

L_

C,H,

atC

theo 0, = 175.63 + (9tr7.98/4) - 20.81 = 394.32 Moles wet a:r = 57000 x (I/'22.4 x ZTB/ {2TB+LS) = 24tZ 1t

Fuel

53.2o/o

J.6J

100 kPa

BURhJER

(

n

CO,

H,

AIR 1

GAS

_

12.54 rl:rr

1668.21 Hcr

/(22t+15)

Free O, = [501.49 -394"32] + {15.97/2) = 115 Nr,

-.

'27

.17 + 1ti,50.55 -- I914

(12

16

HIOMI!TilY

;A_sEous iunus z 23

Analys.is ANS c) .

,n

GAS CO,

o/o

159.66 15.97 I 15.16 1914.02 22A4:91

co o3

N,

7.24 0.72' 5.23 86.81

= 478.gg +

24.A2

,

I rta.k C08J gas

=

d) e)

Exarnpte 6. A pure saturated hydrocarbon (C"Hr"-) is bumed with e.ycess air" Orsat anaiysis of'tiiiiproOucts of combustjor.r shows 9.08% COr, I.630/o CO, S.2Bo/o O, and no'ftee Hr. CaJcutate:-'

+ 2.04 = 510.I

l0li25 100 1000 -

(2204.81+ 5I0.i,) x 2/.4 x

= I5.i9 AIttrS

tb.r" This

burn H, to water, and w.as not accotrnted sirrce water js not included jn the orsat anaJysis. lAtten losses of eombusUble matter such as sdot are small. a1i the Carbon in the fuel are accounted for in the stack gas. The ADTIII{DROGENis t}re hl"drogen in the fuei that useJ O, from airfor combustion. The net hydrogen is equai to the totai hydrogen in the fuel if no Or. is present in the fuei. O, was r-rsed to

water from combustion = 9:57.g2/2 47g.gg = ,moles water

An O" baiance will deterrnine the O, unaccounted

213

+

400

a) The fomrula of tfre hyclrocarbon o/o excess air c) ry dry atr/YS of hydroca-rbon

z't3

b)

Scrlufion-' Basis: 100 kg moles dry stack gas

Prebsure water

in

SG =

I00x5l0.I

,z

(2204.81+510.1)

= 18.79 kpa or 140.94 mm Hg ,lt Antolne Equalion: log t+o.s+ = 7.goo8rT = 58.74"C

58.74'C

9.089/0 CO, 1.630/o CO 5.2gak 02

AIR 1668.21 /(228+1)

BURNER

ANS

I

i

'!:

Eill

\

TIONS BASED ON FLUE GAS ANALYSIS

tn.the fuet is neglig]ble, the N, in rhe flue gasmal, ic be all comil$ lrom 'aj..'

turned

lE O" mav be computeci as:

O, = frt'e C^ - (CO/2) - (h

/?.)

'r\ H un"zr,r2 By dilierenCe: %-N, in the stack gas = 84.01 C" {rom air = 84.01 x {21/79) = 22.33 O, unaccounted for =22.33 - (9.08 + ).63/2 + 5.28) = 7.16 net I-1, = H., iit the fuel = 7.16 x 2 = 14.32 I otaj at H in the fuel - 14.32 x 2 = 28.64

lllC)t'di:ltiy

l,t, C r,t

c

in tj:e fu,el = 9.0g .r i.63 = i0,71 10.7t n

ft H n

GASAL'IIS FL.iEI^S 12i

O, from ajr = 82.69 x {2I/79) = 2L9B Xss O, = 5.43 - (1.37/2) - (0.69/2) =

28.64 2n + Z =-

2.965

or

a)

3

9z= 5.28 - 1.63/2 = +.+O-S

A.j\S

alr = [ 4.465/ i ZZ.eS-+.q6S)]

_Egl. "g .c =- (ro.zi)irrlx[

x

taO

=

21o/o ANS

I

12.33)

tr;

= 7e'62 Ans

t:

torrs

at

BURNER

atH

C

2J<.

2;t

v

4y

o/o o/o

CrHr=

13"2

CH; -- [4.79

I 8.2+4.79)j x i00 = 4O.OSa/o / (3.2+a.79) J x I00 = 59.957o

At 26"C logVP = 7.9668i - t668.211(228+26) Vp = 25.06 mm Hg

gas

9.82o/o

%RH

CHn

x v

Stock Gos

28OC

qrr,

moles

Moies #ater from air = (2L98+82.69) x

AIR

Fuel

x

Cbalance: '2x b+y = 11.19 + 4y = 25.56 balance: SoMng simultameously: k = 3.2 and y = 479

a:r b) M^ole o/o composjtion of the gaseous fuei c) m3 wet air supplied at 26"C, zls torrs Ai zovo RH per kg_ of fuel

j00 rnoles dry bumer

GAS

-

lI

7o excess

Jasis:

(2l..gS-4"4)J

C,H, CI{o

t,

r t

a)

/

100 = 250"/a ANS + 19.82 (t.32 /2)+ 5.43, = 6.045 Moles net H, burned to water = 6"045 x 2 = .12"'Ag Total moles I{, in fuel = 12.09 + 0.69 = L2.78 or.25.56 at H Total at C =.5.82 + 1.37 = 11.19 I-et x = moles CrH, and y = moles CI{+

i

Orsat analysis of the stack gas from ttre combusUon of a gaseous mixture of acetlzlen. ,ort metlrane shows 9.82:(.Q9r,_i.SZ o/o CO, 0.69ohHr,, 5.43% 0, ai-rd 82.6g0/o lVri O.t.r*irr.,'

I

orcess O, = [4.4

O"/.unaccounted for = 21.98

I of the hydrocarbon: CrHr

qtr

o/o

CC,

7.37a/o CO

o.69

H2

5.43o/o O,

82.69% N,

4.4

m-" wet n.r ' U,,

kg

ANS

:

25.ad01) 76s-2s"0q.1)

273+26 \-i'98 + 8296) x22'4;* " -ilr=air {eroerqooe\.,nnn76a

fuel

4.79(16) + 3./.2.6)

= 16.335 ANS

= 2.457

i_:;:ljili)lt< F'tii:)iS 7 !:..i

,

=

+l I't I

f-,qlci"rlA]-ig}ru5 BASE# Snxl FAfiTIAL

a)

ANALITSIS CrF FLUE GAS {CASE $iU lr,,rrr iht: conrplere ana-lysis uI rhe fuei, rhe theoreUca-l O, carr Irr ,llrcrrnirreC: O, ar-rd \ from air can be *pressecl ln tern:s rrl llrr: Li-reoretic::J O, ald tire i,rnknown excess Cr. r ,rrlror) is used as a Lie subsLance to relrrte the fuel u,jth the ,rl ,rr'lt ACIS

b)

/\tR

r_\y_-

il

L__r

co,

Exasr1r.te

.l II

1.550/o CO,

400

i

+

C,l"lr,.

{.\000/4) = 650

I rl .: -r'ss O, () irr,lg1 air= x+650 l'J, lrorrr ;'rr " [-r , CSC] l'iCi2 rl 0 Ir lr ( ) irr st;rck flils = x

o/c

txcess air Complete analysis of the stack gas c) Dew poinl of the stack gas

Soluhon: Basis: 100 kgrncles qaseous

AIR -,c0n LZV / bJ IOrrs

fr.:e]

Rl

Stack Gas t3.16Bit CA" I

l ' ,

,l

tit(l l,

{,

:rl

{22'C. 763 torrs, satd) I2a/o O(),

i

0.4olo CrH* 20.9a/o Ca

(t,l , r.:, , :,olr l ijt*r, :,1;rt:Ii ,q:ts) r'l'

1) .lri iri.l]

'

:r5

6% Il,

I

l|()'ir ( )i

1,,? (')ori, l^i,,

400CIC 735

r

^^ ^/ bU 70 Kt-1

---

llr

3"75

84"70

I r)

llrcr, ( )., .. 400

tttr,l,

"11.55

hi

.

--J

ttlltttttr: i'ji,t:;is: j00 moles

r,,,1,,i

ttk

pressure as the fuel" The cornpr:silion of the fuel shows 9 "20"6 CA 0 "4a''A CzH +" 2A.9o/a CO, 1 5. 6% I{r' ", 1.970 CHo, and 527oNr. The stack gas leaves at 40ffC and 735 mm Hg ard contalns 13.160/tr CO, anC I .84o/o CO on a dry basis. Calculate:

EUR'{ER

--)' Fuel I

= 11.0ti94 ,A-liS

9: A gaseous fuel at 22"i:, 763 terrs arttl saturzited :with watervapor is hurned witir txcess air. fu:"u'lttt 60q/o RH is supplied at the same temperature and

a)

i

(100)

3463.2

Gcs ^r --->- Sfcck 1

n

129.77 2933.43

02 N"

I

r

€xcess

GAS

' 8: Ttie buming of pure butate wjlh excess air gjves : stac!: ga-s';;hich anialvzes ii.55?o CO, on a dry basi ::. Assu min g c ornplete cornbu stj on, calcu late : a) 7o excess ajr b) Cornptetc orsal aLta-lvs,: of the stack gas

.,1111;,f1

C, = il29.7Vi65Aj Orsat Anaiysls ,aNS

0/s

In

ti:im

.L.g4o,/o

CO

GA:titoLls

(iAS |'r ) t,rll{ ('( I il,, 1,ltr Nj

n

() .)

I

"."

0.4 2O.g

AtC

at

9.2 0.8 20.9

i.

15.6

l'lrrr r), = 112.8 +

molesO2

HrC from combusUon = 40.4/2 20.2 = Total water in sia.ck flas = 2g.2 + 2"4llg + 2.647 = 25.285

9.2. -t10.45

3t.2

l.g 52

tri

1.9

7.6

ca

40"4

CompJete analysis of Stack Gas AJ,iS

b) '

GAS

(4O.4/4)

N, HrO

0.I5(moles DSGJ = 32 g rnoles DSG = 21g.67 * ttlrrft:s 99, ," DSG .T3Itj x 2tg.67 2g.TZ Irrrrlcs CO in DSG .01g4 x 218,6i = = = 4.022

lrrt,Or=yi@"A2:j/2) f)2 + (y+23.2510t /?.t)

Y

El

=

+ 4-023+ y + (4.02 t/2) t U + 23.25)(19/21)

+

i2

9.324

o,_= {9.324 /zs.2il) x r00 4l.to/o l'l ::1.11..,? = At'.)'_'"t) Iog\,P= 7.9668I _ r658.2i;e2g+22) : !?= 19.5775 ll,r ) i111111 fuel = 166, *_-19 jI2 _= rsol 153

A.2

=

243t

)

25285

irl.4

i,,

Antoine EquaUon: Iog 76.18 = 7.966g1 T = 46.2 "C

t' r. [']

F

t,

DE\Y Point

-

4G.2

-

1

9

677si 6s)

76s-r9577s(55)

1668.21/ (228 + T

.C flts

PROBLEMS

i"

Ca-lculate the orsat ama_lysjs of tJre products of combusUon

upon buinir.g pure hexane unth -Sg%o excess ;; ,f;---^ a) Combusr_jon is cornpiefe Anstuer: t0"tB%CO;, 6 l39o O^ bl 85% of rt e C bu:rrs [o COr. rhe iest to C(), moia] mtio o/'H, to C0 js l:2. Ansu:er: 8.49o/o COr,

'\,

1 r.q

Parilal Pressure of HrO in SG ZB5 x (2S"2BS/248.}54) = = 26.18

_ 19.6;1 5

/^ ^ ll,r r 1,(;ri; ari _ (9.32a + 2325)

4.64 "2

i.

c)

Itf ir i lr;rl: ,,).t u.(;7 _ 2f...?7

11"79 1.65

243.9s4

1,,,1.

N,

28.77 4.423 11.336 174.54

CO o2

19.65 = 23.25

el y cxcess 02 I l{ lrr}rl irr'r ,= y + 23-25 N, lt,trrr air - (1' + 23.25) x (7g/2I)

t'

%a.

CO,

r9.65

I

Al

i.ulits / 2g

2

1.89/n CO

The s5.nthesis of melhare enrjcherj gas fr"om waier gas a promislng sr:lutir:n to *ie probiem of hydrocib,onis shorta.{es in t}e f1-rtu1e ln one sich,prccess" the folouang gas composiUon is obtained. 34%o melliar e. 3a/oCO, l:9)i CO, 39%o-I-{r, *,g }3ozo Nr" Detennine ftre gross cijor-tfic va}re and net ca.lorific .,*ue cf itre gas in:

CtA:.J:r.li. lsj l'vl, l./lc.{rnoi lr, ,rl,/ll$nol [4.1,u rISCM N.l,

Airs: GCV; 443.62

398.5 106:43 15.82

106.43 18.8 18.48

r/scM

ei m' slacl( gas{}00 kPa; 300'C),r100 s:cles dry (r 7036.8r

(263.39)

e) % Calorific Value iost due

il nllr(.llr: Natural Cas (SNC from a US based planl) has I lrr. rrrr rl;rr composilion: 96.59o/o CHn l.2go/oH, 0.22o/o CO I t)% CO,. Calculare ute CCt'ana ruCff'r", l\4,1/kgmol ArLs: {864.ffi : 779.24) hr';rllkg Itr';rlISCM

t

a1n^r

d

^

(8566.04)

.

lr)

!)5)

11.-;,1

6. l,:

I t

andysis of stack gas

b)

p115,1i66

of CO. A f.vpical composition sitows 4.Zo/o COr"

arid 4.50lo\. If biue water g*. .rt ',llr"(1, 745 torrs ard 90olo RH is bumed in *,et -ax, 3Oo/o rr (.xc(_^ss, supplied at ttre sarne condilions as BWG with l:"" r. Iil i. CaJCuiaLe: ,r) ( )rsat mab,sis of ihe stackgas if lhe rnoia-rrario of CO, l,: (lJ l'8: I-1, tc CO is l:4 490/0 ts2,0.8% CH4

/ir.er il l.5,lozo CO", .l 41o4CO)

t,l

rn

ir-ir/nr3 BWG

l'). i',t.\

B3o/o)

Or:sat ana-lysis of Lhe st.ack gas (400"C,760 torrsJ iI of C bums to CO.r; all ll, hums to Hr0.

il co

rlrrl W;ricr Gas js oblalneci by passing stcatn over reci hot r ,r lx rr r cnricheC coal (cokeJ. The gas is called -Blue'. water 1,,r,, lrr:cause of its blue liar::e] a characterjstic of the I

l"i, (]O,

172"9o/rfi

859/o

Ans: (5.3370COr, 0.9a%,CO) c) GCV in MJ/kgrnoi t3gl.68) d) % calorific value iost due Lo:

tl,:10.66)

r r1 11f

u2)

Carburetted watergas is produr:ed in tl:e san)e way as Lrlue waler gas except Lhat it is done in t},e presenee of cl:acked oil vapors in a carburelor. A t5pieal gas analysis shows 4.7o/oCO r, 7 .Bo/o CrH o, 0.3a/oO r, 36. SozoHr, 35. 5olo C0, B ti% CHn and 6.60/o Nr. if th:s gas is saturated wift HrO at 20"C, 742 torrs"and burned in 10"434 m3 air at 30"C, l0lkFa zmd 600/o RF{ per m3 fuel, caleulate: a) 7o excess O, (l

lo 38%cor, 1.04%ccl , ) ('orrrplete anaiysis cf sla,cl"; gt.;: (r.r 1) l%c02' 0.Bg?6coj ,ll rrr" rlry air aL 28 "C, 768 nm ligr{moje iuel

.[

.(t.+) (8.241

"

t, fr

t

r

t.o

(5.5s)

iv) Sensible Heat f) "Itrern::l efficicnr:y-

t rJb3.5bJ

4 fr rr'l ..rltairrin{75o/o etiane 'and 2so/o proparie is bumecl i,.lllr rlry air. Allthe H, bunrs to HrO ana tne CO, to CO i,rltrr i:+ l0:I. Fifteen percer:t excess air js supplied" r rlr r rl. rle: ,rl Mrrles stack gas/i00 moles fuej

(/:l

ilCO ii) Hz iji) HrO

186.11)

itr.bil,.ry ; i

BWC

)

d) CCV of BWG {Milkgmoll

i6.53

(206.56:

r-t]I;]s /,3 I

ii) jii)

7.

Uncor:densed water ser-rsjble

heat

\r.rpor

{6 s84j

t7"79) i33.661

Bottled Gas (L,iquefied Pebtrleun: Gasj is found to corri..ri;r 1.40./c ethane , 23 8a/r, propa.ne" 2A Tatb i-butane and 114.10/o n-bulane. It is available ;rt P )i.'lkl. l,ssr:ciate.C gas a-nalyzing E3.6% methane, 9"S?io elh;uie, \ 2t)/o Dropale, 0"90./o n-bulane and 4.702b i br.:liane is, ava;}ah",ic atP2.5t/ SCM. A fuel is ra be selecled betwee;t the lwo fcr curing a refractory iined furnace tr\ihich i.q cheapef (An-s: Assr:cjated Gas)

t3

', tr rl( I 1( )t4llTliy I

I

G.ASEoIJS

i

A prrre saturated hydrocarbon is burnt w.jttr oicess ak. t )r;:rl anolysjs of tlie sack S;; ,h;;" Z.9o/o, CO2 t.tgo/o {'(\, Q)4o70 H", S.2S% o,, _ElS.eIv. w, Air js substanrtr 6 s tac k g*E r. u". ;; j r.*_#J ll, i"r; " ,r) (20 excess air {24.s86vA lr) lig airl}g fueI 12r.58) lJ l;crmula of the hydrocarbon {cHJ rl) I)cw point of the-stack gas (54.29,c).

I

t/,

;ff #;;;

I

:II

llotrlcd gases are lhe ,liquefied petroleum gaseS lropane ,rrrrt.trutane. If a sa:-opl.

ormi"g*;;;. bumed jn excess ,rir, a bumer gas of the foilorfiog ,l,ruJy"i. is obtained: -],i''ii.'?"'a"lu:i'"o' 6

45o/oo,. a,-'a

si;u^1U

lil

,

I

I I I

i

..

I

I

I'lrr: bumin8 of frurl;rllryS with dry airgives a stackgas u/lri(.lr aralyzes g.g2Vo CO, f'e-siffia".u t eave.at T4S , ,,1 ,,,, ,g. Assuming compi6te .o,rrf.r"ti?rr, de terrnine: ] ,r) tzo e.\cess air

),

Oonrplete orsat ariaJysis of stack gas -'..!'r bq

(!.,.2o/oO,B4.6E%

Nr)

I)t.rv point of stack gas (lj0 86"C)

()(r

(l

lr) r

I

I t

I I

C_rCeSS O^ 2

t.o4l

{ )111np1g1.

(i

l;".rc:.O

,J (,r_'\:

o.=_ql-lloJy..srs

i I l !

l

l'rrrrjrrcer gas analyz-ing.2_5.3o/o CO, 13.2o/o lf2. O.4Vo C!-Iu, ,',n.y.C^O, O.5o/oO, u,,la SS Zioi Xr-i. U,..o.d in excess air ;rt ,tj,,C, 74F toirJ and 60oZo nff.rpu..rrf orsat arrdysts of t,trt: :.;tack Sas .shou,s t6 13% CO),\.zsu, CO and o.Z2% II., C;rlculate:

,r)

I

l'

1.1,9.97o/o)

lr)

I

I I

&;;ffi,

t,) tror,po-Jr# of the botJed gas E2??*propane)

of rhe' stack

78.860,6N,)"

gas

-

( t t2 96 NUlkgrnol) rl) il.l C;liiniic uai_,,, Iost riire lo CO a:rcl ii., ('t, r''r- ,3.16i)

t.unm u 33

!.

'

A pure saturated hydr,cad;on is bumed in e*eess air. Air is supplled at the rate of 2g4.14 mslki4mol of .*re hydrocarbon. Alr enters at 3trC, i atrn and satorated o,ft} BteI:rapoI" Partial orsat ana$rsls of tJre statffi-sEofrs 8.68% CO, and 1.3olo CCI" ealculate: a) 7o ,excess alr {1Sols} b) Fomnula of the hydrocarbon (CHrl c) Cornplete orsat arraJysis of the staeligas (3 "ffio/o Or, 86.37t26Nr)

ry. A mjxture of a saturated hydrocariron and N, js bumerj in excess air suppli.ed at Zb,C" 240 torrs wjth g0%q RI_I. orsat anatysis gas shows Z 60/o' CA, f1 :{,,,rh^g,:!ack 22.28o1a CO. L74o/o-Hr, 6.037o Or:ana ge.g}o/o q wrm'a dew point of 53.46"e. ihe stack gLes Ieare at 300"C, 765 mm Hg wjth a volurne ratio of i"O+S ms wet sLack gas/ rn3 wet air. Calculate: a) Forrnula of . the hydrocari:on (C,H6) b] vol o/o- analysis of t],e fuel lzi.izVo Crnr) c) 7o excess air (24.ggb)

LJQIJ)l: i.Ut;r.S

LIQUID FUELS

3,2 ( I AssrFtCt-TIoN oF LroUtD FuEis I i'Irlrl lirt:ls may . !e divided,l into two main classes, based on h*r. 11,,.u rvtll be used: i.ight ;ris."*'sprnts and Heaqy oils :rl I ullrl ,ils or spu.rts*suitablel for use _ittr'iot"*"f r rnrlrrrsUon eng;ines and;et engines. It includes: |

)

11 rr.. iighter, more vo]atiie fracf,ons oUtaureJUy]tsuUng ,r. r'racking natura.l petroieum oirs a_nd reratid nat.,rj r lr.; rosits.

't)rc Iight frac.ons obtained by the hydrogenati,n of r.rxrl. coal tar or heavy oil residues. .l) I'lre Light ,?actionsi obtained by the qrnthesis lrvrlrocarbons by the Fisher_Tropsch pro..=" --^ of .l) A.lt:otrolfr pariicularly meth;-t :and olr(irined by slmlhesii or fermentaUon"1fryi" "faonrr, process. Ll lJt.rrzole, ob-tained by the djstillaiion of coal tar or by r.rlr;tcUon from cr:ai gas. t,) Alr:ogas or Gasohol_mixtures of methyi or ethyl alcohol 1.,1

( )l lfrese, only the most volatije ald clearest producLs, pl,r.,rrliur or petrol (natural or syndtetic), ben)ole and irlr ,lrrrl are suitable lor -.hb spart ignriron a"g,".. :t; ,..O lrtlllrr,r iiact_rons of peiroieuir: o:t,"il.ra;e oi LiA s-r,ntheuc

--

COMBUSTION AIUALYSIS

The analysis of licluld fueis is normallygiven in Vo by weight" Thus a unit weight basis is employed which js eonverted [o mnial units when eomparing tle fuel witl-r air and w.rth the combustion gases" In the case of fuel oils, the anatysis in terms of lndlvidu-al cherirical compourrds is rareiy krown. Ihstead the approximate weight 7o elemental alalysis consisUng of C" H, O, N, S are given. Of these, hydrogen is sjgnificant in the combuslion alalysis. We comrnonly speak of Lwo ]r:nds of hydrogen in JiquicJ fueis. One kjrid is that equlvalent to Oxygen jn tl:e compl* compounds of tlre fuel. it is ca-lled COMBINED fJffiROCENand is treatecl as though it were already combined wilh oxygen in the proportions of water called COMBINED WATE.R" This concept of iombined water rs just hffidmffis r:sed n:a;nly ro simplifr calculations. The Secorrd kind of hydrogen js called -NET I{YDROCEIJ. It is defined as the hyrlrogen that uses O, from air 16-r cohEustion. Net hydrogen ptus combined hyr:lrogen gives the total hydroger'). jn the fuel. " The quallrtjty of N and S in the fuel, rs relatively srnall: it is corrunon praclice to ne$ect them rf their c.ombirred percen-.a€e js lr:ss than or equa-l ta 3o/o.

3.3

CANCUMTIONS BASED ON FUEL ANAJ-YSIS.

(risE

rl

ttumple J TJrr uctane numbcr tsc-ocrat-le jn an (C?Hr6)

1:

of gasol)ne

js Lie

.- ---'-'_----

0'r bv

vo)ume rso octane{CuH,.}.--r"t,e ptane

rnixlure u,irh the s;l-me ktocktng lendency ar_rtontobile uses al rrnieacied

as the luel. An

_

35

eiJ, generally included jn the ciass of orls k"rrou,n a-s pelraffin, kerosene ornaphlha ere suitable for:jet errgines. b) hurtace Orls.-include the heayiest gradep of r:atural petroleurn oils and lubricaling oils frorn which the more valuable lubricaling oil and fraeUons have bee:: r:emoved by disUlJation.

CHAPTER

It

/

-'_-_--_---

_

_

'

nnii; i_;

.. Ei4ri:i:-*

rl LIOIJII) r'ui,:t,s

ME-I'RY

gasoline wii-h an ocrane number Of 85. Air is supplied 30%o in excess such that the molal ratio of_CO, to CO is 5:2 rnd H, to CO is i:I i"G. orhaust gas. Ca_lculate the brsat anaiysis of the

e,xhaust gases. of iso-octane is 0.60lg and n-heptane -D-qnsiry is 0.684 g,z

/

37

O, from ziv = 10"97 + 3.29 = 14.26 N, from atr =14.26 (79/21) = 53.64

C converted to CO, = 7.0154 x (5/V) C converted to CO = 2.0

= 5.01

Hz=2

free O, = 3.29 + (212) + (2/2) = 5.29

Exhaust Gas 30% x'ss

Orsat Analysis ANS CO,

5.0r

CO

2 2 5.29

H2t o2

Fuel Gasoline Ociane No.

Assume

N2

:

85

thai

the gasoline analysis from voiyo to

C.H,, ,CrH,.

vol,

Densit5z wt

15

100 kg gaseline

UgD wt

Mw

crH], 95.r44 1t4

CrH,,, I4.tr56

iCo

presSure and B0% Rli" The air supplied js less than the theoreucal arnount required for complele combusUon of the fuel oit; 25o/o of the C burns to CO, the remainder to COr; O, is aJI consumed and the mola-l ralio of CO to H, in the exhaust gas is 3:2. The exhausl.gas ieaves at 480'C and 745 mm Hg. Catculate: ei) o/o of the theor:etical air that is supplied for

wwo 85.144 i4.856

-

combustion

b) m3 arr suppled/kg of oil c) m3 exhaust gas/kg oii d) % of the ca]orfic value of oil

n atC atH 0.7469 5.9752 13.4442 0 i486 1.04c2 2.377,0 ? .i)t 54 I 5.82 I B

O, = f.C;i lt+ + {i5::,')1|=./4} = 10.g7

O,=03x10.97=3.29

7.37 2.95 2.95 7"79 78.94

Exonple 2 An ehglne bums fuel oil anaTyzing&so/o C and l2o/o H with air supplied at 21'C, nomral balometric

wto/o

0,6918 58.803 0.684 / .. l_Q?6 69.063

85

53.64

o/o

67"94

cornpositiori of gasoline car be expressed as ax octane-hepiane- mlxture

ugD

n

.GAS

(411.616 lv{J/kg)

-lost as

j) unbumt CO in the exhaust il) Sensible heat in the e>iraust

.Sc;iiriiorr:

Basis: I00 kg fuel oil

ge$

i.l(,'l' l'' i t;l'L' t il, I ll, ,rvli-:-ilrv

=t

AliR

Siack Gas

., IOC

I

c)

48ooC

:ttm

,.,'

ilt..

C

l'.),t)/o

H

(

,l)

Calorific value Losses il % caloi:ific value l:lst due tcl C0 1t - t1.833 x 28g"18/43'6161 x 100 =

iij

tr6 I.833

CO

rrirsupplied =(8.8054/ 10.33)x i00 = 85.2160,/0ANS

l\trrlr,,, rviil_cr

= 7.96tj8i - 1668.21 /(228+2t) = 18.5 nmHg

liom air

=

(ssos+ + 33125)

.

760

(0

(s.sosa = 331 2s + o 8327),

18

=

103,i57

8)

T,::" !/Jt

"ltl

l,;'lrrt'l

I

UL.)

t,,l,il ilrolirs e;Aei,.:st,.l:,as = 5.5 + 1tl-r-i ()

-i:. .OJ//

.- r)

T :.2:-

+ -i.., i?-5

= 47.2907

+

.:i. ,,

.,

(1535

_

ANS

nCP 251"47 55"71

35"64

994.08 -L9g-92 15:16.42

42l1ooo)' (+uo "

=::::::i-i6

zsJ

[0-----a

I

100

= 16'03'X' Aj!S

3.4

\

CALCULATIOhIS BASED '3N FLUE GAS ANALYSIS

(cAsE lll ExampLe 3: A furnace is fired kg.

-

4.8327

ill

sensible herL ]oss

90lo

wjlh. fuel oil cr:nlainjrr$ 860/o C' va]ue o[ 46;4 MJ / Lo/o N a:rd 0 l0lo '5 wlth a calordic tur is supplied at 25"C' 740 rnin F{g and

l85(08)

x

5.6107

H,O

l;. lrrrn) ,rr'= 8.8054 )t {79/2't) = 33. 125 log\P Vp

33.1 25

N,

rr.ll,rl ( l, lrorn air = Oz for CO, + O, for CO + O, for HrO = 5.5 + (1.E33/2) + {4.778/2) = 8.8054

;\r ','l"(l

1 1)g

H,,

%o

ep 45"65 30.39 29.16 30.01 35 63

n

GAS

ili,.rr {},,:: al C + at})/4 = l8B/L21 + (L2/4) = }0.33 lrr lltl crlrausl tas: r't r,. Iormed = 0.25 x (88/ 12) = S.5 ('() li)nlred = 0.25 x(88/t2) = 1.833 ll, lorrned = 1.833 x (2/3) = 1.222 I l.,r ) lirrmed = I2/2 - 1.222 = 4.773

''r, rrl llrt'ci

_*

100

CO,

+l

----.

+ 480 760x,2'73 * n-.,,' ::.7-45 __ _'U,) _

= 29.8 ANS

Fuel )ll. li8'/o

E,*harrsL Gas

kg fuel

745 mm Hg

r1(l'ff)RH

47.29A7 x 22"4 Y

\.

saturaterl wittiwai er' Average &n'al1;5je of the stack gas shr-r'ws 10'62% CO,' 1.170lo CO' €':3..aY: O'' and 765 Bl.87olo Ny Ttre slack gas iearres at 400"C aro nmr l-lg" Ca]cirlale: a) 9/o e'xcess air ' b) CompleLe elemerrtal a:ral-vsis cf fuel oil c) mu airlkg ilil d) nt3 stack gaslkg oi1 eJ % calorific vaiile Iost cjue 1'c r.tnl-iurilt r:ombr:stible s

1t

I-IQUII) t)tJELS ,/

10O nroles DSC

4l'

At 25'C log\? = 7.96681 - 1668.21 /(228+25) i.VP = 23.6I mm Motes water from ajr

; (2t.zl+ 8I.87) -

= B 4IS -'#{! 740 - 23.6r .

Stack Gas 40ooc 765 mm Hg

70.620/o

CO,

7.17% CO 6.349/o O, 81.87o/o N,

t

\21.76 + 81.87.+ 3.415) x 22.4 x

3..

malr

c)

kg

fuel

'

i64"51

.

760 273.+ 25 :273 740" --;--

.

= 16.34 ANS

c'

Moles water frbm. combuslion moles net H2 + moies Combined water or =. = tolal moles H, = 8.43 + (.0265X1645D/"18 = 8"67 or: = { }0544X164.51)/2 = 8.67

N,c

t

46.4 NIJ/kE

I

\\i,r!r"'r

air = 81 .87 x (2L/79) = 21"76 6.34 - ('1.17/2) = 5.755

in

sLack gas

-

O, = [5.755 / (21.76-5.755]) x 100 = 35.9670 ANS lnaccounted for = 21.76 " [i0.62 + (t.tZ /2 + 6.34] = 4.218

= 8.67 + 3.4f5 = 12.085 !

?-

m" stack

dl

gas

(100 +12.085),< 22.4x

kg fuel

--- x --:=273 765

i64.51 = 32.38

x

Wt of fuel = {10.6Q+1.lV Wt of fuel = t64.bi hg

x

t2

H = (i6.86 /164.5U x 100 = tO.2ba/o ned water = 100 - 86 - rc.25 - I - 0.t = 2.65o/a In Combined u'ate;' = 2-GS x (2/18) = 0.2g4

ln Combined water = 2.GS x (16/ IB) = 2.356 ntal.AnaJysis:of fuel

ai ,= (}O

= L0.25+.294' = 2.356 -l

=0.i

=

oii

70.544

ANS

eJ

o/o beaL

loss due to CO

1"17 =

x 283"18

46"4 x 164"51

x 100 = 434%

\ Example

: 9slane-Lni.rmbers

are u.sed to indjcate the qudi:ty

of a djesel fuei oil for compression igniUon engines.

It is delined as the % by volume of cehrre, Crfl;a meihyt naphtha.tene (9,,4,") m_tGre

ll ,cetalethat Eas rhe@ rhe fuel. A hjgh 'speed diesel engine bums djesel fuel to give an ej
| , rl I

rr, ,rr\ irr',, ,rrrr r,

rr

'

ii \'

(,1 (reLane

is 0.775 1 altd merh-yl naphttraJen-,

;'/tnl

r

is

oF

Assurnre diesel compositjon to correspo;d to cetane

FLUE GAS teASE III) ExampLe 5: A lorv grade fuei oil iCV= 46.4 MJlkg) cont'alnjng appro;mately B10lo C, Bqir 1L' 30la 0,4%,I'tr ar:rl 4 o/oS is burned in a funrace tllat IS weli ilesi$ned a-rld rvell operat.ed glving a Cnmbustjor] gzis, the partial orsat imaiysis of which shows \tr"2-Zohcoz and 1.46% C0" The ilola-l ratio of I1. tc C0 in tlie cornbus'Ucn gas js 1:S Calculaie" a) o/o exC€SS

b) c)

d)

O, m3 air (30'f, 760 rnrr- Hgl/ )q fi:el oii m3 stack gas (250.C, ?65 mm l-Ig)/kg r:il %o calorific vadue lost due to CO a-nd H,

'i

Solutroru Basis: 100

i ,,

lr,,:111s1195

Il .. 3.836 x 4 = ll42

l'tIEL ,,,,.FI,.

n x -u*

r lrll",1J,, : l6x + 1ly = ,t rl lnl ,. 34x + l0y -

11

atc

atH

16x

QA-.

I I rr

i0v

.42

1f:.enA

= 0.255 Y = 0"667 i',,1 rrl ('ctane = 0.255:x 220 / 7T5i = 74.35 rni :,,1 I Mf = 0662 x fqZ / ).a25= g240..t "" ir.r;Lre b.v vol = 174.35/ {92 404+74.35)l xri? 100 = 44.5Etto ' l,rrr' l,l = 44.58 A\5 _r

AIR

tuel oil

Stack Gas

--+

nrrr

O

\.1.220/o CO,

r

765 mm

1

46% CO

t"{g

BURNER

15.34+ = aL [otal H

(

rr

l€

drv E:.hatrsl. Cas

tr, rr inr = 80.34 x {21/7gJ= 21.356 ilr,r, (.rrritc-d [ot.= 2].356 - 7.14 - t4.28/2) - 8.24 3.835 =

rr n I rr I

4-J

3"5 CALCULATIONS BASED ON PAtrTIAt .A"I'{ALYSIS

ENGINE

t..t ,

I.lQLi,;r r:iiili .i'i /

Fuel CIL 810/o C BVo H 3olo O 4olo N

4%S Theo C, =

l9ii)2)

+ (814 \ + W/32)

-

Lety=XssO,

O, from air = 8.78 + y j

N, frem air = {8 78 +

"70

1') x 21

Nr. il.

(

i3l3?.1 =-

B"7E

*1 t:'l

{)l{lHlOMf,l*RY

LlQUur FLIF)$

Ar O l:a-i: 0.1268 (moles DSG) rrroles DSG = 53.233

= Bt/tz

d)

rnoles CO, in SG = 0.1122 x 53.233 = 5.973 nroles CO in SG = .0146 x 53.233 = :V7Z rrteles SOr, in SG = at S = 4/32 = 0.125 rrroies H, in SG 0.2 x A.777 = 0.1554

=

Iiee O, = y + t.777//2) + {.t554'/2) \ in SG = (B.ZB + v) x Zg/Zt +' (4/29)

/

45

A'777 x'28318 x LL'}0 = 4 T { co = 4a4, lo0

o/o

c-{ lost due to

o/o

CV lost due iO H-2'=

x 28E PP 0-1554 x 100 = O"96 - --*j;::46.4 x 1oo

rnoles

,

of 3 lower aromatic Example 6: Motor Benzole is a mixture

l)l;C bal' 53.233 = 5.973 + O.ZZZ + 0.1554-+ 0.I25

{, + Y=

rXr cXCesS

IIrr at kg [u el

7g

pierportions of 75o/a, lSiz-o 31a. 1Q0z.i. bV wei$ht" Its cafbrnc vatue is 41'9 N4J/kg' A nrotor rs nrn us[ng benzole ar.rd glves,ry-Tl1"ilgas whl ch ianalyzes A ?/o C;O2 and L'AZa/a CO' Calculate:

+'0'777

2.

4

2'63E 'r

, _0.21 -

''

excess :iir anaJysis of exhaust Complete b) o/o due to CO loss heat c)

a)

O, = (2.638/8.78)

=_

=

0.1554 ,__^ , -.^._-- + {8.78 + v} x

+'

x

x2i-4

100 =

o/o

30o/o

27i

SolufrorL: Basis: 100 kg benzole

-

Exhaust

100

i3.52 ANS

ll,O in the SG = (B/2) - 0.1554 = 3.8446

,,,rJ rrl

t-.^^^^ ^^ \ .i.^1, 3.1> roo (SS.Z3: + 3 Baa6) x.22.4 x r(dL^ kg

furi

I 00

760 +-. 273+250 X 273 -765

BENZOLE 75o/a C"HG i','

1,".

= l+.iJ

g'as

i-"

I-

li'

'

l5% ciHs 109/0 CsHro

cv = 41.9 MJ/kg

i

t; H T:'

I

t:

*-

o."'?

l#

E3'

t,,t, tn,,n.IET]lY

{A

!.lt1rl 1,, ,' ll,, { 1,,,

trVt 75 15 l0

{ ',1

,,1

lrrIV 78 92 106

atC atH 5.769 5.769 f i41 I,304 0,752 0-994 7.662 8.0 13

n 0.9615 0.163 0.094

PROBLEMS

.

1.

l'lrrrr (-), = 7.662 + (8.0L3/4) = 9.67

lll

1, : X'SS Oz

), Irorn air = -v +9:67 [J, frorr] air = (y + 9.67)

(

x 79/27

Ar (r [ral' 7.662 = 0.1177 x moles DSG nroles DSG = 65.098

co)

b)

| 2, An a]cogas rnixture made up bf 85Vo $asoline [octarte '/ no. = 951 and 15Yo elhar:oi is used as fuel for atr engine in Lhe presence of i7.05 m3 a'irlkg ajcogas supplied the C

frceOr=yt(.697/2) N- = gr+9,.67i x79i21

Y

=

6.965 + .697 + y + t.6g7i2) + (y+6.97) 4'349

x

dry at 30tC ard 740 rnm Hg BO! of essenriJly "CO,, the resl to ClO; r:rolatr ralio of H, to CO is bums to 1:2. Calcuiate: a) Orsat analysis of llie e--thausL gas

79/21

(8.18% COr, 2.040/o CO, I '02o/o Hr)

b)

"rr r'-\ccSS Or= (4"349/9.621x 100 = 44.97otb ANS I\4oles water from cornbustion = B.0l3/2 = 4.C1 (

n

,r,i,

cV

rosi,

cr;c

o/o

6.9965 0.697 4.698 52.738

co o, N" H:O '

4;0i c9.lc8 r"1..

co =

o/o excess

air

(36.143010)

3.'ALernarybie::dofgasollrle(900/ooctaneno)'alcol:ro1(75o/o 15%o efh.anol, 250lo meli.a:;ol) anrj l:enzole 1750/obelene, toluene arrd i0% xylene) is i:rirnerl completely in 350/o excess 02. Anall'sis of 1}re bienci 5!16rvs 70% gasolirre'. 1[-r%o benzole and 1Sclo a]cohol Calculate t'he compleLe ana]Ysis of ttre exharrst $as. io.a tgzo Hrcl) (9.77c/a CO2, 5. )Sa/o A,. 74:689'oN,

)ornplete Analysis of stack gas ANS

GAS QO,

% of the theoretica-l airwhic'h is supplied for comhustror] (70.7o/o)

nroles CO, = 65.098 x.tO7 = e.gOS CO = 65.098 x ,0107 = 0.697 "rnoles

/ r,'i(,1 bal' (,1, (.)98 =

Crude petroleum oil is general)y conside'r"ed tCI be fonrieci from anirnal and vegetable debris acclrmulatjrg iri sea Llacteria basins or estxaries and elecomposed lly anaerohic resulUng in a biackviscous product" A lrroic-ai eietr.lerilal 10/o N,30/o O and 3% S' -.ufrsis"shows EOqZ C, r3orr1, the During a cerlain cornbustjot-1, air sr-rpplied is le'ss lhan the C theore-tical so that all of the (), is used up' 7Ao/o o1' CO; the molal raUo of C0 lo Il, burns to CO, the rest to 'l;2. ealculale: in the exhaust gas is a) Orsat analysls of the exhar:st flas (i2'560/o COr' 5 38%

10t06 1.01

6.8 /o.31 5.8

,/

uses a high eracie iist-iilirte frie'l ojl v'al-h a c:r-lonl'jc r'alue of 13 ljE Vrkg" Ar:eJvsis r-'f Llie st.ack gases at 31 llc ()'37ati'\1"" 7 Ab'+'') anc.l 765 rorrs sho..'s-9% L'0-, ) 21a/o CO

/4r/a'oort*

0,19J:-2s!.-1tl ,1i,v =.-r.71 AI,is 100 x 419

I I

.i'i

i\

, t rl .82.37o/o N,. Assuming thaL the fuel oii consists r rl lrydrocarbons. Calculire:

rrl il,r 1..1gs55 2j1

l,l

,l

(4O.A3o/o)

composiuon of rhe fuel ojl (g4.gs%C, IS.OE% H) ,,,, (.-'V lost due to: Wt,t/o

CI-{AFI

t) Llnburnt combustibles (Z.l7o/o) r,) Uncondensed \4,ater iz igiri Iri) Sensibte Heat il g.5LVo)

t.R

SOLID TTUELS

h ,\ lrrnrace js fired-with fuel oil with a parlial a:ralysis cf g and 2.8"/0 N:gjs1r r' anatysis th;;;r.k;;;r.;;*." -d;';; o';, "f v" H,, a:8 gj 1,,' !)',S Airl 13L,?:' ,.r.t..r'r:-,Nr. .: if'j ?:' J suppiied is:at 23.i, i55 ;;r;; ( i,!,i1

'

!,),1

LirUt.i

(liilculate:e. l.'l I (l;rlcrrlet

,r)

l,) ,

H

)

excess a_rr (3B.AS9A Arralysis of the fuej oil (ZS.Z4%;C, rrr3 arrlkg fusl (15.34) rl4r

lt.

o/oH, 2.460/o61)

I'o,rl lar fuels are l;quld fuels obla-ined by b)erlding coal t,rr riisIillaLion products.such as carbolic ,f, orl, t.reosote bil, a,nthracene oil a:rd ,neairoi,pu.fr. ".plrUi=u-f"rr.

a ',,rrrrple etementa.l aralysis shows gS.go/o C, 6.3%i{:-i'.2V, I i, i; b,lo O rutd l.I % N. If this luel is frrr,r.a-ir_, ;;;;, ,rt ti(J,,C and 755 r.i' Hg wjUr g0% R*r, ;,

;;;-,;;;, " lrrrrrrergas containing 10.64%o CO", 3. lgo/a CO and 0.640/o ll,. Oa]culate; ,r) 'l'u excess air eL.l}otol ,,) Compiete crsat alal-ysis of bumer gas

,

) rr3 srack

r

gaslhg coar

rar [lil(l

I 'l'hc principal motor fuej blerid jn )itjt)-rkr{skof made up of 50%

02' 7s

German_v moto

r

]50luN,)

has

heerr

lseraore(7soft

rc I zerr e, I 5 7o tolucn OUn .1.rvien e), 21c/o I etr:Jtn C,.H,. j ! t d ?.So/o i n d u sr riC 3, c.oh ol (.qOyo e ti,a,r ZO.i ;; J;i?;;ii "l Af t:r cort:i_iL:si.jln ir r i_.:r:tsS aJr i1 "f g"s colL?i;i)ltg =lrck l).,139h CC, a.nd t.E39a H, is obiain..f Coi"rf;;;,"'"""" ;ri 9,h excess ar.r (50S,il l,) corrtpleLi,iL;;:ii.:.r. ,.,j lii,: sLack !;rs I

(

;

t

(8 09%

o,,

80 9b'r,c,\,1

4,I

CIjSSIFICATION OF SOLID FUELS Solid organic fuels are classified into naturirl aind ;u1ificial

fu els.

aj

Natrlral Solid Fuel.s il Wood-May be bunied directly as a fueJ or maybe converled into charcoa or producer gas Sawdust is sornetjtnes bumt at salrmills supplemented u/jth oil to ieduce fuel cost. 2.) Peat-Brown fibrous mass of partiaJly rler_:ayed plarrt malerial that has accumulated" under waier logged conditions:

3) fuginiles-Immature cotls that are inlerrnediate

in composition between peat a;rd bitumipous coals and are about 1 to 100 M years oid. 4) CoaLls-{ompact sfrafiJierJ mass of mummified planl debrjs thaL has acc'unulared dunng past geol;gical ages about(i00-300M years old) ard h:Ls been a_ltered by processes involrrjrg bio ch emt c"al. ac Li c.rn, su brners j u n in water and acUan of heat and pressure.

b) Artificial Solld Fuets 1) Wood ClrarcoaL-Solid

resitlr,ie {rom i]le carbcr:rzatjoi,r wood u,hich invoh,es healilg woocl strongl-v irr rhe absence of oxl,gerr of.

.

4g

I

I

I

.i ,i lllr

SOLID lrl-l!,1^S

lll' )MD]-RY

'.'l l'r:ai Chorcoal--Iviade by carbonizing peat at

iow

l(,rnperature.

',\l I ignite Biqt"ettes-hr dried lignites 'l) lignite Coke--Air drjed and carbonized Jjgnite i,) (loke-Carbonized coal

4.3 a)

EMPIRICAL REIATIONS CIN COAL rtr{ALYSIS AhJD CALORIFIC VALUES

Itulong's FormuloCV = 0.338

l,l el

nrualvsrs oF solro FUErs

ll .ll

lornbined water, netH, N and S. ASl{-Residue t}rat remains when a weighed sample of crr;rl is slowiy heated in a:r open crucible for 2 ho'.lrs at

IrO0- Bl 5'C. lrl.XED CARBOI{ (Fc)--Cbtajned by riifference of the sum of moistr:re, VCM and ash:

from

10070

F-C=100-M-VCM-ASH

l,l

llllirrrcte Anrrlysis"_It is a precise chernica_l deterrrrination oI llrc. o/o by weight of Lhe six basjc components of coal.: Carhon, I Iyrlrogen, Nitrogen, Sulfur, A-eh, and Oqgen (usually ott-tained lrv riifference).

C+

1.44 (H

- Ol8)

+

0'094

S

where: C:l = Grbss calorific value C,FI,O,S - % by wt o{ Ca-r:bon, hydrogen, orygen and sutlirr

l

t'tr\trruile.Anclysis-This important method of laboratory F{,lnllraUon of solld fuel js based upon lheir volaUlizafion r lrrrr,rct.eristics. It invoives t}:e determinaUon of ll M( )ISTURE (M)-ivatei ex;pelled when the coal sample is lrt:;rted for I hour at 104-il0"C. ''l VoI-ATILE COMBUSTIBLE MATTER tVCM)-Tota-l loss:n wcight minus the moisture in coal when coal is heated frrr 7 min in.a closed crucible placed in a muffle fumace ;rt 900"C in the absence of air. It includes volatile C,

Assumptions

1)

2) 3)

b)

in Dulong's formr:Ia:

CV of the fuel is the algebrzje sum of the heaullg valucs of elemental comPonents, Oxygen is combined wjttr trydrogen as in cr:rnbine{ wa!e5 ancl n:oisture, so that surplus moistu're avarlatrle for combustjon NET H) is I-1 - A/8 That the heat of fomalion of eoal is zero"

c,a)derusouT Eqr,t,:tiotrc-useful in finding the total _c:1r]ton content of the coal if Lhe proximate arnalysis and the GCV are known C = 5.88 + 2.206 (CV - 0'094 S) + 0"0053 180 -

i]00

VCMIFC)IIs=

Example ): A furnace js fired with su]:r-Lrituminous B (SubR) coa-l containing -10.3% rnoistdre, 3a% VCM a:ld 7.7o/o e^s,]n.lt is also lqrciurn tr:i contain 1'2% N and I "57o/o S. Its calorific value is 22 M,Ukg' Caleulate its: h-oximate Arralysis b) Modified tuta$tis aJ

r

I

tltxltfteclAncrlysis-Mociifications of the uidinate.euralvsis {br outbuslion ca-lculations. It inch:des: l) C, N, S. ash '.)) Moisiure :') Com],,i;trC r','aier {Ctl1- i.rre u-y,.qen irr rhe coaj(lrot pl-e se Llt jn rlo.islurei is treared as tJrough jt were already combined u.ith hvdrogen. ,1) Net Hvdrogelr (iit-iJ--1-i';tt;-lgelt r'"'iijr:l-r rc..frLlr.c::; O^ Irctni .i jrr

for

co:nbr.rsLiorr.

/ 5i

c)

d) e)

l,ltimate AnaiYsis Anaiysis of VCM Calorific \/a-iue oi VCM

Soiunoru Bv diff-erence: ToFC

=

100

- :34 10.3 - -/'7 = 4d

tr !tr I lt( )ivlDTi?y

sol,iD ruiit.$ ,/ 53

Cl l'lr{ )XIMATE ANALYSIS: It) 1",,M, 34% VCM, Z.Zo/o Ash, 48% FC I t.,tt tt 1

('

ilte

e)

Calorific Value of VCM = gV of Coaj x 100yqsgal:_.y. o{ea$pq{-.leFe

ANS

CaLderu:obd" Equatioru

lt.8B+2"2O6 122- .O94(t5Zl+.005S i8O_100(34/48;1,..,

= -22{]q0)'- 3.8-{48i 34

54.25%

I '.'',t Nl I -

I t,,lt

rt

lhtlong's Forrrulfl; 0.338(54.25) + 1.44 (NH) 2.44o/o

' +

t.

= 22.54o/o

!t4.ZSo/oC, 2.44o/o Neill, 22.54o/o 7.7o/o ash, I.2yo N, l.S7o/o S

I

Irrlrrl H = nelFl + H in combined water and moisture rrr (CW & M) = (22.54+1O.Sl x tZti8) = 3.649 'lirlirl H = 2.44 + 3.64g = 6.0g

ll

Irl.'lllVIATEl ANALySIS: ANS !

E.0g%li,

t,\.2.5o/oC,

ZS. 13o7og,

= 6.25 Arrall,sis of VCM A-IiS VCM wt C NH

'

;^-

o.1,J a AA

o/o

rO.JO

,o.<1 LL.J1

N

7.18 66.29

1.2

Q r.

cl J

)t,t) c,1I

4.62

ClV

34.00

lfhe combustion of coal may be'car:ied

crut by spreading it over a grate and firing or by iniroducing ir a-s p"r"-*.r.J ifi*r. coal and air are brought together at a temperat,re suficient to decompose the coal Jnto fixed carbon and *oiatrle matter and to. cause the fixed carbon'to ignite" Combustion then becomes self supportinf; 'i.e. sufficient heat is evolved tci rnaintain these conditions. However, coal contains noncombusLible matter (ash) which separates irorn rhe materia-ls tJ:at can be gasified ard is removed fi"om Lhe fumace as

REIUSE. This refuse may or mav not contau: unbumt combustible.

b)

For combustion ca]culaUons the combined % of N and S is i-reglected if the total is less tha:r or eqrral to 3%.

I.2%N, Z.Zo/o ash, j.S7olos

in the VCM = Total C Flxed Cal.bon = 54.2i _ 48

Vol;'rtile C

rll

a)

CW. 10.3%oM,

r) rrr (CW & M) = (22.54+1a3) x (i6lt8) = 29.13 r

4.4 COMBUSNON CALCUTATIONS

M()l)lIrIED ANALySIS: ANS

,

ANS

.0094(t.SZ

lry,llllbrence:CW = 100 -54.2b-2.44- IO.3 _1.2_T.T_t.S7

irl

= i6.988 MJ/kg

4.5

COAL COI\{BUSTION WITH NO COMBUSTIBLES IN THE REFUSE {TYPE II

Exampie2: A furnace is fireti wrth high ,cilatile A tritumino,s coa-l whose ultimale a:ra$s:s shows TS.2a1a C. 5.19o/o H,8.72oto O. 1 5% N" 7 B0lo a^sh, a,d t.tj%o S. 600/o excess ;itr rs supplied.. As5un.1e CO t0 (:.n . ralio of 0" 178. Th;;;[;as ]eaves * ZaO.C, ii6 torrs. Calculate: ?) Comp)ete(zrnalys)s of the star:k ,gas if air ts srrpplied at,2,S C, 100 hpa;rnd csserrt.rally rJry. b) m. air .supphecli 100 kg sii 6ocii

/

-._tUi.j,)

11.{ )I(]F{ICITiETFY

Ca-lorific V'alue of Coal d) -qzo of the ca-lorific value losL due to:

ComPlete l'rrai1'sis

c)

i) Unburnt combustibie ii) Uncondensed water iij) Sensjble heat of the stack gas

of

Basis: 100 i1g coal

0.s33 0.05 4-8715 44.245 2'595-

o2 N2

HrO

Stack Gas 3000c

100 kPa 60 o/o x'ss

1.61

0.09 8"40 76.24 4"47

s8.CI275

740 torrs

...* Lt' d! -3

BIJRNER

101325

=(+a.tgi \

lOOkgcoal

2'73 + 28

- x "--nra+l1.7a7)x224**;^ at\) luu

= 1399'83 ANS

Fuel Coal 75.2o/oC

c)

Cv = 0.338,t 5.r1 + t'4":' 15'19 = 31 .472lvIJ/kE ,LhlS

d)

o/o

5.190,r0H

8.72o/cO 1.5%oN

1.6% S

il't '*Co" =

'lheo O, = (75.2/t2) + (5. i9/4 + (1.6/32) - {8.72/32) 7.342 = X'ss O, = 0.6 x 7.342 = 4.405 O, frorn ur = 7.342 + 4.405 = 11.747 N, from air = 11.747 x (79/21) = 44.191 'l'otal N, = 44.791 + tl.5/28) = 44.245 .

0.933x28318 'u'u x I00 I00 x 3i.472

'

6)

^6^n, ANS = 13970

ii) iii)

Sensible Heat

C converled to CO = 75.2 /12 I (0.i75/1.175) = 6.933 C convened to CO. = {75.2/)2) - 0.933 = 5.333

lJv2

Free O, = 4.405 + t0.933/Z) 4.BTt5 =

SO,

CO o2

igiZ - 2 J-t.t

lt""?2/Bll + 0'094(1

2"595 x 44-04 Vapor waler = Uncondensed 1;;;3\A7;

GAS

:-:

-

calorilic va]ue lost due tcl'

7.Bo/o ash

l'l-O from Cnr;:f,r::.iror.t -

.J. 19

b.JJJ

SO,

AIR 280C

ala

n

CO

,$olufurrr'

Lhe stack ga.s ANS

GAS CO,

i'rrLi.:j / 55

N"

}I"C)

n

Cp(30O'C) 4J. ),.

0.s33 0.05 4.87)5 44.245 2.s95

29.63 45 34 30.9E

29.6l *q4.69

*

ll)lj = J.oc

GA

-1

I.;I.UICHIOMPTF.Y

s;lrt..ll) ttt;t';.s

Sum nCp = 1E13.37 % Sensibie heat loss

ner i{ cor:verLed to'pater = 1'6+6 x 4 '' 6 'i84 fotal a[ net H = 6.584 + 2(0.22) = 7^424

-

(18r337/i0c0) 3L.472

r

x

(300-

25)

Ar c bal: 0 e004

tOA

A high gradb semi-antlracite coai was found

to

conr:atn -o}.A4o/oC, 0.790265 and i .2o/o N on an ash arrd moisture free tiasj$ If this coal were burned in excess air saturated with warer at 30"C and I0S ]
b)

.Solutron-'

Ultimate analysis of coal(ash/moisture free) 0z6 excess air

Basis: 100 moles Dry Stack Gas (DSC)

AIR

Stack Gas

300c

10.83% CO,

105 kPa sat'd

1.08olo CO 0.220/o H, B.l7Vo 02

" r,: i::1 : !Ltu,*#

ULTIMAI.E .AruAr.YStS: ANS 90.04Y0C" 4.B23VoH, 3.747o/oO,

,.=,7.12

1.20r'0N

and 0'79%5

.-*-';Stack

756 mm l-ls

Bo%RH

fI

I

I

l-

-'7qn

E;.; cc.-. Aa7r.:. .-,.,-, ,,-< t' t:l.ls{; _ 722;j:: )t/I lrrl -- q,q 1.")_vLt.t (), Uilat:r-ot.,lr,c jbi: j.!,il (l . + .AS/2) +3.17]= L5.lij il 0.83 =')l

12

Soluhon- Basis: 100 kg.coa) AIR

O, fron: t:: = 7?.T y- (21/79) = 21.165 Ijxcess C'. = 3.17 - il.CEz'2) - iA.22/2)

x

Exarnple 4: A medium volatjle bituminous coal(mvb)-hf^"" "as receiv-bd- analysis ri{ 27"13% VCM, 62'529/o FC,7lT;/;ish, 0,95% S and 1"28YoN' Its caLloriic v'a-lue is 32 3 MJ/kg Thjs cr;al is burned in excess alr supplied at 30"C, 756 tors with 800/o RH' ParUat orsat alalysis of the slackgas shows 9'78o/o CO, emd 2.450/o CO. Calcr.:late: a) o/o excess O, b) Compiete orsaL analysis of tl:e stack ga^s . e) m3 stack g'as (270"C' 768 mm l{g)/kg-coa1

9A.O4o/oC O.79oioL1 1.20,6N

tu)

o/o netH jn fr.rel = {7.A24 / L55.729} x }00 = 4.43 % CW = 100 - 90"04 - 4.43 ' A'79 - 1"2 = 3'54 o/oH jrt CW = 3"54 x. (2/l&l = 0.3$3 o/oA ft SXI - 3"54 x (i6//i8) = 3.147 "r'' Yo Total H tn fuel = 4.43 + 0"393 = 4.823

79"7o/o N,

Coal

"1

57

aL

= 15.85 ANS

l,'rttmpl€ 3:

/

27.13o/a YCM 62 52% !-C 7 I loz'o ash

Gas 9.?"8o/o C0,

2.45o/c,

Ca

ST()lCHiOiviE'IF.Y

soLlD FUELS

Qi.dbnuood- EqtLaltiorc ToC = 5

DSG baf'

88 + 2.2}6rc2.3

l+ o.oos3f 80

I

53.3797=5.22 +

- 0.094(.95)J

x

Y

o?iall.55

-

too'1rr

1.308

+ y + (1.308/2) +

/.59

(Y+7.524)

79/21

= 3:7576

I

62.52J

Excess Oz= 13,7576/7.5241x 100 =5Oo/o

a)

0/o

b)

OrsaL AnalYsis

= 78.34

'Bg hnongs Farmulcr o/r\Trr /.Ji\i-L=%

_

,'

F

ICW & M) = 100 - 78.34 - 3.98

-.95-3.24=5.1

H = 3.98 + s.t(z/til) =

_

1.28

-

%Nz

,lct y = excess OQ from air= y i z.SZ+ N, frorn air = g + 2.524) x

+.gi'

at 30'C

-

{7.41/32) = 2.524

=

7.524

7.524 + 3.7576 53.3797

'logVP

= 7.96681

moles HrO from air =

x 100 = 8.26

:i 100 = 79.5I%

: [1666'21/(228+30)l ;VP

+s3576 s3576 r.5h44 +

3i.687{.8)

x

0.2I

= 31'687

756

- 3r 687(.8)

l

Zg/21 Zg.A4/ j2

Moles DSG = S3.3ZIZ - moles ," _SC .O}ZB x S3.3Z9Z = S:22 moles 99,il sG ==.9245 x 53.37g7 90 - = 1.30g -'vvu

t.sol/z x

53.3797

moles wet air = ('7..524 + 3:75761/.21 + 1'864 = 55"586

At C bzil: (.0^978+.0245) motes DSG =

moles -Eqqg1_-q=v+ N, = (y+7.524)

3.7576 + (i.SOSlZ)

7.11

%O=5.1 x(16/t8)=7.41

Theo O, = lTB.S4/r2) + (4.91/4) Or Theo Oz = atC + (at netll,/4) Theo O, =-(TB.B4/1Zl + B.eiiil

-

= 3.98

7.44 9.6

o/o Oz

32.3 _ 0.33g(7g 34) _ 0e4( e5)

Zg/21

ms wet

#=

!g

air

55.586

x 22-4 1QGAl756i '(ZzZ " 100

coal = i3.89

3:q)

t27X

rt,ff

sr,)i"lD f'l)ELS ,/

r.--

{Jt,Eilds d)

.\ sirn:ple of ]ignite i

fI? i:"#;{*$i

:

fi ;t),ftrxrmate Ana]isis

iilf i,:,f

.1,',r

L+.

*lIH'

_Ulurnare b.46o/oH, ^r,"t Sg.5loloo) _ r\ rli AnaJysis of VCM

65.26o709, t.47ot

"dr; ;;t[

;:)' A bur,.jer uses pirroh,,**r coar -,t gg;:A:"::!^:rgh a) excess .air Lr c";;r;;.',fi ,*,,.'trj;:,l o%

turlks coa.i

coa

iir'ffit"

14

r%

9. 8602'o

Or. Calcu lale ttre ftrliowi (65"08%)

n

I I

g:

*-# a,d g

l6iloor'

t26.25)

'as

i-eceived- basis, i]:-:" rhe pi-oxir:^.r- analysis rcpresentaLj'e ^.- . coatft";;.;: Sernirara of s3e6 Fc, ;r;; l ':'3 ii. "":._f*T."te js 32a/aYCM',a ;;l ts'23 78tqJ ik:!.e,. ,1?%N ^;;';'.;%{Iant u:""*,,,"i wrrj j5004 *:cess j,llt o"r,"11,::;#[;,lJ: driso iliat js. 5:l the molal ra.itr of'co' to co .r.rl.i,c ciry a.rr -, at 2 ..] r:J comple,. y* Ilg/x; coal (i6 641 rhe -,u=Soc,^7?,0 flt';';X^s t5.76o,6gg" J r rc"zeuu' r's:lt^:f

0 '28q"'so-, 12.75at.o..76

-4rry;N.

c,"al (2g.Sn

d) m' air/i<,g coal

(13.7e)

ash,

4 7to/oH. z.r6t/oo)

:.i?!i-]-:' !/ ,i, rruf lli ;r f4C.C. ", 77() mn rjfz.xg

l\9.24a/a)

b) UlUmate Anaiysis of Coal (4"530/oH' 6'04%(]) (24"5) c) m'flue gaslI9 coal

i'l,i T?ry'lg ;::,.?: ;:r# .H" f;.",;e#" rrt #:lr.! "!(r ana:\zes g'24o'o co' ' 'wy'a sor' 0.-: r'i:a.lculatei 5a'"/o-rlz "

(9.5270) (4.71olsl

A boiier is fired wjth eoa-l containing 72'$3a6e ' I4Vo ;rsij' L6.o/oN and l.2olo S bumt under eonditions that the elimination of comirustibies frorn the refuse is cotnplete The air enters t}.e fumace at 25"C, 760 mrn i{g with 80yo IlH. The flue gases g,les to ihte stack at 280"C arrri 'i 10 kPa. The al errge flue gas o:sat anaiysis is 8 41% COr' 2,52ok CO, O .7 60/o H, and a) %o excess air

28'o5eocw]

(24.G3 tvrJ/kg

:J m3 ",j SG,/kg tU

tr.r

Uncondensed wa.ter 'Sensible Heat

rs=ixi,:

1r5.43%vcM)

r) caronfic

C\r lost due

Unburrit eornbustiblcs

,, Modrfied Ir) Arialysis (46. IATo/rtC,' .i2olnrlu cr o: ar. ^,. * 9'913cracw) t:/

i.tl

6l

5.

A certain coai is pulvettzedand brirnt in a burrier. Analysis

ofcoa-tshowedTO%C"IA'7o/a;lshandl'20/oI'l"lJ:r:refuse is substantiaJiy frie of combustible. A sampie of tJ.e flue gas collected and analyzed in ar orsat apparat-us 'rver *"r"rry conlains $.$':lzo C0r' 3.320/o CCl, 0'32010 S0*" 3'32%o H, a:rd 9.53o/o O". Air supplieri is at 30"C, 1 atm ;alrd sCturated with water. Ca-lculate: (45' 130./o) a) o/o excess O, coal of b) Complete uitimate anaJYsis (4.68%H, 8.280/o O, 5"140/o S) c) m' flue 6fas (250eC, 1 ahn}/k$ coal (22.721

A hjgh voiatjle B biiuminous

coa-l a:railzing 22ilk YC\\n,

64o/o-FC,4o/aM, 1.4% N and l.60zo S hras a- *;.lcrriic valr-Le of 325 MJ /kg it is br,rmerJ in e-xcess ajr suppllr:d essenlialiy dry at 2B"C alrl 1 atrn. The star:k ,{ases ie ave

at25O'C,'740 rnm tlg and cortain 8.370ia CO,, 4 1990 CO and 2.51oto FIr. Calcuiate: t400tbj a) oz'o excess O, b) Complete crsai anal-vsis of tbe stack gas ( 9.11% O. , 75.82o/o N.) c) mt stack gasl m3 air (i.89)

I I I

:

,

'

-' /

ti.f(

)ici

jioL{F.T.liY SOI-.lD

4.h, ccAr-

c"yy.y:rfoN WrrH ccft,rEusriBlEs

rN TI-!E REFUSE {-rvPE t,} r\40re often in t,e combusuon of sorid fuers, the fumace ashes r r111(;1i11 a significant arnount ;i;;b"rrr combustibre r,ltt:.Live,1z called material me nedSe;;;, instances, to be able to rhe refuse '|'r''t1\'7-e berter, *;;.;; .pinro.a into it to rorm what eiLse i",rr.' ]l' I.', i3 :.f;f"1 " "",ii, "u o,, car c uralion s, these 'l'l rere are four cases CombusUble lost jn the ,r) Case A_Uncoked ofC"ri'il=, refuse: ,, the Refuse js ;m"h;f,coal "orr trr.tlas tosr only its moisrure

coiel r:r:ntairrin{ 4 79/n M' 24o/u Exanple - 5: A fur-naee burls VCNi, 630/o FC, 1'20lo I{, 1.8% Si and B.99zo ash" Ils c4lorjlic value is 32 MJlkg" Deterrnine the 0lo VCM, e anri Calorific Va]r:e lost r-rt t}e r e lrse f it analYzes.

a) 4"8% VCM. I2"6a/a F"e and 82.6% b) 24ak C ar:d 760r'o ash c) 7.fiah VCM, 29"2o/o FC a-rrd 63.$/o

;

*rHra:?i djil :"*rT: :; JiuiH.;r Thus ttre.following (FC/VCM) in greei

l,J asigToked

r*

'Sclunon-'

al

2"62b

."rt = lpgffiM) jn the refuse

Ash

Coai Losr in rhe Re{use \_nKed Joal is coal t-har has lnst lroU, lL. moisLure VCM content. Thrrs and

*,

is less rha:l 0.2t6-;';;.. '- '""v ,-^ uc assumed to carbon.

e.ssenlially

c)

of Coked a::ci ijrrcokeci Coal

ffif-ombinaUon

(FCI\,CM in green coaj

,l)

Pa;+;*-r- Ccl.;rcj CoaJ P.uiil-lir., ,;kiJiE;,1

*

Cr Ll de

(FC/VCMI jn refirse

I OO

ash

LJrreoked eoal

bal:

0"826 x WT Reft:se = 8.9 Wt Refr:se = 10.7'75 Wt VCN{ iri Refuse = 048 x I0 775 = 0"5172 wt FC in Refuse = .126 x 1A.775 = 1'357'7

= (0.5172/241 x 100 =

=

E Q uatia n: 5.8-B + 2.2d\6 132

=

/ /.6J

rut o or7

o/oC

astr

kg coal

= 2.625 Case A:

VCI\4 lost

o/oC

in

i,r;J Lj:ai lra> .lcsl a_ll jis r no jsrurr_ content brit not all VCX{. a"ulyuil'cf rhe refu,ss slrcu,s sr.qn;i;,.;,:;:,"-,].il l.,i;i J..:,,.,^ .li.:,,. cr:itl ;:; ,,ut .,iuot lo r.he i-aiii_. oi eC,",".-r,');#;t:].k:::. r:.

e/o

Lre

The refuse is a mlyture of ash, VCM and FC. The uncoked coa-l that gces i,to ,i_r* .lf,r". co,ntributes vCM and FC; rhe.Iokeci bo{ir ;;j;; goes into ilre refuse only the FC. -fir,r"-t_[. foljc,,l,ing retauon js mTO",es

Basis

Test for ttre Case 63/2al'?= (12"6/4.8)

reiation js true;

-;l^;s of rie refuse ci.ntains negUgible volaule conrlrusiible'rn]rt..; Carbon and ash irie t}re main constituent"-. ;" jcir.i) if Lire o/c VCMin rhe refuse

i)til:ll.S / 6r

ls0 -

-

2.155o1o plJ'!;

0"0i14(1 $)l

iclo(vcMlFCl)Jr

+ .0053

ss

jn the VCM = (77.83 '- 63)124 x ltl0 = 61.790/o

Wt C in tlte refi-rse = FC in refuse + C in ttre VCM in relrrse = 1.3577 -+ 0.6179(.5)721 ,= 1.677 C lost = 1.677177 tl3) x 100 = ') 155%: AIVS 32(roo) - "'_'. 338t63) - .___-._'...'- .. jl_ r-\/ 44 h(8 htj, }-g u\ v1 ^. r//-M 24

o/o

CV lost ozbCV

in

* 4 4.ti08(.5 172) = 68 96 t I; /{32x 100)J .x }00 = 2 l55a/c,

Lhe refr.rsr: = 33.8( 1.3b7V

lost in

tl're R.efuse

,=

[68"961 5

,i,1,,,

r

1'alji,t HIOtu1r:.rTirii,

S{)l.,li) i.'i,i:ilS r' ilS

rV,fe:

Ataiysis oi

oro

nerH ,ost,

o,t,

Cv/ lost, % N lost,% S lost

'r' rr.llj .lost = lyr.eF f., VCNatfUd of VC r"z"ne$r r', vcloa["

0z6

100 = 2.1sso/o

lrrst

l,l

i

I I I I

t I

x]oo

I

=z.lsso/o

I i

I'hus for uncoked coal; ('()VCM lost = g.ol!-fost ahClosl o/oCVlost = yonelH ]ost = = o/o CW lost = oz,o N lost 9/o S lost = = in the refuse l(r.fuse arraJysis: 24o1oF.C and 760/o , ,,ro].S,r".

t-r.pe

oi combusUble is Cokeri

rosr

o/oC

irr VCM = 61

79uto

0/o

Iti 1ost,94 S k:st.

fl6rrslf-LlnYQ_M{u'i-A[Jcl{ln_r_efusc]x 100 = 4.BTSa/o -"=(-o4netH ln VCM)(wt of VC[4 tn gr.Coa!

netH tcxt

o,,c

I t

I

l'

%CW ]ost

I

= t%QW-l!"Y-CMhvt qf VcM-lu.Refuse--l x P/r{:W ,n VCM)(wt of VCM

lri Gr.Coal}

100 = A.;.'I1ato

t I

'l

o/oN

lost = 1%NI!-YAML"WL of N lq-i/eM lr-refuEE] (0/oN tn VCM)(WI of N trr VCM in Gr"r:oa.!

o/oS

lost = !2qtrlYeMJilUlof S ITLVCM ln retuse) -x (%S lrr VCMIWI oI S ln VCM in Gr.Coaj)

f,

x-

100 = 4

BTso/o

t

t00. "

4.37bota

B:g

Wt C in the refuse lt.7l (.2+) = = 2.61 '!6 C lost in lne refuse _ (2.gi/77.g3) _r 100

l^ cv

coal = 77.83o/o;

I

I.

Ash bal: 0.?6 x Wt refr:se Wtrefuse=ll.7l =

I00= 4375olo /J{l;

Note: Analysis of Yo netFl losl, % CW lost,

I

ash

no VCI!{ is present, t{re

x

Wt of e j:r refuse = 4.088 + .6179 (),05) = 4.737 % C lbst ln the refuse = (4.737 /77.83) x J.00 =, 6.08% AN,:i CV iost in the r:efuse = 4.088{33,8) + i.05(44.608) = 185.0.tii o/o (N lost = tl8s.Ol5/(32 x I00)l = 5 78oto ANS

I t

x ]oo = 2.tssa/a

,rr,t, Jtr' lr,...t frl:il= - iozoS tn Vt

arJ o/sC tst C.V= 44 608

From

";##fm]x "' W rast = m#*#Hm###*+*ffi x r00 z tss*,,, =

'rr'['J

VCM lost = t1"C5/24)

in the reruse :

i;:jf'"tr_l = I!"92o/o ANS

/ (]00 x 32)j .x r0o

I.tefuse analysis: 29.2o/o rFC 'r-csr: (63,/?+) .t= ,y1 ::CM, -v'!/e \ and 63.6% ash (2g.2/Z S)' 2.625 * S.Bg3 Case C; coked ar-rri uncoked coa,l A-.;h bal: C.636 x \..t.r relusr = I e wt r:t:s,: = :1 l\t of \'g1u.r ;- r_ -r

liii ci rc r.'i,.,]''== r_!,., ;,.,r=]

Thus for Case C: o/oC lost * % VCM ]ost + o/o CV lost + % neltl lost o/o

in

netll iust

-%o

CW los'. = o/o N losf. = 7o S ]ost = % VCM losi

refuse

ExanpLe 6: .A boiler is fired w:lh co;1l irr:aiyzing 13 80lo VCM. lSala M, I.2o/a S, negligible N arld a r:aJorilic value of 32.95 MJ/kS.The drv refuse rernoved anallzes 5% VCI\4, 27t/o FC ard 680l,: ash. 600.t0 excess air' is supplied at at 32 "C, 758 rnm lJg s,it-h 85cz'oRll. 90?b of the cat'oon Easified bums to CO,, tJ-le rr:st to CO" The molal ratio of H, to C0 rs 2.9. [-liilcr:]ate: a\ o/a C lost in the refuse

',i:t '

b) irr: ajrlkg coa) c) Orsat analvsjs of *re stack {irs dJ m"= stack gas/ke roa) e) tr:ia1 t'z'o CV k:sl

sctt..tn l't rEl-s

6F ,, ,;'l r )ir_HlOt"{ETRy

Easis:

,Soluito,-i-'

1O0

ig coal

AIR 320C /58 mm Hg 60 7o x'ss

Stack Gas 4000c

n;il;

At 32"C:

log VP

= 7'96681 - I658'211t228+32\

VP = 35 532 nim Hg .^ n^-n\ -x (12'333 + 46"3967)

BURNER

HrO from aY" =

Fuel

Refuse.

C,:al

5% VCM 27% FC 680/o ash

13.80/o VCM

8.6% ash 3.07q. M 7.2% S CV= 32.95 MJ/kg

= 2437 ms air b)' +. kg coal

(tz.aea

760 273+32 2::'):2:-ffi.]::Wr n6ss6''.**100

**-

= 15.348

'l'est for the type of combustible: (74.6/13.8) ? t22151 5.406 .=.5.4 Uncoked Coal

Wt of VCM in the refuse = (8.6/0.68) x 0.05 = 0.63235 lost in t.t.e refuse = (0.65235/13.g) x 100 = 4.Sgo/o

free o, = xI55 02

o/oVCM

"

()zn

C lost in the refuse = 4.580/o (\tFC 74.6 tby difference)=

ig

Cat d-erutood equation: o/oC 5.88 + 2.206 (32.95

=

+ o.oosa[so

3

-

+

(0.094)(I.2)

I lt 1

lh

:

l.:;r

a

-Forml.rlcr-'

-rtetH

= 3.68

I..14(nerHl

-

0.r_,94{t.2)

'Ya (l.ii.- l0C El.';6 - 3.o8 - 3 - 8a - I t, -. ).tc

(1

.'lvir.i.;tur'c

=J

. -t

I'ry.i:1

at C lost in refuse

gH.

"UT*

'L

=537

il2:-,i = 0.33t(31.4e) +

o/c

.H,z

= 4'625 - 9-Y*

8lrss

81.46

ig,.

free o,

.:

0 0458(81 46)

L - lgsJ746)

=

:

-jjg:jlqs?.7ss - (85X35.532)

= 6'477 At C gasified = (1 -"0458) 191"a$112) 5'83 b conirefred to CO, = 0"9 x 6'4?7 = 0'647 to C0 = O'l x 6"477 = C "orr"..t.d H, in the qtack $as = a'647 (2/9).= 0"144

I

67

7"71)BZ Theo O" = 18L.46/12) + (3'68/4) = '= 4.625 rreq f) 0.6 x Z TA83 = ii:t"#, ut = 7'7A83 x= 4'625 = 12'333 air = 12'33.3 {79/2t) = 46'3967

765 mm Hg

85%RH

/

eAe

'-YY \ t-l,O jn Srack Gas = (t - 0.0458)-zu It a

,.'

18

= 4.325

-144+2..1?,7

,2ao rt) -

u-0458]-

., 1'

I

\

)t(tIJIOMETPT SOLID ITU}']I^S

)r,i;tt

(

A;:alysis

ANS

Gas

n

,1Oz

o/o

5_83

CO

9.98 1.1I 0.25

0.647 0.144 5.37 46.3967 58.3877

H,

o"2 N,

rrrir.stack Gas kg coal

A

e)

g.2O

79.46

*$a.uzz + as2s) x 224 " *

^zis

! +oa

= 34.4 llr0 from combusUon 4.325 _ = .2.432 = l.g876 9{r CV Iost in the refuse = +jS ,x, oV rost ctue ro co =U6i;;zffi.ol)/(i00x s2.gs)]x100 = 5.56 'r1, CV lost due to

H,

= [(. i4+

= rX,

x

1.25

2g6.03)/ {] 00 x 32.95)l x toO

CV Iost due to uncondensed = [(r.8876 x 44.0a)/ tez.gsflwaler i"l aC = GAS CO,

nn ,LI12

o2

N,

H"o

n

Cp

5.83 44.79 0.647 30.19 0.744 :rti 29.06 C I 4^ 5,42 .r1.JO 46.3967 io ar-9{ aa 35.2

o/:

cv

rosr ci.-.e ro sF{ =

2.52 /

I

AIR- ..-300c

Stack Gas

g.

2500c

735 torrs

zg%co,

1.470/o

ao

745 torrs

gO%RH

BURNER

VCM

I Refuse 32%

I

F-C

620lo ash

78.350/o C

l,

27o/o YC

lr

)

ir

/ . Ie/a ASr)

I 68.52

0.950/o S

r3 _ I52.31

Wt of the refuse = (7.\/0.62) =

9,-c9.Bl

P x )oi) =

I

1.3% N

l 384.

"_,

22,'65 = 36"5604

I

60lo

4.l8

g,ffit#f

2.52,

1.25 +

Solufurru Basis: 100 kg coal

COAL

261. I l 19.55

= 4'58 + 5.56 +

Example 7: A furrace bums coal a:ralyzin g 78.3r.>o/oC, 27ale' VCM, 1.3%N, 7.1olo ash a-nd 0.95705. Aneriysis of tl:e refuse shows 6oloVCM, 32% FC ancl 62Vr: ash. Air supplied is at 30"C, 735 torrs wjth 90% RlI. TLie stack gases at 250"C and 745 lorrs has a . partiai orsat analysis of 9.79% CO, and 1..47% Cro" Assurring that 5. L90/o of the e fired is lost in the ' refuse, calcfulate: aJ Complete ultimate anaJysis of eoal b) Tlpe of combustible in the refuse c) %o ericess O, d) Complete orsat analysis of the stack ga-s e) mt stack gas/ .kg eoal

Fuel

n9p

r

TotatVo.CV iost

,/

O9

11.45

f;;t of C in the refuse = 05i9(78 35) = 4.1166

\\zt of C in VCM r.n ref = 4.066 - ("32.1(i1.45) = 0"402

i2.t 6.r

o/oL'.

in VCM = 1402)/(.06 x ii.45l x 10C = 58.il1 jn coal = 78.35 - (.5851 r 27) = 62.55

oz'oFC

ll

,r'

,

l( il(:l-llUMETIl';'

I

Sr.;.-lli 1'l'r

r,,rrtg the Cd.denuood. Equation: 78 35 = 5,88 + 2.206'{Cv _ 0.94(0.g5ll + 0.0053

I

iso L -

t7 lrss -' roo62.55.1 i

OSG bal:

iv = 32.292 I

t:,ing DLlongs Farmule 32.297 = .338(78.3S) net FI - 3.98y0

ll(.u ,/-rrro.r.r tL, rY qvt/

rr,irl'l

(l{r() rXr

.l

y

+(.BCBl2l + (.trS t9 :t7E35l/$2 (.025q x 9.96)//4 + y + 0.766 =

free O, =

54.973 = 5"38 + 0"808 Y = 4'74

+ t.++ nerll + .0g4(,9S)

^;^ = O,JZ

c)

96 Excess O,

Lrl

a,,o

%o

in (CW&M) = B.Z2 x (2llg) 0.g2 in (CW&M) = 8.32 x ,06/tgl== 2.4

= (4.14/7"5241x 100 =

2.316 ;* 5.333 Coked arrd Uncoked_ coal in Refuse ANS VoVCM lost = o/o CW lost o/o NH lost in ref = ' =.06[1t.45)/27 = 2.54

1j,v:x'ssO, O, (78.35/

'l'l.reo

=

t2) +

(3 98

O, frcrm ar = 7.524 + y N, from al't = t7.524 +'y)

x

/4) = 7.524

7g/2]

At C gasified = (l-.0519) (78.S5lt2J = 6.19 I'SLI = (6 lg/ I l./Si = =4.973 CO, jn'SG = 54 973 x 0g7g = 5 3g CO ;r SG = 54.973 x .U)47 = 0 EOS

Mcrles

i

10C

- 397 A)iS

(t i*:rtnt):lt:,p

!)2

-

zz+t

Total HrO in stack gas = (1-"0254)(3.9812) + (1-.0254) (4"97/tB) + 3.35/iB + 2'24t

- 7.1 = 3.35

J EQtr? * A. UJ.J '

'li:st for the type of cornbusljble: (62.55/2n ?= $2/6) Ll

55"02a,'o ANS

C, in SC = [(4.14 + ""793a\i54.97'ii N, in SG = 79.77

mores warer rrom ajr =

II,TIMATE ANALYSIS: ANS 7ll.35o/oC, 4,9o/p[, 7.4%O, t.3yoN, Z.tVo ash, 0.95705 t

Moislure = ]00 - 2T - 62.55 CW 'k' = 8.32 - 3.35 = 4.gZ

768 + br+7.5241t\79/21)

A- 30'C. VP = 31.687

total H = 3.98 + O.g2 = 4.9

(l4r

+y+.

e)

(s+sza

m3 Stack Gas

+

a63s7)

273 + 250 x 224,|?t, '--^*;;--' Lti\

kg coai = 26.09% AN-S

Example

8.

Coal fired i.n a furnace ana)yaeso/o 340./0V(lM' 44a/oF'C" 7.7o/o as]n, i.2oloN axd 1.570/o S. llhe reli:se contains 6.2010 vcM " 8.750/o FC, 35010 a'sh and

50.05% HrO. fur sr:pplied js at 35"C1, 765 min Hg B5olo Rll' The stach gases leave at 250"C' 766

u'ith

CO. 2.320/o Hr, 9^54ako" itnd 76.5)-0zb

C lcs[ in i]re rrfuse a) o{ coal CV b) e) ijltirrlale tuifl1,sis o{' cca-} d) o./o excess 0" o/o

N,

Calr:r'rlaLc:

I :.i()1,1D lfliL;i..t; ,/ /3

o/o

Stack Gas

AIR tJ(

2560c

l

hlltl l lg

it

. tr\'. 9.37o,COr\ ', 2:.3?a/o

CO+-

t.il1

BURNER

Refuse 6-2o,'o VCi'i;-1

fttr,tl f,4'1,(r

8.75olo FC

VCM

ash

H, 9.5p0/o O, I 76.52% N., I t. ./ I

50.05%HrO .;'

f.

+ 0.0053 [Bo

I

ltrsis:

(2.7t.35) x 0.62 =

.34

5I'36 = t(i2.I05)(12)/282.51j. x 100 = 2'21 100 = /282'811x 7o netH = [6.25065 .2. iCwarra) = 100 - (51.36+2.2L+1"2+7'?+l 5'4 = 35'96 o/oH in (CW&M) = 35'96 x l2/l&) = 4 x (16/18) = 31"96 o/oO in (CW&M) = 35'96

Coa-l

o,/oC

x I00 = 4.01

in the refuse = 4.01

1O0 moles

dry stack gas (DSG)

c)

N, Iiorn asr = 76.52 t ri frorn atr = 76.52 x t2l/79) = 20.341

,rt. net H gasified = i.364 + 2(2.32) = o 'l'olal at netH charged = 6/(1:.0401) = 6.25A€'5

t F = ,;;i cf rirt

in ,i.: iirl

-i '

i2

-

1'57VoS 51.36o/oC, 6.2La/0L1, 31'96outrO, 1'2oloN' 7'7a/a'as]n"

o, = e 54 - Q'32t2) !19'(?*?f

' .

1I-'U.99)

.0401(282.81X0.022l) 4

= 6.672

d) 9'o e,
672)l'x 100 = 4B'81?b

1lJ\iS

DxantpLegrAfunlaceisfit'edlr'it-hcoalu'ill:the'follo"wing 4/' allall'sis: 3O 3oZn\rCN1. 43 6% trC lA Tott:;rsh' ii 29'5 is lt's ciilorillc '"'alur: M. I 2ti,\, a;rtl 5 lozi'S

ir.i,:I

12iC5

ULTIMATE A]ttAlvsts, arus

x'ss

(,7 unaccounted for = 20.34i - (9,3 + 2.32/2 + 9.54) = 0.34] or ;( 1.364 at netll

t\'('.

+ 14'* t6'250651FI

F = 282.8I kg CV = 20.69 MJ/kg

Al C Sasified = 9.3 ;2.32 = IL62 'lirtal -at C'charged = 11.62/(t-.0401) = ti.rO5

lx:

3+1'55 os ]

Soluirrg simultaneourslY;

lr79lo S

O lost

-- I 00

CV = 0.338 x (12.105 x t}/f x 100 + .094,(1.57)

)

f'r,,t lbr combustjble 134/48) ?= (6.2/8.75) 0.7083 = 0.7085 Uncoked

rHr

100

F

l

\ \

'l,'itYo ash I il'Zo N

V(lM lost

x

-.//

357o

rhr

= 6"250651F

-

{Hrl4 FC

I

ir-rel

]2]OtPl x r00 = 5,88 + 2.206[cv - 0"094{1 57)}

I

f uel

in

Calderu:ood Equafr'on: '\

766 mm Hg 2.Spato

neri-i

x I O0

-=1.-ll|rrrry-

SCILIi) ,.LlLl)i)

AraJysis of ihe werted refuse shours l2go *,r^ryC , 65oh ash ar;d ?-39/o HrC. Dn ar. is supplied at

o/oC it DSG = 8.71 + 7.74 = L0.45 r:roles DSG = (5.6687/0.1045) = 54.2459 moles e0, in SG = 54.2459 x .0871 = 4.7248 moles e0 in SG = 54.2459 x .0174 = .943"Q rnoles H, in SG .0035 x 54.2459 = .18986 = moles SO, in SG = 5.1/32 moles free,.O, = y + {"9439 /2) + (,1898612} + (1.9754/

27"C and 1 atm. The stick gases leave at S50"C, Tn|- ^yy' Hg with a parlial orsat a-r:alysis of 8.77VICO2, l.7.inh CO anci O.3So/o H.,. ! Calculate: a) 016 a';cess O" b) Comptete orlat aralysrs of the stack gas c) m3 stack .gas/Ig coa-i .Sohrtforz'

Basis 100 1g coal

moles

r--_-;rsiack

?'/oc

rr;' JJU

'l ;rtm rlry

Gas

l.} n U

745 mnr Hg

BURNER Fuel p% vcM

49.60/o FC

10.7% ash i\,40/o M L2%o N ll. lolo S

121

=y+J31b N, in SG = (y + 6.923XT9/2tl, + tl.2/28j

DSG bal: gives Y = 4.4961.

AIR

rJ6

,/ 75

B.7Ia/oCO, 7.74o/o CC 0.35()/o Hz

a)

b)

o/o

excess O,

= (4.4961/6.923) x i00

=-

64,.94 ANS

Cornpiele Orsat Analysis ANS

= l$r/32)/54.24591x I00 = 0"29 o/o], = [(4.4961+.7315)/54.2459] x 100 = 9.64 .t 4.496r)(79 r 2i) + (t.z tzat, ,' _ \ n,-*.;_ (s.uzs r nn .aA dry o,/^Ni --___ - x 100 ,='79.27 b42459 ' %SO2

Reflrse 72o/o C 6570 asli

HrO from combu$Uon = (3"72/2) - .18986 + i5.88118) ' (3.4/18) = 2.1857

23o/o H"O

ov = 29.5 MJlkg

c)

Ilsing the Calderwood equation: o/oC 7a = o/oCW by difference = 5.gB IIsing Dulongs Formula: o/o netH 3.7?.

lqi

CoaJ

Weight of Refuse = (10.7/0.65) 16..6 \\rt oI C in [he refuse = O.i2 x =16.46 ].gTS4 =

At C gal.tripd = {70 -).975q/)2 5.6687 = 'lheo C), (7Oii2) + = t|.Z2,i,t) + (5.1/32) = 6923 J,ctv=:..'ssO..

=

!3I1*

.r 2E42

:

=

(), fror-i'l ;:-:1 .= -: $.g23 i,: N, from air = (ly" ,r 6.g23) x i7'gi2.1t

:geck-g3: -/--\\

Qxnmple -'---/

/L;

??')

:'?1:#":-:i;# r00

ANS

The ult-imate a-nalysis cf col iired in a borier showed 57 .O40/a tota-l C, p0 5% VCh{, 1.2% N, 9.7% ash and

S. Analysis of the u,etled ;e :se showed FC, 2 1 .1a/a \ CM, 47, 8% a^sh an d 1 5 90./o FIr O. tur is ar 28'C,.756 mm i{g with 760/o RlI" Orsat a;la.iysis of *re sLack gas sltows V.92a/o CC)r, 2 380z6 CO, 39% SO2, 1"79a/aT1r" 10.6570 O, alid 7V.47o/o N,. Calculate : a) 7o VClyl ;ind C jost jn Lhe r"elu..,ir b) Ullirnaie anah,sls ol coaJ 6.30lo 1

3 . 8o/a

"

-]

9,0

7F^'r ', 238!2' for = unaccounte'J O, '-Or'JUUr";;;: 4 1'68 to *''iti = A''42' x = burned H nd! Ai

eX:eSS C,

c) Calorific

Value

of ,Coal

Colutian: Basis: 100 lgrnoles DSG

AIR 280C 756 mm Hg 76 % Rt4

f6t2l At net H =

'Stack Gas

'

7.92o/o CO,

Reir=u

Fuel

[r.oe*I.iq.2I -^.7^ - =+ta

-1l\-

;6)

x 100 = 2'05 rrctH = t4'74/231'151 (zuz ^o2)1? * 100 \t'vt++ r-?qiqg = gasified os@tzat ls) o/o of torerl c that is

39% SO, i.19% I{, 10.65% o, 77'470/o N'

= 9374

100 '93'74 = 6'260/o C lcst in the refi:se =

o/o

Coal

21.5o/o

57.44o/o C 30.5olo VCM 9.7c/o ash 7.2o/o I't

13.870 FC 47.8o/o ash

t

tr6.9%H2o

i

YCM

By difference:

f

l

o/olc'*r

ANS

(21]6) 2"63 ,t#'-J# !'ZZZ, xx (16/18)== 21 06^

70tl;iCrvaY6=z'3'J'1

[: r

l

6.3ozi, S

'tr.o

o/o

2.38o/o CO

BI.JRNER

,

o/o

i:

2'O5 = 4'68 total if in co'i = Z'Og =

r

r..

t t :

o,/NCl/I iost in the refirse

%N lost

(9 / t478) x A.275 X lUU 305

I

= 14.39i, nt*{S

r I

in the reluse = Yo S losi in *re refuse =.L4.Bo/o

t t

I

b)

)(ss

0.053 &\'t fuel) (1-.143) = 0.39 x 32 . Wt of fuei = 23i.15 Moles of ItJ, from'the fi:el that is gasified

-

-

Moles N.. Iroin Moies (1., i:l;n

?a= ar = 72.47 - f)4tr - -;'; ' /,\-:L.., ;tr = 77.1,6,:: .:i (7?./'i)] - ){) v7

Oz = 10"65

* 11e .)

(00626)(41lErygq{ L2

0143(2p115x099)q) -?

r+:)

/-,Qq

6"3'rhs I'2%N' 9'?o/o ash' rn refl4 atC in ref - al- ne*{

qaeirllzto""o' 57.oryo/oc.

. Xss O, = free O^,-'- "Ot':

SLltfilr boJance:

O12(23115) , (i 28

ANS ULflI\4A"lE ANALYSIS

- t e' /t20 5?-8) I x

100 = 63

619/o

c)

9/r e)icess Oz

d)

+ \'4412'O5l +'094t6'3) CV of coal = .338(57.04) ANS 22.82 MJ/kg

-

|"

t

ANS

,,|l

in a furnace

ol 91-tiT ^-o.r anaivsis 5;: -#: : t'r. Tg,.',,27:.:?f?*,.: ll tr3'.:f' i" \ =i.,;"I" tarrs with B0% RH' "#:Sfi,,-#";;;'Li;i'-ida

"izo:"s f#$J,fr

ftrrnace is flred wiih coai wif-h the following proxjrrrate analysis: 5o/o M, 60% FC, 250lo 'vCM and 10olo ash. Its caloriflc value is 31.33 lvil/kg. Calculate the %o VCM lost" %o C lost a4do/o CV lostin the refuse if t}le refuse analyzes: d 250/o FC, 4o/o VCM, 71Yo ash 15.1, 4.59, 2.25) b) 14.4%FC. 60/o VCM; 79.60/o ash (3.02) 8.2. 2.63) c) 19.6% C, 80"40lo ash

l"'A

fl: ::;k

ff

'116'f'ffi

#'

oii

Y'q'**:

(Ie'92 ' 17l']l) ""lHFtila o/ovcM lost in tlte refuse Ui Vo **.u" O, [20:41^-. co'af 1g'OgS) airl}€ uua a:r/KB cl J n-I' ;?B"Cgq,ol'12) ".' of'ililr"tgas (g.170/o 02, 'ana]Ysis di Orsat

',t. A fligh volati.le A bituminous ccal anaJyzing 73.77o/s C, 5.23o/o H, 100/o O, 1.40/o N, B 10/o ash,3.90/o M and 1.50/o S js burned in a fi;rnace together wlth 45% excess a-ir suppiied saturated aL 25"C and I atrn. Ana.lysis of the

5

t:.'1 A hi gh gracl e se mi - a:r thrac*:,

aiTil

" :.TTl;t ffi t3,I;'^"ifil.f1,l T'i"t' o' l3i, tt?ElB'#t:;;^fr'ii' K; g il'Tvll"';t *. T: ?"jf ,Ht:#i "o;';i-iil;

;'r;"n"y:rtfl:

i; |.ii'iiH :*3-:J:3,: ows 8 o5%o g:"' ::,T:119 sh ;'"# :;;\spl?g*S:1?.t:T-; ixi.i,:iJ a)]@rv"* { z"gP/o }\' eaiculate: 2,42% c9 Tj-, co", -% (55) excess Oa) oisat ana]ysis of stack gas Co,r.,pt.te ili 9olo Nr)

VCM" 23.55o/o FC, 32.480,2o ash and27,97o/o HrO. The stackgases leave at 300"C. 7'15 ton-b with a CO to CO; ratio of 0.12. Ca-lculate: a) a/aC and CV lc'st jn-the refuse (1i.18) b) ly"pe of combusti)rle in Lhe refr-rse (Uncoke'i coa]) c) Ors+t analysis of siack- gas (i09/o CO, l.2o/o CA) d) nr3 SG,/)
welted refuse shor,vs

analvzes

fired "';:!1":]t#;^:,1,::"1* rvr' ir' i"'*'"9 1:*::Ti1,.13;'i';."iJr: '# Coal i"1i' ;iir5;" 6i.4% !U, o'ro tjtii::, shows 44ola ush, o"t/kg Analv?i:

160,6

UO.73o/o C2, 75

,r' =t^.i. g"asl mt alr ")

'

,i<' The following datawere obta'necl durirtg coa1 cornbtrsUon: Coa-l: 13.8% VCM, 71.6% FC, 8.6?ar ash, 370 M, 0% N. 1I 00 i,Q. L /Vvt

(1 624)

to A sarrple of coal rvas found

cunran.1"'1:IJl]:3itr1

;"'1": :'^ ::::5,i' i I 3"il$ t ;ilJ8l ;; #$" ;?",i,.;* ;;iEi 1.1;ii,;#dfr"",H;; ,";

?:-*o T*^,?: e87ez6 0' e+Y' so''"l'ffi,'i:l

3:='j;H:t;ryr..i;;f,?";co' zg.zgolo Nz"' calculate"

Ld ulrimate analysrs of coai .t "' C;orr:DleLe tsz iozoc:. 3.950/oll. 12.15ozoo) 117'93% .nal-vti-t ;ith; *iu" if it cont'ajns irt Corlplele '' (54'3% FC' 7'77% VC\{}

CV = 32.9582MJ/kg; Refuse: 4a/o YCM, 4Ao/o FC, 5670 a:;h; Air: 25"C, 740 torrs, 800/cr P'H. 50Yc exsess O, Stack gas: 300"C. 755 torrs. lr,z/Co ratio = l:4 CO/CO, ratjo = I:10 Ca-lculate:

c)

a) ml ajrlkg coal (14.I9i b) Orsa-t a;:ajysis of uie slack 91" i10.39% CO-, 1 C:49'o CC). tr.2Glb i{-)

^sir o/o excess O- ( 39 5ryol

8Yo ash' 1'49lo 57 l?icr' Coal fired in a furnace aralyzes Z+sw'C rrrrd 7ra5o/o N and O.?7a/oS' ti';;f"=tlo"'"= gas shou's 11'21% CO.,' ash. orsat uo"-'ytit"oitit-"iu"rt 7-i-oro N'",,caiciilzrie' isztz.'co, z.+iota o, and 79 (5'Fj5r:'b ]i '2ri [i8% O) r tt= J'"i, '[ ''na] 2i) Corni-'lere trtr:nrii fJ 9t excess O, (40Y0)

i t'

=t"=='t-'t"

t"""t'

'

/

SToICHIoMETRY

8.

Coal flred

in a f-lrmace anallzes 30ozo VCM, |le/o FC, l1o/a ash, So/o M, L6% N ald l.ioto s with a GCV of g0. i MJ/ kg.-leJUse analysis shows 30% FC, iS%s VCM, 4oolo ash Air supptieri is sarurated at 2S"C, Z4O rnm Td-Tf.-HrO. tvtotl ralio of Cq t-o CO is S:t and FI, to CO ," i,r !S The stackgas leaves ai 900"C a:rrd.Z65 *ro'Ug. CJ""r"t., a) ors_at anaJ5rsis of ttre stack gas Y:9Z:,_9.A,. i.E9o/6, CO, J.Egozo Hz, tt.!bo/o b,,

CHAPTER

SULFUR AND ITS CO'MPOUNDS

ZZ-69a/oN2)

b) ms stack gaslm3 atr (Lg6)

5.I SULFUR COMPOUNDS ' One of the most imporlant an
5.2 BURI\IING OF RA\v SULFUR . Raw suifur js a combinaUon of pure S and inert materials. When srrifur is bumed, the foilowjng reaetlons Lake place; Main Reaclion:

S+Or-SO, SiCe Reacuon:

S+3/2Or=SO" I

8l

T ,' ', ir

)11

ill(lME1liv

::

Solution: tsasis: i00

O, calculations rnay be based on any of the above 11,,,;111,",r., 'l'l rerr O, (S conversicn to SOr) At S l'lrr, o, (S con'ersion to Soji = Total aJ = x s,/z

i;;

i

h l,;xcess O, (S conversion

O, Irom air -

rireo O, (S ro rl

theo

ttreo

I

;i

Eap Sr.:tfur Anatysis (case

e I

e

e

i

g*j:, l','lIi::,:::,'l:'in #ua

L' ttot included Itt lll ll]e rcqrrlfc

*;;;;

"l!',

Cinder 10% s inerls

9Oo/r:

Total at S = 95/32 = 2"96875 Theo O, (S to SOr) = 2.96875 O, from ai1 = (1.65){2.96875} = 4"898 N, from ai1 = 4.898 {79/21) = 18.427 Tlreo O, (S to SOu) = 2"96875 x 312 = 4.453

rJ

,n};. ffi;",iI11, i,, *. o :.":.:* -::{, i,li?pffirH] ffi:: ;i:u"::T .:: T.:::: ci rn n ur ;;; il T".; ,' :,, ,*]o :",1 : *. s " " ;;rffi y ;i ;: 3 :1, I**: :H: ?.:;s il"' ?: :::l

i

\\

95%o S 5olo inerts

%F ro so3) x 100

Ii

BURNER

Raw S

-o= tai n s : -con a,sena.a,." l" 11

,?

III

x 100

o, (s to sol

,,lt,""y::"=,,r:::

a)

%o

=

qru .iii, #'ffi Lrrus #as water ;X#

*.

excess O, (S ANS

to SOr) = t(4.8g8 '4.453)14.a531 -r

At 30"c log\P

'VP

= 7.96681 =

-

1668.2t1t228 + 3A)

31.7 mm Hg

^a *.

t.lt).(

l: Raw Su.ifur

anal_r-z:ng g5gtr

S and

)s

30"c, 7.40 mm He ;,;"do#^": "2?!':I:ess ::llil:: ollf the cjnder shcr.r,s jC.:j'S ,", .:L

1^

-^

Ur,u

SO)'

I

i))

It

)

ilt 3arr

tlr.,,!]

illo :,,,,,

i-,1

h:

aCr!

(q.ssa

I /

6)(3i7)

0615

76r) 2'/ i " '.t) . . 18 4'27 = Lt.6L5l ,'224, _.^ , :.:.. 10t)

J

=61127,ANS

.i. ;t1., , L'..1 ..... ..,.. .l :r

c) eortrJ,j,:ie ariaj_vsis of iJle bunter

74A.- |

"1

ineris Ls is JS

.A:-raiysis

inens. 8B0,/o of tilc li gasiieO i.,;,:.. t" ic SOr. Calculate: a) 9/o excess aj:iS tr., Qr\ :,

x

5 5olo, rrtct

ai(s r,: so,) Ar

3,Y::1,*i?

r00

100z6

Moles H,O from ai1= {4.898 + 18.427)

l')turnple

i;l r' B.i

.r *^,, , C. laf,w J

Fuel

ir l,l-xcess O, (S conver.sion to SO.)

O, from air -

j

Sorl-

)

i.

Staek Gas

SOr)

rireo O" (S tro so2

Pi-.i. i N

300c 740 mm Hg 65 7o X'ss

60%RH to

tq

AIR

'l'lrr detemlnaUon of the Excess *9 7o Excess O, shouJd l(lly whether the ca-icr-tlations are ?, oased on t"l:e conversion of lltrr to SO, or SO.. 'l

1-

UI-i'UIr,tj'it, ll'S aofti

gas

14,,,slolc;-rlcMEll.ry

sul-FliR.A-NU i.is 6'e1'4;1r''r

Ineri bal: 0.9 x Vlt crndei- = Wt cinder = 5.5b5

5

Soiuti,crr-- Basis

At S gasified = 2.96gZE - (.t .x 5.555)/32 2.951 = At S convertecl.to SO, = 0.gB x 2.gil 2.SG-"^ = At S converted to SO, O.l2 x 2.g5I 0.385 I\{oles O" i-isec.i

n

s

-Ib-trred

g;;"s

9.7970 SO, 9.169/r, O,

81.057o i't,

BURNER

l2olo inerls

o/o

2"596

10.93

1.771

7.45

18.427 0.355 0.615

77.54 r.49

O- from 2i1 = 8I'05 x l2l/79) - 21"54 o' fo, SO^ = 21.5:4 - (9.79 + 9.16) = 2'59 fuflf** So. fon-ned = 259 x (2/3\ = l'727 = at S convet'Led to SOu

,EO

Total at-S = at S converted to S0, ' Theo

'ir,r".

tne

inea

during combustion. The O, frorn *re determined from the \ ln the bumer- gas since comes from a:r.

ExamlsLe

760 mm Hg

s5

88olo S

Calculations Based on Analysls of Bumer Gas (Case ID In the orsat araiysis of the bumergas, SO. is noi included. To find the moles.of SO.. a comparison of rje oxyqeri-ln

Wut",ipp,ru."om

Hg

'/

Fuel kaw S

L,t I I

23.764

bl

l.OU t-

drv

gr_{o., SO, = O, for S0. "p = 2.596 + ol:ssti/2) = s..tzz

Free O, = O, from air - O, used up 4.ggg _.3.t22 = = Complete Analysis ANS GAS SO, a2 N, SO, HrO

Burner -^.^O^ Gas

A.IR

oro^ 745 mm

=

=

I00 moies dry SO, free }3u;-rter

r'l''

orvgffi

Jr .L

a)

U.

aI of ttrese

2:. Ilaw sul{ur andpirrg gB% S an', l2o/oineris when bumed::ndl.:: a gas wirtr an orcat;al,=t" of 9.79o/o:O, a,nd 8i,05 N;nry,Jt, ,ci,jrr[, is ^?r_6yoq suppliec ai 25,c and zoo nrm lig. A) 9rr, r;:ii ..s Zri:. {S tO ,qC.,J b) 96 excess air (S to SO,) c) nt3 j-,r,r_.-.,..-. gas/rn3 e,,i;

b)

o,

at S converted to SO'

=1.727+9'79=1i'517

to SOr) = 11?11 ,,. .; ol is to sorl = 11'517 x (3r2) = L7"28 (S

7o Excess Pir (S = 87.030/o ANS %o

"+

Excess

= 24.65%

Air

(S

to SOr) = l(21'54: 11"517)

to SOr) = [(21

'54

'

I 1l'il"71x I00

17'281/ 1728)x

L{]0

A-1{S

, ,nt Burnei c) m'alr

(roo * tz2z)

Cas

xzz4,

(zi.s+ + 81.05), =

I706

,{NS

l:* "?7:;#9 '.2'i3

224'

760 /4)

='

''2it

- zt-) ;;'-

'I I,

i,,

ji_'.i

jil

)i,,,,

j:1'5r'

S,iil,rri.)'(,r\Iln ITS COMP()1-1lii,)S Ir

,

:1777 L.3136 .2s8g

F'ree

Solulioru Basis: 100 i;roles SO, iree BumEr Gas

.9d-5.4

AIR

O, = O, nct usecl jn ttre ;-eactions = 3.1165 -.5986 - 1.3i36 = t.2O41

Burner Gas 8.150/o S0, 8.460/o O,

)rsat Analysis ANS.

GAS so, o, N2 Vapor pressure

II,(J fi-oin air

83.38% N,

n 0.355.i 7.2A41 11.723 I3.BB:5 at, 2E

BURNER

O,/-

6.89 6.ti / 84.,44

= {3.1163

+

11.723)

-

*

Fuel

Cinder

Flrites

3.06% SO3

62% FeS, I8o/o gangue

C = 25.61 mm Hg

SO, in Burner Gas = O.3tg2Z

d) E'

89

l,he ieaciion:

4 FeS, + Il O" = 2 Fe,O. + E SO^

(

/

23'61x.8 = 0.388 74O _ 23.61( 8)

.0255 = O.2.g3TZ

O, from ajr = 83.38 x {21179) = 22"164 SO, ir, lhe burner gas = 8"15

In the reaclion:

I ^. uurrrer Cas _ rl3 8825 + o.388 + O29377) x 22 1 ^A- , ?ry::'79 75o' 27;) =----r rr.* lo0 , = 554 ANS

4FeS,+I1 O,= 2FerO,+ ISO, 4"075 I 1.206 2.A375- 8" I5

;n3

O,

f

.or

SO. = 22.164

-

11.206

- 8.46 = 2"498

Ih the reaction: 4 FeS, + 15 O, = 2 FerO, +

.666

tlxcLmple

4:

Drv p_vnte fines contai n)ng B2o/o FeS, and )g% gangue are bu;ned jn a Herreshoff Burner. -lhe cinder produced contains 3.0670 SO, and no unburned FeSr. Orsal arla1_vsos of the du.r., gu.., shov.,ed g.ts9/o sor. g 46% C- a-nd ss.:gt =r, ClJcr:l;ie: aj g.i, o{ the ieS, chil_.ged coirvei_ied Lo -- SC-

b) Zo c.rcess airl.-ts, io SO,i c) (_.rr;tirlet. il.tit_],-. , . ,;-- , ;ic -l;L: it.ra,r

--2

,qaS

Cinder Analvsis: Fe.O. = Q.0375+.3'33) ]60 Gangr,re = {4.075+,666)( i 20Xi 8i82)

I

SCu

1.3325

\ rl

lll

Wt%

e7O QQ J LA

a

tl+.6Cr

-/

OI

?

ar) \1'l i)l -)ll

.'".-

2.498 333

i I

9694

306

cirider = t379.2t+.i2.+ 88) x (.0306r.3694) = l3 9

,l .

.

T

rr',t_

,",

l , ,lCHlulnETR':

SC2- W.A75

rllr ["'e-q2 Cha-rged converied

/

(+.O75+.866)j

I'lrer'l O, iFeS, to SCr) = @.A75 +.666) rl'ir

"

c-xctss a:r(FeS,

to SOr) =l(22.164 -

x(lI/4) = 13.038

13.038)

/

13.0381

x

('ornpleie

of Bumer Gas ANS

iJforl".a

';=;";';" bY t}re reacLion'

uor r H,o = H,sor

/

1O0

\.6

o2

8.46

Q D'7

N2

t1J.JO

82.45 1.12

o/o

8.06

r.3325 1 0 1.13325

l.+ pnopucrtoN oF suLFURlc AclD AND

OLEI"'M

r[u ric Acid has hjstorjca]ly heen produced by two melhods, (lonracf Process and the Ch,anber Process. Both of these llrr Ittrtlrr:rcls involve the formaUo4 of SO, irr abunterusingeitherRaw f3 ur lyrite; foliowed by cortversicn of Lhe SOr-to SOr; ard nlr';orljon of SO, in water lo give Sullurjc AclO of Oieum. I ir

C.rndtct Process 'lhe contact process involves the calaivtic oxidalion of SO, to SOo usirrEi Vanadjutn Pentoxde or Platinum dispersed in irsbestos or sihca gel as cataJ-vst unde;- appropriate condjtions irr an equip:rrent kno'*,n as a Conuefler. The reaction is: qnl

l

f

r.il t:

rj

Sc'co;-iitl;irr/ -{ ii

I -i""'od

sM#{|,''= t"t"f'"'# ap'ent to procluce

absorhing to bL the most efficient otnt*se known.as ,ut]g'. grades of ""ff""t produet utttt to give

'"*"Jo:"::ilffJ1:l';al .at"i

Rllnose= -1".^tn'= if used *' ub'n'u''S a;!ents'

concentralions o[

*HF*so

s

book'

i

i'l:'r-u

1ig 5rr pp

1

in series. a'lrd extra air i

-.J

11.

dirrerent

nav !:, f "-?-:f.';. r-t .,333iJ:: 3 ;qi'li:: "f3l i"9,^-t' q ior s e. tn or n * ;", o xi d a' in the corr'er1e r 8? J,T::H;:# o, the ;";;;;this, gases' the O, ln the wastes illustrated for the Conlacl Process is rl:e

r

The flow ciia$ram

I

lt

below': l----

BURNER

I

:

o

?nmaeY Atr

I

'fir'"ile

Sulluric Acid Soi'n

'

a) Dilule a'cid

Seconcary Arr

CAJALYTIC CONVERTER

tr) Conc 'Atrd

GAs I

ABScRSERI

*_J

1,/2 O" = !SC.

-fV'o o;-more convei-t.ers ina.v be ;

(,,.1:' :' , i)

tt'e o=i"u*Water is added io

SO,

So.

i

.- r ,;.,1 '.

?"titta

(ciow'nwa'r-d)

= 1.332 - (15.9/80) = 1.3325

n B. r5

GAS

(

.J..!'

70% ANS

Moles SO. in'the bumer Sas

Hl

r'.-

gtt!'-t' the conver"lers,l:r3l:iT:,ertt:l The SO., irom rhe the gases [uprfo*t'= Sirlfunc Acrcj .orrni.r.roerrt passage of houid

r, 100 = 85.95% ANS

I

I

,t, ; I CNlrl /'''id Co.wllea aias

ir

i

{.-1lD

'-

m

('( rlVi\'llllli)::l i 'ri SIJI-FiiIi Airi; lllS

lr)

Clzanber Process Aside from the bumer, Lhe pi:ocess involves the use of a GloverT'ower, and the Chari-,bers and Gay Lussac's J'ower. The hotgases frcm ttre burner passes up tlrough the GloverTower wheie SO, is converled to H-SO,. This comprlses ai:out 157o of the total HrSO, product-ion. The baiance of the conversion takes place in the chambers. The chamber process produces a weak sulfurjc acid (70o/o H-SO4). Since the contact process is the more pooular methoti for Sufuric Acid production, it shall be the only oae considereci in the computational analysis of this book" Exompie 5: Raw Sulur, 967o pure js burned in dry exbess air producing a g?s wjth an orsat anaJysis of 18 7o SO2, 0.50% O, ald 81.5070 Nr. The bumer gases are fed to a calalyLic converler together wit}:, 20o/o excess secondaqr air resulting in the oxidatjon of SO' The gases fr-om th9 . 60% of the SO, to converler enier an absolber to produce the acic. Assuming no fi:rt-ire: oxidatjon of the SC, taicng place in tJ-e absorbE:r, citjcr-rlate. a) Compleie .urir'':;is i.,-f ihe bumer gas b) Complete a.t:eji':li; of ihe converler gas c) Wt of an 6592o ccncer:traled LI-SO* sc;luuon per kg raw S charger, if the absorbirig acid is 400/o FlrSOo:

d) wi ;f a 570 oieurri forrned per kg ra"w S charged if the absorbinq acjci js ai 9096 H,SO4 solution.

Ge's moies SO" free Bur;'rer Soir-dioi r-- tsasis: 100 Br.;r RNER

AlrllJ-YSI

S

:

x Q1/79i = 21 66 Primarl' O, fi"om air = 81.5 O, unaccounted for = ir"oo-18-o'5=3'16

x t2/$ = 2'10 S converred to SO" '"" = 3.16 in BG = *ot"" S9'ioy'*d (B:2) (l/"s6) = 670 Toial wL of Raw sl= ti.iitll6's1

a)

ComPleLe

'-sis'of Burner Gas ANS Praly o/s

.GASN

s0, 02 N;

18

,

o'5 B1'5

sbu *2J 102. r

CO I,TIIERIER AN'AIYSI

r.7.63

0.49 79.82 2"06

S:

of SO, to SOu Theo Q, for comPlete, conversion - ttnl." free Orln Bunier Gas = 172 x Moles SO,

=l/2x18-O'5=LI

8'5 x (1"21-= 10'2 37 Secondary 0, Irom air = =ia"z*zgl';-! = 38 g.s6nflary N, from #'=

'tii"-l'$fzt)

SO, converted to SO. = 0.6

x

18

=

10'8

+ 1/2 O, = S0, The Reacbon is: SO, 10.8 5* 10.8 Sulfuric Acid Sol'n

Secondary A,lr(20% r'ss)

a)40% Aciu b) 90% Acid

CATALYTIC

CONVERTER

GAS

ABSCRBE

72 SO, unreacted =- ,3 - 19.3rA =r) - l: A + 1L/,1 = 5.3 'i: O, iJter reactjon = tl.J '38.37 ti9E7 + = N, after reac[lon ; 81.5 12 s 8 10 + = 2'1 ;b;;.;leacti'rn =

tlt5,z s r-,ric t{l{i^.1ii'I-r'r'

SUl,iLi R :\ND iTS COiv'l](']lrj'iDS

5.:, HOAsfiruG 0F

lEtOhi P-fHlTEs

Iron pr,rlres reler to rhe sullide ore n:ost commoniy burrred for SO, rnarufacture. It consists primarill, cf jro! Sulllde (feSrl sma1l amounts of meLa-llic sulfides and appreciable antounrs 01 totaliy jncombuslibie mateials. These inconnbustjble materja-ls ue reported as GA.N'GLE in the a-r:alysis. The following reacUons take piace ir the combustjon of

*filiZt,^

+ 11 o, = 2 Fe,'o,+ B so, y' .Reacijon:4 + Fe.S, 15 O, = 2FerO, + 8 -sO./ SiAe fl Reacuon: 4 FeS,

Solu.&on: Basis: 100 kg Pynte

s)

ca]c

u

a)

o/o

la{ e:

excess air(Fe-1,

t-.] o,l

lc

SO-)

cf lltc I'eS. ;:zr=.ei iu.Sl ir', -ilrt ,:jr:rl::ic) C:-s:iL an.,ai-lvsis r-,i' iiit b,:;;ier .3.as d) mt cl l;'.:me;- gas at 3511 f-: a,t,-l lfii tr:;':: l-j:'./ 1.<. ir-.i.rr:-

3500c

740 mm Hg BO% RH 17 33% x'ss

750 mm Hq B U RhIER

t cinder

t---------

Fuel

1 L .1

Raw S 150/o $a;r$ue

N4c,ies FeS,

10lo FeS,

66.630/o FerO, 2.670/o SA.

85%o FeS,

19.6% gangue

= 85/t2a = 0'70833

to qO,) = 919!?l x (\t/4) = 1.948 .;-r.,o^ n' fFes to so;) = 0 70833 x (15/a) - 7- h,5b ij"#o# ;'";' il Tllli " 2 656 -- 3 I i63 t r't o,-,-, air = 3 ll€ill x Qg/21 = 17'723

Tkrec O, (FeS,

a) o/oexcess

O, (FeS, to SO, = [(3'1163

- l'948) I

1'948]

x

lO0

= 59.97% ANS Carngue Ba.l: 0'196 x Wt of 3inisl = 15 tVt oI cinder = 76.53 Wt of FeS, in cinder = 0'tiiIi76 53l = 8'503

Catculations Based on P1'rite Ana-lysis

Example.3: $rrite Fine s conLarning E50/o FeS, and 15% g2ngue are charged to a bumer. An arralysis of *re c;lnder shows I 1. 1 1plo FeS,, 66.6302'o FerO., 2.620/o SO. and 19.670 gangue. Air js supplied lT.Z3a/o in excess . (FeS, to SO") ar 25"C. 740 nrm FJg md S0?e Rli. Il 8o/a of IJre SO-, fcrmed js absorbed in Lhe cjnder,

Burner Gas

AIR

^,-o^ lcw

As in the bumji:g of raw S, the tJ:reorelica-i O, and.o% excess ajr have to be defined as Lo wheLher based on conversion of FeS, to SOz or SO. .,.,)r' 'Iheo O, (FeS, to -qC,,) = Tctal rr:c;les FeS- x ),7/4 Theo O, {FeS, to SO.) = Total moles FeS, x I5/4

Dr:ring buming, the gangr-:e a;:d lhe ircn oxide goes to the cirrder. Unbur:red FeS^ rnay alsc be :;resefrt aiTFcsbibiy a smajl arnount of the ciiva-leai oxide n:a-v a-lso be formed" The latter is small enough and mav be neglectrri ilr a ri,eli cperated'furnaceThus t}e rnain Sulfur cornpout-lcis in the cinder are SO" which is absorbed on rhe cinder by rJre tnaFffi F.Sr_

/ 87

b)

FeS, lost in the cinder = (E'503185J x 10tl Moles iSO, fo,med = 0 0255/'08 = 0'319"27

Yo

ln the reacuon: '1 FeS^ - ]5 u: .

r.:

iv'Jrrles

F'Z?:-- 6 SO,

-? .0796 i596 o.sgso

-'31s2'v

FeS. cotivill'€cl Lo SO, = :".'::= f).t,77'7

.".S0

+t.'ffia.,

=

i0ozb ANS

I

r

Comolele Anaiysis of

C,--;nVe:-Ler Cais AJiJS

GA.S

ft

SO,

71

o

119.87 'l? a

I\i2

So.

1At

aa

ihe i:bso;"i:ers a:rarirze J.950zir S,i)r, 7"820;,b 0. iurd 9l.2301; N, Calcuiate: a") Cermpiete analysis of tlre brrmer gas b) (% conversion of SO, to $0, in fi:e coriverler

o,/o

/j.. ":)"

Yfr

b3

,J Wi of

a 6C9/o H"SO. neecled tr: p;:orlirce a cor:centated 9002b I{?Se4 solution /irr d) Wt of an 88% H,SO4 aciri needed to produce

82.51

8.88

120lo

Oieum/tr

r\II.SORBER ANALySIS:

[-ct y = wt of 85% HrSOo solution formed j, - I2.g(80) = y I tC32 = wL ai 4Oo/o H"SO* useC

Waste Prirnary

+1032{9Sl80)=0.85y y= 1892 kg/i00 motes Se free BG

r')

i ^,.^.,_* |.9Y':i9{ - | BURilER ls a,r.

1032)

ra*

Wt of 8596 Actd/kg ra* S = tB92/620 2.g23 ANS = I,et z = wt of 596 oleurn fonnerl z - 1032 = wt of g0%o H-SO. ar:id useC

'l)

Example

6:

l00O

/kg

raw S = 30.t 4.83/ 6Z0 = 4.5 AN,S

l€/1r $rntes arLalyzirrg

gangue js bumed in t:xcess

g*_*lf

gl9.o FeS,

and lgo/o at to produci a burner

orsar anaiysis af b-.84% SOr. 9.22o/o O, N,. Analysis of the cin'rjer: shows B.2go,c,unbumei FeS, L:d : af ra SO, t"l. g_r., from ttre bumer entei a catal-l,tic conierter _he.. SO. js oxidized to SO.. parlial orsat arra_11_s;s of lhe conl,erter gas shorvs 7"87i/, so,. l,rc acldjrjctc :r3ccrda;r. ?-:r- iS s..rpj,rlierl ;;, ihi coi:i.et1ei. .j-he conve rt:rga.rse S at_e dtet: sent lo ar: absorber w.here .li:1rcl w';,.t l::-;, i;,-1,:s pllc:. Tii.l.r.i.r:_.-.ie ga: L,cn,

and

Sol'n a) 60% Acid

.al

84.44010

-*^.-"1

b) 88% Acid

tnrrr^JX' I cor.rvrnlrn -I' Bo ooo," *, '----|' | cind., ' Pyriie B.Z9 % FeS2 l_ _ 1CC0 kg,hr 3 81 % S03 converter cas s

I

I

81%

Fe52

1

19% gangue

SO, Balarice: \q\a 0.9 (z - 1032) lsoigS) * :0gz = .c5 z + 95 z (80/98) z = 3014.83 kgl100 moies f::O, fi.ee BG

M't of 57o Oleurn

Sulfuric Acid

91.2;!,6 lr2

H,SO4 Ba-la:rce:

Oa$ -

G:s

0.95% SO2 7 Eza/, A2

Ar

a) 90% uonc. Acid b) 12

96

Oleum

.B'{utbsoz

Solulion: Basis: 100 moles dry,S{}r-{+ee Br:mer Cas BURNER AI.IAIYSIS. O, from atr = 84"44

x (2t/79r =.22.446

For the RedcLon: . 4 FeS, + 11 O, = 2 FerO., + 8 SO, 2.92 8.03 1.46 s.84

,

O,

icr conversion oftseS,

tO SO.

-

2.2

44€,

E.iJ3 - ii.72 = 4 696

For the Reacl.ion: 4 FeS, +- 15 Or'.= 2FerO, + 8 SO,

t.2522 4"696

0.6261

Cinder ,A"na]vsisi FeS, - (',v rlroies) 12C FerO- =, {1 .a6+.52611(}60j

2.5045 \1ry'

bti,

t 2(i.v :137 "i 7b

a.l i

!1i

"'{?*

96

/

srorcritoMETRi'

G -a:rgu

e = (2.92+ I .2522+w)t1

so. = a motes Tota-l

S $dd dsd*l 2Ol i I I /8 I ) \ tt +y' * 2S ) 4,{w I .

\

y"

/.u

SIiLI'-Lln AJ'jD

b)

%o

con'r,ersion of SO, to SO. = (4.0846/5 84)

i

NRSORBEF- ANALYSIS:

SO, in BG = 2.5045 - .25 = 2.2548

.

n 5.84 9.72

N2

SO,

88

Vo

84.M 2.2545

9"51

n

,rr'fr= tO.

GAS n SO, 5.84-b a2 9.72 - .5b N2 r i00 . 1.5b forSo^: 584-b =org7 ' i00 - i.5b b = 4.0846

ah

l.B7oto

84 ++

SO.

.88'

lrt y = wt of 6070 H2SO4 acid charge

82.58 2.2

y + 7 .21g i^(80) = y + 577

-528 =

-- ^^ formed wi of 9Oo/a FI?-SO{

_t

SO, Balance:

(80/98) ,156/98) (.6) + 577.528 = (y + 577.528) Y = 625.655

CON\DRTER ANALYSIS: I.el b = moles SO, converted to SO. in converter

The reacuon. is: SO,

I/2 02 .44

SO, avaiiable for absorplion = 6.339i + '88 = 7'2tgt

5.71

02.2545

.

O, in waste $as = (84.44/.9123) x 'OZB2 = 7'238 O, reacling = 7.€i77V - 7.238 = 0'44

For tlre reactiotl: SO, +

Complete AnaJysis of BG

ci.s

100 = 70 ANS

= ###

w=0.36268a=0.25

'fu*,07, Wt of Pfrite/1O0 moles SO, free BC = (2.92+1.2522+.3G268XI20) / .81 = 6Zt.S4

SO, o2

x

n Converter Gas t'7554' SO, = 5.84 - 4.0846 Or'=O.ZZ = i"5(4.0846) 7'6777 84'44 N, = sb, = 2.2545 + 4.o846

Wt of cinder = 451.216 + 148"l4g w + g0 a

SoMng simultaneously:

n)

IlS COitl;'C;UivnS '/ 97

c)

('9)

Wt of dilute 600/o acjd/ hr.= (625 655/671"834) x 1000 = 931.26 FJ'JS i$^st:) 6yu,,\ o(1ro1

L1i"old Ylh(

{

l-et z = wt of 88% acid z + 577.528 = wt of l2o/o oleum H^SO. Balance: olAA ) + 577.528{98,180) = + 0.88(z+577.528)

(0. 12Xz+577 .528){98

I 80)

1';'7 QOr, -l_-ttt.aJJ -

o}i{tof88%acid/hI=|777895/67].834]-x1000=1]57.87ANS

!., '

I /

.utro-'

'-

$J

ito

SLJi,rLiR .4"ND i'T:

tJre gases f::om the

sur-rurbumer ere passeci thror-rgh a coorer, an entrajnment separator ald t].en llrl() ax absoqption tower. It the tower, it is made to corile.mto rtact with MiIk aJ Dme or sld
F,euylf< /-'

only O, and N,. Assunring nci furtlrer oxidalicrn of S0, to SO, and forn:aUon of HrSC* in tl:e lower,

I a-^i"-

calculat

/

r[o\

r tte tl')-

i

.n

t

lrarT J

Cy'\

,

, FI

MgO+H,O=Mg(OHi,

e:

a) Wt of Lhe bisulfite iiquo;: b) Lime consumptron/hr c) Wt of water used for slaking/hr

u

'

su'1

7-+';,is" -{ baL "t

.Soluhon-' Frorn

SL.{HER: CaO + FI,O = Ca(OHJ,

8x.6, Eas;s. 100 ir:oles SO, fi-ee Burner Ga:;

ABSORPTION TO\,VER:

Main Reacrions:

+ 2 SO, = Cq(HSOr), Ms(OH)", + 2 SO, = _C_"!9y],

_C_"f.9p,

+ SO. =

7.820A

SLAKERI -jr--

02

91.23% N2

82'k ceo x6% Mso ?o/" Inens

CaSOn + H,O

Se1ou1 I so, = Mgsoo + Fi,o yzO*SOr=HrSO, SC" + I/2 02 - SO,

i--i__ Cinder 8:29 % FeS2 3.81 % SO3

To determi,e i.f oxida'cn of SO" to SO, takes place in the ,lls.rber', the waste ge.ses are compi;ed wii]- tlie coored burner fiitses. If the o" in the waste gases js less t_l-ra_n t-i\e o" in the cooled ,lrrr_rler gas, oxidatjon took pffi-.-----.The rnixture of caEd Nag nisurfires, ca ancr Mg sulfates, ll?SO' inerts and watermake up the Bisulfite liquor. T)-ie anaJysis ,l' t].e bisulfite liqucr is usuaJl-v reported in terms of the 9/oSo, lI contains, boLh 'free" ard present as bisu]fiLes; e.g. A bisuulte llqrror contains i0% so, ofi,hich Bo/o is 'free'and the rest are Example 7.. Using Lhe pvrjtes and Bume.r Gas in L.xzrmpie 6, the burrier gases are cooled ard made to cbme jnto contacL with Mjtk of Lime jn ar absorplion Lcrr,,er. . Tlre doloinitic lime rrsed is 32!i Cr,O, 150/c }1sO a;rrj 21'o jner-Ls.'ihe it:suJire llq.,:or l,r"oraiC ccriain_< 7.Clo/o toral SO, of wh;ch i.rSyo l. -fr..ar:d lhe resi 5.9clzo belrg i;;-es::i :r: l-;isr:llirrs ,1::: r-'.il-l:e f_i:-g *'as1.e .!l:tS tl.i(:r;,.,:.: il.t:,.

jt

.t.a.iii.,

jil.S

Bisulfite

Liquor

7 05?; SO2

1.15%free SO2

( // \ 5 9olo as Brsulfrtes r*€

\t{L pynLe/ 100 moles SO, free BG = 671

Bumer Gas: 5.84 moles SO, 9.72 moles O, 84.44 moles N, 2.2545 moles SO, from exarnple

J)resent as bisulfites.

.,--t]11.,1-.;5:;gr

rLime lc

',Vaste Gbs 0,959t SO2

YglY_s_ct,l

Side Reactjons:

(-l()l'lPOlli{llS. i !}9

, ,rv{q

I5,5 BI5I-'LFITE LiCIUO,? PRODUCT'*r*

l. bisuifite liquor produci:Ion,

.'

lrry'?

Let

834

6

iLa r-i

y - wt of tie bisulfite lir;uor

-

i:jsr:ifi te I)q'Lr orlhr 789.i.17 A]\s

.

53()l 5{i ; ll(r()a,/C7 t

u

,., MaO <---

). = S:Ot 56 kg

iig

a{

srr-tr

-

3oz

I

't

SCl, Ba]ance: 0 0705 .v = 5.64 (6it

al

oxida,h't'-n

Surbtrr

ttiert+ks

,rf

.ifl

x F"q$

l0c / silrcHIoMETRY Moles Cao & MgO converted [o Bisulfites = (5301.56)(.059)/64 x 1/2 = 2.444 Moles Cao & MgO converted to Suifates = Moles SOs = 2.2545

anrd

, Wt of lime/hr = 252.6 x OMB in the Ahsorber

(100A/67I.834) = 375.986 ANS

Wt Br-rrner Gas + Wt Lime + WL HrO for slaking = Wt waste Gas + Wt Bisuifite"Liquor SO, + SO, + O,

.' N, + lime + HrO for slaking

/ i0l

X n^* Sulfur which is 75% pure is burne.d iR e'tccss alr ' suppiied at Lhe rale of 4.7 13 m3 /kg erf raw' Srrlfur at 25"C,

745 mm Hg wit.h B0% RH. lf 87o/a of the suilbr charged bums to S0, and the rest lo SOr, cdculate" a) Vo excess air{S to SO,) (65o/d b) Vo excess air(S to SOr) (l0y0l c) 'Cornplete analysis iif tle bu*ret gas 2" ( I0" 88% 5A u, 2 .32r:to O r, 77 .62a/o Nr. I 63Yo S0r, 560/o

MgO= 82/56 + L6/4O.i) =.I.86

Wt lime/100 moles Bumergas = (J 00/1.86) x 4.6985 = 252"6

SUi,FLjR A.N-I) l'l-s i:or": x;i.it'lDS

PROBLEMS

Ioial Moies CaO & MgO supplied = 2.444 + 2.2545 = 4.6985 Fcr lOC \g linic: ivioies Cao

;l

"

Hr())

/,

The burrter gas from a sulfur burner analv-zes I20lo $Q, 7.l3ak O, a:rd 83.67o/a Nr. The raw Sulfur: cirarged contains 82a/o pure Sulfur and andysis of t1e einder shaws 2090 unburned sulfur" Ca-lculate:

a) olo excess ai(S to SOr) (60or'0) b) o/o excess'air{S to SO.) (6.670l,rl c) msof saturated air(28"C" 750 torrs)/kgraw 'S {5.076) d) mn of trumer gas (300"C, 730 torrslllg mw S (E.75)

78olo FeS, and 22a/a gargue is hurned at kg/hr. Anaiysis of Lhe ctr:der shows 7 22o/o S as unbur-ned.FeS, and SO, ahsortred hy FerC.. Alr supplied is 70% in excess based on conoerbion of FeSr'to SOr. The ratio of SO, to SO, in the br.rrner gas is 3.48:1. Ca]culate: a) o/o excess air(FeS, to SO.J t24.67%1 b\ a/o of the FeS, oharged lost in ljre cinder (l?9/o) c) Complete anaJysis o"f the trurner ga-s (6.260/o SOr" 9,570lo C)r, 82.35a/a Nr, I 820/c SO")

S ffrite ar:aJyzing Lhe rate of 1000

O, and N, in bumer gas = O, ald N, in waste.gas '+ 5.84(64) + 2.2545(B(t) + 252"6 H,O for S]'aking = 5301.56 Water for Slaking = 4494.84

c)

Wt water for slaking/hr = 4494.84 x (1000/671.3a) = 6695.32 ANS ,-.,

i

Fuo llJ

C,

/ /n -=*

i-.

w@ttcw Sur'furc

4 Irr the burning of pynle coritaining 92ak FeS, and B0lo . gargue, i30/a of the FeS, charged js losl in ihe cjnder.'fheA p-anjal anall:sj5 oI lhe cinder also show.s 5.31% S0,,. orsai tural1,sjs of the bumer qa.ses sirows 6"75910 SO,, 6.880,/0 O, a:ro 86.3804 N, AIr supplied is at 23''C" 74ll; rnnt i-Ig iLnd SB0Z RII. C;rl:uialt a) 7o excess air (!-eS", to -!Or) (40q4,) bi % ercess air (FeS, to SO^i 12.676o/oi

I

I

SUl.,Fi.jll. Al.ll-r

()2 // S'1CIC;IIOMETRI'

c) m3 air / kg pyr:te (3.58) d) m, bumer gas(25O"C, 750 mrn

X

c) k€ of a;r

Hglii€ plTrte {b.9261

Raw Suifur containing 83%o pure S is burned together.r 8Ao/o excess air (S to SOr). a51 analysis of tne .iriJ.i

dth

"fro*u unbumed sulfur and 800/o tnerts. Air is supplied saturated at 30.C and 750 rnm Hg. The gases fi-orn the br,rrner enier a converter where cataly'tic o*ldatirrr of SO, to SO3 tales piace. A partial orsat anaJysis of the converter 2096

gas shows 7.37a/o S0r. The gases from the converter enter arr absorber where aiter absorpUon in acld,soluUon forrns awaste ga$ analyzlngO.55o/o SO2, Il.9go/o O, and 82.460/o

Nr. Calculate per 1O0 hg raw sulfuri a) Complete ar:alysis of the bumer gas (9.59% SO2, 9.O3oh Or, 76.070/o N2, 1.07% SOr, 4.25o/o H2CJ b) % of u:e SO, enlering the converter that is conve:rted to SO, (B8.3olo) c) Welght of a 60% dilufe H2SO4 needecl ro produce an

B7o/o HrSO4 Q48.C4) d) If the absorbing a:id is is g49lo Ii2SO4,- what wejght of a l4o/o oleum js formed (587.6i) ;

,^*.

(XD ern," containi;.rg 807o FeS, aytcl20o/o gangue js burned jn \'Js .lxcess ,-r.ir to produce a gas with a complete ana,rysis of 7.78o/o SO2, i .39o/a Oy Bi.OAolo Nr, 4 g29lo SO. md-S.gSq. i-lrO. AnaJysjs.of the cinder shows a.tolal sullur content of 6.46rlo due to the presence of unburned FeS, and SO. absorbed by FerO.. tur supplied is at 27"C, Z4S mm Hg and satr-rrated wjth vapor.f'l-he burnergases then enter a converter Logether wjth. 30% excess secondirry air ( supplied at the same condjlions as primary ajr) based on the comclete conversion of all SO, [o -sO" Z5o/o of t]re SO. acti.rally bums to SO,.f fn. .orrr.*.r'gur.r .;;-# absorber ald absorbed in acid solution. The u.aste gases fom:ed h.as a partlal orsat aralvsjs of 0.7010 SO.. Ca,lcr:lale per: i€ oi pynie a) ',r e)^ccss air (S to SO,j il\.l7) Lr) CorrrricLe analysis of the con\.crlrj- ri,. il 7ltar, JCs. I .5:?,r1.; C, L?,.'i]\it it,. J.!;5Vo.iir"),, .i.q2,7. 1-j. i-)

BCto.,ir

HzSCo acjci formed 'from

charged (i"84)

d) kg of a

jI'S rI(),\,i),t)tII'lD:-r / i[)::

75o/o H2SO4 needed

lo Prociuce

a

'400'zo ac:ci

ltlo./o oleurn

(0.662)

The buming of rav; S consisting of 95% S and 50/o i:rerts produces a gas whose orsat analysis shows 1t'39%o SO' 7 .zA'/, O, arra 80.840/o Nr. Ten %o of the total strlfi-rr charged is lost io tf.. crnder. fhe burner ga$es are eooled 'dr:ld absorbed in milk nf linre c'bra-ined by slaking a"Jime consisUng of 580/o CaA, 32o/o MgO and ]0010 inerts witlt wa'"er, Tiie bisuifite hquor formed contains LZVo SA, of which 2o/o'is free and"the rest present as tris'-rffites' Orsat alalysis of the wastc gas shows thal jt contajns V '39o/o O, and 92.610/o N, Calculate: a) KS bisuifite liquor/kg'raw sulfur (9'65) b) G hme consrjmeel/kg raw sulfur t0.BB32) t G of water used for siaking/k€ raw sulfur (6.92)

The roersliirg of pyrites axalyzing 8570 FeS, and 1502 gangue utlhzes 4001e excess air (FeS, to SOr)suPglie! 1t tne iate of 35Q m3lhr at 23"C, ff3 mm Hg ard BB% RI-l' A partial 'aneiiysis of the cinder showed 25,920/o FeS, andt7.839/o gangue 9llly 95% 0{ @ r:onverted to so^ and the rest tcr so". The bumer gases are cooleE arldTnar$edTo-a conve fter togetJ:er with slalied lime from a dolomiUc iime contain ing?S1/o CaO, 250lo MgO'

liquor are produced u'ith nc oxjdation of SO, to SO" taking place" Assume all SO" converled lo bisulfite, Calculate: a) kg/hr of lime t33.-i24) bl k€/hr of rvater for slaftjrrg 1704.7'7 c) Comp)eLe aratysis of t-he' bumer gas (5.35olo SO, ' 8.83a/o O,. 81.06?6 l\rr, 2.15o/a S0, a-r:d ?-.61a/o TI"O)

If 850 kg/hr of bjsullit.e

PROI}UC}i']OI'J U}T ]-,IME

CFiAPTER

6

FRCI}UCTICN OF Lrh4E

,'

iLiS

Ca-icuiaUon Anal1'sis depend on whether tle ftrel (:onlaj:rs ncgllgible or considerabie Nr. .U the N, in tlle fuei r9 negiigjbf :. the

G, \e,r

fuel G related with the kiln gas us@

tf the N, in the fuei js considerable, the nA-sEbsGnce js the sr- qf V N, Jrom the fueI and N, for

subgtance; theoretica)

@ w,ri

Or"

- Another solution aside from the tie substance iuralysis is to u.se the aigebraic mettrod and the materjals are r:elated by a Czubon, O, ancl N, ba"larrce. \

6r.? CALCUIATIONS BASED ON NEGUGIBLE N2 rN THE FUEL ICASE U Exarnple

Lime 'can be formed frr:m the C.rilcination of Limestone. .lElruaitv a rmxtu;-e of caco.,, Mgco" and jnerts. @s-tq Ca-lcjnation tatesltaG-in .Ei, *nEF]Lffi from the combuslcn of a fuet. The fot-towing ..;;,r.";il.:

l: ftre buming of fimestone containing 65% CaCO, 25olo MgCO, and 100/o inerts, using a gas mD
a bur:ner gas containing 3"A20/o

'

a) Fuel"Ratip by wt b) o/o excess air

:i.T::

22.A7o/o COr, 0.9% CC,

A, and 74o/o Nr" Calculate:

.

,

650/o CaCO^

*d EgdS co[ect to form rhe liqs..In some 94 @ may ^^^3.calcrilaton L;ases' not be coniprete so the uncieffimec urne _may contain small amounlis ot"."O,_@ rep?fed in rerms of irs eO; conGnf The kirn gases Enntd-mer combuslion and

ca-icination contain aside 1iom the products of combusUo", Lh; CO, f..* U* ca-Icinalion of lime; likeu.jse jf u,et limestone is introduce d, waier from It may vaporize ard go wjth the kiln gas. ffius from ca-icinarion rnu st be ieparateo lrom *il .;;,; CO, urO UrO ;;' #oar. rc u,hen detennL,rg tl. i".t consumpuon and rirne :l^"3-T_!:=tir],1 producLicn.This:aiic.5rr,ihea:.niunl"i-*uf"l"irJJ;;.;;;rr;

of ffuel vr uL/ useu ,,"" uscu r5 is ca:l:i c3jia3 ir.---T:Zal.---=.. l,qLci .;ic:lc. : oFr. r,6Q

6t

+ )

i.*--

l;M€. !9n|^ ' Qs

,ned (r)" ++rA^.,..4 cacau ssuo)

_,::-

-=-:-i it/t,

;;tu.,

25a/o

NlgCA,

]00lo inerts

Limestone

t<-fu,L

cc

3.02910 tO.: 744/o N,

Air BURNER {r{irtt',, 'rq1

t7i;c2

cl1):'r l-;-Jz

\ i

t Lime

Fuel 25o/o ra 7Sc/r,

.

22.470/o CO,

Burner Gas 0.9%

I-1

CH

act(c\.\), I "., l.ta.) (rH) ,

";"3:,

! -.,a

r _i_-. z. S.; irl(:::iOtsiii.:fli,

PII.{:)DUCTION OF. i,J}VJE,/

&luribn-. Easis: iCC moies riry

kln gas

For i00 moies oi

IVfe$rod 1: O, from atr = 74 x (21/Zg) = Ig.67i f-i:eo Oz = 19.671 - (3.02 - 0.9/2) = tZ.iot

Yk,rT)

25

For 100 moies of fuel:

crHn crH*

n 75 25

Theo O, = 225 + 650/4 = Tie Substarlce: Theo O,

atC 150 75 225

45A

200 650

x l7.t0l

O^

'

= 4.4]3

o-lo

Non-volatile Marter in hmesrone = ro0 Wt of lime = 1357.05 x .5772 = ZgJ.2g lq

z? -- !',/ ^f r:wt Cr::I-iJr::.iOile

S.o

650

100

Ba-i:

in C6, of LT + O, from ajr = Oz in kiln gas

.4228L/4a + .211i + 22.A7 + -9/2 + 3.02 + 6'5/4)x

N, Birl: N, fr;:m air = Nz iri kilrr gas O79Y = 74 42.28o/o

42.2g = 5z.T2o/o

FueI ratio = 7B3.2gS/(0.75 x 4.415 -x 30 + 0.25 x +.+lS = 5.3 ANS

b) 9zo excess air = 113.62 - .g/Aii7.ro;1 x

2AA

At C Eai: At C from fuel + Ar C from I-T = At C in FJln Gas 2.25x + .42282/44 *- 22"07 + 0'9 Moies O,

Carin ijmestone = 65 x(44/tO0) + 25 xtaa/BO.a) = of limesrone = 13.04(M)/0.422E = 1357.05 tq

2;

nn

i* 'i^o

.

!_o -il/t

I-et x = moles of fuel gas Y = moles of air

150

arH 450

For 100 kg of Limestone: oh CO2 = 42'28Vo o/o . N\M = 57.72o/o

atll

At C from tr,e f.,ei= ; * 1.413= 9.93 At C from Limestone = 22.07 + .g - g.g3 = i3.04

Method

atC

3,87,5

Motes of Fuel:= (I0O/3gT.S)

a)

r l\n

X: n .75

crHu c.Ho

1u17

Solving si:nr: ItaleousiY: y = 93.67 moles air x = 4.413 rrioles fuei z = 1357.A5 kg limestone See method

xq+)

= 15.03% ANS

I

for

artswers-

gxsrqLe 2: A vefi.ical shaft icilri is c'harged wiuf -+-!o11tt-ryt of lirnestone cor:Laining 54alo CaCO., 3B% MgCO' )% SiOr, 1.202i, R,O, (iron oxide) and 3 8ozo flz-a' 125 kS of fuel oil conta'rning 86oz'oC' 10 59/oH' 24o/oO' 1%N a-nd 0" I9loS is charged per tonne of Lmesione' 1lne ljme product leaves t'i.e bott-om artd conLains

Air suppiied i-q at 25"C, 755 mm Hg ';:ld saturaled rryilh u:ater. Pariial orsal arla]vsis of the lci1n pas 5i.r"rrt'5 20.6101, CO, and ] 189/T CO' 2.3o/a CO.,

Caicr-rl;rle:

a) 4 of hme fonned/hr b) o/o e-rcess ajr c) complete alalvsis tf the kil;r

gas

'108

/

srotcHroMETRy

FIloDUCttoN

54o/o CaCO" iierozo

(.)F

LIME

/

\Oq

Wt of li::re = 2153.94 kg/i"rr ANS C bal: C from CO, ln'LT + C from fuel = (l jn lime + C ln dry kiin gas

ugco,

3olo SiO" li2o/o \6, 3r8oh HrO

Lirnestone

B

(0.0a359x4 AOO)/44 + (0.86 x 500)/12 = (.023x21 53.94 / 4a+ .0.2 }79(moles DKG)

unner Gas 20.610/o CO,

r.18% CO

llry Kltr Gas = 341"14 Moles-CO, ln DKG = .20611341"i4) = 7O"309 Moies CCI:tn DKG = .01i8(341"14)"= 4"025

,i.4oles

Air

l*ty=XssO,

BURNER

Theo O, = ("BGx5OO)/12 + (.1.05x500)14' (.024x50O)/32 = 48"583

Fuel (125

oil ltU"

kt/k*'l:E

860/o

O, floin a-tr'= y + 48.583 N, fiom air = I + 48.583) x79/21 Free O, in DKG = y + .01i8(341.14112

Lirn':e n \o./^ (-.!'\

341.14 = 70.3C3 + 4.025 + y + 2.0J3 + (Y + 48.583)t79/21) y = 17"226

C"

]0.50lo H .o)

NI

o/o

= (17.226/48.583) x 100 = 35.460/o AJ{S Sas = 17.226 + (4"025/2) = 19"2365 \ in kiln Sas = ('r7.226+a8.583) {79/21], = 247"567 HrO from limesione = .038(4000)/18 = 8.44 7o excess O,

Free O, in kiln

O.1olo S

Soiufron- Basis:

+ 2.01.)

Dry Kibt Gas Bel:

2.4o/o O

i.o%

=v

t hr

CQrin ]imestone = 54xQ4/!OO) + 38 x {44/84.3)

\?

at 25"C: 23.61 mm Hg

= 43.59%

i{,O from ajr'= NW'I bal: NYM in Ume = I!"/]VI in liriesicne 0.977fr1.'t oi )ime) = r-4e. 1t4 \- 'l i-;f tnl

H"O lrom fuej Tota-l

"vafe:

23

17.226 + 48.583

7s5

=

-

6l .--lntl 23 67

i05(500)/2 = 2t,"25

in kilu

gias = B

44

'

IO.i

I ', 2.G.25 = 59 !17

PRODUCI]OI{ OF. I-IME

r:)

Ccmpiete Anali:s;s cf G,.qs

CO, CO o2

\

Hro

t[in

52 c/o CaO 2.tYo MgO

Gas.a-NS a/o

II

70.309 4.425 t9.2385 247.567 _59.97 401.1095

35"89b, CO:} 1"00/6 CO 63.zvo tu,

0.33o/o S10,

1'7 trD

t..22o/o o/o

A\O, H28

1.00

1"2

4.80

Lirnbstone

61.72 14.95

/ ] 1I

Bunrer Gas

Air

6.3

BURNER

CAI.CUI.ATXOfiIS BASED

ON CONSIDERABLE r{2 xr{ ThtE FUEL {CASE irl

In this case, it is more convenien; to reiate the fuei with the Iorn gas using the.surn *,. N; ;;; rhe fuet arrrl the \ for l.f theoretica_l O" as tie substan"..'F.o.r, ,l-r. fr.rl"uirl,r, ,n. theore,cal O^-can he delemlrnea, lrr"., IV, from fuel -r N, for theo O, = \ frqr; fuel + rheg A, x (7.:) i2I)

Fuel Gas ?"7/o CA I2o/o CO,

Erom the kiln gas an..ilysis. l-nc cxcsss C, carr be ietennined. 'fhus: N" from

tuei +

Exampte

r,

N,"f;;';;""1;; = rc,ta_r - xss o, \

lll:rjone Diasr

js calcined jn a ro.rary

ll? ,"0

isa

lilo/oft. O, and 63.20/o

ia_tn

fired wirJ.

S9/r,Cff,-r"J S+X - u''2.

#i;;;;;;;;i;r;

[,. Calculate: air ' *.

a) o/o excess b) Fuel Rauo {irg/moteJ'

H,

5o/o CHn

54olo N,

ee br*i fr;;"I g* 2o/o ,

2o/o

x

AriaJysis cf tj:e Cao, TT1.-.-8T 2.to/o Mga, t.zu u,o,, r 2,r;"ii"","6.rur^ "to". "iro_l SZoZ,

+s co^ contains 27o/o Co, t2Vo b,Or, gases tear.Ing ,rr"

Lime

Fuel

".

Soiulron-' Basis: I00 males dry klin gas

Xss O, = free O, = l N, frori fuel + \ for theo O, = S,2 For l0O moles Blasl Furrrace

n

ntC

27

27

12

12

u5r

).

5

54

:_

*

44

1,+

i{,

Il79/21) = 59'4381

Gas

GAS CG co - -2

Lro , t2

-

at II

molee O, 13.5

l2 d.

20

o
I i ?,,' .9'1'616iti.lviE'l,.)' Irq{)nLlCti.ir)},j i_ti. t..ttrlfr

,+ .. Tlreo O, = 44 + 24/4 _ 2S.S 24.5 = N, iionifuet + \ tor rh.;;;, = 54 + 24.5{7g/2i) = )46"1,1 Moles etast FuTace Gas = 0Oo/146.1V x59.43g1 = 4i1.1i6i"3, Theo o,'= (24.5/t4e.rn xsb.iger = 9.962

a) 1:.o:.:" O, = {r/9.062J x . UU" tjal: C0" from

100

=

4:

ExampLe

flO.lrom Lr : 35.s - o.++tqa;dia = ,r.s, ()', N\n4 in LT = 100 - 43 lS - 1.2 35.656/o =

in kiJ,

A calcjnaiion p)anl ry;a;:t:faclr:txig I 0 tonnes ljme./ day ccxsisting of 83% CaO, 5% CaCO, and 12o/o

inefis. Ttre fuel used is cclai gas arlalloing

co,

'

5.9or" 0.70lo O, r::rd 4.1 Vo CCr, CIJ4, 53.2% 14r,29.fia10

6.5% N, entering at 25"C, 7"40 mm Flg with 800/0 RH. Orsala analysis of the kiln gas shows 10.630/o COr, 0.6ffr'0 C(), 0.66% Hr, €'"75010 O, zutd 81.llolo

to:g4olo ANS

LT + CO. from fuel = CO,

g;is

Nr. Calcu.late: a) 1€ of Urnestone charged/elaY b) m' ol Coal gaslcjay c) 7o r{rcess O,

.

Wt of Lime = tZ.gI(44) x (.5565/.4315) = i016.32

b)

Frrel Ratjo = (10I6.32 /40.6ffin =

Zi

Irg lime,/mole fuet ANS

Methorl 2: kt x = moles of fuel

Lirnestone

Kiln Gas

83% CaO 57r: CaClO,

= rnoles air z = weight :f limestone

For 100 n;oles Blast Frrrnace Gas(see Ivfethod aL C = 44 at-H = 24'moles O, 25.5 = .

\nerLs

I0.6370 {-'0, 0.66% C0 0"66% H, 6.750h A, 3i.2olo N,

12o/ct

v

Arralysis of LT: 43.l1o/o CO, l.Zoto FIrO

ald

--) 1J:

Air

55.650/o N\,J\4

BURNER

At C Eal: O.++x + O.43tSz/44 = 35.8 ir4oles^Or^B al:-.2SSx + 0.431 Sz/44 + =,Jb6 + l +.2a.x/4

\

.2Iy

bzJ: 0 5a1+ .079y = 63"2

Solving Siniuitareously; x 40.66 = .:2.207 -v = z = tS:S.Ci+ See I, leril.ci

I fcr [rd

a;.:su.:ls

,r I J.i

Fuel

luel'^baS 5.9 % CO l'1 o/^ (-i

L; -a q ()/^ 7U !1. \)J.L

6 9/a CH. 6.5 o/o N, 4.7 atb O^

2?t

i 14 / s;otcjiiorv,ETi?y

{bltion:

PRaiii.j(11()N t)l'- l.lMf /

Basis: 1 day Moles HrO frcm coa-l ges = (576"66)

Weight of lime = 10 tonnes or j.0000 1g

a)

Wr of limesrone-/day = .83(10000X100/56) + (.05)tOOO0) + .12(iO000) = 16521.43 ANS Moies CO, from LT= Moles Cao .g3(I0000) (t x =

/56)= I48.2I

For 10O moles Dry lfiln Gas; -.!ss O, = 6.75 - .66/n - .66/2 = 6.00 N, from fuel + \ for theo O, = Bt.3 _ 6.09(79/21) = 56.39 For I00 moles Dry Coal Gas: GAS

atC

Il

CO

5.9 53.2 29.6

rL CH, CO,

29.6' ,1 .1.

4.1

o"

o.7 6.5

N,

atfl

5.9

moleeO, 2.9

106.4 r

r8.4

I

.:

4.1

o.7

39.6

224.8

iru

fheo O, = 39.G + t224.8/4) _ Z.ZS = 88.O5 N, from fuel + N, for theo O, 6.5 + AA"CtitigtZt) = = 337.73,tj I-et

x

= moles Dry ki.in Gas moles dry coal gas

at C ba-iance: 0.396y

+

l4B.2I = (10.63r.66)/l0O x

Tie subslance: i337.736lt00) y (58.39/IOOJ = x Soii,l ng S jmu jta-neo ??o( rl .\* *- uuuJ,lf

u

slr,:

1<

, --: '.

Dr..

?

'-,'L)

--

m3 coal gas./day

1273+25)/273

=

i.y.:ii6t 1566.1? t /(22,g+21i 6i :nm ljs

2,1

--=15.1

74A -, CI.s(23.61)

= (576.66 + 15.1)(22.4iU6A/740) 14860'35 ANS

Theo Or'= (88.05/100) x 576"66 = 5A7^75 Xss Or-= (6.09/100) x 3335-41 '= 2Ai3"72 96 excess

O, = (20i' 12/507.75)

x

100 = 40% ANS

PROBLEMS

i. A pla.nt is buming limestone analyzn$

47o/o"eaCOr" 45o/o tvtgCOr'ana B%o inerls. The lo1n is fired with producer gas 25.3o/o CO" I 3 290 "0 : 4oh CH4, 5 1'4olo AO r, 0'1Vo "ont^ii'ri"g o, and S{.zvo Nr. The kil" E,t ts sampiecl nd the average analysis is foundto be2l.9Tlo COr" 3.54% CO and l2'A9f./o If the fuel ralio is 20 kg of lime/mole of producer gas, "

ca]culate: aJ o/o excess

air

(44.557oi

Lr) Complete analysis of the BJln gas {7.74o/o ()2, 61.44% N?)

,A high sujfur fuel oil eontaining 75.2o/oC' 9'59% S and negilgible N is bumerl in excess air to suPp-iy -the heat n*".r"ary lo calcine a stone consisting of 52"3% CaO,

I

2.5n/oMrgO, 43.1% CO, and 2" i7o moisture' The operauon

of ttre kilrt i*" such rhat the lime is incompletely bumed arrd coniairs 6.2ola C0,. The average ana-tysis of the kilrl gas shows 25.4ok CO2," 1.9% CO' 0.5% '50r, 5Vr O, a;rQ 07 2a/c N^. Ca-iculate:

Y = 576.66 At

vl

8(23 6 i) x

a) Completi: ulriurate a,rra-lysis of the fuel 17 .77o/c H, 7 44ah A) i;) i;r-itl raii,: (€j.57 kg lirr;c,'kg oii)

I

I

lt

ll

tl

if;

I

i6 / srcicHi{l:.tr'iny

3. .

A luei gas made up ,*'f a rnj-xture of r::rethane'and eLharre is bui-ned ln lxcess air anci tjre heat grven off is used to calcine ccmpietely a stone containing 950/o CaCO u And

5o/o

ineris. Compiete andysis of the kiln gas showJ 2|.4Toto CC, , 5.54o/o O,, 62.54Vo N, and 10.50/o H,O. Calculate the anaiysis of the fuei gas and t}.e fuel raLio. (TS.IG o/o CH,+ a:rrd 24.84o/o CrHr; I0.5 kg hme/kg fuel)

4.

I

A kiln is used to ca.lcine a timestone analyzingl2Vo CaCOt^, 30olo MgCO., 5o/o A\Ar, 470 il.icr"ts, 60lo SiO, and 3% moisture. Coal is burned to supp$ heat of calcination. A;ralysis of coal shows 13.89/o VCM, 8.60lo ash, Jo/a moisture, L.Zo/o S, negUgible N \rlh a.caloi:ific vaiue of 32.95 MJ/lg,Ana-lysis oitlre kiln gas shows l8.SVo/o CO, Io/o CO, 0.22c/olr 8.390uo O, and Zl.82o/o N,. Calculate: a) i\g llmestone/kg coaj { 7.48)

b) Fuel ratio

419/o COrand 70io jnerts using coke that ana15.zes 90% C arld I0olo ash. The lin:e prociuct obtajned contajns 3ozo CO, and 1o/o unL,urned C. The top gas shows 22Vo COz, 1% CC

artd

a

APPENDIX T TABI-E oF STANDARD HEAT oF COMBUSTION ln4l/Kgmolf

(4.37)

5. A pia;rt js burnjng limestone whjch ana-lyzes 52o/o CaC, Nr. Calcuiate: a) kg limestone/\g coke (I.9) br) Fuel RaUo (1.16)

6.

APPENNIX

Compound AcetalrlehYde

*.,",,;-l**o;" -1 193.15

cH3cHo

ACeTiC ACid

CH.COOH

AceLone

C H.O

"872.28

!

B7o/o

A p)arrt produces )ime analyz-ing 53% CaO, 35% MgO anti 12o/o inefls. Watergas ana-lyzing 38.30lo CO,52.8o/o , O.4o/o CH^, 5.5010 CO2, 0.1o/o A, and 2.90/a N, is used as fuel. Anaiysis of itie kiln gas shows 15.710/o COr, 3.3I?6 CO, 6.6}% , 9.Bl o/o O, assd 64.560/o Nr. Calcu)aie: a) Vrreight of lirnestone/mc:,\e water gas (7.69)

b) %

dxcess

air

i40%J

Acetylene Benzene

iT

'crH,

1300.50

ct b

-

L,^11-

I

CH^

d

-3269"8I -3303.72

6 t)

n-Rutane

I

il

ir I

i i

1

Isobutale

6 b

-2E50.92

i

-2870"63

I I

ll lt

il

tl.7

It Ir

ti

il Ir

I i

I

"".I'p[NDi]

I I

/ I l"

I

I i

Forrnula

Compound

l-Butene Carbon Disulfide

Cilrbon MonoXde

I

I

I

J:

."1075.88

CS, UD,

-1103.3i

C,H,

n-Heptane

NLI

6 b

-14r eI -*---"J 1

L4 73

I

-482a

b

-4856

n-Hexane

CuH,n

I

-4165.91

s).

Hydrogen

H2

t>

d

:286.03

m'

Metharre

CHu

56

-8E0.95

Methyi Alcohol

cHsoH cH3oH

I

-72V"O4

d t)

-764.47

li::

CO

6

cct4I ccl4t

i

-283^ rB

-352.4 AA *Ji5C.ZJ ^A/

d b

c2H5cl

6 b

-t422.09

Cumene

c6H5cH(cH3)2

I

c6H;cH(cH.)'

o

-5218.93 -5264.11

pr

H--._

FI tr: i{

E

!(r r-.

F F

:

C.H,,

I

-3922.53

Nrf , "6, 12

d

*:

-3955.65

Mettryl Chloride

cHscl

Methy! Cyclohexane

CrHru

.-767.15

LI, l

l.r

-4568:34 -4603.76

CuH,o

I

C-H ) tu

6 b

-3293.09 -3321.77

I\'letyhl-

cyclopentaxe

C.H,u

I

-3940.36

Ethar-te

C^H^

6

-1560.92

Nilrobenz-ene

C.H-NO-

I

-3094.04

Erhyi Acetale

cH3cooczH_

I

-2255.68

n-Pentane

C"H,,

1

-35 r i.89

CH -5''12

6

^

d

-222.1"52

6 o

-2059.85

Cyclopentane

Erhyl AJcohol

etirl't

Berw-ene

367.83

crFIsOH

I

c2HsolI

l>

c6F{sc2H5

I

cH

6.

-4567.92 -46\0.21

I

-2732.26

b)i:

Ethr,l Etirer

I

I

I I I

l4,|t..

Chloroetha:re

Qyclohe>;ane

Ethylene

I

C-H. -

{.- :

lj t,-

ffi

i I

t.

t-

t

I{e

State

t!.

-2720.40

CnHu

Carborr

Tetrachloride

Formula

I

c^H-

rfll- lJr L2r ur=vv-r

r

-14i0.18

d

il it Itl __.._l

.-

Fropale Propen.e

.CrH, C^H^

:i-Prop-li Al cohol

D

c^i-r

o

"11.)o. c

I

I

A-rl'|::ll;l.i

; I 2l

I{FFEIUDIX 2 }.IEAT CAP/\CITY OF INEAL GFSES

C.inlpi:und

kVkgmolK

r:-Pi'op;zI Ben::sr-"e

-522r.74

Styrene

c6HscHCH,

-4441.78

t o1!._lene

c6HscH3

3912.56 -3950 58

Acetlziene

5.

r32

1"952

c6H4(cFI3)2

-39 ]2.'56

Air

c ?(6

0.575

c6H*[cH3)2

-4s97.6

-0.206

3s"064

c6H4{cH3)2 c6H4(cFI3)"

-4555.91 -4599.37

Car"bon Dioxide

5.457

1.045

-t.157

c6Ho(CFI3)2

-4 555. g

Carbon Moonoxide

J.J /O

0.557

-0.03

c6H4(cHe)2

-45Ft8.32 Chior-irre

4.442

0.08d

-4.344

Dinitogen oxicie

5.328

\.211+

a.928

m-Xylene

o-?ry]€ne

Chemical Species

i

I

i

H2CO

Diniirogen Telroxide

a

11.66

-2./c,/

t-\tr"7

Ethane

i.13

i

19.225

-5.56I

Ltnyiene

1.424

i4.394

-4.392

Hydrogen

a.

qao

a.422

Irrydrogen Sulficie

2Cl..t

1"49

Me&ane

l:742

9.08l

lriilric Cxide

4.982

1.195 I

0.593

,'). -1,6

t

m

/

s-iotr--H lr:rMi:t ri',

Chemical

B

Species Oxygen

tr

3.639

ooo!

C

roooooo)

-4.2)7

0.506

REF-ERHNCES

1. 1

Ftopane

1.213

28.785

-o.oz+

Propylene

i..oJ /

22.7C6

-6.9r 5

l

.lr

j,',t

Sulfur-Dioxide

5.699

0.801

Sr'tlfur Trioxide

8.06

1.056

Toluene

0.29

47.052

Water

i' j.:]',.'i j ir.:',

,1.+

/

1 A.r.

-

1.015

l'.

Arrstin G.T., Shreve's Ciremical Process Indust:-ies" Mc Hill Book Co", New York, 1984.

-t5.7)6

, q.121

Grarn,

Bhatt B.l. and Vora S.M., Stoichjonret-ry, Tata Mc Graw Hill Book Co., New Delhi, 1976 Fra;rcjs W. arrd Peters Pergamnon Press, l9B0

M., Fuels ard Frrcl

Technolopy,

4

Hougen O., Watson K.M., and l{agatz RA., Chemical Process priniiples. Part I, John Riley and Sons, 1966.

E J.

l-ewis V/.K., Radash A.Il. iLncl Le'wis H.C , Industna] Stoichiometry, 2nd Ed., Mc Graw Hiil Book Co., New Yorlr ]

966.

Perty R.H. ard Green D", Peny's Chernica1Er-tgineers'Haldl:ock 6th Ed., Mc Graw Hill Book Co", New York 1984.

Petcrs M., Elemen(ary Chenrical Llngineennq, Mc Graw l-lill Book Co., New York, 1984. a

Regel E.R. Inclustnal Chemjslrv. Iieirihold Pu.};lishut! Cc.. )943.

\\rilli:lns

E.'1. ar-rcl Johnson R. C., Stoichrorrretry for Chenticai Engineers. Mc Grall, Hill Book-Co-; lJc1,,; Yorli-,i953.

lr)a I -1- -)