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INDEXI Calcgory A l Rcliancc I~iduslricsLi~~i i lcd Modulc No.Fl:lrc S~scc~ns P;~ial&?;la$?Tnitiilig S .stcn~ TES TS P 014

I

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I ICntcgon. A1 Rcliancc lndustncs L I I ~ I I I C ~ Modulc No.lnrc Svs~crns Patalgaflgil T n~ nl ng ys~cm TE S-T S- P-( 11 4

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1 0 INTRODUCTION i

Calcgoy A lFlarc Systems

I

I1.1 W h a t s f lar i r~gMany industries genera te significant amounts of waste streams such ashydrocarbon vapors which must be disposed of on a continuous or intennittentbasis. Some of the examples can be like off-spec product or the bypass streamsgenerated during startup operations. Direct discharge of waste gas streams andvapors into th e a tmosphere i s unacceptable due t o safety and environmentalcontrol considerations.

Rcliana: lndustricsLimitcdh t a l g a n p Training S ~ s ~ c m

Gas flaring is a standard operation aimed at converting flammable toxic andI corrosive vapors into environmentally acceptable discharges. Gas flaring convertsflammable toxic or corrosive vapor to less objectionable compounds by means of

combustion. Flaring is a critical operation in many plants where design must bebased on strict safety principles. i~1 2 Whv s flaring re uired ?

Mod~llcNoTES-TS-P-014

I In general proper planning and layout of process plants require that specialI consideration be given t o the design of van ous safety facil~ties o prevent

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There are basically two types of flare systcm ~larncly,Elevated FI:~rcs \I. :ro~~nctFlrrrs .In an clevnted flare sy s~en l, otnbustion rcactlons are carried out : ~ t he top of apipe or stack w iere thc b t~ rn er nd igniter arc located Rclicving gascs are sentthrouzh an elevated stack from a closed collection systcm and Lmrned c T at thetop The flame generated is open in this casc E 2 the flarcs of PX and LABplants at RIL - PG I

Carcgop - l Rclial~ccndustries Li~ilitcd

A sround flare is also similarly cquipped except that the combustion takes place ato r near ground level The flare flame is contained in a flare chamber

hlodnlc No.

Three types of ground flares are in general use - I

Flarc Svstcllis Palnlg:injg 1'r;tioing S\slclll TES TS P 014I

The type that uses a water spray t o disperse the combustion gasesa The venturi type that depends on the kinetic energy available in the wastegases to inspirate and mix the proper amount of air with the gase s3 Multi Jet ground flares where the fiow of the waste ga s is distributedthrough many,srna l burners

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3 potential water d a rn a~ eo ~n~trumcntatlonI

I

The vcnturi type ground flare is alniost obsolc.tc because of ol~jcctionnble h i ~ hnoise levels.

ategory - A

The multi jet type norrnally used has high initial costs and capacity liinitcdIIn contrast, an Elevated flare requires less gdund arca Becatlse o . i ts high

elevation, it can be locatcd within a process arca or on the periphery of tlic plantsite, since radiation effects and ground level concentrations of pollutants can bcmaintained within allowable limits P~ ping osts tend to bc lower du c to snlallerand shorter pipe runs Also th e distance between the point o f discharge fromsafety valves and the flare stack is less than that in the case of ground flares

Rcfi: ~icc r~d~~sfrics.ini1tcd

iproblem with elevated flares is that initial and opera ting costs are high.Maintenance is also difficult a d edious. The visibility of the flame is the mostserious disadvantage and sometimes causes objections from local community.These systems also require more steam to produce a smokeless flare. Afinaldisadvantage is that noise levels are relatively high.

hlodul~ oFlare S\.stcms P : l f n l g ~ T ~ l i ~ i r ~ ~ :vsfcrn

The selection of the type of flare will be iduenced by availability of space,characteristics of the flare gas i.e com position, quantity and pressure eve ),economics including both initial investment and operating cost and concern over

I ES-1 s-1 -01.1

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I-~C:ncgon A Rcli;~ilcc ~ldt~s~ricsill~ilcd Module No.FI:lrc Svstclils PJ I : I~~I I ILXI'r:1111i11g VSICIII TES-TS - ~ - O l 4

IAs wc know by now, that n a t1;irc systc ~n , clicving gases are sent t h r o i ~ ~ l lnclcvatcd stack from a closcd holiccliotl systcnl and burned ofiat the top. ;

I

Thus, a typ~c al lare systcm is conlpriscd of tlic following con1ponct:ts .

Relief, safety and dcpressurising valves ('wldch elieve the fluid to bc flarcd)I

Pressure - relieving headers that convey discharges from safety valvcs andpressure control va lves in the process unit to the flare.Knock out KO drum located before the flare stack in orde r to separateany condensate or liquid from the relieving vapors (it is hazardous to bumliquid droplets)

I I4 Flare stack consisting o f riser structure, M olecular seal and burner tip

The relieving gases from safety relief valves and pressure control valvts arecollected in a horizontal or vertical hock-out drum through a flare main teader.

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flare system Mo re infornlatcon on a niolccular steal is givcn in on e of tile cbmingchapters Uriclly, t rescmblcs a bubble cap and creates a seal by usidg thebuoyancy of tile pur sc g as to create a Lone where tlle pressure is greatek thana niosplienc pressure

,

Tlic t u r ~ c rip 5 sealed to the molecular seal outlet .r\cccssories on the burner tipinclude about three or fo~crgas pilots, a similar number of pilot gaslair mixtureasseniblies, and steam supply nozzles for steam injection

IAt the top of the burner tip, pilot burners, whichare autoniatically lighted from arem ote place through the igniter line, are positioned The steam connection is alsoprovided for smokeless flares and a purge gas connection is provided formaintaining an air free system and to prevent flash back by maintaining pres sire atthe molecular seal higher than the atmospheric pressure. This arrangementprevents air from re-entering the stack from ambient surroundings

C I I C ~ O ~A1

F i ~ r e - 1how s a schem atic diagram o f the entire Flare System.

l'larc Svncrtts

In the next few chapters, we shall go through the flare system design guidelines,

Ilcli;tncc I~tduscncs iltlitcdP~I:II~:IIIELr~111ingvsIc~n Modllle No. :TES-TS-P-OI I '

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3 2 I

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Catcgor . - A l Rcliancc lnduarics Liniilcd Module NoPiarc Svsrc~lls hlalpng3 Tnining Systcm TES-TS-P-014Itlic relief occurs Th e vaporization rate, here as well, can get affected by rise in

pressure

If the reboiler controller n1alfu"ctions for any reason, the rate of vaporization nlayincrcasc If the vaporization rate exceeds the rate o f condensation, the pressurewill build up in this case, the relieving rate should be the difference between the~iiasim uni ate o f overhcad vapor and the maximum rat e of condensation of thecondenser. In thc absence of data, the relieving ratc may be assumed to be thenomial vapor load to th e condenser.The column can also get subjedted to high pressuk, if the reboiler is an exchanger.carrying the hot utility like steam ) at higher pressure than the column bottomspressure and the exchanger tube leaksor relief load.^ drr to fire :I I

The surface area of a vessel exposed to fire, and which is effective in generatingvapor, is that a rea wet ted by its internal liquid level up to a maximum heightlimitation of 5 B above giade, which is the normal practice based upon the flamelength. GRADE s defined as any horizontal solid surfac e on which liquid couldaccun~ ulat e .e. roofs, solid piatform etc. I h e conten ts under variable leveli l l

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3 /racliorialirtg coltmrrn iIUsually fractionation columns operate with a nb rm a~ iquid level n the bottom ofthe column plus level on each tray liowe ver, the entire wall of a fractionatingcolumn within a fine height limitation of 25 fi should be considered as wetted

hlodulc Noarcgory - A l

Here the liquid level is independent of oper& ion , and therefore the rnaxiniumliquid level should bc used for determining the we ttcd surface. The wettedsurfaces of spheres and spheroids are calculated as the area of the bottom half ofthe vessel o r up t o a height of 25 ft. which ever $ives the greater surface area.

Rcliancc Indusrrics Linlircd

Ifeat absorbed bv ve v

Flare SVS~C IIIS

Where suitable drainage is provided to preclude an accumulation of flammableliquids directly under vessel, the total heat input rate to the vessel may becomputed as follows :

Parnlfiinga Tninittg Systcnl T E S - T S - P - 0 1 4

Where,

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I3,000 DTUn1rlfl2for 4 insular~oriI --

IThese values are based on the wcttcd surfitcc iipto tl~enornial liquid level.provided tlic insulation is fire proofed. Ifin sirl atio l~ s not fire proofed, the vessclshould be assumed as bare. i

i

nlcgon A1.( I-'l:~rcS\.S CIIIS

Vapor generated for t fluid below critical point i e at relieving rempera \lre andpressure) tlic rate of vapor released 1s -

Rcli;~ncc ~~dustricsi1111rcd hlcxlulc No.I % t : ~ l p n g ' c ~ i ~ ~ i n g\ \ t c n ~ T E S - T S P 014

where,W = Vapor release rate in lbs/HrQ = Total heat input BTUIhr

= Latent heat of fluid in vessel evaluated it the relief valve inlet pressure,BTUilbINo credit is normally taken for th e sensible heat capac ity of the fluid in the tank

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related contingency). If the electrical system had an alternate sorlrcc of supplythen only the loss of steamwould be considered, provided t11c elapsed time forpower supply source switching w as not too long to be i~~c lTcctiv e. In thissitua tion power failure would not be a contingency directly related to thc loss 01steam. ISince, double jeopardy is not usually considered, the niasirnun~ oad can be basedup on any one of the following con tinsencies.

Xlodulc No.T E S T S P 0 1 4Catcgory AFlnrc S ~ s t c t ~ ~ s

IElectrical Power Failure- Cooling Water failure'- Steam failureInstrument Air failure

I

Rcliai~ccndustries LinrilcdP;~mlg:~n~graining ~ s'icnl

For the fire case, a cause of fire is normally lochized. The who e plant is dividedinto different fire zones. Th e flare load is generally calculated based up on o ne o rtw o related zones. How ever, it is not unusual to consider the total loadIAnother consideration is tha t th e tim e delay relative to the discharge o f individualvalves caused by the same and related contingencies should be properly studiedwhile determining the maximum load. A similar line of reasoning will in somecases apply to a tire affecting several vessels where product composition andp:es:urc v ii yideiy.

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I

Tlie relievin~ al~orsro111 difl'erent I'IIVs and deprcssurising valves must first becollected in individual il; ~r e sul)licuders lo cited near each process arca. Subheaders must be intcrcorir~ected o a main flare header \\~l~iclieads to a knock outdrurii. Condens:ttes carried over by vapors are scpnrated n this vessel. Vaporsleaving the KO drulii from c,p iliovc up the flare stack where they aresubsequently burneil a t l ~ eip.The no. of main flare headers and the individual sub headers connected to themdepends up on tile type of vapors handled, temper ture and the back pressurelimitation of PRVs.The pressure level of the flare header depends on the type of pressure relief valvesused to protect the equipment and the pressure levels of the equipment connectedto th e flare system. In the conventional type of PRV, th e performance depends onthe back pressure. A maximum back pressure of 10% of the maximum allowableworking pressure is a limit f o r the conventional type o f PRV. For the non-conventional valves like balanced bellow type, piston type or pilot operated type,the maximum allowable back p ressure may be taken a s high as 40-50% o f th cvalve set pressure.

Rcl t :~ t~cct ~ d r ~ s l r ~ c si ~~ i i l C d Modulc No.TES TS P 014

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Calcgon A Rclinncc I ndus lna L i n r~ l cd Modulc No.F1:lrc Svs cnis P;ii:ll;;~ilg:~ Trninil~g vstcm TES-TS-P-014the flare stack is [lot known by that time, t may be assunled to be 500 R from t l ~ clast piece of equiptilent.A trial estimate is nladc for determining the dianlctcr of the flare header bascd upon tile m u rclievin : flare load and considerins thc back pressurc limitation of10% for couventional valves and 40% for balarlccd type valves. Note, however, asingle main header in many cases, may be too large to be economically fcasiblc.

The second trial is rcquircd for two main flare headers, one collecting thc LowPressure (LP) flares (usually 5 to I0 psig) and t t iL othe r collecting relatively HighPressure (HP) flares (usually 15 to 20 Psig) Th? two hcadcrs are connected totheir individual KO drums Thc vapor lines koin the K O drums are combined intosingle header connected to the flare stack.Maximum simultaneous load in each header must be calculated separately and thepressure drop must also be computed for the entire length of the pipe includingcombined len :th from th e KO drum t o the stackThe load in a subheader used for the line sizing: need not be same as the loadwhicn is utilized for designing the main header o r the flare stack.

7 The next consideration is the cost of constructio" m aterisls This determines thefinal no. o f flare headers. Vapors that normally require expensive materials may belisted a sl

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S \Yet flare and Dry llarc : Some tinies, relatively hot vapors carrying condensatesmay be separated from the d j old vapors. They do not run as separate headersbut either L,P or H P flare headers tnay be associated with any one o f them. Thu s awet flare header inay be in fact the LP header and he dry flare header may bc thcI IP flare or vice versa.

I

I .After thc total no of flare heade rs has been estabhshed, it may be necessary torecheck the vapor load in individual headers since introduction of a separateheader may allow subtraction of the flow quantity from earlier header to which itwas added initially. II

C:~tcgon A lFlare Systc~iis

For Example : IA typical coal gasification plant usually has

HP wet flare headerHP dry flare headerAn H2S header containing vapor which has more than 5% H2S

ali er running a certain distance by themselves may be safely conibined either. withI the low pressure mail{ flare header or the HP main flare header depending uponthis @rating pressure.

I

Rcliancc lndustrics Limitcd Modulc No.P a m l m Training Svslc'n~ TE S-T S-P -OI J

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A quick method for sizing compressible isothermal flow is developed by Lapple.As per this,

IFor a purc gas II

Cnlcgoty - AFhrc S?slcnis

Gci = Mau mass flow o r critical mass flow, lb Isec R2Po = absolute upstream pressure, Ibhn2A4 = molecular weightTo = upstream temperature, RankineZ = Compressibility facto rThe actual mass flow G ( Ib /sec ft2 ) is a functior. of critical mass flow Gci, lineresistance N, ratio of downstream to upstream pressure. This is represented byfigure 2. In the area below the line in the figure 2, the G / Gci ) remains constant,which indicates that the sonic flow has been established. Thus, for sizing flareheader, the plo tted pc;int must b e above the line

Rcliancc lndustrics LimitcdR ~ t n l g a ~ wmininp SvsIc111

4fL

Modulc No.TES TS P 014

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dr op dt niolecular seal and psi pressure drop due to flow through the stackheight

I Cnrcgon.- A tFlnrc Svsccnis

3 As a tirst trial, inside pipe diameter is calculated based on 0 Mach ( 60% of thesonic velocity ) corres ponding to pressurc temperature a ~ S f I s a c k ,2 psis and temp = To ( as it is assumed to be isothermal flow )

0*

sonic velocity, Vs = 223 * (I

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Tlie sum of all pressure losses starting from flare stack up to the safety valveyields the total back pressure This back pressure niust be lower than the ninuback pressure allowed in the system corresponding to the lowest set pressure ofthe safety valve

I

i

Tlie rnmimum flare load of a system is 1,000.000 Soiiir of vapor Tlie prcssurc ziie base of the flare stack is 2 psig, the average MW of vapor is 50 and temp is200 F. The distance from the dnrm to stack is 500 t The line has two 90 degreeweldins elbows and an orifice with Ki factor of 0 2 The total pressure drop at thcknock out drum is 0.5 psi. Dete rmine pressure at inlet of the knockou t drum . Also,given are

ategory - A lFlan: Svstcn~s

Solution :P = ( M t P ) / ( R * T )

= SO* (2+ 14. 7)1 ( 10.73 (200+460))= 0.12 1bIit3

I

Rclint~cc~ldustrics in~ilcdhta lgnnga Training Svslcnl Modulc No.T E S - T S - P - 0 1 4

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Now, G = Wl( rrd214

Po will be replaced by downstream pressure, i.e. 2 + 14.7 = 16.7 psia and figure 3will be used2

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f lcnce total pressure drop = 1 inc AI' KO dnl m P= 2.5 = 3 psi

IICntcgon l I Rcli:iricc Indos~ricsL~riiitcd hlodul No

I

Tllus the pressure a t inlet of the KO drum is 16 7 4- 3 e I9 7 psia or ps s

Flare Svstcm s I ' : I ~ ~ ~ : I I ~ ~ ; ITr:~i~ii~ig\SICIII T E S - T S - P - 0 1 4i

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.:~fcgon Rclt:ll~ccI~lduslncs i~iiilcd hlodulc No.Fl:trc S~srcnis I ? ~ f n l $ i t ~ gTrmning S\.sfcm TES-TS-P-0145.0 DE SIG NIN G TI IE I;I,AIIEST:\Ck L ACCESSORIES

IThe hydrocarbon relief streams are ~rln~nlyapors, but they niay carry son]?liq u~ d hat condcr sr n tile collectins lines A panicle that is 150 micron or less,can be burnt in the flare ~wthoc~tazard Larzer particles arc removed in the KOdrumKO drums are either florizontal or venical They are also available n a variety ofco nt ipr ati on s and arrangements which includeHorizon tal drum with vapor ente rins at one end of the vessel exiting at the topof the op posite end (no internal baming)Horizontal drum with vapor entering at each end on the horizontal axis a centraloutlet.

I3 Horizontal drum with vapor entering in the center exiiing at the tw o ends on thehorizontal axis.

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. .llc residence time 01 [he vapor shollld be eci"al to o r Srea ter than the timerequired for a liquid droplet to travel the available ve~iicalheight at dropoutvelocity of the liquid particle.2. Sulticient volume should be provided for the liquid accurnulatio~~n the knockoutdrr11>1. i

II

Tan propos-d I:? tollw+btng tornlula t o deternri e si re of horizontal drum , validfor particle size o f4 0 0 micron

IWhere,

Modulc No.T E S - T S - P - 014C:ltc~on A lI:l:~rc Sisccl~ls

W = vapor flow , lblhr~= liquid density, lblA3p = gas density, lblfi3M = molecular weightT = Vapor temperature, RP = KO drum pressure, psiaD = KO drum diam eter, t i

Ilcli:~nccndttstncs L i r ~ ~ i f c dP : I ~ ~ ~ J $ I I I GIr3111ingvstc111

If the calculdted KO drum diameter for 400 micron pzticle Daoo i s t o be

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I t is also a k ,eneral practice to assunlc a liquid holdup time between 10 and 3ruinu tes In absence of data. volume of 2000 gals of.tiquid can be a goodapprosinlation.

I

5 2 Sr al svqtcnl

C:~tcgon lFl:~rcS~srctiis

Seals arc provided in the flare system to flash back . If seal is notprovided, a continuous quantum of gas may be bled to the flare to inaintain apositive flow. The scals can be of two main types iquid seal and gas scal.

1,iquid seals are further classified as seal drums and seal pipes In the former, aliquid seal is used in a seal drum located between the KO drum flare stack Sealdrums can be horizontal or vertical. the selection mainly depends on the availabilityo f space F~ gu re shows a horizontal and a vertical seal drum Instead o f a drum,sometimes, a piping seal is used as a seal leg located at the bottom of the stack.Thi s is often an integral part of the stack. I

Rcli~ttccndusrrics Lin~itcdP i ~ ~ a I g a ~ i g ~r;iiliing Syslcm

seal drum maintains a seal of several inches on the inlet flare header, preferably~ i o t xceeding inches. More is th e height o f the seal, more is the back pressureSealing liquid is usually wate r with a continuous flow, the ovefflow go ins to theI

Modnlc NoTES TS P 014

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Seal pipes (Fig 5) located at the base of stack are cheaper than drums. lloweverthey can cxpericnce pulsation of the gas flow to the flare under very low flowco nd it~ on s Also during a large gas release, the water seal may be blown out of thetop to the flare stack I

I

G1rrdc 1it1c sor s r z i ~ ~c l legs

C31cgory A l

1 Slope o f the inlet line 1s designed to provide a volume of water below the normalsealing water level equivalent to inlet pipe volume of 10 A2 Depth o f water seal should not exceed 12 to &event gas pulsation

Rcliaricc l~lduslrics itaitcd

3 Seal water level is maintained by a continuous flow of wat er at about 20 gpm

Modulc No.

Normal overflow is taken off the bottom of the seal through a seal leg height ofwhich is equivalent to about 175% of the pressure at the base of the stack durinsmaximum vapo r release so that ga s release at the base of flare is prevented.

TES-TS-P-014lnrc S stcols

as seals

Pnl3lp:lngn T n i ~ i i ~ ~ gystcn~

A more recent gas seal type of device that has been developed to prevent flashbacks in the flare system is 'Molecular' type seal. It uses a purge gas of molecularor"

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where,C\ = mass flow rate, Ibl srp = gas density, lb/R7V = exit velocity, 111sAc = CISarea, 11

Cntcgo:01? A1Flnrc S~ sl cm s

Vapo r dcnsity .p,; 10 73 TExit velocity correspon dins to 20 of sonic velocityv = 5 (g K R T / ~ ~ )

Rcliancc I~idus~r~csi t~~i lcdk131gnt?p~r.ltaitlg S?.slc111

Flare tip cross-sectional area, Ac = d2144where,

Modulc KOT E S - T S - P - 0 1 4 -

M = molecular weightP = absolute pressure ofvapor = 14.7 psiaT emperature, Pg = acceleration d ue t o gravity = 32.17 ft/sec2

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800.000 ( 760/5O) *i).51370Hence, d 47.7 i.c. 4S inch.MP

Vapor density, ~ ; ----------1 0 7 3 T= 50*14.7/(10.73*760)= 0.09 Iblft3

Modulc No.TES-TS-P-014;llcgon A lFlare S .slcms

Max Velocity = W/ 3600* p~ *d214 )= 1C00,000*4/(3600*0.09*3.14*(48/12)*(48/12))= 246 ftlsec

Rclinncc Ind~~stricsi~iiitcdP;~ tn l&lngT r ~ i n i n ~vstc111

.. based on max flow

Son ic velocity, V, = (g K R T / M O . * I

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5 6 i l lrr stark drsignI

I I c i~ I i tof the flare stack depend% pon - I

I

I Icnt rclcascd by the flarc sas i n Dl'lJAl:'- Clia:acfc~is ics o ft h e fianic flame Ic ng*.> Emissivity of the flame4 Radia tion intensity o f the flame in R'TUIhr R25 Ground level concentration of toxic sases present in tlic flare stream i n the eventof a ilarne blow o ut. I

Calcgoq 1I;I:lrc Svsrcrns

Flame burning characteristics and flame lcngth are of considerable importance insizing the flare stack.Flame burning characteristics are shown in Fig.7 A which identifies zones of theflame spectrum in terms of dimensionless numbers. Figure-7B enables estimationsof tlie critical flame points in each combustion zone . Figure-8 helps to visualizeho w a flame profilc may be superimposed on the loci of Figure-7B. Note that th eflame height increases appreciably when combustible gas flow is sufficientlyreduced s o as to c m s e a shift back in to laminar zone. By designing flare tip whichinduces premixing of ga s and air or sele cting a smokeless design which ind sces

Hcliancc Industries 1.1111ilcrlI?t~:tlgang:~I.~:IIIII%vs~c~ii .\ lodulc No.TES TS r 014

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l'lle tliernial radiation and escap e timc car1 bc cstinra ted from tlic data in table-'.Valucs arc based on cspcrir~~cn:alata on tlic tllrcsllold limit of pzirl to the humanbody as a functiori of the radia tio r~ lltctisity i n ~ T U l l~ l r I R2 ,enerated by a flame.A silfe level of heat rad iat iot~ ntensity for unlimitcti time espo surc has been foundt a b c 440 BTUnlrlttZ. I t is apparent that a time interval with varying radiationintensity must be allowed, to per~ilita I1unia1l to esc ape fro111 a sl~ ddc rlly eleasedirltense heat source. Th e varyins radiation intensity results from an irldividualincreasilig his distance from tlie s ou rce o f heat.

hldolc No.nlcgor\. 1

Assum e a person is at the base o f a flare stack when heat is suddenly relea'sed.The average individual reaction time is between 3 and 5 seconds. Hence, duringthis short reaction time interval, the full radiated heat intensity will be absorbedThen follows another short interval (20 IUsec is normally assumed to be theaver age escape velocity of a m an) during which continually decreasing amounts o fheat will be absorbed until safe distance is reached (heat intensity for a safelocation is 440 BTU/Hr/sq.fl.)

I.'l;~rc \S ICI~IS I ; I I ; I ~ ~ : I II C : I 'Tr:r~tri~igVSICIII TES TS P 014cil:l ~rr c 11du5trics1 i11iilcd

I

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I

C:;lcgon - A I?cli ll~ccnd~~stricsi ~ ~ l i f c d Modulc No.FI:irc SYSICIIIS P : I~ ~ ~ ~ : I I I I$ J' r : ~ i l ~ i ~ ~ f ivgcnl TES-TS-P-014 I\v11ere.I - radiation intensity, h ~ ~ ~ l ~ r l s ~ . l t

f ernissivity o f th e flame(2 - 11~31 enerated by the flame, BTUIllr= distar~cc rom center ofllanle , Mnl feet above ~ r a d eo point (F i s rc - l o )

Flatllc criiissivity valves for colnlllon gas es are as followsI

Gas fI-iydrocarbons 0 4Propane 0 33Methane 0 2A relationship between f and the net calorific value of a gas can be used in tlleabsence of data -

Whe re hc = net heat value of a ga s (LHV ) in BTUIscf (60 deg.F, 14.7 psia)

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Icnce. from cqilations I and L i l and ror tnau radiation density qtl ) at flare basc~vllerc5-0,

f0

I

eel

Cntcgo:or?.A l

I l e t ~ c e , is derived as -I f = 0 s { [ ~ + ( ~ I r ; q \ l ) ] ~ - ~ ~- - - - - - ( IV )

(1,6

I and we note that y = radial distance from the base o i th e stack = [ x~-H(H+L)]

The shortest stack is obtained when q \ l = 3,300 BTU/hr/sq R ( orfrom figure 9 at te = )

t9

Allowing for the speed of escapc 20 ftfsec) we have -y = 20 te = [ x H H+L)] n ----- ( V )

Rcli:~ticcndustries LimitedPalal~lngn mi~~inl:\ s tc~n

The lim~ting afe radial distance from the flame is -f QX = (----------I R i e x = Q / 5 5 3 04 n 440I

Modi~lcNO.T E S - T S . P - 0 1 4

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i l l 2 Iny = [ x2 (I + (Xm-H)cos 0 ] + (Xm-13) sin ------ V )*

This fbrniula establishes the liin itina houtida ry for wind circulation Wlien-evaluating wind erects on flame tilt, an average wind intensity should be used inthe calculations.

iC:ltcgon. - lI;I lrc S.VSICII~S

Since heat load of the flare, the flam e length, an; the safe radiation intensity (440BTU/hr/sq A) remain the same, decreasing the stack height leads to an increase inthe safety radius Another importa nt consideration is the type o f support providedfo r the stack In general, the higher the stack the greater the structural supportcosts

d6d

Rcliancc ndustries LimiiCdPalalg;111g:1 rniliilig Sysic~n

IFor high flaring rates, ilie stack height calculation previously described leads to a1 very tall stack. Part of th e reason for this conservative estima te is thatcalculations arc based up on tile thermal effect on bare skin. If proper cloth in isprovided to personnel before entering the flare stack area and proper sllielding isinstalled at the stack or at the equipment to reduce the radiation effects, therequired stack height can be giea tly redu ced. However, there is a tradeoff in thatthe safe boundary limit must be increased.

Modolc NoTES-TS-P-OIJ

i

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a:ound SO0 deg .F, corresponding to heat intensities of 1300, 3000 and 4000BTUAlrIsq respectively This meanc that wooden structures and vegetationexposed to heat intensities of 3000 to 4000 BTUltirlsq tt and higher may catchfire and bum Paint on equipment also may also be damaged

Cntcgory - A l

Therefore, it is recommended that equipment located in this area be protected byproper heat shielding or emergency water s pra ys.The following s teps outline caiculations by the alternate method :

Rcliancc lndunrics Limiccd

I1 From equation 11, the radial distance from the flame at Q = 1500 RTUlhrlsq.ft. iscalculated.2 The safe radial distance at Q = 440 BTUhr1sq.A. is calculated from the sameequation

Modutc No.~ 3 r c .SICIIIS Palal&~ngaTninil~g yacn~

3 A suitable value for Q is assumed at the base of the stack = 3000BTU /hr/sq.ft. is a good start since protective shielding will be provided in th is caseat the stack.

E S - T S - P - 0 1 4

4 From equation IV, H i s calculated.rig tlle- 14 illustrates the differen t heat intensity loci that should be examined

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440 = 0.258 * 1 1370S 10" 3 X' ) -- 410 is snk intensity \salusNencc, safe radial distance, ? - 728 6 RTl~clamc icngh, L = 1 S D --------as per equation ( I J

= 1 IS *4 as the stack diamctcr is 4S i e. 4 tt= 471 f i

* The stack height, II - 0 5 [ I. 1Q rt ']\I ) 1 ' L } --as per equailon ( IV )For sl~ortcst tack, escape t~ ~nc ,e =: 0 Figure 9 s~vesorresponding value ofq 3300 BTU/llr/sq tHence, H = 1 19 6 li = 120 RThis is the shortest possible stack hc~ght, ut is not a practical height as it assumeste = 0.a If a reasonable escape time i e te = 30 sec. is assumed, then figure 9 givesq,,= 1330 BTUhrlsq A Then, H = 245 f l ( as per equation IV )

oi Now 20 te = [ x2 H(H+L)] In ixer equation ( V )We have: X = safe radial distance = 728.6 A

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1Now, y = [ XZ (H (Sm-H)cos 0 ] (Sm-t sinSubstituting the values, wc get y = safe radial dictance from thc bnse ofs:nc ,618 fi.

ARer the stack height has been established from radiation intens~ty ,slues, thcmaximum permissible ground level concentration of toxic gases in the event of aflame blow out should be evaluated Table 3 represents toxicological thresholdlimit as allowed by the environmental protection agency (EPA)Estimated ground level concentrations should be based on the emergencycondition of flame blowout. Th e calculation is normally done for a range ofc imatological conditions at the plant site.For a rough estimate, th e following empirical formula may be used

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.l'herc arc generally thrcc typcs of'llarc stack supports Guyed type, i>crricb ant1sc lr supporttngs a rous li y i d c t o thc cco ~~ om icsf'tl~csc rl~r cc ypcs of flare structures, the

comparative costs for material al?d lal;cr s fi~:>c i~n:f s:;i:k hcight a re tnbul;~tcdas r o l l o ~ s

Least expensive Derrick type Derrick typeSelf sup portin g Guyedivfost expensive Guyed Self supporting

Installation LaborLeast expensive Self supp orting Derrick

Guyed (Self supportingM os t expensive Derrick Guyed)*

GuyedDerrickSelfsupporting

Gv-rrerl.DerrickSelf

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n tlie pilot igniter system, tlie gas pipe is connected to a 3 venturi type burner-,~vhiclis located at the bot:om o f the stack. The fuel gas flows th ro ug i~ nozzle toinsp iratc air to for111 a comb ustible mixture. Th e isniter with spark g ap is locatedapprox. 3 above the burn cr. When the igniter button is pushed , tlie resultingspark ignites the gas air niisture. T h e flame front generated travels up t he pipe atthe top of the flare and ignites the g as from th e pilot nozzles.

ICalcgon AFlnrc S~sfcms

Typical narc pilot systc lns f ~ in elcvated flarr: stack is sllown ill figu~ c-15. Tilesame type of assenibly insralled horizonta lly may be used for flares.I

iTile pilo is piped to the top of the flare stack via a 2 venturi burner. Nozzles arepr-ovidcd at the end of tllc pi pe . In so me designs, nozzles are hooded and shbuldthe flatnc blow out, the heat o f t h e nozzle will ilnmediately rei ~ n it et.

Rcliann: l~rdusrrics i~~litedP;~I:~lglog:~rilling Svslcnl Modulc No.TES-TS-P-014

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6 0 OTHER IIESICN CONSIDERATIONS

6.1 Rlatrrinls f Con strllrt ion

Catcgoq - A1FIarc Svstcms

Followinl: table outlines nlaterials of colisttuctlon for different com ponents o f t l ~ eflare system

Com ponent hlaterial of construction

Rc1i:incc Iriduarics LiiiiitedP:~lalgniigaTraining Svscc~ii

Up to 20 deg.F Conventional carbon steel

Mod~ilcNo.TES -TS -P -0 1 4

Up to - 50 deg.F Special low temp. carbon stecl150 deg.F & below 18-S stainless steel

IAbove 750 deg.F High temp. resistant alloyl

Bottom section Gunite line (cemented for

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*( 1 Bv the addition o f steam'4.

0

Mod~tlcNoTES-TS-P-014Catcgory AFlnrc Syslcms

a I2 By making a premix of &el and air before combustioti so as to providesufiicicnt oxygen for efficient combustion

~ ~

Prevention of sm ok e in flares in normally accomplislied in three different ways :

Rcliancc In du str ia LimiccdPala1g:lng Tnining S .stctn

I3 By distribution o f t h e flow of raw gases through num ber of small burners

IAmong these m ethods, the addition o f stearn isimo st commonly used to produce asmokeless flare for economy and superior pe rfo hanc e. n steam addition, the rawgas is preheated before it enters the combustion zone of the flare. If thetemperature is high enough, cracking of the hydrocarbons may occur. Thisproduces free hydrogen and carbon. When the cracked hydrocarbons travel to thecombustion zone, hydrogen reacts much faster than carbon. Unless the carbonparticles are burned away, they cool down and form smoke. Consequently, inorde r to prevent smoke, e ither the hydrogen atom concentration m ust be decreasedto ensure uniform burning o f both hydrogen and carbon or eno ugh oxygen must beprovided for complete com bustion.There arc several theories which try to explain the chemistry of smokeless flares,using steam. One of them assumes that the steam separates the hydrocarbonmo ecules, thereby ~ilinim izing polymerization reactions and forms oxygen

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It may be observed From this that the highertlie mol. wt., the hi~Jrcr the rcquiredsteam . This may be associated with the tlicory tl ~ a t he liiglicr t l ~ c ~iol.wt, rllclower the ratio of steam to C 0 2 after combt;stion, resulting in a greater tendcncyto smoke. I

i I

Since, steam consumption is rather high about 0.46 4 ib/lb of hydrocarbons withmol. wt.50 , it is too expensive io provide for s~nokeless urning for tile masflare load. Normally, 20 of tile mas. flare load is designed ibr smokelessburning. This is well supported by the fact that massive failure is very larc and in90% o f occurrences, smokeless flares are produced.

Catcgor). A

6 3 Fuel requirementI

Fuel gas supply to the pilots and igniters must have high reliability. Since, normalplant fuel sources may be upset o r lost in the plant upsets, it is desirable to providea backup system connected to the most reliable aiternate he1 sou rce with provisionfor automatic cut in on low pressure. The flare he 1 system should be carefullychecked to ensure that hydrates are not present to cau se problems. Because ofsmall iines, long exposed runs and large vertical rises up the stack, us e of liquidb o c k out poi is frequently warranted to remove condensates that may havecollected in the fuel line especially during winter. It is a g ood practice to p rovide a

Flan: Svstctns Patnlgtng:~ ninitlg S stctil TES-TS-P-014M = hfo ecular weight of hydrocarbon

I

R c l i ~ n c cndustrics Lir~~ilcd Modulc No

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Emergency purging is used to compensate Sbr thcr~~inllirinkasc, .Allcr ccssntioliof 11 1 vent gas flow. the systcnl residual %aswill shrink as it cools to the ambienttemperature. I t nornlally takes about 15 ni inu~ cs o reach ecluilihriuni. U111css hcpurge is admitted,to the sys ten ~. he shrink will draw air back i n to the flare hc3dcrThe shrink problem can be overcome by sensin: thc systc~ il tcnlpcrnturc andaddins makeup gas at a rate commensurate wit11 the system voltrmc ;ind lllc niax.anticipated gas temperature. :

6 5 Noise poll~ltionNoise pollution from flares has for too Ion? been a n inconvcnicnce, acceltted inpctrocllemical plants as an inevitable byproduct of flarin~ rocess. I t has beenestablished that major individual source o f noise from tlare is usually a t the flaretip itself. This is especially true when the flare tip is of the type used for sn~okclcssflaring of hydrocarbon gases utilizing steam injection.Basically noise is created because of two reascns, steam energy losses at the highpressure steam injectors and unsteadiness in the combustion process.Ground flares are normally quieter than elevated flares. This is probably due to thefact that the flame contained inside a box is protected from wind effects and thest~b i iring effect of the hzat re-radiated from the refractory walls reduces therandom characteristics of combustion. The walls themselves will absorb some of

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Rclinocc Induslrlc 1.irtiilsdFI:IIC S\SIL III>~ TES TS P OIJ

6 7 I ~ i ~ t c ~ ~ r n r n t a t i o nr~cl olitrols

Typical flarc system in?trurnentation and controls a re as follo\\s

I)csi;11 of disch;lr;c pipin: requires care li ~l nal .sis of the possible thermal and111ccl1;1nic;11crcsscs i~~iposcdn the pressure relief' \.alvcs. I'roper anchors ,s u i ~ l ~ l r t snd l)~o\ .isioni ~ rlevibility of (lischnryc pipins can prevent these stre sses .

l

I TO ensure smokeless burning, a suitable control systeni is provided to regulatesteam injection into flare tip. Normally, a flow sensor is provided on the main flareheader. The flow sensor is in ratio control uith the steam. Alternatively, thelurninosity o f flame i s aeasured by a flame no nit oi ing device, ~ viiicil ets the steamflow in o rde r to m aintain the sniokeless operation o f the flare.

l\'iri~cri/.in: of 111c l;~rc ysta n depends upon tile severity ofanlbient temperatures.is norln;~ r;lclicc to slope ihc tlare hcadcrs lowards knock out drum 4 in per0 1 I . h is cllables condensate to tlow ir.10 KO drum, thereby reducing thepossil,ility of ;,ipc li.cczc up due lo l e n ~ t l ~ yxposure to lo:,, ambient temperature.I

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.l l ~ c larr st;t~tupand s~iutdbwriprocedures &ay differ from a plant to plantdcl>cr~dingti rhc flare systenl' it has. [{ere arc some general guidelines, which arefollo\vcd wllen starting up or slluttilig down a flare system.

I

II ltrili rlc l ~ ~~cko r r ~

After cornplction of construction, the system should be thoroughly flushed withwat er to remove scale and debris. Pressure testing should be conducted whererequired. Special attention should be given to all flanged joints, valves andconnections. All leaks found should be repaired and re-tested.

2 The flare KO drum pump should be checked for ease of operation and correctI rotation.

R I I ~ ~ I I I I ~ L I S I ~ I Si ~ ~ i i t c dP : I I ~ ~ ; I I ~ ~ Ir : ~ i ~ i i ~ i gvstcrii

3 All instruments sbou d be checked fc r proper connections and performance

Modulc No.IT.S-TS-P-014

4 Eqvipment su ch a s flare tip, molecular seal, flare front generator, wa ter seal, flow

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Tltc tot;ll flare svsrc~ii nri olily bc shu tdown and isolated af te r all tlie process unitsal-c shut dowri, drained o f liydrocarbons, dcprcssuriscd and purged as necessa ry.l'hcri llarc sy stc rl~ s pirrgcd wit11 nitrogen before opcning up the KO drum,rnolccular scal ctc. l i ~ r ny rnaintenalicc.Individual proccss units or pipes of equiprrtent cat) be isolated from operating flzlresyslc ~ii ltcr tltcy arc shu tdo\r,~ iy closin s block valvcs and installirig blinds, whenniaintenancc is rcquircd.

The flare inspection is carried out generally in the plant turnaround.In the inspection, the flare tip and tlie pilot burners, the steam nozzles etc ar echecked and replaced if required UT testing is done for the flare shell welds. T heflare shell thickness is measured at different locations. General visual inspection isa so carried out.

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1

The flare i n the PX plant is designed to llandle maximum flow rate o r 500,000kgllr of hydrocarbons. This load can arise whell there is plant wide elcctricityfailure. The normal operating flow in the flare design is 640 k ~ r .he flare has amolecu ar scal, with height of 15 fl and diameter of 80". Minimum purge gasrequired is 7 21: nm3Ihr. The riAer height is 305 and the riser diameter is 42".The flare tip is From 'John Zink' and is of 31OSS. The re are 3 pilot burners and 21steam jets. It uses LP 6 bar g ) steam for sm okeless operation.

I I

I

8.0 1:LARES :\I RIL I'G

0 1 ;I

The system had a ZOO M control Zink Optically Operated Monitor ) for ensuringthe smokeless operation in the original design. This was supposed to mon itor theluminosity of flame by a remotely located detector and adjust the steam forsmokeless operation Rut i z not conaiss icned 2s some of :h: criticalcomponents of the control system are not available. Currently, the steam control to

II n P a t a l ~ a ~ l ~ ; ~omplcs of IIIL, there arc t\vo flares one each i n PX and LABplants. Thc detailed information of both the flare systems is available withrcspective plants. Hcre is a brief introductio n to both flare systems.

II

Cnlcgo? A lTl:lrc S ~ s t cm s Rclinncc 111dustricsLili~ilcdPtllal@ng Tni~iinp, vslcnl hlodulc No.TES-TS-P-014

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ITnble 2 lcrt radintion nd escnpe t ime

I

Radiation intensity( B T U ~ K I A ~ )

Catcgory A1

Time to pain threshold(Seconds)

Rcltancc Industrtcs L~nitl cd htodul NoFlnrc S\stcrns Pnln1gnn.c.. T n in in g S~ st cn l T E S - T S - 1 - 0 1 . 1

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AcrnlcinArv lan i t reAmmoniah y l cculrh y l cohulh d m cArrinlc&-nc&TI hlatidcBmmdcBulrdlrneBu vl dcoh0IB u v l u n i r rG r w o 4'0,id~G r b n &sulfidetrrbonm utvb r utnch l3 t ideGdarincaombrwcncCs cx amC d all uorrm)Cycloheunc

C:ilcpry A1

-- . . , . .-- PPAf C I . ~ .) 1

2 310Im0 J

2

I1.000la,:5 m

20la,5175 ila, . >403

R c l i ~ n c cndos ~ nc s i t l i t l c dFlilrc S ~ s ~ c n l s ~ I J E ~ I I ~ Ir3 i111112S~. ,s\stct l l

Elbyl bmmidcElhy l chloride

h l d o l c NoTI:S TS P o14

Ethyl r thr iElhylrnc rhlomhydtinEth~lcncdt ivn inc

T r r l ~ l c l ' l t r r s l ~ o l d l i r ~ l i t so r s o n ~ cox ic s t ~ b s t n ~ ~ c r sg:~scs:III~npors

H y d n u n eHydrogen vicnidcHvdmecn rdlidcI ~ p h 0 r m ~l ropm~y lun ineMc t iv I ox idcMethyl cam.h b th yl r q l m c

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dbM.GMn

Rcncd

AMHmg

A

R0

ID

109

P

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I.. I1.1g11rc I rrssl~rrdrop c r:trt li ~o\r t i p s t r r s l n condit ions by Lnpple )I Cnlcgon - A I~c l l i l l l c ct l d~~s t r i cs~ n ~ ~ t c d odulc No.1-inrc S .s cna P:I~&:III?~ T r a i t ~ i ~ ~ c~SICI T E S - T S - P - 0 1 4

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I ig~tre - Prrsstlrc dr op clt trt knowrt tlownslrcarn co r~ di ti on s by L o c bI

Modulc No.TES TS P 014

Cnlcgon AFlnrc S~stcnis Rcli;~ncc nd~rslricsLinlrtcdP:~tnlg:~npr3 ing ~ s l c m

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. ., FROML o w o o w N D U V

SLOPED FROM FLAREc-E,

SEAL DeEP ENOUDH r-TO FILL VERTICAL 1.6 DRAIN

BECTION OP VAPORNLCT LINE IN EVENTPLAEHBACK, 6 LlOUlD

LEVEL ,

SEAL LIOUID

a

( A )

f;igt~re - A) Ilorizontal seal drun~ U) Vertical seal drum

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I

Pp~dbHGM;nc

RodvAM.Ha

A

db

R0

D10O

P5o

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lodulcNo.TES TS P 014

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r c A ) Ilurr~ ing l~ar;lctcristicsof fl:rnrcs fronr circular ducts dischn rgingcrtically irrto qrricsccn l a i r ~ i l l ~ o r r trclf~ixirig

xcgon A lFlarc S~stcnls

13) Plot oC(IJ1)) versus rrrncl~n~rrrrl~cr

Rcli:tncc It~dusrncsLintllcdP:~l:~lg.~n& a rainill : Svstcni

h lodulc No.TES-TS-P-01.1

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e C: rcgon A Rclinncc Induscrics LinlilcdFl:~rcS~lsrcn~s Mcdulc No~ : l l : l l : : l l ~ ~ ~r ~in in g vsfcm I T S - T s - P - 0 1 4

e I zoo

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I; ig ~ ~ re Plot of m:txirn~ltt~ adi:~ tion intensity vcrslrs escape time, nssrt~ ningscc ond rcrct ion t ime.

I

>COwCz b7-zOc

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Figllrc 10 F l n rc s t n c k n n d f l r n ~ cn strtgrtal l t s ttrrot~ndings

I C J I C ~ O ~A Rc1i:incc I~idustricsLimilcd hlodulc No.Flnrc Svstcnis P:ihl ::~i~ ..;i n il li nr svs icm TI S TS I (114

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igure I lare stack and flame in k i n d blown stlrroondingt

I

I C3rcgoq Rcliancc lndustrics Liniiccd Modt~lcNoF h r c S\.stcnis f'3131pn l T m i n i n ~ vstcln T E S - T S - 1 ' - 0 1 4

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I Figllrc 2 Plot o T t r n i ~ ~ c r ~ t ~ ~ r cf steel cqcril rrrr~ltvcrsrls rxposllre tintr for di f kr r ~ r trndiant l~enIntcnsitics. Clln2csnrc based or1 0.25 [tl:~te lrirklrcss wirh nn rfirtivrcmissivity of 10 nlrd vier f:rctor of 0.5. Coolinx r:~l~srd~ y o~~vcrtioritc. nrcncglectcd.

c3lcgon. l Rclinncc lnd~lstrlcs .in11tcd M@?:lc No.FI:rrc S\~srcn~s l ; ~ t a l y t ~ pr:t~ni:l: SYSICIII TES 7.; P 014

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C;ltcgon A cliancc Ind~~slncstnl~lcd hlodtrlc NoFlxc S ~slems I'nlnl;nri~:~ Tr:~inin~:vsicrn T E S - T S - P - 0 1 . 1Figure 13 Plot or r q i t i l i l > r i r ~ n ~cn p rr :ttttrc vc rs lj s r : ~ d i: l n t l ~ c a t r ~ t c n s i t ~ .1 11~Cltrve s fo r mctnl c q ~ ~ i [ ) n ~ c n th i l e c t t n r c 2 i s f or woot l .

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. ................ -.... .............. .a u S A F E B O U N D A R Y

3.. :. 4 4 0 B T U / H R / S Q . F T . )

.............. :-: :.BOUNDARYi F O R R A D I A N T...~ i E A T I N T E N S I T Y...........= Z. . ( 1 5 0 0..... ). . B T U / H R / S O . F T . )- N O R M A L L Y F E N C E D

I C:llegon AFlitrc SYS~CIIIS Rclinocc lndustrics Lillliicd Modulc No._ P: irn lg :~~~pra~nin :Svstcm E S T S P 0 1 4

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I:i:t~rc 5 - 'Typ ica l f lnrc p i lo t a n d igt t i lcr

Ca cgon - A I

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fo l lo \ \~r?gcli rcnccs havc bccn u\cd ~ v l~ il c~ r c p , ~ r i ~ ~ gllis moduleI

I Flnrc Gas Systc n~ s ocket Ifandbook by K. ~ an c r j cc , . P Chct-cm isinotTct. al

I .> ~Im cric an etroleun~ Institute, l ie lir it~ y ~ dctice s, 20 and 521

lnfonnation regarding statutory requirerncnt and LAB flare system has beenobtained from Mr. A. E. I atil ( T and Mr . U. D. Deshpande ( TS ).II

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I

11.0 QU ES TI ON NA IR E FO R \ ALIDATIOIVII

I'ollowin~ s a list of some of the questions which can be useful for validation oftraining on this module.

I \Vhat is fl; ring ? Why is it required ?

Modulc No.E S - T S - P - 0 1 4Calcgory A lFlnrc SVSICIIIS

Wliat are direrent types of flares? Wliat are tlie advantages and disadvanta~esassociated with then1 ? I

Rcli:~t~ccndustrin LiniilcdP:~lnl&?ng.nTnin i~ i f ivslcnl

I What ar e the comp onents of a typical flare system4 what a rc the causes which lead to overpressurization o f a process system ?

I5 How is the relieving lo td calculated in case of a external fire ?

I6. How is the maximum load t o be flared is arrived ai ?

I

7 Describe the guidelines to estimate no. of flare headers in a plant.8 Outline briefly the m ethod o f sizing the lines in a flare system.

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I 2 What are the types o f flare purging ? Why is pursing rcqi~ircd21 \\ hat is typical ins trunlenta tion and control associated with a flare system ?

27 Wliat are the steps in startu p and shutdown of a Ohrc system23 Wliat are the inspection ch ecks carried out on the flare stack

I

24 \\Illat are the things, oper ations crew sho l~l dmonitor 111 tllc normal operation o f theflare 7

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l ,\T/\L(;ANC;A TR AI NI NG SYSI ISRITopi Fla re Systems & I o d u l e No :TES-TS-P-O 4C a t e e n r y t : .IMC & ion Si teSr. N J

1

.

3. --

.I

.CONTENTS

Rcquirclncnt orfl: ~rin g11)pcs f n rcsCo~ llpn cnts of t ltcflare systemDe tc rn~ in i~ lgvzpourloads to be flare6Dcsign of collection

thc MGMdcsigt~ MGMconsidentions

Flarc opcra lio~ ~s MGMFlares at RIL - P MGM

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