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## Document

Number: 

# 142 ) ll-J- 4

Docket Number: 

# A-90-1 9

Printed 11/26/20088:52:04 AM

Sheet 142 of 204P. 2

Federa l Registe r

/ Vol

. 55 , No

. 12 6 /

Friday , Jun e 29 , 19 9 

# A-90-1 9

ll-J- 4 !

ENVIRONMENTA L PROTECTIO N AGENCY 4 0 CF R Par

t 6 0 [AD-FRL-2823-6 ) PI N 2060-AB5 5 Standard s o f Performanc e fo r Ne w Stationary Sources ; Volatil e Organi c Compoun d (VOC ) Emission s Fro m th e Syntheti c Organi c Chemica l Manufacturin g Industr y (SOCMI ) Reacto rProcesse s AGENCY : Environmental Protectio n Agenc y (EPA)

. ACTION : Fropoi-^drul e an dnotic e o f publi c hsanr.g

. CU5*MAi"Y:Th

e propose dstandard s woul dhm! ? the ernissior. s cf VO C fro m netv

. nic'lfied

. en dreconstructe d SOO.! : rt : icto r

proces s facilities

. Th e prupoie G standard s implement sectio n 1 • ; 1 o f the Clea n Ai r Ac t (CAA ) an d ar e base do n th e Administrator' s determinatio n that

emission s fro

mth e SOCM I caus e o r contribut e significantl y t o ai r pollutio n whic h tr.a

y reasonabl y b t anticipate dt

o endange r

publi c health cr welfare

. The inten t

i s t o requir e new , modified , an d reconstructe dSOCM I reacto r proces s facilitie s t o contro l (.'mission s t

o th e leve l achievabl e b y th e les t demonstrate dsyste mo

f continuou s emissio n reduction , considerin g costs , r.onai : qualit

y health an denvironmenta l impacts , an d energ y requirements

. A publi c hearin g wil l b e held , i f ;-quested , t

o provid e intereste dpartie s

. ' r
. opportunit

y fo r ora l presentatio n c

f data , views , o

r argument s concernin g the propose dstandards

. DATES : Comments. Comment s mus t b e receive don o

r before Septembe r

12 , 1990

. Public Hearing. I

f anyon e contact s EP A requestin g to speak

a t apubli c hearin g b y Jul

y 20,1990

. apubli c hearin g wil l b ahel don Augus t

7,199 0 beginnin g a t 10:0 0 a.m
. Person s intereste di n attendin g th e hearin g shoul dcal l Ms

. Ann Eleano r

at (919) 541-557 8 to verif

y tha t ahearin g wil l b e held

. Request to Speak at Public Hearing. Person s wishin g t o presen t ora l testimon y mus t

contac t EP A by Jul y 20 , 1990

. Incorporated

by Reference. Th e incorporatio n by referenc e o f certai n publication s i n thes e standard s wil l b e approve dby th e Directo r

o f th e Federa l Registe r a s o f th e dat e o

f publicatio n o

f th e fina l rule

. ADDRESSES : Comments. Comment s shoul db e submitte d(in duplicat e i f possible ) to : Centra l Docket Sectio n (LE-131) , Attention : Docke t Number A

83-29 , U.S

. Environmental Protectio n Agency

. 40 1 M Street , SW. , Washington , D C 20460

. Public Hearing. I

f anyon e contact s EP A requestin g apubli c hearing , i t wil l b e hel da t th e EPA' s Offic e o

f Administratio n Auditorium , Researc h Triangl e Park , Nort

h Carolina

. Person s interesis din attendin g th e hearin g o r wishin g to presen t

ora l testimon y shoul d notif y Ms

. Juli aStevens , Standard s Developmen t

Branc h (MD-13) , U.S

. Environmenta l Protectio n Agency

. Researc h Triangl e Park , Nort h Carolin a 27711

. telephon e numbe r

(919) 541-5578

. Background

Information Document Th e backgroun dinformatio n documen t (BID ) fo r th e propose dstandard s ma y b e obtaine dfro

mth e U.S

. EP

A librar y (MD-35) , Researc h Triangl e Park , Nort h Carolin a27711 , telephon e numbe r (919) 541-2777

. Pleas e refer

t o "Reacto r Processe s in Syntheti c Organi c Chemical Manufacturin g Industry— Backgroun dInformatio n fo r Propose d Standards, " EPA/450-3/85-O05a

. Docket. Docke t

Number A-83-29 , containin g supportin g informatio n use d i n developin g th e propose dstandards , i s availabl e fo

r publi c Inspectio n an d copyin g betwee n 8 a.m
. an d4 p.m. , Monday throug h Friday , a t EPA' s Centra l Docke t

Section , Sout

h Conferenc e Center , room4,401 M Stree t SW. , Washington

. D C 20460

. A reasonabl e fee may b e charge dfo r copying

. FO RFURTHE RINFORMATIO

N CONTACT

: Mr

. Doug Bel

l o r Ms

. Debbi e Stackhouse , telephon e (919) 541-556 8 an d5258 , respectively , concernin g regulatory decisions

. Mr

. Robert E

. Rosenstee l o r

Mr

. Lesli e B

. Evans , telephon e (919 ) 541-560 8 an d5410

. respectively , concernin g technica l aspect s o f th e industr y an dcontro l technologies

. Th e addres s fo r th e abov e contact s i s Emissio n Standard s Divisio n (MD-13) , U.S

. Environmenta l Protectio n Agency , Researc h Triangl e Park , Nort h Carolin a27711

. SUPPLEMENTAR

Y INFORMATION

: I

. Introductio n A. New Source Performance Standards

— General Ne w sourc e performanc e standard s (NSPS o r "standards" ) implemen t sectio n 11 1 o

f th e CAA

. Th e NSP S ar e issue dfo r categorie s o

f source s whic h causa , o r contribut e significand y to , ai r pollutio n whic h ma

y reasonabl y b e anticipate dt o endange r

publi c healt h o r welfare

. The y appl y t o ne w stationar y source s o f emissions , i.e. , source s whos e construction , reconstruction , o r modificatio n begin s after

astandar dfo

r the mi s proposed

. contro l emission s tpith e level»achievabl» r b y "bes t demonstra t

_ "BDT, " whic h i s defSwd»inHtenrB:d ; below

. 

### dt@naiog\i'RrOCC. C

B. The NSPS Decision

Scheme A n NSP S i s th e produc t

o f aserie s o f decision s relate dt

o certai n ke y element s fo

r th e sourc e categor

y bein g considere dfo

r regulation

. Th e element s identifie din thi s "decisio n scheme " ar e generall y th e following : 1

. Sourc e categor

y to b e regulated

— usuall y a n entir e industr

y but can b e a proces s o r

group o f processe s withi n a

n industry

. 2

. Pollutant(s ) t

o b e regulated—th e particula r substance(s ) emitte dby th e sourc e tha t

th e standar dwil l control

. 3

. Regulator

y approach—th e genera ! strateg y fo

r regulatin g sources
. 4

. Affecte dfacility—th e piece s o r group s o f equipmen t

tha t compris e th e source s to whic h th e standard s wil l apply

. 5

. Emissio n point s to b e regulated — withi n th e affecte dfacility , th e specifi c physica l locatio n emittin g pollutant s (e.g. , vents , stacks , an dequipmen t leaks)

. 6

. Bes t demonstrate dtechnology—th e technolog y o n whic h th e Agenc y wil l bas e th e standards , i.e. , * * * applicatio

n o f th e best technologica

l syste mo f continuou s emissio

n reductio n whic h (takin g int o consideratio

n th e cos t o f achievin g suc h emissio n reduction , an

dan y nonai r qualit y healt h an denvironmenta

l impac t an denerg y requirements ) th

e Administrato

r determine s ha s bee

n adequatel y demonstrated

. (Sectio

n 111(a)(1))

. 7

. Format fo r th e standards—th e for

m i n whic h th e standard s ar e expressed , i.e. , a s apercen t

reductio n i n emissions , a s pollutan t

concentration s o

r a a equipmen t

standards

. 8

. Actua l standards—base don wha t BD T ca n achieve , th e maximu m permissibl e emissions

. Note : I n general , standard s d

o no t requir e tha t aspecifi c technolog y b e use dt o achiev e them

. Th e sourc e owner/operato

r ma y selec t th e metho dfo r achievin g th e pollutio n control required. ) 9

. Othe r considerations—i n addition , thi s NSP S includes : modification / reconstructio n considerations , performanc e tes t

methods , monitorin g requirements , an dreportin g an d recordkeepin g requirements

. C. Overview

of This Preamble Thi s preambl e will : 1

. Summariz e th e importan t feature s o f thi s NSP S b y discussin g th e conclusion s reache dwit

h respec t t oP. 3

2695 4 Federa l Registe r / VoL 55 , N a 12 6 /

Friday , June 29 , 199 0 / Propose d Role s

each o f the element

s in th e decisio n scheme . 2
. Describ e th e estimate d environmental , energy , and economi c impact s o f thi s NSPS
. 3
. Presen ta rationale fo

r eac h o f th e decision s i

n th e decisio n scheme . 4
. Discus s administrative requirement

s relevantt

o thi a action
. II. Summar

y of th e NSPS J4

. Source Category to be Regulated Th e source categor

y t o b e regulated i s th e SOCM L Tlies e standard s affec

tth e reacto r proces s subcategor y of the SOCM L A reacto r proces s i s the mean s b y whic h on e o r mor e syntheti c organic chemical s ar

e produce d by the reactio n o f feedstock s o

r chemica l intermediate s othe r ma n air
. (Processe s using ai r ar e covere d in a separat

e NSPS. ) B. Pollutant

to be Regulated Th e propose d standard s woul d contro l emission s o

f VO C fro m reacto r proces s ventstreams . C. Regulatory Approach Rathe r tha n develo p a separat

e standar d fo r each chemica

l produced i n reacto r processes , thi s proposa l i s a singl e standar

d covering all reacto r processe s producin

g on e o r mor e designate d hig

h production volum e chemicals
. Thes e 17

3 hig h production volum e chemical s accountfo

r about90 percen to f tota l chemica l production fro m the SOCM

I an d ar e estimate d t

o accoun tfo r th e majorit y o f th e emission s fro m reactor processe s a s well . Thi s same approac

h wa s use d in th e tw o previous proces s ventstandard s fo r th e SOCM I (distillation
. 48 F

R57538 , and air oxidation
. 48 F

R48932)
. D. Affected

Facility Th e facilit y affecte d by the proposed standard s i s designate d a s a singl e reacto r wit

h it s ow n recovery syste m (if any ) o r the combinatio n o

f tw o or mor

e reactor s an d th e commo n recover y system the

y share . E. Emission Points to be Regulated Th e emissio n points t

o b e regulated includ e VO C discharged fro m chemica

l reactor s eithe r directly fro

m a reacto r o

r indirectly afte

r passin g fro

m on e o r mor e reactors throug

h on e o r mor e produc trecover y devices
. F. Best Demonstrated

Technology A variet y o f control technique s are capabl e o f reducin g VO C from reacto r proces s ventstrea

m b y 9 8 weight
percen to r t o 2 0 part s pe r millio n by volume (ppmv l However , certai n combustio n control s (therma l incinerator

s and flares ) ar

e th e only device s tha tare applicabl e to al l reacto r proces s ven tstreams . The selectio n of th e bes tdevic e fo

r a n individua

l strea m depend s o n th e proces s ven tstrea m characteristic s an d othe r site-specifi c considerations
. Bac

h o f thes e tw o devices , however , i s capabl e o f achievin g 9 8 weight-percentVO C destructio n or 20 ppmv. Fo r facilitie s where th e cost s of combustion control by therma l incinerator

s or flares ar

a reasonable , BD T i s 98 weight-percentcontro l o r reduction t

o 20 ppmv, whicheve r i s les s stringen tFo

r facilitie s wher e th e cost s t o contro l VO C by combustio n ar

e not reasonable , BD

T i s n o additional contro L Th e standard s d o no trequir e tha ta specifi c devic e o r technology b e use d t o compl y with th e emissio n reduction requirements
. Rather , any contro l can b e use d a s long a s itca n b e demonstrated tha

ti ti s atleas ta s effectiv e a s BD

T atreducing VO C emissions
. Tri

e EP A i s unable , wit

h availabl e information , t

o identif y subcategorie s o

f reacto r processe s fo

r which VO C control technique s othe r tha n incineratio n or flarin

g (e.g. , catalyti c oxidatio n an d carbo n adsorption) hav e bee n demonstrate d t o alway s apply . The applicabilit y of thes e device s ma

y b e greatly affecte d b y th e ventstrea m flow rate , wate r conten t temperature , VO C concentratio n and VO C properties suc h a s solubility , molecular weigh tand liquid/vapo r equilibrium
. Thes e characteristic s var y widel y withi n th e SOCM

L Therefore , consideratio n of

thes e device s i n developin g regulator

y option s wa s no t feasible
. Eve

n wit h greate r resources , thi s analysi s woul d b e Infeasibl e becaus e i twoul d requir

e a stream-by
strea m characterization , ultimately resulting i n di e nee d t o create a separate standar d for eac h reacto r proces s facility
. Hi e numbe

r of standard s require d t o regulat

e th e sam e numbe

r o f source s woul d increas e significantly
. Th e Agency believe s tha

tsuch a n approac h t o regulating SOCM

I reacto r processe s woul d b e administrativel y infeasibl e and therefor

e environmentall y counter-productive
. Thi s approac

h doe s notpreclud e late r regulation o

f subcategorie s o

f reactor proces s facilitie s shoul d diatbecom e feasible
. C. Format

ofthe Standards The forma

to f th e propose d standard s woul d allo w owner s and operators o f affecte d facilitie s t

o compl y with th e standard s b y controllin g emission s or b y maintaining or addin g produc trecovery devices
. Wher

e m e cos teffectivenes s of control s i s reasonable , a percentag e reduction o

r concentratio n limi t whicheve r i s les s stringen twoul d apply . Wher e the cost s o

f contro l ar e unreasonably high , n o additiona l emissio n reduction woul d b e required
. Th e cutof f i s calculate d b y using a se to f equation s and coefficient

s in th e regulation tha

tproduc e a tota l resource effectivenes s (TRE

) inde x value . A TR

E index valu e o

f 1. 0 o r les s indicate s th e nee d t o control . Thi s forma

tpermit s owners and operator

s o f facilitie s near, bu tbelow , th

e 1. 0 cutof f t o chang e the proces s operatio n o

r equipmen

ti n orde r t o reduc e emission s and , thereby , rais e the TR E index valu e t

o a poin tabov e the cutoff
. H. Actual Standards Source s wit

h TR E value s o

f 1 JO o r belo w woul d b e subjec

tt o the following : (1 ) A 98 weight-percentreduction o f th e tota l organic compounds (minu s methane and ethane ) i

n the reacto r vent stream , o r a reduction t

o 2 0 ppmv , whicheve r i s les s stringent ; (2 ) i f a boile r o r proces s heate r i s use d t

o compl y wit h the standards , the reacto r ventstrea m mus tb e Introduce

d int o the flame rone ; (3 ) i f a flar e i a use d t o compl y wit h th e standards , i tmustcompl

y witi i th e requirement

s se tfort h i n 4 0 CF R60.18
. Fo r source s where th e cost s o f combustio n control resultin a TR E index valu e greater tha

n 1.0
. n o additiona l VO C contro

l i s required
. Facilitie s wit

h lo w flo w rate s (les s tha n or equa l t o 0.01 1 scm/mln ) an

d facilitie s whic

h ar e in proces s unit

s wit h lo w production capacitie s (les s tha n or equa l t o tgigagra

m pe r year fo r all chemical s produced) woul d b e exemp t fro m th e standard s excep tfo r certai n recordkeeping and reportin g requirements
. Batc

h processe s woul d als o b e exemp tfro

m th e standards , /

. Modification/Reconstruction Considerations A n existin g facilit

y woul d b e require

d t o meetthes e standard s i

f i ti s modifie

d o r reconstructe d a s determined unde r the Genera

l Provision s o

f 4 0 CF Rpar t 60
. Wit h som e specifi c exceptions , a n existin g facilit

y i s considere d t

o b e modified i

f a physical o

r operationa

l change results in a

n increas e i n VO C emissions
. Fo

r example , i

f a reacto r i s adde d t o a grou p o f existin g reactors and i f a n Increas e i

n VO C emission s results , al l reactors—existin g an d new — woul d b e subjec

tt o the standard s becaus e th e facilit

y had bee n modified
. A reconstruction occurs whe n component

s o f a n existin g facilit

y ar a replace d t o such a n exten ttha

tthe fixed capital cost s of

th s ne w component

s excee d S O percento f

di e fixed capital cost s tha twoul d b e require

d t oP. 4

Federa l Registe r /

Vol

. 55

. No

. 12 8 /

Friday

. )un e 29

. 199 0 / Propose dRule s 2695 5

construc t a n entirel y ne w facilit

y comparabl e t o th e existin g facility.. A facilit y wil l b e considere dt o hav e bee n reconstructe donl y i

f i t i s technologicall y an deconomicall y feasibl e fo r th e facilit y t o mee t th e standards

. /

. Compliance Testing Initial performanc e testin g i s require d to demonstrat e tha t

afacilit y complie s wit h th e TR E provision s o

f th e standar d or , fo r facilitie s complyin g wit

h th e emissio n reductio n requirements , that contro l device s achiev e 9 8 weight

percen t contro l o f VO C emission s o

r 2 0 ppmv
. Facilit

y owner s o

r operator s seekin g t o demonstrat e complianc e wit h th e TR E inde x provision s mus t determin e ven t

strea mflow rate , heatin g value , VOC emissions , an dth e presenc e o r absenc e o

f halogenate dcompounds

. Th e ven t strea mheatin g valu e an dflow rat e ar e use dto selec t

th e appropriat e TR E inde x coefficient s fo

r calculatin g th e TR E inde x value

. For

facilitie s tha t see k t o comply with th e 9 8 weight

percen t reductio n requirement , a

n initia l performanc e tes t

i s require di

f an incinerator , asmal l boile r o r smal l proces s heate r

(les s tha n 15 0 millio n Btu/hr ) i s used

. Th e initia l perfonnanc e tes t fo r aflar e include s ameasuremen t o f exi t velocit y an dstrea mhea t

conten t t o verif y tha t th e operatin g specification s ar e met

. Th e initia l performanc e tes t

ha s bee n waive dfo

r larg e boiler s an dlarg e proces s heater s (greate r tha n 15 0 millio n Btu/hr)

. K. Monitoring

Requirements For facilitie s usin g an y combustio n devic e to comply wit

h th e emissio n reductio n requirements , ven t strea m flo w t o th e combustio n devic e woul db e monitore db y us e o

f flow indicators

. Fo r facilitie s usin g therma l incinerators , smal l boiler s o

r smal l proces s heaters , continuou s measurement s o f firebo x temperature s ar e als o required

. For facilitie s usin g larg e boiler s o r larg e proces s heaters , record s indicatin g whe n th e devic e i s bein g operate dar e als o required

. For

facilitie s usin g aflare , th e regulatio n require s continuou s monitorin g o

f th e presenc e o

f aflame

. Fo r facilitie s usin g catalyti c incinerators , th e regulatio n require s continuou s monitorin g o

f th e ga s strea m temperatur e immediatel y before an d after th e catalys t

bed

. Fo r facilitie s usin g produc t

reco % er y device s to maintai n aTR

E inde x valu e greate r tha n 1.0

. th e followin g parameter s ar e require dt o b e continuousl y monitored : Th e temperatur e an dspecifi c gravit y o f th e absorbin g liqui dwher e a n absorbe r i s th e fina l produc t recovery device ; th e exi t temperatur e o

f th e ven t strea m wher e acondense r i s th e fina

l produc t recover y device ; an dth e carbo n be d temperatur e an dregeneratio n strea m flow wher e acarbo n adsorbe r i s th e final produc t

recover y device

. L. Reporting

and Recordkeeping Requirements A s require dunde r

th e Genera l Provision s o

f 40 CF Rpar t 60

. th e recommende dstandard s requir e thre e type s o f reports

. First , ther e ar

e notificatio n requirement s unde r th e Genera l Provisions , whic h woul denabl e th e Agenc y t o kee p abreas t o f facilitie s subjec t t o th e standard s o

f performance

. Second , ther e i s th e reportin g o f performanc e tes t

results , whic h woul d sho w tha t afacilit y i s meetin g th e standard s initially

. Third , ther e i s th e semiannua l reportin g o

f exceedance s o

f certai n monitore dparameter s an dan y chang e i n equipmen t

o r proces s operatio n tha t

coul daffec t

complianc e with th e TR

E o r emissio n reductio n requirement s o r

with th e lo w flo

w an d lo w capacit y exemptions

. Th e propose d standard s woul drequir e record s indicatin g prope r

operatio n an d maintenanc e o

f th e contro l devic e o

r produc t recovery equipment

. First , specifi c operatin g parameter s woul db e monitore dan dth e result s recorded

. Second , record s o

f period s whe n th e measure dvalue s of

thes e parameter s significantl y deviate dfromth e value s measure di n th e mos t

recen t performanc e tes t

woul db e maintained

. Third , ther e woul db e recordkeepin g o f major change s tha t

coul daffect

th e TR E inde x valu e o r

th e lo w flew an dlo w capacit y exemptio n status

. Finally , record s an dreportin g o

f period s whe n contro l devic e ar e no t

operatin g o

r whe n th e ven t strea mi s no t

route dt o th e contro l devic e woul db e required

. III

. Impact s o

f th e NSP S A. Air In th e fift h year afte r thi s NSPS i s proposed , i t

i s estimate dtha t nationwid e emission s o

f VO C wil l b e decrease db y 2,10

0 megagram s per

year compare dwith projecte demission s calculate dt o occu r

i n th e absenc e o

f th e standard s (baseline)

. Durin g th e firs t 5 year s o f th e standards ' apphcability , e n estimate d5 8 facilitie s woul db e candidate s fo

r th e contro l attributabl e solely to th e requirement s o f thi s NSPS

. I t i s estimate dtha t

7 o f th e 5 6 facilitie s ar e anticipate dto b e require dt o meet th e 9 8 weight-percen t

reductio n requirements

. However , th e VO C emission s fro

mth e 7 facilitie s accoun t fo r abou t 9 0 percen t

o f th e tota l fro

mal l 5 6 facilities

. Any increas e i n emission s o f othe r ai r pollutant s a s aresul t

o f controllin g VO C emission s wil l b e negligible

. B. Water A Negligibl e increas e in tota l plant wastewate r

i s projecte dunde r

thi s NSPS

. C. Solid Waste. Noise

and Radiation N o soli dwaste , noise , o r

radiatio n impact s ar e expecte dunde r thi s NSPS

. D. Energy I n th e fift h year afte r thi s NSPS wov.! d becom e applicable , energ y consumptio n i n th e SOCM

I nationwid e woul db e increase db y a s much a s th e equivalen t o f abou t 14 1 barrel s o

f crud e oi l pe

r da y i f incinerator s an dflaxe s ar e use dt o comply wit

h th e propose dstandard s whe n compare dwit

h th e existin g energv consumptio n associate dwit h th e baselin e level

. E. Control

Costs During'th e fift

h year o f applicability o

f th e propose dstandards , th e nationwid e annualize dcost s o

f contro l a t facilitie s covere dby th e standard s woul damour , t t o $3. 7 millio n (198 2 dollars ) per year
. Th e nationwid e cumulativ e 5-yea r capita l cost s fo

r contro l unde r

th e propose dstandard s woul db e $5. 9 millio n (198 2 dollars)

. Thes e cost s ar e base do n th e assumptio n tha t flare s o r incinerator s woul db e use dto comply with th e propose dstandards

. I f les s expensiv e contro l device s suc h a s boiler s an dproces s heater s ar e used , th e cost s woul db e significantl y lower

. F. Economic

Effects N o chemica l tha t

i s projecte dbot

h to hav e new , modified , o

r reconstructe d facilitie s buil t

in th e firs t

6 year s o f th e standard s an dt o b e require dt o contro l emission s beyon dcurren t Stat e requirement s i s projecte dt o hav e apric e increas e greate r

than 5 percent

. Furthermore , chemical s tha t ar e produce ddownstrea mo

f di e liste d chemical s wil l no t

hav e pric e increase s over 5 percer.i

. Mos t

o f th e projecte d pric e increase s fo

r th e liste dchemical s an dchemical s produce ddownstrea m ar e small : 8 1 percen t

ar e under

2 percent

. Lr.pact s o

n industry structure , industry growth , inflation , foreign trade , an dcapita l formatio n ar e projecte dto b e insignificant

. IV

. Rational e fo

r th e Propose d Standard s A. Selection

of Scarce Category Th e EP A priorit y list , 4 0 CF R60.1 8 (4 4 F R49222 , Augus t

21,1979) , rank s major sourc e categorie s fo

r whic h NSP S ar e t o b e promulgated

. Thi s lis t

implement sP 5 

# T

Fsdem l asgistiB F /

Vo L 55 , No

. 12 8 /

Friday

. Jun e 29 , 1SS 0 / Propose dRule s
sectio n 111(b ) o

f th e Clea n Air

Ac t an d reflect s th e Administrator' s determinatio n tha t

emission s fromth e liste dsourc e categorie s contribut e significantl y t o ai r

pollutio n tha t endanger s health o r

welfare

. Th e SOCM I wa s ranke dhighes t

priority fo

r NSPS developmen t

o n th e final priority lis t o f 5 9 major sourc e categories

. Organi c chemica l plant s ar e amajor sourc e o f VO C emission s tha t

contribut e t o ozon e formation

. Th e VOC s ar e emitte dfro mfou r mai n subcategorie s o

f source s withi n th e SOCMI : Losse s fro

mstorag e an d handlin g o

f volatil e organi c liquids , fugitiv e leak s from valves an dproces s equipment , evaporativ e losse s from liqui dan dsoli dwaste s (secondar y sources) , an demission s fromproces s vents

. A breakdow n b y sourc e typ e indicate s tha t

ove r hal f o f th e VO C emitte dfro

mth e SOCM

I ar e from proces s vents

. Proces s ven t

emissio n source s ar e typicall y associate dwith produc t recovery system s i n aSOCM I chemical manufacturin g facility

. Proces s ven t emissio n source s consis t

primaril y o

f th e ventin g o f VOC-containin g inert

gase s an devacuatio n o

f equipmen t

fo r vacuu mprocessing

. Fo r

purpose s o

f developin g an NSP S fo

r th e SOCMI , EP A ha s divide dproces s vent s int o tw o categories : Continuou s an dbatch processes
. Batc h proces s vent s ar e currentl y bein g evaluate db y th e Agency

. Continuou s proces s vent s includ e distillatio n uni t

operations , ai r oxidatio n processes , an dreacto r process
. Standard s fo

r distillatio n uni t operation s wer e propose do n Decembe r 30.198 3 (4 8 F

R57538)

. Standard s fo

r ai r oxidatio n processe s wer e propose do n Octobe r 21,198 3 (4 8 F

R48932)

. Th e standard s bein g propose dtoda y addres s th e thir dtyp e o

f proces s vents : Reacto r processes
. A reacto r

proces s i s th e mean s b y whic h on e o

r more substance s o r reactants

. otiie r

tha n air

. ar e chemicall y altere dsuc h tha t on e o r more ne w organi c chemical s ar e formed

. Th e VOC s ar e emitte dfromreacto r proces s vent s in on e o

f tw o ways : (1 ) Indirectl y fro mth e reacto r

followin g produc t recovery (e.g. , tiirough condensation, absorption , o r

adsorption) , o r

(2 ) directl y fro mth e reacto r

t o di e atmosphere

. A

n estimate d8 percen t

o f th e tota l VO C emitte db y th e SOCM

I sourc e category ar e fro mreacto r processes
. I n developin g standards , environmental , cost , economics , smal l business, an dothe r

impact s ar e examined

. It

woul db e very resourc e intensiv e an dtim e consumin g t o analyz e al l o f thes e impact s fo

r eac h o f the man y chemical s produced

. Th e resul t o f followin g suc h a mapproac h woul db s t o dela y developin g standard s significantly , (resulting i n hi mi n a significant los s i n emissio n reduction

. Therefore , EP

A ha s decide dt o limi t

th e scop e o f thes e standard s initiall y t o a relativel y smal l numbe r

o f hig h productio n chemicals

. Th e Agenc y performe da n analysi s to determin e th e probabl e effect s o f

ouch alimitation

. Tw o alternative s wer e considere dfo r limitin g th e scop e to nig h productio n volume syntheti c organi c chemicals

. Th e first involve dlimitin g th e scop e o f th e standard s t o abou t

87 0 organi c chemical s produce di n quantitie s greate r tha n 4,50 0 Mg/y r (1 0 millio n Ib/yr)

. Thi s woul dcove r

roughly 9 7 percen t

o f organi c chemical productio n bu t woul d resul t i n a n unworkabl e numbe r of chemical s fo

r th e impac t

analyses

. Th e secon dalternativ e woul dlimi t th e scop e o f th e standard s t o 17 3 organi c chemical s generall y produce di n quantitie s greate r

tha n 45,00

0 Mg/y r (10 0 millio n lb/yr)

. Th e chemical s covere d unde r thi s secon dalternativ e woul d accoun t fo r abou t £ 0 percen t of tota l U.S

. productio n of

organi c chemicals

. Therefore , th e Administrato r conclude d tha t limitin g th e scop e of

th e standard s t o di e 17 3 chemical s generall y produce d i n quantitie s greate r

tha n 45,00

0 Mg/y r woul dprovid e aworkabl e scop e whil e coverin g th e grea t

majority of

organi c chemica l production

. A lis t o f th e affecte dchemical s i s include di n th e regulation

. B. Pollutant

to be Regulated In additio n t o VO C emissions , othe r pollutant s ar e emitte dfromreacto r proces s source s i n muc h smalle r quantities

. Thes e includ e carbo n monoxid e (CO)

. Nitroge n oxide s (NO J sulfu r oxide s (SO J an dhydrochlori c aci d(HCI)

. Th e VO C i s b y fa r th e primary pollutan t

emitte dfromreacto r processes
. Du e t o th e siz e an d complexity o

f thi s sourc e category , acquirin g th e informatio n t o determin e th e applicabl e technolog y fo r th e othe r pollutant s tha t

hav e lo w emission s a t th e sam e time th e Agenc y analyze s th e pollutan t covere db y thes e standard s woul dhav e bee n a n unmanageabl e task

. Therefore , th e pollutan t

t o b e regulate d by thes e standard s i

o VOC

. C

. Selection of

Regulatory Approach Tw o genera l regulatory approache s wer e considere dfo

r us e i n developin g standard s fo

r reacto r processes
. Th e first approac h woul dinvolv e establishin g standard s fo

r eac h of th e 17 3 specifi c chemical s include dunde r thes e propose dstandards

. S t woul db e very difficult

t o develo p standard s usin g thi s approac h du e t o th e larg e numbe r of chemica l reaction s an dchemica l product s tha t

ar e produce db y reacto r processe s an dth e variabl e emissio n characteristic s associate dwit h each

. Ther e ar e abou t

3 9 separat e type s o

f chemical reaction s usee * t o produc e th e 17 3 chemical s tha t

accoun t fo r th e grea t majorit y o f th e emission s fro

mreacto r processes
. Th e secon dapproac h involve s th e developmen t

of standard s o n th e basi s o f simila r type s of emissio n source s an d applicabl e emissio n contro l techniques

. Thi s approac h woul dallo w atimel y an d resource-efficien t

regulatory developmen t

becaus e alarg e number

o f specifi c chemical s ca n b e covere dby onl y on e regulation

. Usin g thi s approac h woul dmea n tha t

a n NSP S fo

r th e SOCMI reacto r

processe s coul db e develope din arelativel y shor t perio do f time a t muc h les s publi c cost , compare d t o th e chemical-by-chemical approach

. Despit e th e larg e numbe r

o f reaction type s an dchemical s produce db y reacto r processes , VO C emission s fro m reacto r proces s unit s ca n b e controlle d b y commonl y use dcombustio n an d noncombustio n contro l techniques

. Becaus e regulatin g th e entir e grou p woul db e more resource-efficien t an d th e chemical-by-chemical approac h i s fo r practica l purpose s infeasibl e an d lack s an y clear

advantage , th e Administrato r

ha s determine dtha t

a singl e regulatio n shoul db e propose dfo r al l reacto r processe s i n th e SOCMI

. Thi s approac h i s consisten t

wit h th e approac h take n fo

r th e SOCM

I distillatio n an dai r

oxidatio n standards

. D. Selection of

Affected Facility Th e choic e of

th e affecte dfacilit

y fo r thes e standard s i s base do n th e Agency' o interpretatio n of sectio n 11 1 o

f th e Clean Air

Ac t an do n th e judicia l constructio n o

f it s meanin g [ASARCO. Inc., v. EPA. 57 8 F.2 d31 9 (D.C

. Cir

. 1978))

. Unde r

Sectio n ill

. th e standard s o f performanc e fo

r ne w stationar y source s mus t

appl y t o "ne w sources. " "Source " i s define da s "an y building , structure , facility , o r

installatio n whic h emit s o r ma y emi t an y ai r pollutant " (sectio n 111(a)(3))

. Mos t

industria l plants , however , consist , of numerou s piece s o r group s o f equipmen t

tha t emit ai r pollutant s an dtha t

ma y b e viewe d a s "sources. " Th e EPA

. therefore , use s - th e term"affecte dfacility " t o designat e th e equipmen t

withi n o particula r

kin d o f plan t tha t i s chose n a s di e "source " covere db y agive n standard

. I n designatin g th e affecte dfacility , EP A mus t decid e whic h piec e o r

grou p o f equipmen t

i s th e appropriat e uni t

(th e source ) fo r emissio n otandard o in th e particula r industria l context

. Th eP. 6

Federa l Registe r

/ Vol

. 55 , No

. 12 8 /

Friday , Jun e 29 , 199 0 / Propose dRule s Agenc y mus t

d o thi s b y examinin g th e situatio n i n ligh t

of th e term s an d purpos e o f sectio n 11 1 o

f th e Clean Air Act

. Th e mai n purpos e o

f sectio n 11 1 i s t o minimiz e emission s b y requirin g th e applicatio n o

f BD T a t al l new , modified , an dreconstructe dsource s (considerin g cos t nonai r quality healt h an d environmenta l effects , an denerg y impacts)

. Th e EP

A believe s tha t

in mos t case s anarro w affecte dfacilit y designatio n wil l bes t

further thi s purpose , becaus e i n mos t

case s a narro w designatio n ensure s tha t ne w emissio n unit s wil l b e brough t unde r th e coverag e o

f th e standards

. If

, fo r example , a n entir e plan t

i s designate d a s th e affecte dfacility , n o par t o f an existin g plan t

woul db e covere db y di e standar dunles s th e replacemen t cause d th e plan t a s awhol e t o b e "modified " o r "reconstructed. " I

f eac h piec e o

f equipmen t

i s designate da s aseparat e affecte dfacility , the n a s eac h piec e i s replaced , di e replacemen t piec e woul d b e ane w sourc e subjec t

t o th e standards

. For

thi s reason , EP

A generall y presume s tha t

th e narro w designatio n i s appropriate

. Th e EP A treat s th e narro w designatio n onl y a s apresumption , however , becaus e i n som e case s a broade r affecte dfacilit

y designatio n ma y b e more consisten t

with th e ptirose s o f sectio n 111

. Fo r

example , th e Agenc y migh

t choos e abroade r designatio n i

f i t conclude dtha t

eithe r (a ) i t woul dresul t

i n greate r

emission s reductio n tha n woul danarro w designation ; o r

(b ) th e otiie r

relevan t statutor y factor s (technica l feasibility , economi c cost , energy , an dnonai r quality healt h an denvironmenta l impacts ) poin t

t o abroade r

designation

. Th e EP A analyze dsevera l alternativ e affecte dfacilit

y designation s fo

r th e reacto r proces s standards , includin g (1 ) eac h individua l reacto r

witi i it s recovery system ; (2 ) tiie group o

f reactor s whos e ven t stream s flo w togedie r

throug h a singl e recovery system : an d(3 ) th e entir e plant

. Usin g th e presumptio n mentione dabove , EP

A examine da s a singl e affecte dfacilit

y eac h individua l reacto r whos e ven t

strea mi s sen t

t o it s ow n recovery system

. Th e EP A concluded , however , tha t

whe n reacto r ven t stream s ar e joine dan dsen t throug h asingl e recovery system , th e group o f reactor s an dthei r

recovery system , rathe r

tha n eac h reactor , shoul d b e asingl e affecte dfacility

. Th e EP A estimate s tha t

agreate r reductio n i n nationa l VO C emission s woul dlikel y resul t

unde r th e broade r designatio n of

affecte dfacility

. Thi s conclusio n io base dupo n th e behavio r o f th e industry with regar dt o th e expansio n o f reacto r capacit y an d replacemen t

reconstructio n o r modificatio n of

existin g reactors. Capacity expansion s wil l occu r eithe r a s aresul t of ne w facilitie s bein g buil t

o r existin g one s bein g expanded

. Whe n expandin g productio n capacit y e t a n existin g reacto r

facility , i t

i s commo n industry practic e t o ad dne w reactor s t o existin g set s o

f reactors an drecovery systems

. Whe n thi s occurs , ther e ar e tw o possibl e outcome s unde r th e broade r affecte dfacilit

y designation— both o f whic h wil l result

i n agreate r emission s reductio n tha n woul doccu r unde r amore narro w designatio n o f affecte dfacility

. On e possibility i s tha t th e tota l emission s fro

mdi e grou p o

f reactor s wil l increase

. I n thi s case , i t woul dbrin g al l (ne w plus existing ) reactor s dischargin g int o acommo n recovery syste munde r

th e standar db y virtu e o f th e NSP S Genera l Provision s regardin g "modifications. " Th e secon d possibility i s tha t

th e owner s o r operator s of

th e plan t coul dcompletel y offse t th e increase demission s fro mth e ne w reactors b y increasin g recovery. Althoug h thi s outcom e i s unlikely , th e resul t i s tha t agreate r emission s reductio n wil l occu r

unde r th e broa d rathe r tha n th e narro w designatio n of affecte dfacility

. Th e reason i s tha t b y completel y offsettin g th e increase d emission s fromth e ne w reactor s throug h additiona l recovery , th e emission s from th e ne w reactor s hav e bee n controlle d a t 10 0 weight-percen t

effectiveness

. Thi s exceed s th e contro l effectivenes s (i.e.

. 9 8 weight-percent ) requiredunde r tiiis standard

. Replacemen t

o f existin g reactor s rarel y occur s withi n th e industr y becaus e reactors ar e expensiv e piece s o f equipmen t

designe dan dusuall y buil t t o las t th e lifetime of

th e plant

. Reacto r replacement s usuall y occu r a s aresul t

o f proces s change s (e.g. , fro

mchlorinatio n t o hydrochlorination ) o r

a s aresul t

of fire s o r explosions

. Whethe r

i n multireacto r

o r singl e reactor

facilities , th e replacement s o

f individua l reactors (a s oppose dto replacement o f entir e facilities ) ar e rare
. Whe n reactor replacement s d o occur , however , al l reactor s ten dt o b e replaced , and , therefore , th e reacto r

replacement s woul dbrin g th e entir e facilit y unde r th e standard s unde r

th e broade r

affecte d facilit y designation

. Reacto r change s tha t

sourc e owner s ' coul dmake tha t

migh t b e considere d modification s ar e substantia l change s i n catalysts , reactor

conditions , o r

produc t separatio n purificatio n equipment

. Th e cos t o f thes e change s i s s o great , however , tha t

mos t owner s woul d choos e t o buil dane w group o f reactors rathe r

tha n radicall y modif

y individua l existin g reactors. Therefore , fe w reactor s woul dunderg o proces s change s tha t migh t b e considere damodificatio n unde r an y designatio n of

affecte d facility

. Thus , greate r

emission s reduction s ar e likel y t o occur

unde r thi s broade r designation

. Fo r

tha t reason , th e Administrato r

ha s determine dtha t

th e appropriat e affecte dfacilit y designatio n i s a n individua l reacto r

wit h it s ow n individua l recovery syste m(i f any ) o r th e combinatio n o

f tw o o r mor e reactor s an dth e commo n recovery syste mthe y share

. Whe n severa l reactor s feedven t stream s int o acommo n recovery system , th e characteristic s o

f th e emission s vente dint o th e atmospher e fro mth e recovery syste mar e determine db y bot h th e ven t stream s fro

meac h o f th e reactor s an dth e efficienc y o f th e recovery system

. Unde r

th e narro w designation , i t

woul dhav e bee n require d tha t onl y tha t portio n o f th e combine d ven t strea mcontribute db y an y new , modifie do r

reconstructe dreacto r

unit comply wit

h th e standard s whe n th e uni t share s arecovery syste mwith existin g units

. Therefore , th e TR E inde x valu e woul dhav e bee n determine dfo r th e portio n o

f th e strea mcontribute db y tha t uni t only

. A t leas t thre e samplin g locations woul db e use din thi s case
. Two o f th e location s (i.e. , before an d after th e commo n recovery system ) woul db e use dt o determin e th e overal l efficienc y o

f th e commo n recovery system

. Thi s efficienc y woul dthe n b e applie dt o th e emission s measuremen t take n a t th e thir dsampl e locatio n whic h i s jus t prio r t o th e ne w o r

change duni t bein g joine dwit

h an y othe r

vent stream

. Thus , thre e sampl e locations woul db e neede dt o determin e th e contributio n b y di e ne w o r

change duni t

t o th e tota l emission s fromth e commo n recovery system

. However , unde r

th e broade r

affecte d facilit y optio n selecte dabove , onl y on e samplin g sit e i s necessar y to determin e th e facility' s TR

E inde x value

. No estimatio n o

f th e recovery system' s efficienc y o n individua l reactor s i s required , becaus e th e standard s cove r th e entir e ven t

stream

. Therefore , ther e i s n o nee dt o determin e whic h portio n o f th e fina l ven t strea mfro

magroup o

f reactor s i s attributabl e t o new , modified , an dreconstructe dreactor s an dwhic h portio n i s attributabl e t o reactor s tha t hav e no t bee n change do r

added

. Thi s result s i n performanc e testin g tha t i s simple r an dcheape r

becaus e fewer samplin g site s an dsimple r analyse s ar e needed

.P. 7



### 2695 8 Federa

l Register /

Vol

. 55 , No

. 12 6 /

Friday , June 29 , 1990 /

Propose dRule s

Th e Administrato r

ha s decide dt o exclud e fro mthes e standard s reactor s tha t ar e operate di n abatc h mod e rathe r tha n operate dcontinuously

. Th e dat a upo n whic h th e standard s ar e base d (includin g th e cos t

an dcontro l devic e perfonnance ) assum e acontinuou s o r nea r continuou s typ e o f

operation

. Als o exclude dfro mthes e standard s ar e facilitie s i n plant s witi i ver y lo w capacitie s o r

wit h ver y lo w ven t

strea m Hows

. Mos t

researc h an ddevelopmen t o r laborator y scal e facilitie s ar e no t designe dt o produc e mor e tha n on e gigagra m(Gg ) pe r

year
. I t i s no t th e inten t o f th e standard s t o cove r suc h facilitie s becaus e the y ar e generall y intermitten t

operations

. Moreover , th e contro l technique s tha t

ar e applicabl e t o industry-scal e productio n facilitie s woul dno t

necessaril y b e appropriat e fo r thes e operations

. Fo r

tiiese reasons , EP A ha s decide dt o exemp t

facilitie s whic h ar e par t o f proces s unit s wit h on e G g productio n capacit y pe r yea r o r les s o f ai l chemical s produce dwitiii n di e proces s unit

. Similarly , facilitie s wit h ven t strea mflow s belo w 0.01 1 standar d cubi c meter s pe r

minut e (scm/min ) ar e exclude dfro mth e standards

. N o facilit y wit h flow s belo w thi s cutof f ar e anticipate dt o hav e TR E inde x valu e les s tha n 1.0 , an dthu s t o includ e die m unde r th e standard s woul dimpos e unnecessar y reportin g an d recordkeepin g requirement s o n thes e facilities

. Fo r

th e lo w flo w facilities , onl y a n initia l measuremen t an drepor t i arequire dt o verif

y entitlemen t

l o ike exclusion

. In addition , owner s an d operator s o f

bot h lo w capacit y an dlo w flo w facilitie s ar e require dt o notif y EP A i f achang e occur s tha t

woul dresul t

i n productio n capacitie s o r Cow s abov e th e respectiv e cutof

f levels

. E. Selection of

Control Techniques Th e Clea n Ai r

Ac t require s tha t standard s o f

perfonnanc e b e base do n t;: 3 bes t syste mo f

continuou s emissio n reduction , considerin g costs , energ y usag e an dnonai r

healt h an d environmenta l impact s ("bes t demonstrate dtechnology " o r BDT)

. A s discusse di n th e BID

. on e o r mor e combustio n technique s (boiler , proces s heater , incinerator , o r

flsri's ) ar e cpplicabi s t o art

y redcio r proces s ven t strea man dca n achiev e a ! leas t G o weight-percen t

contro l o r

20 pprn v i n th e outle t gss
. However , combustio n contro l device s ar e th e onl y type s o

f contro l device s whic h ar e applicabl e t o reacto r processes
. Th e EP A examine dsevera l VO C contro l technologie s tha t achiev e th e sam e o r

les s emissio n reduction

. suc h a s absorption , adsorption , condense r

devices , an dcatalyti c oxidation , bu t foun dtha t

tiiese contro l technologie s ar e no t

applicabl e t o al l reacto r proces s ven t

streams

. Moreover , EP A i s unable , wit h availabl e information , t o identif

y subcategorie s o f reacto r processe s fo r

whic h th e abov e mentione dcontro l technologie s hav e bee n demonstrate dt o alway s apply

. Th e applicabilit y an deffectivenes s o f thes e device s ma y b e greatl y affecte db y th e ven t strea mflo w rate , wate r content , temperature

. VO C concentration , an d VO C propertie s suc h a s solubility , molecula r

weight , an dliquid/vapo r equilibrium

. Thes e characteristic s var y widel y withi n di e SOCMI

. Therefore , ther e i s n o wa y t o evaluat e technologie s for applicatio n t o reacto r

proces s unit s fo r whic h tiiermal incineratio n an d flarin g hav e bee n determine dt o b e to o costly

. Eve n wit h greate r resources , thi s approac h woul db e infeasibl e becaus e i t woul drequir e astream-by-strea m characterization , ultimatel y resultin g i n th e nee dfo r

aseparat e standar dfo r eac h ven t

strea mfro maproces s use dt o produc e areacto r

chemical

. Combustio n device s wer e foun dt o b e applicabl e t o an y nonhalogenate dven t stream

. Fo r

incinerators , operatin g condition s ca n b e identifie dtiiat wil l ensur e 9 8 weight-percen t reductio n o r

2 0 ppm v tota l organic s (minu s methan e an d ethane ) i n di e outle t

gas , whicheve r

i s les s stringent

. Boiler s an dproces s heater s wer e foun dt o b e capabl e o f achievin g 9 8 weight-percen t reductio n i

f th e organic-lade n strea mi s use da s a fue l an di s pu t

int o di e flam e zone
. I n recen t tests , smokeles s steam-assisted , air-assiste dan dnonassiste dflare s wer e als o foun dt o b e a s efficien t a s thes e othe r combustio n device s i n achievin g 9 8 weight-percen t

reductio n o f

VO C i f the y wer e operate da s specifie di n 4 0 CFR60.18

. I n term s o f

cost , boiler s an d proces s heater s ar e generall y th e leas t expensiv e combustio n devices , becaus e thes e unit s ar e alread y i n plac e i n SOCM I plant s an dbecaus e o f hea t recover y fro mth e VOC-containin g ven t streams

. Flare s ca n contro l mos t nonhalogenate dVOC-containin g stream s fo r

les s cos t

tha n incinerators

. Incinerator s wer e foun dt o b e th e onl y device s applicabl e t o halogenate d stream s becaus e incinerator s ca n accep t awid e variet y o f

strea mtype s an dca n b e constructe dt o tolerat e th e corrosiv e effect s o f halogenate dstreams

. Furthermore , a n absorbe r ca n b e use dt o remov e halogen s fro mth e offgase s exitin g th e incinerator

. I n summary , 9 8 weight-percen t contro l o r reductio n t o 2 0 ppm v i s achievabl e for al l halogenate dan dnonhalogenate d reacto r proces s ven t

stream s usin g on e o f th e combustio n device s discusse d above

. Thus , thes e fou r combustio n device s ar e candidate s fo r BD T fo r th e emissio n sourc e categor y o f organi c chemica l reacto r

processes
. Sinc e ven t

strea mcharacteristic s withi n thi s categor y var y widely , i t i s t o b e expecte dtha t

di e cos t pe r uni t o f emissio n reductio n amon g stream s wil l als o vary
. Th e potentia l environmenta l impact s o f

usin g acombustio n devic e t o contro l VO C emission s var y fro mven t strea mt o ven t

stream

. Th e Administrator , therefore , ha s analyze d th e environmental , economic , an d energ y impact s an ddi e cos t pe r uni t o i emissio n reductio n fo r

reacto r processe s ven t stream s include di n th e scop e o f tiiese standard s t o determin e if

. du e t o advers e impact s associate dwit h th e us e o f di e mos t applicabl e combustio n devices , BD T fo r

certai n classes , types

. o r size s o f reacto r processe s migh t

b e n o additiona l control

. Th e followin g section s discus s thes e additiona l impacts

. Consideratio n o f

Environmenta l Impact s Th e potentia l advers e environmenta l impact s tha t

coul dresul t

fro mreacto r proces s standard s wer e assessed

. Th e generatio n o f

NO , b y th e combustio n proces s wa s examine da s apossibl e nativ e impac t

o n ambien t

ai r quality

. Th e principa l factor s affectin g th e rat e o f NO , formatio n durin g combustio n ar e th e amoun t

o f exces s ai r

available , th e pea k temperature , an ddi e rat e o f coolin g o f

di e combustio n products

. Relativel y lo w combustio n temperature s o f approximatel y 87 0 ° C (1,60 0 °F ) ar e associate dwit h contro l o f VO C usin g therma l incinerators , an dresidenc e time s ar e generall y to o shor t t o b e conduciv e t o NO , formation

. Therefore , th e rat e o f

NO , formatio n i s expecte dt o b e lo w if incinerator s ar e used

. Introductio n o f

areacto r

proces s ven t strea ma s asupplemen t t o th e fue l an d combustio n ai r

normall y introduce dint o aboile r o r proces s heate r

could , i n som e cases , resul t

i n increase s i n NO , emissions

. Th e combustio n temperature s i n thes e device s ar e wel l i n exces s o f 2.00 0 ' F an dar e therefor e conduciv e t o NO , formation , an dsum s reactc r proces s vent s bein g controlle dwoul d contai n nitrogenou s organi c compound s o r nitroge n fro mai r

i n th e ven t

stream

. However , reacto r

proces s ven t

slream s woul drepresen t

onl y asmal l par t

o f th e tota l inpu t

t o th e boile r

o r heat t r
. Also , i n man y case3

. ir.troducuo n c f th e reecto r proces s ven t

strea mwcul dresul t i n lowere dfue l requirement s an j coul d resul t i n lowe r NO , emission s if

th e nitroge n fro mnitrogenou s organi c compound s i s les s tha n th e fuel-boun d nitroge n o f

th e fue l bein g replace dInP. 8

Federa l Registe r /

Vol

. 55 , No

. 12 6 /

Friday , Jun e 29 , 199 0 / Propose dRule s 2695 9
addition , measure s t o minimiz e NO , formatio n coul db e implemente ddu e t o NO , standard s unde r

developmen t

fo r industria l boilers

. An

y Increas e o r decreas e i n NO , emission s du e t o introductio n o

f th e reacto r

proces s strea mwoul db e slight

. Onl y limite ddat aar e availabl e fo r NO , emission s fro

mflares

. I n arecen t stud y of steam-assiste dan dair-assiste d flares , th e highes t

estimate dNO , emission s wer e wel l belo w th e reported NO , emission s tabulate dfo r industria l boiler s an dproces s heater s firing ga s o r oil

. Becaus e NO , emission s fromflare s ar e les s tha n th e NO , emission s from boiler s an dproces s heater s (whic h ar e themselve s slight) , NO , emission s fro m flare s ar e considere dt o b e insignificant

. Therefore , an y increas e i n NO , emission s resultin g fromth e combustio n o f areacto r proces s ven t

strea mi s expecte dt o b e relativel y small

. I n addition s t o generatio n of NO, , th e contro l of VO C emission s fro

m halogenate dven t

stream s b y therma l incinerator s may result

i n th e release o

f halogenate dcombustio n product s t o th e environment

. However , Du e ga s quenchin g an dscrubbin g coul db e use d t o remov e thes e compound s fromth e incinerato r

outle t stream

. Stat e o r

loca l regulation s ma

y requir e us e o

f thes e scrubber s i

f di e halogenate dcombustio n product s ar e i n high enoug h concentrations

. Curren t

industry practic e amon g reacto r

proces s facilitie s wit h halogenate dven t

stream s tha t emplo y combustio n device s i s t o us e flue ga s scrubbin g to reduc e plan t maintenanc e cost s b y preventin g corrosio n o

f equipment

. Th e capita l cos t an doperatin g cost s associate dwit h flue ga s quenchin g an dscrubbin g wer e take n int o accoun t

i n projectin g th e cos t impact s fo

r th e standards

. Contro l o f VO C emission s usin g combustio n device s woul dno t resul t i n an y significant

increas e i n wastewate r discharg e b y reacto r

processes
. N o wate r effluent s ar e generate db y th e combustio n device s themselves

. Us e o f a n incinerator/scrubbe r

syste m fo r contro l o f VO C emission s fro

m halogenate dstream s woul dresul t i n increase dwate r

consumption

. Th e increas e i n tota l plan t

wastewate r woul db e relativel y smal l an dwoul dno t affec t plan t wast e treatmen t

capacit y o r sewe r capacity

. However , i

f th e scrubber effluent i s no t recovered , i t ma y b e necessar y t o adjus t

th e p H o f th e scrubbe r

effluent b y treatmen t

wit h causti c (NaOH ) befor e i t

i s releasedint o th e plan t wastewate r

system

. Th e sal t (NaCl ) forme db y th e causti c treatmen t mus t b e purge dfro

mth e syste man d properl y disposed

. Brin e solution s ar e currentl y dispose do

f i n avariet y o

f way s dependin g o n site-specifi c conditions

. Thes e includ e direc t discharg e t o sewe r

system s an dsurfac e water s (fres h an dsal t

wate r bodie s o r rivers), discharg e t o evaporativ e lagoons , an dinjectio n int o adisposa l well

. Becaus e i t

i s no t possibl e t o determin e whic h option s will b e selecte db y th e individua l facilitie s analyzed , i t

woul db e impractica l t o represen t al l of thes e type s of

brin e disposa l i n th e cos t

analysis

. Therefore , th e cost s mos t

likel y t o occu r

a t affecte d facilities , handlin g halogenate d compounds , wher e considere dinstead

. Th e Agenc y ha s investigate dbrin e disposa l cost s an dha s foun dtha t th e dee p wel l injectio n cos t

represents th e cos t associate dwith th e mos t expensiv e disposa l optio n available

. I n addition , availabl e dat aindicat e tha t thi s cos t i s appropriat e fo

r disposa l of

hazardou s waste s i n dee p wells , no t

nonhazardou s brin e solutions

. Furthermore , th e cos t associate dwith thi s optio n i s no t applicabl e t o th e majority o f facilitie s generatin g brine

. Fo r th e reacto r

processe s NSPS , th e cos t fo r brin e disposa l wa s considere d t o b e negligibl e an dno t

include di n th e TR E equatio n becaus e th e disposa l option s mos t

likel y t o b e use db y affecte dfacilitie s ar e of

arelativel y lo w cost

. Thes e includ e ocea n dumping ; direc t discharg e t o fres h water , brackis h water , an dsewe r

system s wer e permitted , an dinjectio n int o existin g oi l o r ga s well s tha t

ar e locate don-site

. Th e Agenc y see s n o reason wh y an y facilit y woul dhav e t o choos e th e mos t expensiv e optio n o

f dee p wel l injection ; therefore , thes e cost s wer e no t include d i n th e TR E equation

. Fo r eac h o f th e 17 3 chemical s unde r consideration , th e advers e environmenta l impact s o

f VO C contro l usin g combustio n device s woul dno t b e significant

Therefore , thes e impact s d o no t provid e abasi s fo

r exemptin g an y o

f th e chemical s fro

mth e propose d standard s o r

affectin g th e selectio n o

f BDT. Consideratio n o

f Economi c Impact s A n economi c analysi s wa s performe d t o determin e i

f th e pric e of

an y o f th e 17 3 chemical s o r

chemical s produce d fro mth e liste dchemical s woul db e adversel y affecte db y contro l a t th e 9 8 weight-percen t

reductio n level

. Assumption s tha t

ten dt o maximiz e projecte dpric e increase s wer e use di n th e analysis

. Some o f th e 17 3 chemical s ar e basi c chemical s produce ddirectl y fro mth e petroleum , whil e other s ar e intermediate s o r

end-us e chemical s produce dfro

mth e basi c chemicals

. Th e pric e increas e cause db y th e us e of a combustio n devic e fo r aparticula r chemica l wa s assume dt o b e reflected als o i n th e pric e of

al l chemical s produce dfro

mtha t chemical

. Th e projecte dpric e increas e wa s calculate d assumin g tha t

al l contro l cost s woul db e reflecte da s pric e increase , an dtha t non e woul db e absorbed

. Th e pric e increas e wa s calculate db y dividin g th e estimate dannualize dcontro l cost s b y th e annua l productio n o

f afacility

. Th e pric e increas e wa s the n rolle dint o th e pric e o f chemical s tha t

ar e produce d downstrea mo

f th e liste dchemicals

. N o chemica l tha t

i s projecte dboth to hav e new , modified , o r

reconstructe d facilitie s buil t

i n th e first

5 year s o f th e standard s an dt o b e require dto contro l emission s beyon dcurren t Stat e requirement s i s projecte dto hav e apric e increas e greate r

tha n 5 percent

. Furthermore , chemical s tha t ar e produce ddownstrea mo

f th e liste d chemical s wil l no t

hav e pric e increase s ove r 5 percen t

Mos t o f th e projecte d pric e increase s fo

r liste dan d downstrea mchemical s ar e small : 8 1 percen t ar e unde r

2 percen t whil e 9 0 percen t ar e unde r

3 percent ; an y actua l pric e increase s ar e expecte dto b e les s tha n thes e projections

. Impact s o n industry structure , industry growth , inflation , foreig n trade , an dcapita l formatio n ar e projecte dt o b e insignifican t Consideratio n o

f Cos t an dEnerg y Impact s After i t ha dbee n determine dtha t th e 9 8 weight-percen t

VO C emissio n reductio n coul db e achieve dfrom a variet y o f combustio n control s withou t significan t advers e environmenta l o r economi c impacts , th e Administrato r nex t examine dth e cos t

energy , an d cost s pe r uni t o f VO C reduce d(i.e. , cos t effectiveness ) o

f thes e control s o n th e projecte dnew , modified , o r reconstructe dreacto r

proces s units

. Base do n EPA' s previou s experienc e i n developin g a n NSP S fo

r SOCMI proces s vents , th e Agenc y anticipate dtha t th e cos t o f removin g VO C fro

mth e ven t stream s o f som e o f th e proces s unit s woul db e unreasonabl y hig h an d therefore , conducte dadditiona l analysis

. Th e analysi s requiredt o determin e costs , energ y requirements, an dcost s pe r uni t o f VO C reduce dinclude dth e followin g steps

. First , th e tota l numbe r o f new , modified , an dreconstructe d proces s unit s with ven t

stream s whic h woul db e affecte db y th e standar d durin g th e first

5 year s wa s estimated

. Thes e includ e al l proces s unit s with ven t stream s projecte dt o no t

us e combustio n i n th e absenc e o f a n NSPS

.P. 9

2696 0 Federa l Registe r / Vol

. 55 , No

. 12 6 /

Friday , Jun e 29 , 199 0 / Propose dRule s
Th e proces s unit s wit

h thes e uncontrolle dstream s ar e assume dt o b e thos e tha t woul dincur

th e cos t an d energ y impact s resultin g fromth e contro l requirement s o

f th e standards

. Th e cost s o

f controllin g th e emission s fro mthes e proces s unit s wer e the n develope dfo

r each

. Thes e proces s unit s wer e the n ranke daccordin g t o cost s o f contro l pe r

M g o f VO C reduced

. Fro m thi 3 ranking , ase t

o f regulatory alternative s consistin g o

f increasingl y larg e number s o

f controlle dproces s unit s wa s developed

. Th e remainde r o f thi s sectio n provide s adiscussio n o f th e approac h an dresult s o

f thi s regulator

y analysis ; I n orde r to projec t th e numbe r

o f proces s unit s tha t

woul db e affecte db y th e standard s durin g th e first 5 year s o f it s applicability , estimate s o f SOCM I growt h st dreplacemen t

capacit y wer e determi.v.i l fo

r eac h o f th e 17 3 chemicrls

. Thi s ste p identifie dal l ofth e chemical s whic h ma

y hav e new , modifie do

r reconstructe dproces s unit 3 built betwee n 1985 an d1990

. Th e nex t ste p wa s t o identif y whic h o f thes e chemical s woul dlikel y hav e unit s buil t wher e combustio n device s woul db e applie din th e absenc e o

f a n NSPS

. A tota l o f 2 2 chemical s wer e identifie da s where combustio n woul db e applie da s aresul t o f existin g regulation s o r industry practices. Any impact s associate dwit

h proces s unit s makin g thes e chemical s woul dno t b e attribute d t o th e NSPS and , therefore , thes e chemical s wer e eliminate dfro mtiie analysi s o f impacts

. Th e nex t

ste p wa s to estimat e th e number

an dsiz e o

f new , modified , an dreconstructe dproces s unit s producin g chemical s whic h woul d likely no t us e acombustio n devic e i n th e absenc e o f an NSPS

. A tota l o

f 5 6 suc h unit s wer e projecte dto com e on-lin e an dthes e wer e th e facilitie s include din th s analysi s o

f impacts

. T o determin e th e emissio n characteristic s o

f thes e 5 6 proces s units , a n extensiv e dat abas e o n existin g reacto r processe s wa s developed

. Thi s dat ab3s e o

r Emission s Dat aProfil e (EDP ) cover s 12

7 reacto r proces s unit s an di s discusse din detai l i n th e BID

. Th e emissio n characteristic s containe din th e EDP wer e use dt o represen t th e emissio n characteristic s o f th e 5 6 proces s units

. It

wa s assume dth e ED

P wa s representativ e o

f unit s makin g al l o

f th e chemical s associate dwit h th e 5 6 units

. Th e ED

P i s base dupo n reacto r proces s unit s rathe r

tha n affecte d facilities

. A proces s uni t

i s define di n di e BI D a s on e o r

more combination s o

f reactor(s ) an drecovery system(s ) locate dat acommo n sit e an dproducin g th e sam e chemical

. Therefore , i t shoul d b e note dtha t

thi s regulatory analysi s i s base dupo n an industry uni t which , in som e cases , ma

y includ e more tha n on e affecte dfacility

. Th e EP

A doe s no t believ e tii3t

thi s differenc e wil l affect th e validit y o

f th e conclusion s o

f thi s regulator y analysi s becaus e wher e a proces s uni t

contain s more than on e affecte dfacilit

y i t i s likel y tha t emission s fro

mbot h facilitie s wil l b e ducte dto acommo n contro l device

. Thi s i s th e situatio n represente din th e regulatory analysis

. A s previousl y stated , th e 5 6 proces s unit s projecte dt o come on-lin e betwee n 196 5 an d199 0 ar e estimate dt o hav e ven t stream s tha t

woul dno t

b e controlle din th e absenc e o f a n NSPS

. Th e VO C emission s fro

mthes e 5 6 proces s unit s ar e estimate dt o b e abou t 2,40 0 Mg/yr

. Tota l emission s fromth e 7 7 proces s unit s makin g th e 2 2 chemical s anticipate dto us e combustio n i n th e absenc e o f a n NSP S ar e estimate dt o b e 91 0 Mg/yr

. Therefore , th e baselin e emission s fo

r al l new , modified , an d reconstructe dreacto r

proces s unit s projecte dt o come on-lin e betwee n 198 5 an d1990 ar e estimate dto b e 3,31 0 Mg / y r (th e sumo

f 2,40 0 an d910)

. Baselin e represent s condition s tha t woul dexis t

i n th e absenc e o

f astandard

. Th e propose d standard s woul daffec t

th e 2,40 0 Mg/y r fromth e 5 6 proces s unit s with uncontrolle dven t

streams

. I n orde r t o ran k th e 5 6 proces s unit s an dt o conduc t

th e regulatory analysis , th e cos t fo r controllin g eac h o

f th e proces s unit s wa s determined

.

Estimatin g th e cos t

o f controllin g VO C emission s fromreacto r

proces s unit s consist s of

first designin g th e contro l syste man dthe n costin g th e system

. Th e genera l approac h use dconsist s o f determinin g th e desig n parameter s fo r a contro l syste mapplie dto aparticular reacto r proces s tha t

emit s VOC

. Th e syste mwa s coste dbasedupo n thes e desig n parameter s an dby usin g cos t equation s develope dfro

mdat asupplie d b y vendor s an dindustry

. I t wa s no t possibl e wit

h availabl e dat at

o identif y thos e reacto r

proces s ven t

stream s fo

r whic h th e us e o

f catalyti c incinerators

. proces s heaters , an dboiler s woul db e applicable

. Therefore , only tiiermal incinerator s an dflare s wer e use dto develo p thes e cos t

data

. Flare s o r incinerator s (whichever

wer e determine dto b e les s costly ) wer e applie dt o nonhalogenate dstreams

. Incinerator s ar e applie dt o ven t stream s containin g halogenate dVOC becaus e flar e ti p corrosio n ma

y prohibi t us e o f flare s an dbecaus e halogenate dstream s ma y creat e secondar y emission s tha t requir e flue ga s scrubbin g (whic h i s not possibl e fro

mflare demission)

. Becaus e thi s regulatory analysi s i s base dupo n th e assumptio n tha t

facilitie s wil l us e flare s an dincinerators , whe n i n fact , th e les s expensiv e boiler s an dproces s heater s (becaus e the y ar e alread y i n plac e an dthe y accru e hea t recovery credits ) wil l b e use di n som e plants , th e cos t impact s ar e overstated

. Onc e th e cos t

an demission s reduction s fo

r eac h o f th e 5 6 proces s unit s wer e estimated , th e cos t pe r M g o f VO C reductio n fo

r eac h proces s uni t wa s determined

. Then , eac h o f th e 5 8 unit s wa s ranke db y cos t

effectivenes s (i.e. , fromth e lowes t

to th e highes t

cos t pe r M g o f VOC)

. T o illustrat e ho w impact s chang e a s aresul t o f increasin g th e numbe r

o f unit s controlled , nin e regulatory alternative s wer e develope d' base do n discret e cost-effectivenes s cutoff s from acontinuu mo

f al l possibl e cost-effectivenes s values

. Thes e alternative s ar e presente din Tabl e 1

.
TABL E 1.—SUMMAR Y O F ENVIRONMENTAL , COST , AN D ENERG Y IMPACT S O F NIN E REGULATOR Y ALTERNATIVE S ' [Al l Costs are i n Third Quarte r 198 2 Dollars ]

Regulator y alternatives

(1 ) l « i l H I i v : . v v l Theoretica l * wors t casecost effectivanes s cutof

f valu e ($/Mg ) (2 )
1,20 0 2.50 0 5.50 0 20,00 0 50,00 0 Averag e cos t pe r M g o f VO C removed ($/Mg ) (3 )

50 0 1.70 0 1,80 0 2,10 0 2.90 0 Cost

s pe r M g o

f VO C remove d ($/Mg ) (4 )

250-76 0 2,00 0 5.40 0 5,600-14,00 0 21,000-43.00 0 Numbe r o f unit s controlle d
(5 ) 0 4 7 9 2 1 3 3 Emissio n reductio n fro m baselin e (Mg / y ) (6 ) 0 30 0 2.10 0 2.30 0 2.30 0 2.30 0 Percen t

"controllable " emission s reduced * (7 ) 0 1 3 9 0 9 1 9 7 10 0 Nationa l annualize d cost s (millio n $/yr ) (8 ) 0 0.1 5 3. 7 3. 9 4. 7 6. 7 Nationa l energy requirement s (TJ /
' iD' (9 ) 0 3 32 0 34 0 39 0 43 0P.1 0 

## V )

Federa l Registe r /

Vol . 55 , No . 12 6 /

Friday , June 29 , 199 0 / Propose d Rule s 2SSS 1

TABL E 1.—SUMMAR

Y O F ENVIRONMENTAL , COST , AN D ENERG Y IMPACT S O F NIN E REGULATOR Y ALTERNATIVE S "—Continued [Al l Costs or

e i n Thir d Quarte r 198 2 Dollars ]

Regulator y alternatives

( D VI I „ .... . VII I

_ I X Theoretico l * wors t casscost effectivenas s cutof

f valu o (S/Mg ) (2 ) 200,00 0 500,00 0 > 500.00 0 Averag e

cos t pe r M g o f VO C remove d ($/Mg ) (3 ) 3.20 0 3.50 0 4,00 0 Costs ps r Mgo f

VO C remove d ($/Mfl )
(4 ) 64.000-110.00 0 280.000-4S0.0O 0 > 4.000,00 0 Numbe r ot

unit s controlle d
(5 ) 4 2 4 a S3 Emissio n reductio n fro m baselin e (Mg / yr) (6 ) 2.30 0 2.3O 0 2.30 0 Percen t

"controllable " amiason o reduced ' (7 ) 10 0 10 0 10 0 Nationa l annualize d cost s (millio n S/yr ) (8 )
7. 4 8. 2 9. 3 Nationa l energyrequirement! ) (TJ / yr) d (9 ) 44 0 45 0 52 0

" Calculate d fo r th e firt h yea r o t th e NSPS

. * Thi s b a theoretica l cos

t effectiveness

. As oxplained elsewher e i n thi s document , at

) tr e unit s wit h calculate d costs ps r M g srhic h approac h th e indicate d valu e ar e expecte d t

o mak o proces s adjustment

s an d thu s no

t experience contro l costs o o hig h o o indicate d b

y thi s theoretica l wors

t case . ' Controllabl e emission s or e th o 2,40 0 Mg/y r tha

t woul d be controlled i

f al l 5 6 unit

s ner s controlle d a

t 98-aeight-percen t VO C destructio n efficienc y (i.e.

. o t th e mos t stringent possibl e alternative , Alternativ e IX)

. 0 Expressed i n Terajoutes pa r year . ° Baseline , o r condition s tha t woul d exis

t i n th e absenc e o

f th a standards

. Colum n 1 i n Tabl e 1 identifie s eac

h o f th e nine alternatives
. Regulator y Alternative I represent

s baselin e o

r th e condition s whic

h woul d exis ti

n di e absenc e o f a standard . A tthe other extrem e i s Alternative IX , which woul d contro l all 5 6 units
. Th

e numbe r o f unit s controlle d abov e baselin e fo r each alternative i s presente d i

n Colum n 5
. Th e ranges o f cost s pe r M g o f VO C removed withi n each alternativ e ar e presente d in Colum

n 4
. Thes e ranges represen tth e additiona

l cost effectivenes s value s achieve d a t successivel y highe

r alternatives
. Colum

n 3 present s th e average cost s pe

r M g o f VO C remove d fo r each alternative
. Thus , fo r example , Regulator

y Alternative II

I could theoretically contro l 7 o f tiie 5 6 proces s unit

s wit h a n average cos to

f Sl.700/M g o

f VO C controlled (i

n 198 2 dollars)
. Colum n 6 in Tabl e 1 presents a

n estimat e o f th e VOC emission s reduction ove r baselin e fro m di e 5 6 units
. A tbaselin e 2,40

0 Mg/y r o f VO C woul d b e emitted by th e 56 units
. Under Alternative II

. 4 unit s woul d b e controlle d resulting i n a reduction o f 30 0 Mg/yr
. However , unde

r Alternativ e III

, a total o f 7 unit s ar e Uieoretically controlled resulting in a

n emissio n reduction o

f 2.10 0 Mg/yr
. I f al l 56 unit

s were controlle d a

t9 8 weight-percent (Alternative IX) , ther

e woul d b e a reduction o

f 2,30 0 Mg/y r o f VO C being emitte d fro

m th e 5 6 units
. Thi s alternative i s th

e mos tstringen t possible
. Thes e 2.30

0 Mg/y r o f VO C emission s ar

e th e maximu m availabl e fo r control . Colum

n 7 present

s th e percentage o

f th e "controllable " emission s tha

teach regulator

y alternativ e woul d control "Controllable " emission s ar

e 98 percento

f tota l emission s fro

m the 56 unit

s (9 8 percen t o f 2.40 0 Mg/yr)
. I ti s eviden tfro

m Column

s 6 and 7 tha tmos to f the emission s reduction occur s a s a resulto

f controlling only a smal l fraction o

f the 5 6 proces s units
. Fo r example . Alternativ e II

I woul d contro l only 7 o f the 5 6 proces s units
. Fo r example . Alternativ e II

I woul d control only 7 o

f th e 56 proces s unit

s bu t woul d accountfo

r abou t80 percento

f the controllabl e emissions
. Colum n 8 presents the nationa

l annualize d cost s requirement s fo r eac h alternative
. Thes e cos timpact s rang e fro m $0.1 5 millio n (198

2 dollars ) fo

r Alternativ e I

I t o $9.3 millio n fo

r Alternativ e IX

. Capita l cost s accumulated ove r the 5-yea r perio d (no

t show n i n the table ) rang

e fro m $270,00 0 fo r Alternativ e I

I t o $17.3 millio n fo

r Alternativ e IX

. Thes e cos tan

d cost effectivenes s dat

a reflec tdi e cost s o

f controlling thes e unit

s a t98 weight
percentVO C reduction throug h th e us e o f incinerator

s an d flares
. The actua

l cost s and cos teffectivenes s shoul d b e considerabl y les s tha

n thos e indicate d i n Tabl e 1 fo

r tw o reasons . First

, plant owner s and operator

s ma y b e abl e t

o us e boilers , proces s heater s o r catalyti c oxidizer s rathe

r tha n th e mor e expensiv e flares and incinerators t o compl y wit h the 98 weight-percent reductio n requirement

. Secondly , a s wil l b e discusse d late r in thi s preamble , plan towner s and operators ma y b e abl e t o increas e the efficiency o f produc t recover y sufficiently t

o compl y wit h thi s standar d an d thereb y woul d nothav e t o appl y 98 weight-percent-efficient reduction controls . To the exten ttha t thi s alternativ e mean s o

f compliance i s used ; cost s a s wel l a s emissio n reduction wil l b e lowe r tha n thos e indicate d i n Tabl e 1
. Colum n 9 presents the energ

y impact s o f di e variou s alternatives
. Electricit y i s frequentl y require d t o operat e th e pumps , fans , blower s and instrumentation tha

tma y b e necessary t o control VO C using a

n incinerato r or flare. Th e amoun to f supplementa

l fue l neede d t

o increas e the heating valu e o f ventstreams depend s o

n ven tstrea m temperature, ne

theatin g valu e o

f ven t stream s depend s o n ventstrea m temperature , ne

theating value , flo

w rate , combustio n temperature , an d typ e o f heatrecover

y used . Du

e t o th e us e o f heatrecover

y techniques , combustion o f som e reacto r proces s ven

tstreams woul d resulti n a ne

tproduction o

f energ y even tthoug

h supplementa

l fue l woul d b e necessary fo

r flam e stability
. Tota l electricit y need s ar

e relativel y small compare

d t o energ y requirement

s i n the for m o f supplementa

l fue l fo r combustion
. Th

e fift h year nationa

l energ y us e woul d rang

e fro m abou t3 terajoule s pe

r yea r (TJ/yr

) (45 3 barrels o f oil/yr ) fo r Alternative I

I t o 51 7 TJ/yr (85,00 0 barrel s o

f oil/yr ) fo r Alternative IX . A s wit h th e cos tdata , thes e impact

s ma y b e overstate d becaus e some facilit y operators wil l choos e t

o compl y wit h th e standard s throug

h the alternativ e device s and mechanism s previously discussed
. F. Selection

of Best Demonstrated Technology A s explaine d previously , th e contro l o f reacto r proces s unit

s woul d notresult in unreasonabl e nonair environmenta l impact s o r caus e an

y o f di e chemical s t

o experienc e a significan

tadvers e economi c impact

. Therefore , th

e Administrato r analyze d th e cos tpe r megara m o f emissio n reduction an

d energ y impact s befor e determinin

g whic h regulator

y alternativ e should b e selected . Thi s analysi s assure s tha tth e cos to f unit s being controlle d i s reasonable , no

tonly in term

s o f economi c impacts , bu

tals o i n term s o f the emissio n reduction s tha twoul d result. I n thi s analysis , th

e cos tdat a i n Tabl e 1 wer e firs

tconsidered
. The energ y impact s show n i n Tabl e 1 indicate dia

tmer e woul d b e no unreasonabl e advers e energ y impacts
.P.1 1

2696 3 Federa l Registe r / Vol

. 55 , No

. 12 6 /

Friday , Jun e 29 , 199 0 / Propose dRule s

eve n i f al l unit s wer e controlle db y combustio n devices

. I n selectin g cutoff

s relate dt o applicability o

f NSPS , EP A look s a t a variety o f factor s including : (1 ) Th e technica l feasibilit

y o f additiona l control ; (2 ) di e economi c feasibilit

y associate dwit

h differen t contro l alternatives ; (3 ) th e magnitud e o f emissio n reduction s associate dwit h a contro l alternativ e (e. g , aslightl y higher cutof f coul db e selecte di

f i t le dto a substantia l increas e in th e emissio n reductio n achieve db y th e NSPS) ; (4 ) di e cos t effectivenes s (C/E ) o

f di e contro l alternativ e i

n term s o f annua l cos t

pe r megagra m($/Mg ) o

f emission s reduced ; (? ) th e qualit

y o f th e cos t estimate s (e.g. , wors t cas e versus realisti c estimates) ; (6 ) potentia l reduction s i

n othe r ai r pollutant s no t

specificall y regulate db y th e NSPS resultin g fro

macontro l Biieina':-

. e ; an d(7) th e locatio n o f ihe source s (e.g. , urba n versu s rural)

. Becaus e thes e factor s vary fro m industr y to industry and , in sem e cases , withi n th e sam e industry , decision s o n th e appropriat e leve l o

f contro l ar e mad e o n acategory-by-categor

y basis

. Afte r evaluatin g th e abov e factors , di e Administrato r

conclude dtha t

Ui e cos t o f requirin g contro l o

f any reacto r

proces s uni t belo w di e $2,500/M g cutof f (198 2 dollars ) i s reasonabl e an dfounddia t di e followin g consideration s wer e ke y t o electin g di e cutoff

: (1 ) Th e cos t effectivenes s o

f NSPS fo r VO C emission s previousl y promulgate dby EPA ; (2 ) th e probability dia t

thes e maximumcost s wil l no t

actuall y b e incurre dby industry : an d(3 ) di e presenc e o

f potentiall y toxi c compound s i n SOCM I reacto r proces s ven t

stream s an dtb e fact

tha t man y o f th e facilitie s ere locate di

n urban areas
. I n th e past , th e estimate dcos t pe r megagra mo f VO C remove dha s sometime s range da s hig

h a s $2,800/M g (138 2 dollars ) fo

r affecte dfacilitie s covere dby othe r

NSPS

. (Se e Docke t Ite mNo

. II-B-64)

. Th e Agency' s experienc e i n implementin g thes e standard s reveal s tha t

NSP S requirin g thi s leve l o

f contro l hav e prove dauseful too l i n bringin g abou t

th e installatio n o

f much emission s contro l technology , significant reduction s in emissions , an d correspondin g improvement s in ai r quality , ye t

hav e no t impose dcost s tha t appea r "grossl y disproportionate " t o di e emissio n reductio n achieved

. Portland 11. 51 3 F.2

da t 508

. Suc h a n approac h simpl y make s thi s NSP S consisten t (a s to dollar s spen t

pe r metri c to n o

f VO C removed ) wit

h th e existin g bod y o

f NSP S regulations , al l o

f whic h hav e eithe r bee n promulgate dwithou t legal challeng e o r

hav e bee n judiciall y upheld

. A s indicate din colum n 2 o f tabl e 1 , th e cost-effectivenes s cutof f o f $2,500/M g use din di e standar d correspond s to Regulator

y Alternativ e III

. Thi s alternativ e i s estimate dto resul t in anationa l annualize dcos t o f $3. 7 millio n (198 2 dollars ) b y controllin g seve n proces s unit s wit

h aVO C emission s reductio n o

f 2,10 0 Mg/yr

. Th e rang e o f cos t effectivenes s woul dvary fro m$250/M g t o $2,000/M g wit h a$1,70 0 averag e cos t

pe r megagra mo f VO C reduced

. Becaus e o f th e conservativ e assumption s use dto develo p di e regulator y analysi s an dbecaus e o

f th e flexibilit y inheren t

in di e mean s b y whic h industry can comply wit h th e standards , i t

i s ver y unlikel y tha t

an y facilit y woul dactuall y hav e to incu r a cos t o f $2,500/M g (di e cost-effectivenes s cutoff)

. Dat ao n curren t

capita ! cost s o

f therma l incinerator s indicat e that unit s ar e no w availabl e at

substantiall y reduce dcost s compare dto tiiose use din developin g thes e propose dstandards

. Lowe r capita l cost s woul dresul t i n lowe r annualize dcost s Uia

n previou s estimates , thoug h di e chang e i n annualize dcost s wil l no t

b e a s significant a s di e chang e i n capita l costs

. Thi s i s a n importan t facto r t o conside r in selectin g di e appropriat e regulatory alternativs

. Anothe r consideratio n i s th e fac t

dia t natura l ga s price s use dt o calculat e th e cos t effectivenes s fo

r eac h strea mar e overstate db y abou t

40 percent

. Thes e conservativ e assumption s hav e resulte d in higher cos t an dcost-effectivenes s estimate s tha n woul dactuall y occur
. In addition , a s discusse dearlier , di e regulatory analysi s assume s (fo r costin g purposes ) dia t

flares an dincinerator s woul db e use dt

o comply wit

h th e standards

. I

n fact , i t ma y b e feasibl e fo

r thes e facilitie s t o us e boiler s o r proces s heaters

. I f the y ar e abl e to us e thes e devices , di e cost s o

f complianc e woul d b e significantl y reduced

. Cost s woul d als o b e reduce dfo

r reactor s dia t

shar e contro l system s wit

h othe r proces s vents

. Finally , di e propose dstandar d woul dencourag e pollutio n preventio n b y no t requirin g 9 8 weight-percen t reductio n i

f aTR E inde x greate r

tha n 1.0 i s maintained

. A s detaile din th e sectio n entitle d"TR

E Index, " di e cost s show n in tabl e 1 d o no t

tak e int o accoun t

di e ability o f facilitie s t o compl y with Ui e standard s throug h change s i n di e equipmen t

o r operatio n o

f di e proces s facility , in certai n cases , thereb y avoidin g additiona l contro l devic e costs

. Availabl e dat aindicat e dia t reacto r proces s facilitie s witi i aTR E inde x jus t belo w di e 1.

0 cutof f (equivalen t

t o $2,500/Mg ) woul dprobabl y op t t o comply witi i th e standard s b y makin g a

proces s chang e suc h a s addin g recover y equipmen t

t o reduc e VO C emission s an drais e tiieir

TR E inde x abov e 1.

0 ratiie r tha n b y combustin g th e ven t stream

. Th e objectiv e o

f makin g a proces s chang e i s t o reduc e VO C emission s widiou t

disposin g o

f th e VO C to th e poin t

at whic h th e cos t effectivenes s associate dwit h combustio n i s over

th e cutoff

. Fo r example , reacto r

proces s far.ihip s wit

h TR E value s a s lo w a s 3 0 percen t belo w th e cutof f coul dpotentiall y appl y produc t recovery device s t

o comply wit

h th e standards

. Due to thi s ability , n o reacto r proces s facilit

y i s likely t

o incu r th e maximu mcost-effectivenes s va'u e o f $2,500/Mg

. Th e highes t

valu e tint a facilit y woul dactuall y incur

by usin g a combustio n devic e i s estimate dl o b e approximatel y $1,700/Mg

. A thii dconsideratio n i

n th e selectio n o f tiiis regulatory alternativ e i s that SOCM I reacto r proces s ven t

stream s contai n awid e variety o

f suspecte do

r confirme dtoxi c compound s (e.g , benzene , acrylonitrile

. butadiene , ethylen e dichloride

. ethylen e oxide , carbo n tetrachloride , an dchloroform)

. A documen t listin g di e know n toxi c effect s fo r th e chemical s covere db y tiiis standar dha s bee n place din Docket A

83-2 9 (ItemII-I-168)

. Dat aon th e emission s source s o

f mor e tha n 8 0 potentiall y toxi c ai r

pollutant s indicat e tha t di e SOCM

I emission s accoun t

fo r a disproportionat e shar e o

f potentiall y toxi c constituent s compare dt o othe r VO C source s (se e Docket Entr y II-A

39)

. I n addition , a s state din di e EPA' s Ai r Toxic s Strateg y publishe di n Jul y 1985 , di e Agenc y wil l conside r th e likel y toxi c pollutan t

contro l benefit s i

n di e cours e o f carryin g out

it s responsibilitie s unde r sectio n 111

. Thi s strateg y reduce s emission s o

f potentiall y toxi c compound s fro

mne w source s an dfro

m industrie s a s tiieir

facilitie s ar e reconstructe dan dmodified

. Thi s approac h i s to wor

k in tande mwit

h EPA' s effort s to contro l existin g an d ne w source s o

f specifi c toxi c compound s unde r

sectio n 11 2 o

f th e CAA

. I n settin g a n NSPS unde r

sectio n 11 1 o f th e CAA , th e Agenc y evaluate s al l relevan t

factor s (includin g costs , contro l technologies , environmenta l en d energ y impacts , an dsecondary impact s o r benefits)

. Contro l o

f potentiall y toxi c compound s b y thi s NSP S i s asecondar y benefi t that wa s considere dby th o Administrato r

in determinin g di e reasonablenes s o

f di e cos t o f different regulatory alternatives

. Therefore , althoug h EP

A ha s no t yet decide d whethe r t o lis t many o f thes e compound s unde r

sectio n 11 2 o

f th ee g / Vo l 55 , No

. 12 6 /

Friday , ]un e 29 , 199 0 / Propose dRule s
CAA , th e Agenc y believe s tha t i t ma y properl y conside r

tiieir potentia l toxicity alon g with otiie r

relevan t factor s whe n choosin g th e cutoff

. Many SOCMI facilitie s ar e locate di n urba n area s and , a s aresult , man y peopl e wil l b e expose d t o an y hazardou s ai r

pollutant s emitte d fro mthes e facilities

. Consideratio n o

f al l o f di e abov e factor s confirme dEPA' s belie f dia t a TR E valu e o f 1.0 (i.e. , $2,5C0/Mg) represent s a n appropriat e cutof f fo r determinin g whic h facilitie s mus t reduc e VO C emission s b y 9 8 weight-percen t o r t o 2 0 ppmv
. Th e cutof

f i s specifi c t o di e SOCM I reacto r processe s sourc e categor y an dwoul dno t

necessaril y b e appropriat e fo

r otiier sourc e categories ; therefore , i t

shoul dno t

b e viewe da s a benchmar k fo r othe r standards

. It

i s no t surprising , however , tiiat

di e cost

effectivenes s cutof

f fo r reactor s o

f S2.500/M g (198 2 dollars ) i s equivalen t t o th e $1,9C0/M

g (197 8 dollars ) cutof

f fo r di e SOCM

I ai r oxidatio n processe s an d distillatio n operation s standard s considerin g tha t

th e industry , th e pollutant s emitted , an dtii e emissio n control s ar e th e same
. Th e onl y difference s amon g th e source s ar e th e processe s tha t

ar e th e source s o

f VO C emissions

. C Selection of

Format for the Standards Severa l format s coul db e use dt o implement

th e propose dstandards

. Sectio n 11 1 o

f th e Clea n Air

Ac t require s tha t numerica l standard s o

f performanc e b e prescribe dunless , i n th e judgment o f th e Administrator , i t

i s no t feasibl e t o prescrib e o

r enforc e suc h standards

. I

n thi s case , sectio n 111(h

) allow s di e Administrato r

t o prescrib e design , equipment , wor

k practic e o r operationa l standards , o r

combination s thereof

. Unde r tha t Sectio n th e term "no t feasible " i s applicabl e i

f th e emission s canno t

b e capture dan d vente dthroug h aven t

o r stac k designe d fo r tha t purpose , o r

i f th e applicatio n o

f ameasuremen t

methodolog y i s no t practicabl e becaus e o

f technologica l o r economi c limitations

. Becaus e emission s fro mreacto r vent s an demission s fro

m incinerators , proces s heaters , an d boiler s ca n b e measured , a n emissio n limitatio n (performance ) standar dfo r thes e combustio n device s woul d generall y b e appropriate

. Becaus e o f th e variet y in proces s ven t flow rate s an dVO C content s fo r many chemica l reaction processe s an d facilitie s i n di e reacto r

sourc e category , mas s emissio n rate s fro

msource s usin g 9 8 weight-percen t

efficien t contro l device s woul dvary considerably

. Consequently , amas s emissio n limi t base don an averag e sourc e woul d requir e tha t

more tha n 9 8 weight-percen t contro l b e selecte da s BD T a t some facilitie s an dles s a t

others

. Therefore , a mas s emissio n standar dwa s considere d inappropriate , becaus e i t

woul dno t requir e di e BD

T a t eac h source
. Reacto r proces s ven t

stream s hav e a s muc h variatio n i n volume percen t organic s concentratio n ao i n mas s emissio n rates

. Any standard s base dsolel y o n a concentratio n limi t

woul dals o requir e more tiian BD

T a t som e facilitie s an d les s tha n BD

T a t others

. Therefore , standard s base dsolel y upo n concentratio n wer e considere d inappropriate

. However , a s discusse d below , aconcentration s limi t migh t b e use di n combinatio n with anothe r typ e o f emissio n limi t

i f di e applicability o

f di e concentratio n limi t

wer e restricte d to facilitie s withi n alimite drang e o f proces s ven t

ga s VO C content

. A weight-percen t

reductio n standar d woul db e feasibl e fo

r incinerators , boilers , an dproces s heater s becaus e th e contro l devic e inle t

an doutle t

emissio n rate s ca n b e measured

. A weight

percen t reductio n standar dwoul dresul t in di e applicatio n o

f BD T a t al l sources
. Furtiiermore , agive n se t

o f incinerator , boiler , o r proces s heate r

operatin g condition s tend s t o resul t

i n agive n weight-percen t

reduction , rathe r

tiian in a n absolut e outle t

organic s concentratio n o r

emissio n rate

. A s discusse dabov e i n di e sectio n entitle d Selection of

Best Demonstrated Technology, al l ne w incinerator s ca n achiev e a t leas t a9 8 weight-percen t reductio n i n tota l organic s (minu s methan e an dethane) , provide dtha t di e tota l organi c (minu s median e an d ethane ) concentrato n o

f di e proces s ven t strea mi s greate r

tha n approximatel y 2.00 0 ppm v (correspondin g t o 1,00

0 ppmv VO C i n di e incinerato r inle t strea mbecaus e ai r

dilutio n i s typicall y 1:1)

. Therefore , aweight-percen t reductio n standard , base do n di e mas s rat e o f organic s exitin g th e contro l devic e versu s di e mas s rat e o f organic s enterin g di e device , woul db e approxriat e fo

r ven t stream s with tota l organic s (minu s median e an detiiane ) concentration s abov e approcimatel y 2,00 0 ppmv
. Fo r

ven t stream s with organic s concentration s belo w approximatel y 2,00

0 ppmv , i t ha s bee n determine ddia t

a n incinerato r

outle t concentratio n o

f 2 0 ppmv i s achievabl e b y al l ne w incinerators

. Therefore

. EP A conclude dtha t

th e forma

t o f di e propose dstandard s fo

r reacto r proces s vent s usin g a n incinerator , boiler , o r proces s heate r

shoul dinclud e a combinatio n o

f aweight-percen t reductio n standar dan davolume concentratio n standard

. Th e propose d emissio n limit s woul db e a9 8 weight

percen t reductio n i n tota l organi c compound s (minu s methan e an dethane ) o r reductio n t o 2

0 ppm v tota l organi c compound s (minu s methan e an d ethane) , whicheve r

woul db e les s stringent

. Th e concentratio n limi t o f 2 0 ppm v woul db e base do n a3 percen t ven t strea moxyge n concentratio n in th e outle t stream

. Boiler s an dproces s heater s can achiev e a9 8 weight-percen t reduction , provide dtha t

th e wast e strea mi s introduce dint o th e flam

e zon e wher e temperature s ar e highest

. Unlik e incinerators , i n whic h furnac e temperature s ar e fairly constant , furnac e temperature s i n heat-generatin g unit s ar e highest

. Ulik

e incinerators , i

n whic h furnac e temperature s ar e fairl y constant , furnac e temperature s i n heat-generatin g unit s ar e hightes t

i n th e flam

e zone , an d atemperatur e gradien t

i s experience d betwee n di e flame zon e an dth e walls

. Th e combustio n kinetic s ar e much mor e rapi di n tiie flame zone , du e to th e higher temperature s (2.8O0°

F t o 3,000'F)

. Thi s result s i n very smal l residenc e time requirement s (much les s tha n furanc e residenc e times ) t o achiev e 9 8 weight

percen t reductio n o r

greate r tha n i s require di n a n incinerator

. Whe n burne d a s afue l i n th e flame zone , th e organi c compound s t o b e destroye dar e expose d t o thes e highe r

temperatures

. A s aresul t o f di e more rapi dcombustio n kinetic s a t thes e temperatures , hig h destructio n efficiencie s comparabl e t o thos e achieve db y incinerator s ar e attainable

. I n test s o f di e combustio n o

f organi c compound s burne da s fuel s i n boiler s an dproces s heaters , greate r tha n 9 8 weight-percen t

destructio n efficiencie s wer e demonstrated

. Therefore , areacto r proces s ven t

stream , whe n combuste din aboile r o r heater , mus t

b e introduce d int o th e flame zon e t o ensur e tha t i t reache s sufficient

combustio n temperature s fo

r destructio n o

f th e VOC

. I f th e wast e strea mi s no t introduce dint o th e flam

e zone , measurin g 9 8 weight-percen t efficienc y acros s th e contro l devic e ha s n o valu e (i.e. , doe s no t

assur e th e strea mi s bein g reduce db y 9 8 weight-percent ) sinc e reacto r proces s ven t

stream s compris e generall y asmal l portio n o f th e tota l combustibl e strea mto th e hea t generatin g unit

. It

i s infeasibl e t

o "measure " whethe r

th e wast e strea mi s introduce dint o th e flam

e zone
. Therefore , wher e aboile r o r proces s heate r i s use da s th e contro l device , i t i s appropriat e unde r

sectio n 111(h

) o f th e CA A to hav e acombinatio n forma t o f performanc e standar dan doperationa l requirement

. Th e propose demissio n limi t therefor e woul drequir e any owne r o r operato r usin g aboile r

o r proces s

### 2696 4 Federa l Registe r / Vol

. 55 , No

. 12 8 /

Friday , Jun e 29 , 199 0 / Propose dRule s
heate r t o introduc e th e reacto r

proces s ven t strea mint o di e flam

e zon e o f th e combustio n device

. Unlik e boilers , heater s an d incinerator s in whic h combustio n take s plac e i n an enclose dchamber , flarin g i s an ope n combustio n process
. It i s very difficult , therefore , to measur e di e emission s fro

maflar e to determin e it s efficiency

. I

t ma y b e technologicall y possibl e to measur e tiiese emissions , bu t th e cost s involve ddu e t o th e necessit y o f hoodin g th e flare an dotiier equipmen t need s woul db e economicall y impracticable

. Th e Administrator , therefore , ha s determine dtha t i t i s no t feasibl e to measur e di e emission s fro ma flare

. Consequently , a n equipmen t standar dwit

h state dspecification s i s bein g propose da s di e forma t fo r di e us e o f flares

. A s describe di

n di e BiD , tes t

dat a sho w that flares meetin g certai n condition s achiev e a9 8 weight-percen t emissio n reduction

. Th e propose d standard s requir e th e us e o f aflare dia t meet s tii e requirement s o

f 4 0 CF R60.1 8 to comply witi i th e standards

. Thi s mear. 3 dia t

only flare s that

ar e steam assisted , ai r

assisted , o

r nonassiste d ma y b e used

. Furthermore , di e ne t heatin g valu e o

f th e flaredga s mus t

no t b e les s than 11.2MJ/scm(30 0 Btu/scf ) fo r steam-assiste dan dair-assiste d flares o r less s tiia n 7.4 5 Mf/sc m(20

0 Btu/scf ) fo r anonassiste dflare

. I

n addition , di e exi t

velocit y o f di e flare ga s at th e flare ti p mus t

no t excee d18. 3 m/se c (6 0 ft/ssc) fu

r steam-assiste dan d nonassiste dflares , excep t fo r di e following conditions

. I

f th e ne t heatin g valu e o f th e ga s bein g combuste di s greate r tha n 37. 3 MJ/sc m(1,00

0 Etu/scf) , th e exis t velocit y o f th e flare ga s a t

di e flar e ti p mus t ro t excee d12

2 m/se c (40

0 ft/sec ) fo r steam-assiste dan d nonassiste dflares

. Whe n th e ne t heatin g valu e i s les s dian 37. 3 M;/sc mbu t greate r than 11. 2 MJ/scm

. th e maximu m exi t velocit y fo r nonassiste dan dsteam

assiste dflare s i s afunctio n o f di e heatin g value

. Air-assiste dflares mus t als o operat e belo w amaximu mexi t velocity , whic h i s dependen t upo n di e r.d t heatin g valu e cf

th e flaredstream

. Ther e aro th e only condition s fo r whic h EP A ha s dat asupportin g di e findin g tiiat flare s achiev e 90 weight-percen t emissio n redjeuon

. Anothe r consideratio n in developin g th e equipmen t

standar dfo

r stream s usin g flare s i s th e potential fo r proces s variation s suc h a s flow surge s tha t ca n caus e aflare to smok

e fo r shor t period s o f tim e unti l di e flar

e can b e adjusted

. Fiv e minute s i s areasonabl e perio do f time fo r alleviatin g di e smokin g condition s by makin g th e neede d adjustmen t t o th e stea mo r

ai r t o th e flare. Th e provision s i n 4

0 CF R60.1 8 limi t visibl e emission s t o n o more tha n 5 minute s withi n an y 2-hou

r period

. Som e reactor s proces s facilitie s recycl e al l vapor s t o di e manufacturin g proces s and , therefore , d o no t emi t VOC

. For others , di e produc t

recovery device s remov e virtuall y al l o f di e ven t stream

. Analysi s b y EP

A indicate s that , eve n witi i larg e ven t

strea mVO C emissio n rate s an dhea t

contents , n o ven t strea mwiti i flow rat e belo w 0.01 1 scm/mi n (0.3 0 scfm

) woul db e require d to implement

combustio n controls

. Thes e facilitie s woul dhav e a n unreasonabl y high contro l cos t pe r megagra mo f VO C destroye d(greate r tha n $2,500/Mg)

. Fo r

thi s reason , th e propose dstandard s exclud e facilitie s wit h flow rate s les s tiian 0.01 1 scm/mi n fro mdi e provision s o

f di e standard s excep t fo r an initia l measuremen t

an d reportin g requirement

. H. TRE Index Afte r selectin g th e cost-effectivenes s cutof f abov e whic h additiona l contro l o f VO C i s no t

required , i t

wa s necessar y t o develo p ametho dfo

r us e i n th e regulatio n tiiat

woul ddistinguis h thos e reacto r proces s unit s belo w th e cutof f (whic h woul db e require dt o mee t th e 9 8 weight-percen t

reductio n requirements ) fro mtiiose proces s unit s fo

r whic h n o additiona l VO C reductio n woul db e required

. Th e EPA , therefore , ha s include dequation s i n di e regulatio n t o calculat e a n inde x t o determin e whetiie r furthe r contro l i s required

. Thi s inde x i s terme dTRE

. j\ n importan t featur e o f thi s inde x i s dia t

i t i s independen t

o f cos t change s ove r

tim e s o tha t

i t i s no t necessar y t o periodicall y revis e th e calculatio n t o reflec t

curren t yea r dollars

. Th e equation s includ e di e parameter s use di

n calculatin g cost s considere din selectin g th e cutoff

. Thes e parameter s ar e th e ven t

strea m characteristic s o

f flow rate , ne t

heatin g value , mas s flow o

f tota l organi c compounds , an dcorrosio n propertie s (presenc e o

f halogenate dcompounds)

. Ther e parameter s ca n b e measure d easil y an dobjectively

. Th e TR E valu e calculatio n allow s th e owne r o r operato r o f an effecte dfacilit

y t o determin e i

f tha t facilit y woul db e require dt o reduc e VO C emission s b y 9 8 weight-percen t o r to 2 0 ppmv
. Th e standardize d calculatio n allow s objectiv e enforcemen t

sinc e al l TR

E value s woul d b e calculate dbase don th e sam e parameter s an dcalculate dby iY.e sam e method

. Th e TR E inde x o f aproces s ven t strea mi s calculate daccordin g to on e o r bot h equation s give n in 9 60.704(e)(7)

. Th e TR E inde x cutof

f a s calculate db y di e equatio n i s 1.0

. Affecte dreacto r

proces s facilitie s wit

h aTR E inde x o f les s tiian o r

equa l t o 1.

0 woul db e require dto reduc e VO C emission s by 9 8 weight-percen t

o r t o 2 0 ppmv , whicheve r i s less , whil e affecte dfacilitie s wit h a TR E inde x abov e 1.

0 woul dno t

b e require dto comply wit

h emissio n reductio n requirements

. Th e se t o f coefficient s use di

n th e equation s tha

t appl y to aproces s ven t

strea mca

n b e obtaine dfro

mTable s 1 an d2 o

f th e regulation

. Thes e coefficient s wer e derive ddirectl y fro

mth e ccs t

an d emissio n reductio n equation s associ.tt-. i wit h contro l o

f VO C emission s fro

m reacto r proces s facilitie s by flares an d incinerators

. Th e standard s requir e tha t apla n I owne r o r operato r calculat e th e TR

E c f th e proces s ven t

strea mbasedo

n th e specifi c characteristic s o

f th e ven t stream

. I f th e ven t strea mcontain s halogenate dVOC , th e equatio n fo r determinin g th e TR

E valu e fo r incineratio n mus t

b e used , alon g wit

h th e appropriat e coefficient s (i n Tabl e " ) base dupo n ven t

strea mhea t

conten t an dflo w rate

. Fo

r ven t stream s containin g nonhalogenate dVOC

. th e plan t owne r o r operato r mus t calculat e TR E values , usin g bot

h th e incineratio n equatio n an dth e equatio n fo r flares (selectin g th e appropriat e se t o f coefficient s in Tabl e 1 o r

2 base dupon hea t conten t an dflow rate)

. Afte

r calculatin g bot

h di e incineratio n an d flarin g TR E values , di e plan t

owne r o r operato r mus t selec t di e lowes t

TR E valu e fo r purpose s o

f determinin g complianc e wit

h th e standards

. I

n mos t instance s incinerator s ar e mor e expensiv e tha n flares fo

r controllin g nonhalogenate dven t

streams ; bu t

i n som e instance s th e revers e i s true

. Fo r thi s reaso n th e regulatio n require s thai di e leas t expensiv e techniqu e b e u»ed fo r TR E inde x calculatio n purposes
. I f tiiis requiremen t

di dno t exist , i t i s possibl e tiiat aplan t

owne r o r operato r coul davoi ddi e emissio n reductio n requirement s b y no t

selectin g th e leas t cosil y contro l devic e i

n determinin g TRE

. Th e ven t strea mo f an affecte dfacilit

y i s considere d"halogenated " unde r th e propose dstandard s i

f i t i s determine d t

o contai n aconcentratio n o f halogenate d compound s o

f 2 0 ppm v (by compound ) o r greater

. Thi s lo w 2

0 ppm v halogenatio n cutof

f wa s chose n fo

r th e analysi s to avoi dcontro l cos t an dTR E underestimates

. Eve

n smal l amount s o

f halogenate dcompound s ma y b e corrosiv e an dcan necessitat e incinerato r

temperature s greate r

than 87 0 °C t o achiev e a9 8 weight-percen t control

. Therefore , i

t wa s judge d^7" ~

Federa l Registe r / Vol

. 55 , No

. 12 6 /

Friday , Jun e 29 , 199 0 / Propose dRule s 2SS3 5
essentia l t o se t

alo w cutoff

, s o tha t th e contro l cos t

an dTR E woul dno t

b e underestimate dfo

r an y facility

. Thi s doe s no t imply tha t

flares , boilers , an d proces s heater s ar e prohibite dfro mus e o n stream s containin g more tha n 2 0 ppm v halogenate dcompounds

. Th e BD T selecte dallow s flexibilit y in implementin g th e standards

. Fo r source s belo w th e TR

E inde x cutof

f wher e tiie cos t o f combustio n contro l i s considere d reasonable , BD

T i s th e us e o

f acontro l devic e capabl e o

f achievin g areductio n o f 9 8 weight-percent , o r

t o 2 0 ppm v tota l organic s (minu s methan e an detiiane ) whicheve r

i s les s stringent

. Contro l i s achievabl e throug h th e us e o f combustio n device s suc h a s incinerators , boilers , proces s heaters , an dflares. Incinerator s may b e th e onl y applicabl e combustio n devic e fo r us e on stream s containin g halogenate dVOC

. Abov e th e TR

E inde x cutoff

, BD T i s n o additiona l control

. Th e us e o f aTR E inde x cutof

f wil l als o permi t

di e us e o f recovery technique s o r

proces s modificatio n in a n effor t to rais e di e TR

E inde x to apoin t abov e th e 1. 0 cutoff

. Th e parameter s use dt o calculat e th e TR

E inde x ar e measure dat

th e outle t o f th e recovery system

. Additiona l recovery ca n b e use d t o chang e th e value s o

f di e parameter s (e.g. , decreas e di e emissio n rate ) an d subsequentl y increas e th e TR E inde x value

. Th e tota l cos t

to afacilit

y fo r improve drecovery to excee ddi e TR E cutof f may , in some cases , b e much lowe r tha n di e tota l cos t

o f aflare, boiler , o r incinerator

. I

t may , therefore , b e economicall y advantageou s fo r suc h afacilit y to choos e t o improv e it s recover y syste mo r

make som e otiie r chang e witiii n th e process
. Th e decisio n by th e owne r

o f afacilit y concernin g di e desig n an dresultin g VO C remova l efficienc y o

f achang e withi n th e proces s i s primaril y mad e prio r

t o di e construction , modification , o r reconstructio n o

f tha t facility

. A s a practica l matter , EP

A ha s n o ability t o asses s th e exten t

to whic h VO C remova l efficienc y i s influence db y economi c versu s regulator

y considerations

. A s such , th e source's motivatio n fo r establishin g aparticular

proces s desig n i s no t considere dwhe n tiie TR

E inde x valu e i s measured

. Conside r a n exampl e wher e di e owne r

o r operato r o f afacilit y choose s t o improv e di e facility' s recovery system

. For

thi s typ e o

f proces s change

. EP

A presume s tha t

th e recover y system s ar e integra l t o di e proces s an dtha t

therefore , BD

T i s bes t determine daccordin g t o di e characteristic s o

f th e strea mexistin g di e las t recovery device

. /

. Selection of Actual Standards In summary , unde r

di e propose d standards , source s fo

r whic h th e cost s o

f combustio n contro l ar e reasonabl e woul db e subjec t

t o th e followin g requirements : (1 ) A 9 8 weight-percen t reductio n o

f ui e tota l organi c compound s (minu s methan e an detiiane ) i n di e reacto r

ven t strea mo r

areductio n t o 2 0 ppm v tota l organi c compoun d (minu s median e an detiiane) , whicheve r i s les s stringent ; an di

f aboile r o r proces s heate r

i s use dt o comply wit

h th e standards , di e reacto r ven t strea m mus t b e introduce dint o th e flame zon e o f th e boile r o r proces s heater , o r

(2 ) whe n aflare i s use dt o comply wit h th e standards , asmokeles s flare i s require d an dmus t b e operate di n accordanc e with th e requirement s i n 4 0 CF R60.18

. A s previousl y discussed , facilitie s with lo w flow rat e (les s tha n o r equa l t o 0.01 1 scm/min ) an dfacilitie s wit h lo w capacitie s (les s tha n o r

equa l to on e Cg / year ) woul db e exemp t

fro mthes e standard s excep t

fo r certai n recordkeepin g an dreportin g requirements

. For source s wher e di e cost s o f contro l ar e no t reasonable , th e propose d standard s woul drequir e tiiat th e TR E inde x b e maintaine da t

avalu e o f 1. 0 o r above

. Thi s TR

E concep t i s explaine din Sectio n H

. /

. Compounds

Used in Determining Compliance Th e propose dstandard s ar e intende d t o reduc e emission s o

f VO C throug h th e applicatio n o

f BD T (considerin g cost s an dothe r impacts) ; an dth e emissio n limit s i n di e standard s ar e designe dt o reflec t di e performanc e o

f BDT

. Wher e a contro l devic e fo

r areacto r proces s i s BDT

. tha t contro l devic e (i.e. , combustion ) doe s no t

selectivel y contro l VO C (tha t

is , di e proportio n o

f th e organic s tha t

i s regarde da s photochemicall y reactive) , bu t rathe r thes e technologie s contro l al l organi c compounds

. Moreover , th e numerica l value s o f th e emissio n limit s (9 8 weight

percen t reductio n an d2

0 ppmv ) in di e cas e o f reacto r processes , wer e base d o n tota l organi c compound s dat atha t exclude dmedian e an dethane

. T o reflec t accuratel y di e performanc e o f thes e contro l device s an dt o mak e di e emissio n limit s consisten t witi i th e dat a an dtes t method s fro

mwhic h th e limit s wer e derived , EP

A ha s expresse ddi e standard s in term s o

f organi c compounds , minu s methan e an detiiane

. Fo r th e sam e reason , di e tes t procedur e in th e propose dstandard s prescribe s measuremen t

o f tota l organi c compounds , excludin g median e an d ethane

. I n short , EP

A i s relyin g o n contro l o f tota l organi c compounds , minu s median e an dethane , a s th e bes t surrogat e fo

r controllin g VO C whic h reac t to for mozon e in th e atmosphere

. K. Modification/Reconstruction Considerations Th e propose dstandard s woul dappl y t o al l affecte dfacilitie s whic h commence dconstruction , reconstruction , o r

modificatio n afte

r th e dat e o f proposa l o

f th e NSPS

. Modificatio n i s define di

n 4 0 CF R60.1 4 a s an y physica l o r

operationa l chang e t o a n existin g facilit

y whic h result s i

n a n increas e i n th e emissio n rat e to th e atmospher e o

f an y ai r pollutan t t o whic h astandar dapplies

. (Sectio n 60.14(e ) list s th e si x exemption s whic h woul dnot b e considere dmodification s eve n i f emission s increased. ) Reconstruction , a s define din 40 CF

R60.15

. occur s whe n component s o

f a n existin g facilit

y ar e replace dt o suc h an exten t that : (1 ) Th e fixe dcapita l cos t

o f th e ne w component s excee d5 0 percen t o f th e fixe dcapita l cos t

tha t woul db e require d to construc t

acomparabl e entirel y ne w facility , an d(2

) i t i s technologicall y an d economicall y feasibl e t o mee t th e applicabl e standards

. Potentia l modification s involvin g SOCM I reacto r processe s includ e proces s equipmen t

changes , change s in operatin g parameters , o

r both

. Tw o type s o f proces s change s that

ma y resul t in modificatio n are : (1 ) Feedstoc k (i.e. , basi c chemical ) o r

reactan t substitutio n in reactor s whic h wer e no t designe dto accommodat e th e ne w feedstoc k o r reactant

. an d(2

) proces s equipmen t changes

. Man y o f di e chemical s produce di n reactor s ca n b e manufacture dfro mtw o o r more feedstocks

. For

example , cyclohexanon e ca n b e produce dusin g eithe r pheno l ( areacto r

proces s reactant ) o r

cyclohexano l (a

n ai r oxidatio n reactant)

. I

f afeedstoc k chang e wer e mad e an dif

: (1 ) Emission s increased , an d(2

) a s require dunde r § 60.14(e) th e reacto r

wa s no t designe d t o accommodat e th e feedstoc k change , th e feedstoc k

chang e woul dresul t

in a modification

. I

n th e exampl e cite d above , al l di e reactor s coul dhav e to b e rebuilt , possibl y requirin g acapita l expenditur e i

n exces s o

f 5 0 percen t

o f th e capita l cos t

o f th e affecte dfacility

. I n thi s case , areconstructio n coul d result , regardles s o

f th e emissions

. Th e secon dtyp e o

f proces s chang e i s aproces s equipmen t

change

. A s discusse dearlier , thi s typ e o f chang e rarel y occur s withi n tile industry

. Example s includ e di e replacemen t o f a fixed-be dreacto r

witi i afluidized-bed reactor , di e expansio n in th e siz e o f aP.1 5

2696 6 Federa l Registe r / Vol

. 55 , No

. 12 6 /

Friday , Jun e 29 , 199 0 / Propose dRule s

reactor , o r di e replacemen t

o f a n absorbe r o r substitutio n o

f a condense r fo r a n absorbe r

in th e ga s treatmen t system

. I f an y o f tiiese proces s equipmen t

change s resul t

i n a n increas e in emissions , amodificatio n coul d result ; i f an y o f th e change s require s tiie expenditure s o

f more tiian hal f

o f th e replacemen t

cos t o f th e affecte dfacility , the n areconstructio n coul doccur
. L. Selection of

Monitoring Requirements and Test Methods Followin g i s adiscussio n o f di e monitorin g requirement s an dtes t method s selecte dfo

r demonstratin g complianc e wit

h bot h di e emissio n reductio n an dth e TR

E provision s o

f di e propose dstandards

. Percent Reduction/Concentration Limit Th e combine dga s chromatograph/ flame ionizatio n detectio n metho d(GC / FID ) (Referenc e Metho d18) i s th e bes t availabl e procedur e fo

r determinin g emission s fro

mreacto r proces s facilities

. I t ha s th e advantag e o

f bein g abl e t o measur e individual organi c compounds

. Detail s concernin g th e us e o f thi s methodology , includin g sampling , analysis , preparatio n o

f standards , calibratio n procedures , an dreportin g o f result s ar e discusse din Referenc e Metiio d18 , "Measuremen t o f Gaseou s Organi c Compoun dEmission s b y Ga s Chromatography, " whic h wa s promulgate dwit

h th e NSP S fo

r SOCM I equipmen t

leak s (4 8 F

R48328)

. Th e owne r

o r operato r o f afacilit y usin g a n incinerato r

to comply wit

h th e propose d9 3 weight-percent/2 0 ppm v emissio n limit

woul db e require dto determin e complianc e accordin g t o Referenc e Metiio d1 8 durin g an y performanc e test

. Referenc e Metho d1 o r I A woul db e required , a s appropriate , t o b e use dfo

r selectio n o

f th e samplin g site

. Th e contro l devic e inle t samplin g sit e fo r determinatio n o

f reductio n efficienc y woul db e require dt o b e prio r to th e inle t

o f an y contro l devic e an d after al l produc t

recovery devices

. Referenc e Method s 2 , 2A , 2C , o r 2 D woul db e required , a s appropriate , t o b e use dfo r determinatio n o

f di e volumetri c flow rate

. Referenc e Metho d3 woul db e require dto b e use dfo

r a n ai r dilutio n correction , base do

n 3 percen t

oxyge n i n th e emissio n sample

. I f an y proces s ven t

stream(s ) frc

m outsid e th e affecte dfacilit y wer e normall y route dthroug h di e produc t recovery syste mo

r directl y t o th e contro l devic e o

f th e affecte dfacility , th s propose dstandard s woul dpermi t suc h astrea mt o b e route dnormall y durin g an y performanc e tes t t o determin e complianc e witi i th e propose d reductio n requirement

. Th e Agenc y considere drequirin g suc h stream s t o b e reroute do r

turne doff

, i n orde r t o assur e tha t 9 8 weight-percen t

reductio n o r reductio n t o 2

0 ppmv woul db e achieve d fo r contro l o f di e reacto r

proces s strea m itself

. However , th e Agenc y determine d dia t i f aperformanc e tes t

conducte do n suc h afacilit

y whil e routin g it s ven t stream s fro

manonaffecte dfacilit

y showe dcomplianc e with di e propose d emissio n limit , tha t

limi t woul dals o b e achieve db y th e combustio n devic e whe n onl y di e reacto r

proces s ven t strea mi s route dthroug h i t provide d tha t th e combustio n devic e operatin g parameters , suc h a s temperatur e an d residenc e time, remaine dunchanged

. Therefore , th e Agenc y conclude dtha t requirin g th e nonaffecte dfacilit y proces s strea mt o b e reroute do r turne d of f durin g aperformanc e tes t woul db e unnecessary
. Th e Agenc y believe s tha t boiler s and

. proces s heater s witi i adesig n hea t inpu t capacit y o

f 4 4 M W (15 0 millio n Btu/hr ) o r greate r woul dachiev e areductio n efficienc y o

f 9 8 weight-percen t

o r reductio n t o 2

0 ppmv , s o lon g a s th e reacto r proces s strea mi s introduce d int o th e flame zone
. Therefore , tiie Agenc y believe s tha t

an initia l measuremen t

o f contro l efficienc y woul dno t b e necessar y fo

r boiler s o f thi s size

. A s explaine di n th e discussio n o f combustio n kinetic s give n in th e BID , afirebo x temperatur e o

f 1,10 0 °C an d1 secon dresidenc e time represen t di e condition s tiiat

might , i n th e wors t

case , b e necessar y t o achiev e 9 8 weight

percen t reduction , eve n i

f di e organic s wer e halogenated

. Boiler s (an dproces s heaters ) with adesig n hea t inpu t capacit y o

f 4 4 M W o r greate r ar e operate da t

temperature s an dresidenc e time s greate r

tha n 1,10 0 ° C an d1 second , respectively

. In som e cases , th e residenc e time i s les s tha n 1 second

. However , i n tiiese cases , th e firebo x temperatur e i s much greate r tiian 1,10 0 °C , an d9 8 weight-percen t reductio n woul dstil l b e achieved. ) Otiie r tha n an adequatel y high temperatur e an d residenc e time , th e tw o primary condition s necessar y fo

r hig h combustio n devic e contro l efficienc y ar e stabl e flow rat e an dadequat e mixin g c f gases
. I t i s th e economi c advantag e o f th e owner s o

f facilitie s usin g boiler s o r proces s heater s to desig n an doperat e the mwit h stabl e flow rate s t o avoi d upsets

. For

di e sam e reason , suc h device s woul db e designe dan doperate d wit h adequat e mixin g o

f gase s t o maximiz e th e exten t

o f di e combustio n efficiency , tiiereby maximizin g th e steamo r hea t generatio n rate

. Fo r thes e reasons , th e Administrato r ha s decide dtha t

usin g aboile r

o r heate r wit h adesig n hea t

inpu t capacit y o

f 4 4 M W o r greate r t o contro l VO C emission s fro

mreacto r proces s operation s i s a n acceptabl e mean s o f demonstratin g complianc e wit h th e propose dstandard s i

f di e ven t streami s introduce dint o di e flam

e zone
. Therefore , i n accordanc e wit h S 60.8(b)

. th e Administrato r

ha s waive ddi e requiremen t

fo r aperformanc e tes t

o n suc h devices

. A

n initia l report

i s require dwidii n 18 0 day s o f start-up

. describin g th e locatio n at

whic h th e ver. i strea mi s introduce dinto th e boile r o r proces s heater

. Th e referenc e method s applicabl e t o incinerator s describe d belo w appl y t o di e smaller (i.e. , les s than 4 4 MW ) boile r an dproces s heaters

. A s explaine dunde r

Selection of Format for the Standards, an operationa l standar dwa s selecte dfo r case s wher e aflare i s use dto meet th e standards

. Therefore , aperformanc e tes t measurin g percen t

reductio n i s no t require dfo

r stream s equippe dwit

h flares. However , th e standar drequire s dia t th e flare operat e in accordanc e wit h th e requirement s in 4

0 CF R60.18

. Flow rat e an dhea t

conten t o f th e flare d strea mar e t o b e determine din accordanc e wit

h th e procedure s prescribe di n $ 60.703

. Incinerator s use dt o comply wit h the propose demissio n limi t

nee dt o b e maintaine dan doperate dproperl y i f eitiie r a9 8 weight-percen t

reductio n o

r reductio n t o 2

0 ppm v i s to b e achieve d o n acontinuin g basis

. Monitorin g can generall y b e use dt o ensur e suc h prope r operatio n an dmaintenanc e ar e occurring

. Tw o metiiod s o f monitorin g t

o ensur e di e prope r

operatio n an d maintenanc e o

f di e contro l equipment use dto comply wit

h di e propose d emissio n limi t

wer e considered

. Thes e method s wer e continuou s emissio n monitorin g an dcontinuou s combustio n contro l devic e paramete r

measurement

. Example s o

f suc h parameter s ar e combustio n temperatur e an dvent strea mflow. Continuou s combustio n contro l de -

. ;c e inle t an doutle t

emissio n monitorin g woul db e th e preferre dmetho do f monitoring , becaus e i t

woul dprovid e a continuous , direc t

measuremen t

c f actua l emissions

. However , n o continuou s monito r

measurin g tota l organic s (minu s methan e an d ethane ) ha s bee n demonstrate dfo r incinerator s becaus e eac h o

f di e many differen

t compound s i

n reacto r proces s ven t stream s woul dhav e to b e identifie d separatel y an dth e concentration s o f eac h determined

. Therefore , th e Administrato r

ha s determine dtha t continuou s monitorin g o

f complianc e wit h th e propose dstandard s i s no t feasible

.P.1 6

Federa l Registe r /

Vol

. 55 , No

. 12 6 /

Friday

. Jun e 29 , 199 0 / Propose dRule s 2696 7
Provide dtha t

combustio n parameter s tha t accuratel y reflec t

th e leve l of combustio n devic e efficienc y ca n b e identifie dan dmonitore dcontinuously , monitorin g o

f suc h parameter s alon e woul dhav e severa l advantages , suc h a s lo w cos t an dhig h reliability

. However , a disadvantag e o

f combustio n parameter s monitorin g alon e i s tha t

th e correlatio n o f th e parameter s with th e numerica l emissio n limi t

i s no t exact

. However , exac t correlatio n i s no t

necessar y i

f th e paramete r monitore dwoul d demonstrat e prope r

operatio n an d maintenanc e o

f th e contro l device

. Th e combustio n devic e operatin g parameter s tha t

affect incinerato r performanc e wer e analyzed

. Thes e variable s ar e temperature , mixing , typ e o f compound , residenc e time , inle t concentration , an dflow regime

. O f tiiese variables , di e inle t

concentratio n wa s judge dt o hav e onl y asmal l impac t o n incinerato r

performanc e (provide d reacto r ven t concentration s ar e a t

leas t ? 30 0 ppmv)

. Residenc e tim e i s tssentiall y se t

after incinerato r constructio n unles s th e ven t strea mflow rat e i s changed

. At

temperature s abov e 76 0 "C , th e compoun dtype ha s litd e effect o n combustio n efficiency

. Temperatur e an dflow rat e wer e the n analyze di n mor e detai l t o defin e thei r impac t o n performanc e an dth e ability t o monito r

diem

. Temperatur e wa s analyze dfirst. Tes t result s an dtheoretica l calculation s sho w tha t lowe r temperatur e ca n caus e significant decrease s in contro l devic e efficiency

. Tes t

result s als o indicat e tiiat temperatur e increase s ca n als o adversel y affec t

contro l devic e efficiency , apparenti y b y decreasin g di e thoroughnes s o

f mixin g o f proces s ven t gases , burne r

gases , an dcombustio n air

. I n term s o f cos t temperatur e monitor s ar e relativel y inexpensive , costin g les s tha n $5,00 0 installe dwit h stri p charts , an dar e easil y an dcheapl y operate d Give n th e larg e effect

o f temperatur e o n efficienc y an dth e lo w cos t o f temperatur e monitors , thi s variabl e i s clearl y a n effectiv e parameter s t o monitor

. Th e propose dstandard s would , dierefore , requir e th e owne r o r operato r o f a n affecte dfacilit

y usin g atherma l incinerato r

t o compl y witi i th e propose d 9 8 weight-percent/2 0 ppm v emissio n limi t t o install , calibrate , maintain , an d operat e accordin g t o manufacturer' s specification s a temperatur e measuremen t

device

. Thi s devic e woul d b e require dt o b e equippe dwith a continuou s recorde r

an dhav e a n accurac y o

f 1 percen t o f th e temperatur e bein g measured , expresse di n degree s Celsius , o r

±0. 5 *C , whicheve r

i s greater

. Th e devic e woul db e require dt o b e installe di n th e firebox. I f a catalyti c incinerato r

wer e used , th e temperatur e measurin g devic e woul db e require dt o b e installe di n th e ga s strea m immediatel y befor e an dafter th e catalys t bed

. Flo w rat e of

th e reacto r

proces s ven t strea mt o th e combustio n devic e wa s di e nex t parameter s t o b e analyze da s a potentia l monitorin g parameter

. Wher e a combustio n devic e i s use dt o incinerat e VO C stream s alone , tota l flow rat e int o th e uni t

ca n provid e usefu l informatio n regardin g destructio n efficienc y sinc e i t

relate s t o residenc e tim e i n th e combustio n device

. Reacto r proces s ven t

strea mflo w rate s ca n b e smal l i n compariso n t o otiie r stream s tha t may als o b e ducte dt o th e sam e combustio n device

. Sinc e tota l flo w rat e mus t b e monitere di n orde r

t o provid e reliabl e information , an dreacto r vent s may b e combine dwiti i otiie r nonreacto r vents , the n th e monitorin g requirement s woul db e applie dt o vent s tha t wer e no t intende dt o b e covere db y th e standards

. Flo w indicators , a s oppose d t o flow rat e monitors , ar e relativel y inexpensiv e an deas y t o operate

. Therefore , becaus e i t

give s a n indicatio n dia t th e organic-lade n strea mi s bein g route dfo r destructio n an di t

i s monitore dinexpensively , indicatio n o f flow i s als o a n effectiv e paramete r t o monito r fo r combustio n devices

. Th e propose dstandard s would , therefore , requir e th e operato r of a n affecte dfacilit

y usin g a n incinerato r

t o compl y with th e propose demissio n limi t t o install , calibrate , maintain , an d operat e a flo w indicator , accordin g t o th e manufacturer' s specifications

. Th e flow indicato r

woul db e require dt o b e installe da t

di e combustio n devic e inlet

. Thes e tw o combustio n parameter s (temperatur e an dflow ) woul db e require dt o b e monitore ddurin g th e origina l (o r

mos t recent ) performanc e test

. Temperatur e woul dthe n b e monitore dt o determin e i

f i t deviate d fro mdi e value s measure ddurin g di e performanc e test

. Flo w indicator s woul d b e require dt o determin e whethe r di e ven t strea mwa s bein g continuousl y route dfor destruction

. I f a reacto r proces s ven t

strea mi s introduce dint o di e flame zon e o f a boile r (o r proces s heater ) o

f an y size , i t i s necessary , fo

r th e purpos e o

f ensurin g proper operatio n an dmaintenance , t o kno w tha t th e boile r

(or proces s heater ) i s operatin g an dt o kno w tha t th e ven t strea mi s bein g introduce dint o th e boile r (o r proces s heater)

. Th e maintenanc e o

f record s (suc h a s stea m productio n records ) woul db e require d tha t woul dindicat e tiie period s o f operatio n of

th e boile r

(o r proces s heater)

. Th e Administrato r mus t b e notifie di f th e locatio n a t

whic h th e ven t strea mi s introduce dint o a boile r o r proces s heate r

i s change dafter

th e initia l performanc e test

. Th e natur e o f th e record s t o b e kep t

t o comply wi m thi s requiremen t

ar e lef t t o th e discretio n o

f th e owne r

o r operato r o f tiie facility , bu t

the y mus t

b e readil y availabl e fo

r inspection

. T o ensur e dia t th e ven t strea mi s bein g introduce dint o th e boile r (or proces s heater) , th e propose dstandard s requir e owner s o r operator s t o instal l an doperat e aflow indicato r tiiat provide s arecor do

f ven t strea mflow t o th e boile r

(o r proces s heater)

. Fo r hea t generatin g unit s (boiler s an d proces s heaters ) o

f les s tha n 4

4 M W (15 0 millio n Btu/hr ) hea t

inpu t design , performanc e testin g i s require dto ensur e efficient

VO C destruction

. Fo r thes e units , jus t

a s fo r incinerators , temperatur e woul db e require dt o b e measure ddurin g di e original (or mos t recent ) performanc e tes t

an dt o b e monitore dt o determin e i

f i t deviate d fro mdi e value s measure ddurin g th e performanc e tes t

Monitorin g o

f temperatur e woul dno t

b e require dfo

r hea t generatin g unit s with adesig n hea t capacit y o

f 4 4 M W o r greater

. A flare wil l b e i n complianc e wit h th e propose dstandard s provide di t i s operatin g i n accordanc e with 4 0 CF R 60.1 8 (i.e. , i t

i s operatin g smokelessl y (n o mor e tha n 5 minute s o

f visibl e emission s fro man y 2-hou

r period) , a flam

e i s present , di e minimumhea t conten t requirement s fo

r th e flaredga s ar e met , an damaximu mexi t

ga s velocity i s no t exceeded)

. Becaus e flares ar e no t enclose dcombustio n devices , i t i s no t feasibl e t o measur e combustio n parameters

. Moreover , temperature s an d residenc e time s ar e mor e variabl e throughou t

th e combustio n zon e fo

r flare s tha n fo

r enclose ddevice s and , therefore , suc h measurement s woul dno t necessaril y provid e agoo dindicato r o f flare performanc e eve n i

f measurable

. Th e typica l metiio do

f monitorin g continuou s operatio n o

f aflare i s visua l inspection

. However , i

f aflare i s operatin g smokelessly , i t

ca n b e difficul

t t o visuall y determin e i

f aflame i s present

. Th e presenc e o

f aflame ca n als o b e determine dthroug h th e us e o f a hea t sensin g devic e o n aflare's pilo t flame, suc h a s athermocoupl e o r ultra

viole t (U-V) bea msensor
. I

f aflame i s absent , th e temperatur e prob e ca n b e use dto aler t

th e plan t operator

. Th e cos t o f availabl e thermocoupl e sensor s range s fro m$80 0 t o $3,00 0 pe r pilot

. (Th e more expensiv e sensor s i n thi s pric e rang e hav e elaborat e automati c religh t an dalar msystems. ) Th e cos t o f aU-VP

. 1 7

Federa l Regigte g /

Vol

. 55 , No

. 12 6 /

Friday , Jun e 29 , 198 0 / Propose dRule s

senso r i s approximatel y $2,000

. Whil e U

V sensor s ar e designe dprimaril y t o monito r flame s withi n enclose d combustio n devices , the y ca n b e applie d to ope n flame s s o lon g a s an y outsid e interference s ar e correcte dfor

. Th e us e o f eithe r tiiermocouples o r

U-V sensor s i s suitabl e fo

r indicatio n o

f di e presenc e o f aflame. Th e propose dstandard s woul drequir e continuou s monitorin g t o indicat e di e presenc e o

f aflame t o ensur e prope r

operatio n an d maintenanc e o

f aflare, bu t

th e standard s d o no t

specif y aparticula r monitorin g technique

. Among th e criteri agovernin g th e us e o f flares unde r

di e propose dstandard s i s maximumexi t

ga s velocity requirement

. Complianc e wit h tiiis requiremen t

i s determine db y performanc e testing

. Method s 2 , 2A , 2C , o r 2 D (se e § 60.704

) ar e use di n performanc e test s t o determin e th e actua l exi t

velocit y o f flares

. Thes e test s mus t b e performe dunde r

representativ e flare operatin g conditions

. Exceedance s o f velocit y limitation s durin g period s i n whic h on e o r

more processe s (tiia

t ven t to di e flare) start-up , shutdown , an d malfunctio n ar e no t

considere da violatio n (se e i 60.8(c))

. Thes e test s ar e use dt o ensur e dia t

di e flare i s designe d to b e an di s capabl e o

f bein g operate d withi n di e velocit

y limitatio n durin g representativ e proces s conditions

. Curin g nonperformanc e tes t periods , operator s mus t

maintai n an doperat e flare s use dto comply wit

h Subpart RR R i n amanne r

consisten t

wit h goo dai r pollutio n contro l practice s fo r minimizin g emissions , eve n durin g period s o f start-up , shutdow n an d malfunctio n (se e § 60.11(d))

. Th e formul aspecifie da t

§ 60.70 4 require s tha t

Metiio d2 , 2A , 2C , o r

2 D b e use da s di e tes t

metho dt o determin e di e volumetri c flow rate

. Thi s flow rat e shoul db e determine din di e flare heade r o r header s tha t

feedth e flare becaus e th e volumetri c flow rat e determine di n thes e header s reflect s th e flow rat e i n th e flare": Afte

r thi s flow rat e i s determined , an operato r

woul dus e desig n an dengineerin g principle s t o determin e di e unobstructe dcross
sectiona l are ao

f th e flare tip. Witi i thes e tw o factors , th e actua l exi t velocit y i s determined

. Th e TR E Inde x Cutof

f Calculatio n o

f th e TR E inde x valu e fo

r an affecte dfacilit

y i s dependen t

upo n measuremen t

o f th e proces s ven t

ga s volumetri c flow rate , net

heatin g value , tota l organi c compoun demissio n rate , an dcorrosio n propertie s (presenc e o r absenc e o f halogenate dcompound s int o th e stream , an dals o prio r to th e inle t

o f an y combustio n device)

. Subjec t t o di e requirement s jus t mentioned , th e samplin g sit e woul dals o b e require dt o b e downstrea mo

f al l produc t

recovery equipmen t

excep t a s discusse di n di e remainde r

o f tiiis section

. In th e situatio n wher e ven t

stream s fro

mne w an dexistin g reactor s ar e ducte dt o a commo n produc t

recovery system , a singl e TR E measuremen t

i s require d downstrea mo

f th e commo n produc t recovery syste mfo

r th e contro l o

f th e combine dne w an dexistin g reacto r ven t streams

. Th e final piec e o

f recovery equipmen t wil l no t alway s b e associate dwit h onl y th e affecte dfacility ; i t

ca n sometime s includ e nonreacto r

proces s facilities

. Thes e ar e configuration s dia t coul d influenc e di e locatio n an dnumbe r o f samplin g site s required

. On e possibl e exceptio n t o th e previou s discussio n involve s aven t

strea mfro

man affecte d facdit y tha t i s normall y route dthroug h a fina l recovery syste mtiiat

i s share dwiti i anonreacto r

proces s ga s stream

. Th e Agenc y considere dwhethe r o r no t to requir e in th e propose dstandard s tha t suc h nonreacto r

proces s stream s b e bypasse ddurin g an y tes t

t o determin e di e TR E index

. Th e efficienc y o

f di e recovery syste mincludin g both di e reacto r an ddi e nonreacto r

proces s ven t strea mwoul doften b e different fro mth e efficienc y o

f simila r device s designe dt o handl e eac h ven t

strea mseparately

. Furthermore , i t

i s reasonabl e t o conclud e diat , especiall y fo r recover y devices , thei r

desig n woul db e different fo r reacto r an dnonreacto r

ven t stream s constituents

. Therefore , fo r purpose s o

f determinin g complianc e with th e TR E inde x cutof

f o f suc h cases , di e Agenc y require s tha t

th e TR E inde x b e determine dbase dupo n di e portio n o f th e recovery outie t

strea mcontribute d b y th e reacto r

proces s facilit

y alone

. Thus , i t i s necessar y t o locat e samplin g site s directl y upstrea man ddownstrea m o f di e recovery syste m(to determin e tiiat overal l contro l efficienc y fo r th e devic e o r devices ) an dals o directl y downstrea mo

f di e reacto r

proces s facility

. I n al l cases , complianc e witi i th e TR E inde x cutof

f woul db e determine d fo r di e tota l portio n o

f th e ven t strea m contribute db y areacto r

facilit y b y determinin g th e effect s o

f th e overal l efficienc y o

f th e devic e upo n di e characteristic s o

f th e ven t strea m determine dfro

mth e upstrea msamplin g sit e (or sites ) an db y measurin g flow rat e an dmola

r compositio n a t

apoin t jus t downstrea mo

f eac h affecte d facilit y (i.e. , downstrea mo

f di e final recovery device)

. Fo r an y samplin g site , di e volumetri c flow rat e woul db e require dt o b e determine daccordin g to Referenc e Method s 2,2A

. 2C , o r 2D , a s appropriate

. Th e molar

compositio n o

f th e offga s stream , includin g di e tota l mola r concentratio n o

f halogenate d compounds , woul db e require dt o b e calculate daccordin g t o di e propose d Referenc e Metho d18 , Measuremen t o f Gaseou s Organi c Compoun dEmissio n b y Ga s Chromatography

. Th e wate r vapo r concentratio n o

f th e ven t stream woul db e require dt o b e calculate d accordin g t o Referenc e Metho d4

. Th e ne t heatin g valu e o

f th e proces s ven t strea m(25 "C , 76

0 m mHg ) woul d b e require dto b e calculate daccordin g t o a n equatio n specifie di

n th e regulation

. Thi s equatio n woul dmak e us e o f di e mola r compositio n o

f th e proces s ven t

stream , a s measure db y Referenc e Method s 4 an d18

. Th e ne t hea t o f combustio n o

f eac h ven t

stream componen t

woul db e require dt o b e determine dusin g AST

M D2382-7 6 i

f publishe dvalues ar e no t

availabl e o r canno t b e calculated

. Thi s metiio do f determinin g net

heatin g valu e wa s chose n becaus e i t

woul dno t

requir e a separat e tes t

procedur e fro

mtha t require dfo

r determinatio n o

f reductio n efficienc y an doffgas halogenation

. Moreover , th e Agenc y believe s tha t th e propose dmetho dfo

r determinin g ne t heatin g valu e woul db e mor e accurat e tha n an y availabl e direc t

experimenta l measure , suc h a s bom

b calorimetry

. Th e tota l organi c mas s emissio n rat e o f th e proces s ven t

strea mwoul dals o b e require dt o b e calculate daccordin g t o a n equatio n specifie din di e regulation

. Thi s equatio n woul dmak e us e o f th e mola r compositio n o

f th e offga s stream , a s measure db y Referenc e Metho d18 , an do f th e volumetri c flow rate , a s measure db y Referenc e Metiio d2

. After a n initia l performanc e tes t t o determin e complianc e wit h th e propose d TR E inde x cutof

f value , variation s i

n proces s parameters , proces s modification s o

r imprope r operatio n o r maintenanc e o

f recovery equipmen t coul dlea dt o highe r

emission s an da tru e TR E inde x belo w th e cutoff

. Som e metiio di s necessar y t o determin e i f th e TR E inde x measure ddurin g di e initia l performanc e tes t

ha s changed

. Method s considere dwer e continuou s monitorin g o f selecte doperatin g parameter s o f th e final piec e o

f produc t recovery equipmen t

in di e affecte dfacilit

y an d periodi c performanc e testin g o f th e TR E inde x o f di e facility

. A s explaine d previously , continuou s ven t sti'ea m mola r compositio n an dflow rat e monitorin g ar e no t

feasible

. Th e first metho dinvestigate dfo

r determinin g i

f di e initia l TR

E inde x ha dchanged , involve ddi e monitorin g o f produc tP.1 8

Federa l Registe r /

Vol

. 55 , No

. 12 8 /

Friday , Jun e 29

. 199 0 / Propose dRule s 2696 9

recovery devic e parameters

. Th e operatin g parameter s o

f tiie thre e type s o f produc t recovery equipmen t commonly use di n reacto r processe s wer e analyze dfo

r correlatio n witi i produc t recovery devic e operatio n an d maintenance , whic h i n turn woul dgiv e an indicatio n o

f change s i n TR

E index

. Th e tiiree type s o

f produc t recovery equipmen t

ar e absorbers , condensers , an dcarbo n adsorbers

. Fo r a n absorber , tw o operatin g parameter s wer e identifie da s di e primar y determinant s o

f produc t recovery devic e operations : absorbin g liqui dtemperatur e an dspecifi c gravity (o r som e othe r

paramete r

use db y a facilit y t o measur e absorbin g liqui d saturation)

. I n th e absenc e of th e propose dstandard , facilitie s employin g a n absorbe r

fo r produc t recovery would , i n general , monito r

continuousl y some paramete r relate dt o di e degre e o

f saturatio n o

f absorbin g liqui dwit

h recovere dmaterial

. Specifi c gravity i s on e suc h paramete r

tha t i s frequentl y monitored

. Absorbin g liqui d temperatur e monitor s an dspecifi c gravity measuremen t

device s ar e availabl e a t

areasonabl e cost

. Th e estimate done-tim e combine dcapita l investmen t

fo r suc h equipmen t

i s $8,000

. Thes e absorptio n parameter s woul db e require dt o b e measure ddurin g eac h performanc e test

. (I

f approve db y di e enforcin g Agency , a n alternat e paramete r tha t woul dindicat e th e degre e o f absorbin g liqui dsaturatio n coul db e measure ddurin g eac h performanc e test. ) Thes e absorptio n parameter s woul dthe n b e monitore dt o determin e i

f an y valu e ha dchange d sinc e di e performanc e test

. Thi s monitorin g woul dindicat e whetiie r th e absorbe r wa s bein g operate dan d maintaine dproperly

. Therefore , a n operato r o f an affecte dfacilit

y fo r whic h a n absorbe r

wa s th e final devic e i n th e produc t recovery syste mwoul db e require dt o install , calibrate , maintain , an doperat e accordin g t o a manufacturer' s specification s a n absorbin g liqui dtemperatur e monito r an dspecifi c gravity measuremen t devic e (or an alternat e devic e tha t

woul d measur e th e degre e o

f absorbin g liqui d saturation , i

f approve db y th e enforcin g agency) , eac h recorde dcontinuously

. Fo r acondenser , th e exi t

(produc t side ) temperatur e o

f th e offga s wa s identifie da s th e primary determinan t o f produc t recovery devic e operation

. Condense r

temperatur e monitor s ar e availabl e a t

areasonabl e cost

. Th e estimate done-tim e capita l investmen t fo r suc h equipmen t

i s $3,000

. Th e condense r

exi t (produc t side ) temperatur e woul db e require dt o b e measure ddurin g eac h performanc e test

. Th e temperatur e woul dthe n b e monitore dt o determin e i

f th e valu e ha d change dsinc e th e mos t

recen t performanc e tes t

Thi s monitorin g woul d indicat e whethe r

th e condense r

wa s bein g operate dan dmaintaine dproperly

. Therefore , a n operato r

o f a n affecte d facilit y fo r whic h acondense r

wa s th e final devic e in di e produc t recovery syste mwoul db e rquire dt o install , calibrate , maintain , an doperat e accordin g t o manufacturer' s specification s acondense r temperatur e monito r equippe dwith acontinuou s recorder

. Fo r acarbo n absorber , di e carbo n be d temperatur e (after

regeneratio n an d completio n o

f an y coolin g cycle) , a s wel l a s th e amoun t

o f stea muse dt o regenerat e th e adsorptio n bed , wer e identifie da s th e primary determinant s o f produc t recovery devic e operation

. Steamflow meter s dia t

indicat e di e quantit y o f stea muse dove r

aperio dof tim e an dbe dtemperatur e monitor s ar e availabl e a t

areasonabl e cost

. Th e estimate done-tim e capita l investmen t fo r suc h equipmen t

i s $10,000

. Thes e adsorptio n parameter s woul db e require dt o b e measure ddurin g eac h performanc e test

. Thes e adsorptio n parameter s woul dthe n b e monitore dt o determin e i

f an y valu e ha dchange d sinc e di e mos t

recen t performanc e test

. Thi s monitorin g woul dindicat e whethe r th e carbo n adsorptio n uni t wa s bein g operate dan dmaintaine dproperly

. Therefore , a n operato r

o f a n affecte d facilit y fo r whic h acarbo n adsorbe r i s th e final uni t

of th e produc t

recover y syste mwoul db e require dt o install , calibrate , maintain , an doperat e accordin g t o manufacturer' s specification s a n integratin g stea mflow mete r an dacarbo n be dtemperatur e measuremen t

device , eac h equippe dt o b e recorde dcontinuously

. Som e carbo n absorbers , adsorbers , an dcondenser s may includ e ven t strea morgani c concentratio n monitor s t o ai doperator s maximizin g th e recover y of

ra w material s o r

products

. Suc h device s equippe dwiti i a continuou s recorde r

ma y b e use da s a n alternativ e t o monitorin g th e otiie r operatin g parameter s fo

r absorbers , adsorbers , an dcondenser s specifie di n di e regulation

. Th e enforcemen t

agenc y woul d specify , o n acase-by-cas e basis , appropriat e monitorin g procedure s o r requirement s wher e th e owne r o r operato r o f a n affecte dfacilit

y use s emissio n contro l o r

produc t recovery technique s othe r

tiian tiiose specifie dt o compl y with di e propose dstandards

. Th e Agenc y ha s determine dtha t a n affecte dfacilit

y wit h aTR E inde x valu e greate r tha n B. O coul dno t

lowe r it s TR E inde x valu e belo w 1 withou t aproces s change

. Therefore , facilitie s with TR E inde x values greate r

tha n 8. 0 ar e exemp t fro mth e monitoring , recordkeepin g an d reportin g requirement s othe r than the initia l performanc e tes t

requirement s unles s aproces s chang e i s mad e to th e facility

. I f aproces s chang e occurs , th e TR E inde x valu e woul dhav e to b e recalculated

. I

f th e recalculate dTR

E inde x valu e i s belo w o

r equa l t o 8. 0 an d greate r tha n 1.0, th e facilit

y woul dhav e t o compl y witi i th e monitoring , recordkeeping , an dreportin g requirement s o

f di e standards

. M. Reporting and

Recordkeeping Requirements Th e Genera l Provision s fo r th e NSP S regulation s (40 CF

Rpar t 60 , subpart

A ) requir e submitta l o

f severa l one-lime notification s fo

r occurrence s suc h a s construction , modification , reconstruction , schedule ddate s fo r performanc e tests , an dperformanc e tes t results

. Owner s an doperator s o f boiler s an dproces s heater s wit

h desig n hea t inpu t capacitie s o

f 4 4 M W (15 0 millio n Btu/hr ) o r greate r woul dno t

repor t performanc e tes t

results , sinc e th e propose dstandard s woul dwaiv e th e requiremen t

o f suc h atest

. Instead , operator s woul db e require dto fil e an initia l report

describin g th e locatio n a

t whic h th e reacto r

ven t strea mi s introduce dint o th e boile r (or proces s heater ) t o b e used

. Owner s an d operator s o

f flares use dt o comply wit h di e propose dstandard s woul db e require dt o file a n initia l report on th e result s of performanc e testin g t o determin e complianc e witi i th e visibl e emissio n requirement s an dth e hea t conten t an dmaximu mexi t

ga s velocit

y criteri afo r flares. Th e propose dstandard s exemp t reacto r proces s facilitie s fro

mth e quarterl y report

require db y th e Genera l Provisions

. However , record s o f start

up , shutdown , an dmalfunctio n woul d stil l b e required

. Also , record s indicatin g whethe r contro l equipmen t

i s bein g operate dan dmaintaine dproperl y woul db e required

. Th e propose d standard s woul drequir e owner s o r operator s o

f thos e facilities , exempte d becaus e tiieir

operationa l flow rat e wa s les s tha n 0.01 1 scm/min , to sen dan initia l report

t o th e Administrato r containin g ameasuremen t o f th e operatin g flow rate , maintai n record s o f an dreport

semiannuall y i

f an y change s i n equipmen t

proces s operatio n occu r tha t woul dincreas e tnei r

flow rat e abov e 0.01 1 scm/min

. Similarly , owner sP.1 9

2697 0 Federa l Registe r / Vol

. 55 , No

. 12 6 /

Friday , Jun e 29 , 199 0 / Propose dRule s

o r operator s o

f thos e facilitie s tha t woul db e exclude dfro

mcontro l requirement s becaus e th e proces s uni t in whic h the y ar e locate dha s adesig n capacit y belo w 1 Gg/yr , woul db e require dto sen dan initia l report t o th e Administrato r

ofth e desig n productio n capacity

. The y woul dals o b e require d t o recor dan dreport

change s tha t increas e thei r

proces s uni t

capacitie s abov e th e on e Gg/y r

cutoff

. Record s indicatin g prope r operatio n an dmaintenanc e woul db e basedo n th e monitorin g o

f contro l devic e o r

recovery devic e parameter s discusse di n di e previou s section

. Tw o type s o f record s woul db e required

. Th e first woul db e th e monitorin g result s themselves

. Thi s informatio n can b e automaticall y recorded , an dtherefore , essentiall y th e only labo r necessar y fo

r keepin g thes e record s woul dconsis t

c f filing automaticall y recorde dparameters

. Th e secon dtyp e o

f recor dwoul db e a tabulatio n o

f period s whe n th e measurement s o

f thes e automaticall y recorde dparameter s significantl y deviate dfro

mmeasurement s ofth e sam e parameter s durin g th e mos t recen t performanc e test

. Althoug h thi s require s mor e effort , i t i s anecessar y ste p fo

r bot h th e owner

o r operato r an d enforcement

agenc y t o ensur e tha t

th e contro l equipmen t

i s bein g operate dan d maintaine dproperly

. Thi s informatio n woul db e necessar y fo

r th e owne r

o r operato r t o kno w whe n t

o make necessar y correction s t

o th e contro l equipment

. For

thi s secon dtyp e o

f recor di t woul db e necessar y fo

r th e owner o r operato r to recor dcontro l devic e o r produc t recovery equipmen t operatin g parameters , a s appropriate , durin g al l performanc e test s an dkee p thes e record s fo

r purpose s cf comparison

. Th e owne r

o r operato r woul dno t b e require dto recor dal l deviation s fro

mIhes e measurements , bu t only certai n deviation s a s liste din ih n propose dregulation

. All record s woul dbe require dt

o b e kep t u p to dat e an di n readil y accessibl e file s fo r 2 years
. Th e paramete r

boundarie s include di n th e propose dregulatio n woul dallo w fo

r norma ! fluctuation s i

n operatio n o

f th e equipmen t

monitored

. Th e VO C reductio n efficienc y o f th e contro l devic e woul dno t

b e affecte dby suc h normal fluctuations

. Wher e arecover

y syste mi s use dt o comply wit

h th e propose dTR

E inde x value , th e propose dstandard s woul d als o requir e recordin g o

f an y chang e in productio n capacity ; feedstock ; typ e o f catalvst ; o r

ofth e replacement , removal , o r additiona l o

f produc t recovery equipment

. Whe n an y suc h chang e occurs , th e TR

E inde x valu e woul dhav e t o b e recalculate dto documen t dia t di e facilit y continue s t o hav e aTR

E inde x valu e abov e 1.0

. Suc h recalculatio n ca n b e base do n di e bes t

engineerin g estimate s o

f th e effect s o

f th e chang e o r o n emissio n tes t

data

. A recor dwoul d b e maintaine do

f di e recalculate dTR

E value

. I f th e recalculate dTR

E inde x valu e fo r th e facilit y i s belo w 1.0

, di e owner , o r operato r o f th e facilit y woul d hav e t o demonstrat e complianc e witi i th e 9 8 weight-percen t

reductio n o r

2 0 ppm v emissio n limits

. Performanc e test s mus t b e conducte da s soo n a s possibl e after th e proces s chang e bu t

n o late r tiian 180 day s fro

mth e time o

f th e proces s change

. I f th e initia l TR

E inde x valu e fo

r a facilit y wer e abov e 8. 0 an dth e recalculate dvalu e wer e belo w o r equa l t o 8. 0 bu t greate r tha n 1.0 , th e facilit

y mus t report th e recalculate dTR

E inde x valu e t o th e Administrato r a s soc n a s possibl e afte

r th e chang e an dn o late r tha n 180 day s after

th e change

. I

n addition , aperformanc e tes t mus t b e complete dwitiii n th e sam e tim e perio d t o verif y th e recalculate dvalu e an dt o obtai n th e initia l operatin g parameters

. Th e performanc e tes t

i s subjec t t o th e requirement s o

f § 60. 8 o f th e Genera l Provisions

. Th e facilit

y mus t begi n complyin g wit

h th e monitoring , recordkeeping , an dreportin g requirement s immediatel y after th e performanc e test

. I n additio n t o th e one-tim e notification s an dperformanc e tes t report s discusse dabove , semiannua l reportin g o

f recorde ddat awoul db e require dfo

r instance s wher e monitore d parameter s excee dth e allowabl e limitation s se t

fort h i n di e standards

. Thes e dat ainclud e th e operatin g parameter s cite dabov e fo r combustio n an dothe r contro l devices

. Othe r instance s tha t

woul db e reporte d semiannuall y a r

period s o f n o flow t o contro l device s use dfo

r complianc e wit h th e standard s an dperiod s wher e ther e i s n o flame presen t

fo r flares use d fo r complianc e wit

h di e standards

. Th e requiremen t

fo r semiannua l reporting , however , i s waive dfo

r affecte dfacilitie s i n State s wher e di e programha s bee n delegated , i

f EPA , in th e cours e o

f delegation , approve s reportin g requirement s o

r an alternativ e means o

f sourc e surveillanc e adopte db y th e State

. Suc h affecte dfacilitie s woul db e require dt o comply wit

h th e requirement s adopte dby di e State

. Durin g th e first

3 year s o f thi s regulation , th e averag e annua l burde n o f di e reportin g an drecordkeepin g requirement s woul db e 7. 9 person-years , base do n a n averag e o

f 2 7 respondent s pe r year
. V

. Administrativ e Requirement s J4

. Public Hearing A publi c hearin g wil l b e held , i f requested , to discus s th e propose d standard s in accordanc e witi i sectio n 307(d)(5 ) o

f th e CAA

. Person s wishin g t o make ora l presentation s shoul dcontac t EP A a t th e addres s give n i

n di e ADDRESSE

S sectio n o

f th e preamble

. Oral presentation s wil l b e limite dto 1 5 minute s each

. An

y member o f th e publi c ma y file awritte n statemen t

before , during , o r withi n 3 0 day s afte

r th e hearing

. Writte n statement s shoul db e addresse dto th e Centra l Docke t Sectio n addres s give n i

n th e ADDRESSE

S sectio n o f di e preamble

. A verbati mtranscrip t

o f th e hearin g an dwritte n statement s wil l b e availabl e •fo r publi c inspectio n an dcopyin g durin g normal workin g hour s a

t th e EPA' s Centra l Docket

Sectio n in Washington , D C (se e di e ADDRESSE

S sectio n o

f thi s preamble)

. B. Docket Th e docke t

i s an organize dan d complet e fil

e o f al l di e informatio n submitte dlo , o

r otherwis e considere d in , di e developmen t

o f tiiis propose d rulemaking

. Th e principa l purpose s o f th e docke t

are ; (1 ) T o allo w intereste d partie s t o identif

y an dlocat e document s s o diat the y can effectively participat e in di e rulemakin g process , an d(2 ) to serv e a s di e recor din cas e o f judicia l revie w (excep t

fo r interagenc y revie w material s a s note din Sectio n 307(d)(7)(A))

. C. Clean Air Act Procedural Requirments Administrato r

Listing—Sectio n 111

. A s prescribe db y sectio n 11 1 o f th e CAA , a s amended , establishmen t o f standard s o

f performanc e fo

r SOCM I reacto r proces s unit s wa s precede dby th e Administrator' s determinatio n (4 0 CF R60.18

. 4 4 F R49222 , date dAugus t

21 , 1979) that SOCM I contribute s significanti y to air

pollutio n whic h ma

y reasonabl y b e anticipate dt o endange r publi c health o r

welfare

. Periodi c Review—Sectio n 111

. Thi s regulatio n wil l b e reviewe dwitni n 4 year s fro mth e dat e o

f promulgatio n a s require dby th e CJ\A

. Thi s revie w wil l includ e a n assessmen t

o f suc h factor s a s th e nee dfo

r integratio n wit

h othe r programs , th e existenc e o f alternativ e methods , enforceability , impiovement s i n emissio n contro l technology , an d reportin g requirements

. Externa l Participation—Sectio n 117

. I n accordanc e wit

h Sectio n 11 7 o

f th e Act , publicatio n o

f tiiis proposa l wa s precede dby consultatio n witi iFedera l Registe r / Vol

. 55

. No

. 12 6 /

Friday , Jun e 29 , 199 0 / Propose dRule s 

### 2697 1 appropriat e advisory committees , independen t

experts , an dFedera l department s an dagencies

. In addition , numerou s meeting s wer e hel dwith industry representative s an dtrad e association s durin g developmen t o f di e propose dstandards

. Th e Administrato r wil l welcom e comment s o n al l aspect s o f th e propose dregulation , includin g economi c an dtechnolgica l issues

. Economi c Impac t

Assessment

— Sectio n 317

. Sectio n 31 7 o f th e CA A require s th e Administrato r t o prepar e an economi c impac t

assessmen t

fo r an y NSP S promulgate dunde r

sectio n 111(b ) o f th e Act

. A

n economi c impac t assessmen t

wa s prepare dfo

r th e propose dregulation s an dfo r othe r regulatory alternatives

. All aspect s o f th e assessmen t

wer e considere di n th e formulatio n o

f th e propose dstandard s t o ensur e tiiat

th e propose dstandard s woul drepresen t

th e bes t syste mo f emissio n reductio n considerin g costs

. Th e economi c impac t

assessmen t

i s include di n th e BID

. D. Office of Management

and Budget Reviews 1

. Paperwor

k Reductio n Ac t Ther e ar e n o reportin g requirment s b y othe r governmenta l agencie s fo r th e informatio n require db y thes e standard s whic h woul dresul t

in overlappin g requirements

. I

n particular , ther e i s n o overlap wit

h th e reportin g requirement s o f the Superfun dprogram
. Th e Superfun dprogra

mwa s establishe din 1980 b y th e Comprehensiv e Environmenta l Response , Compensation , an dLiabilit y Ac t (CERCLA

. Pub

. L

. 96-510 ) an d authorize s th e Federa l governmen t t o respon ddirectl y t o release s (or threatene dreleases ) o

f hazardou s substance s an dpollutant s o r contaminant s t o an y medi atha t may
. endange r publi c healt h o r

welfare

. Under tii e notificatio n an dliability provision s o

f sectio n 10 3 (se e 4 8 F

R 23552

. Ma y 25,1983) , CERCL

A require s tha t person s i n charg e o

f vessel s o r facilitie s fro

mwhic h hazardou s substance s hav e bee n release di n quantitie s tha t

ar e equa l to

. o r

greate r than , th e reportabl e quantitie s immediatel y notif

y th e Nationa l Respons e Cente r

o f th e releas e (800

- 424-8802 ; in Washington , DC

. metropolitan are a202-426-2675)

. However , ai r

release s whic h qualif

y a s Federall y permitte dreleases , suc h a s VO C emission s tha t

ar e regulate dunde r sectio n 11 1 o

f th e Clean Air

Act , ar e no t subjec t t o th e notificatio n o r

liability provision s o

f CERCL A unles s th e ai r release s ar e i n exces s o

f th e allowabl e NSP S emission s b y a n amount equa l t o o r

greate r tiian th e reportin g quantity ; i n thi s case , person s i n charg e mus t report th e exces s ai r

release s t o th e Nationa l Respons e Center

. (Reportin g unde r CERCL A doe s no t

excus e di e person s i n charg e fro man y responsibility , includin g reporting , o r

liability unde r

th e NSP S program. ) Th e informatio n collectio n requirement s in thi s propose drul e hav e bee n submitte dfo

r approva l t o th e Offic e o f Managemen t

an dBudge

t (OMB ) unde r

th e Paperwork

Reductio n Ac t o f 1980,4 4 U.S.C

. 350 1 et

seq an d ha s bee n assigne dan OM B contro l number

. Comment s o n thes e requirement s shoul db e submitte dfo r approva l to th e Offic e o

f Informatio n an dRegulator

y Affair s o

f OMB ; 726 Jackso n Place , NW. ; Washington

. D C 20503 marke d"Attention : Des k Office r fo r EPA. " Th e final rul e wd l respon dt o an y OM B o r publi c comment s o n th e informatio n collectio n requirements

. Publi c reportin g burde n fo r thi s collectio n o

f informatio n i s estimate dt o b e 15,77 1 hour s pe r

year , wit h a n averag e o f 58 4 hour s pe r

response , includin g tim e fo

r reviewin g instructions , searchin g existin g dat a sources , gatherin g an dmaintainin g th e dat aneeded , an dcompletin g an d reviewin g th e collectio n o f information

. Sen dcomment s regardin g th e burde n estimat e o r

an y othe r

aspec t o f thi s collectio n o

f information , includin g suggestion s fo

r reducin g thi s burden , t o Chief , Informatio n Polic y Branc h PM

223 , U.S

. Environmenta l Protectio n Agency

. 40 1 M St.

. SW. , Washington , D C 20460 ; an dt o th e Offic e o f Informatio n an dRegulator

y Affairs , Offic e o

f Mangemen t

an dBudge t

Washington

. DC 20503

. 2

. Executiv e Orde r

1229 1 Revie w Unde r Executiv e Orde r

12291 , EP A mus t judg e whethe r

aregulatio n i s "major " an dtherefor e subjec t t o th e requiremen t

o f aRegulatory Impac t Analysis

. Thi s propose dregulatio n i s no t major because ; (1 ) Th e nationa l annualize dcontro l costs , includin g capita l charge s resultin g fo r th e standard s tota l les s tha n $10 0 million ; (2 ) th e standard s d o no t

caus e amajor increas e in price s o r

productio n cost s fo

r mos t o f th e chemical s considered : an d (3 ) give n th e lo w level s o

f investmen t require dan dth e smal l pric e increase s estimate dfo

r chemical s with lo w TR

E values , th e effect s o

f th e regulatio n on domesti c competition , employment , investment , productivity , innovation , an dcompetitio n i

n foreig n market s wil l b e negligible

. Thi s regulatio n wa s submitte dt o OM B fo r revie w a s require db y Executiv e Orde r

12291

. Any writte n comment s fo r OM B an dan y writte n response s b y EP

A wil l b e include din Docke t A-83-29

. Thi s docke t

i s availabl e fo

r publi c inspectio n at

EPA' s Centra l Docke t

Section , whic h i s liste d unde r di e ABOBE83E

8 sectio n o

f thi s notice. E

. Regulatory Flexibilit

y Ac t Complianc e Th e Regulator

y Flexibilit

y Ac t (Pub

. L

. 96-354 , Septembe r

19,1980 ) require s tha t specia l consideratio n b e give n t o th e impact s o f al l Federa l regulation s on smal l businesses , smal l governments

. an dsmal l organizations

. Thes e standard s wil l hav e n o know n effect s o n smal l government s an dsmal l organizations

. Som

e smal l businesse s ma y b e affected

. However , th e economi c analysi s describe dabov e indicate s tha t thes e standard s wil l hav e n o significant

. advers e economi c impac t

o n firm s producin g affecte dchemicals , regardles s o f fir msize

. Furthermore , n o burde n wil l b e place dupo n smal l businesse s disproportionat e to thei r

potentia l contributio n t o VO C emissions

. Th e pric e increas e screenin g analysi s use s man y conservativ e contro l cos t assumption s an ddemonstrate s tha t no t eve n smal l plant s shoul dincur contro l cost s in exces s o

f 5 percen t o f productio n costs

. Ther e shoul db e n o capita l availabilit y o r

industria l growt

h problem s associate dwit

h thes e standards

. Thus , n o significant , advers e economi c impact s o n smal l businesse s ar e anticipated

. No burde n wil l b e place don any fir m disproportionat e to th e VO C tiiat i t woul demi t

i n th e absenc e o

f thes e standards

. Thi s i s ensure db y applicatio n o

f th e TR E index , whic h identifie s facilitie s tha t

woul demit

a substantia l amoun t

o f reasonabl y controllabl e VO C i

n th e absenc e o

f thes e standards

. Pursuan t t o th e provision s o

f 5 U.S.C

. 605(b) , I hereb y certif

y tha t thi s rul e wil l no t hav e asignifican t

impac t o n a substantia l numbe r

o f smal l entities

. List o f Subject s i n 40 CF

RPar t 6 0 Air pollutio n control

. Reportin g an d recordkeepin g requirements

. Incorporatio n b y reference

. Intergovernmenta l relations , SOCMI

. Dutud : Jun e 13 , 1900

. Willia mK

. Reilly

. Adminiszrctor. PAR T 60—[AMENDED ] I t i s propose dtha t

4 0 CF Rpart 6 b e amende da s follows : 1

. th e authorit y citatio n fo r part 6 0 continue s t o rea da s follows : 

# u

pFedera l Regjste g / Vol . 55 , No . 12 8 /

Friday , Jun e 29 , 198 0 / Propose d Rule s Authority : Sees
. 101 , 111
. 114.116
. an d 30 1 o f di e Clea n Air Ac t(CAA) a o amende d (4 2 U.S.C
. 7401
. 7411
. 7416

, 7601)
. 2
. B y addin g a ne w subpar tRR Rt o rea d a s follows : Subpar t RRR=-StomSard o o f Poriormonc o fo rVolotll o Organi c Compoun d (VOC ) Emlcolon o fro m Syntttott o Organi c Chomtea O Manufacturin g Industr y (SOCMI ) RGGCSOS

Processe s Sec

. 60.70 0 Applicabilit

y an d designatio n o

f affecte d facility
. 60.70 1 Definitions
. 60.70 2 Standards
. 60.70 3 .Monitorin

g o f emission s an

d operations
. 60.70 ; Tes tmethods an

d procedures . 60.70 5 Reportin

g an d recordkeeping requirements
. 60.70 6 Reconstruction
. 60.70 7 Chemicals affected by subpar tRRR . 60.70 8 Delegation o

f authority
. Subpar t RRR=Standarti s ot f Performanc e fo rVolatil e Organi c Compoun d (VOC ) Enrtiasion o fron a Syntheti c Organi c Shomies l Manufacturin g Industr y (SOCMI ) Reacto rProcesse s § 60.70 0 Applicabilit y an d designatio n of f affecte d fcctlity

. (a ) Th e provision s o f

this subpar t eppl y to eac h affecte d facilit y designate d i n paragrap h (b ) o f thi s sectio n tha tproduce s an y o f th e chemical s liste d i n § 60.70 7 a s a produc t co-product , by-product , o r intermediate , excep ta s provide d i n paragrap h (c ) o f this section
. (b ) Th e affecte d facilit y i s an y o f di e followin g fo r whic h construction , modification , o r reconstructio n commence d afte r June 29,1980
. (1 ) Eac h reacto r proces s no t dischargin g it s ven tstrea m int o a recover y system . (2 ) Eac h combinatio n o f a reacto r proces s an d th e recover y syste m int o whic h it s ven tstrea m i s discharged
. (3 ) Eac h combinatio n o f tw o o r mor e reacto r processe s an d di e commo n recover y syste m int o whic h thei r ven t stream s ar e discharged
. (c ) Exemption s from th e provision s o f paragrap h (3 ) o f

thi s sectio n ar e a s follows : (1 ) An y reacto r proces s tha ti s designe d an d operate d a s a batc h operatio n i s no ta n affecte d facility
. (2 ) Eac h affecte d facilit y tha tha s a tota l resourc e effectivenes s (TRE) inde x valu e greate r tha n 8. 0 i s exemp tfrom al l provision s o f

this subpar texcep tfo r i § 60.702 ; 60.704(d) , (e) , an d (f) : an d 60.70 3 (h ) an d (1)
. (3 ) Eac h affecte d facilit y i n a proces s uni twit h a tota l desig n capacit y fo r al l chemical s produce d withi n tha tuni to f les s tha n 1 gigagra m pe r yea r i s exemp t fro m al l provision s o f

thi s subpar t excep tfo r th e recordkeepin g an d reportin g requirement s i n paragraph s (j) , (1)(8) , an d (n ) o f

6 60.705
. (4 ) Eac h affecte d facilit y operate d wit h a ven tstrea m So w rat e les s tha n 0.01 1 scm/mi n i s exemp tfro m al l provision s o f

thi s subpar texcep tfo r th e tes tmetho d an d procedur e an d th e recordkeepin g an d reportin g requirement s i n g 60.704(g ) an d paragraph s (i) , (1)(5) , an d (o ) o f § 60.705
. (Note : Th e inten to f thes e standards i s t

o minimiz e th e emission s o

f VOC throug

h th e applicatio n o

f bes tdemonstrated technolog y (BDT)
. Th e numerica

l emissio n limit

s in tiiese standards ar

e expresse d i

n term s o f tota l organi c compound

s (TOC ) measure d a s TO C les s methan

e an d ethane . Thes e emissio n limit s reflec tthe performanc

e o f BDT. ) g 60.70 1 Oeflnrdono

. A s use d i n thi s subpar tal l term s no t define d her e shal l hav e th e meanin g give n the m i n th e Ac tan d i n subpar tA o f par t60 , an d th e followin g term s shal l hav e th e specifi c meanin g give n them . Batch process mean s an y noncontinuou s reacto r proces s whic h i s no tcharacterize d b y steady-stat e condition s an d i n whic h reactant s ar e no tadde d an d product s ar e no tremove d simultaneously
. Boilermean s an y enclose d combustio n devic e tha textract s usefu l energ y i n th e form o f

steam . By compound

mean s b y individua l strea m components , no tcarbo n equivalents
. Continuous recordermean s a dat a recordin g devic e recordin g a n instantaneou s dat a valu e a tleas tonc e ever y 1 5 minutes
. Flame zone mean s th e portio n o f th e combustio n chambe r i n a boile r occupie d b y th e flame envelope . Flow indicatormean s a devic e whic h indicate s whetiie r ga s flo w i s presen ti n a ven tstream . Halogenated

vent stream mean s an y ven tstrea m determine d t o hav e a tota l concentratio n (b y volume ) o f compound s containin g halogen s o f 2 0 ppm v (b y compound ) o r greater . Incineratormean s an y enclose d combustio n devic e tha ti s use d fo r destroyin g organi c compound s an d doe s no textrac tenerg y i n th e for m o f st.re m or proces s heat . Process heatermean s a devic e tha t transfer s hea tliberate d b y burnin g fue l t o fluids containe d i n tubes , includin g a! ! fluids excep twate r tha ti s heate d t o produc e steam . Process unit

mean s equipmen t assemble d an d connecte d b y pipe s o r duct s t o produce , a s intermediate s o r fina l products , on e o r mor e o f di e chemical s i n § 60.707
. A proces s uni tca n

operat e independentl y i f supplie d wit h sufficien tfee d o r ra w material s an d sufficien tproduc tstorag e facilities
. Product mean s an y compoun d o r chemica l liste d i n § 60.70 7 whic h i s produce d fo r sal e a s a fina l produc ta s tha tchemical , o r i s use d fo r di e productio n o f

othe r chemical s o r compounds . By-products , co-products , an d intermediate s ar e considere d to b e products . Reactorprocesses are uni toperation s i n whic h on e o r mor e chemicals , o r reactant s othe r tha n air , ar e combine d o r decompose d i n suc h a wa y tha tthei r molecula r structure s ar e altere d an d on e o r mor e ne w organi c compound s ar e formed
. Recovery device mean s a n individua l uni to f equipment , suc h a s a n absorber , carbo n adsorber , o r condenser , capabl e o f an d use d fo r th e purpos e o f recoverin g chemical s fo r use , reuse , o r sale . Recovery system mean s a n individua l recover y devic e o r serie s o f suc h device s applie d to th e sam e ven tstream . Total organic compounds (TOC ) mean s thos e compound s measure d accordin g t o th e procedure s i n § 60.704(b)(4)
. Fo r th e purpos e o f measurin g mola r compositio n a s require d i n § 60.704(d)(2)(i) ; an d hourl y emission s rat e a s require d i n g 60.704(d)(5) , an d g 60.704(d)(6) ; an d TO C concentratio n a s require d i n g 60.705(b)(4 ) an d g 60.705(g)(4) , thos e compound s whic h th e Administrato r ha s determine d d o no tcontribut e appreciabl y t o th e formatio n o f ozon e ar e t o b e excluded . TRE index value mean s a measur e o f th e supplementa l tota l resourc e requiremen tpe r uni treductio n o f TO C associate d wit h a n individua l ven t strea m fro m a n affecte d reactor proces s facilit y base d o n ven tstrea m flow rate , emissio n rat e o f

TOC , ne theatin g value , an d corrosiv e propertie s (whetiie r or no t th e strea m contain s halogenate d compounds) , a s quantifie d b y th e equatio n give n unde r g 60.704(e)
. Vent stream mean s an y ga s strea m discharge d directl y from a reacto r t o th e atmospher e o r indirectl y t o di e atmospher e afte r diversio n throug h othe r proces s equipment
. Th e ven t strea m exclude s relie f

valv e discharge s an d equipmen tleak s including , bu tno t limite d to , pumps , compressors , an d \alves
. g 60.70 3 Standordo
. Eac h owne r o r operato r o f an y affecte d facilit y whic h i s subjec tt o th e requirement s o f

tiiis subpar tshal l compl y wit h paragrap h (a) , (b) , o r (c ) o f

### Federa l Registe r /

Vol

. 55 , No , 12 6 /

Friday , {une 29 , 199 0 /

Propose dRule s 2697 3
thi s sectio n fo

r eac h ven t

strea mo n an d after di e dat e o n whic h th e initia l performanc e test , require db y S 60-f l an d § 60.704 , i s completed , bu t no t late r tha n 0 0 day s after

achievin g th e maximu m produclio n rat e a t

whic h th e affecte d facilit y wil l b e operated , o r

18 0 day s afte r di e initial : start-up , whicheve r dat e come s first

. Eac h owne r

o r operato r shall : (a ) Reduc e emission s o

f TO C (les s median e an dethane ) b y 9 8 weight

percent , o r

to aTO C (les s methan e an d ethane ) concentratio n o

f 2 0 ppmv , o n a dr y basi s correcte dto 3 percen t oxygen , whicheve r

i s les s stringen t

I f aboile r o r proces s heate r

i s use dt o compl y wit h thi s paragraph , the n th e ven t strea m shal l b e introduce dint o th e flame zon e o f di e boile r o r proces s heater

. (b ) Combus t

di e emission s i n aflare

. Flare s use dt o comply witi i thi s subpar t shal l comply witi i tiie requirement s o f S 60.18

. (c ) Maintai n aTR

E inde x valu e greate r tha n 1. 0 withou t us e o f aVO C emissio n contro l device

. S 60.70 3 Monitorin g o f emission s an d operations

. (a ) Th e owne r

o r operato r o f a n affecte dfacilit

y tha t use s an incinerato r t o see k t o compl y witi i th e TO C emissio n limi t

specifie dunde r § 60.702(a ) shal l install , calibrate , maintain , an doperat e accordin g t o manufacturer' s specification s th e followin g equipment : (1 ) A temperatur e monitorin g devic e equippe dwith acontinuou s recorde r an dhavin g a n accurac y o f ± 1 percen t o f di e temperatur e bein g monitore d expresse di n degree s Celsiu s o r ±0.5°C , whicheve r

i s greater

. (i) Wher e a n incinerato r

othe r tha n a catalyti c incinerato r

i s used , a temperatur e monitorin g devic e shal l b e installe din di e firebox. (ii ) Wher e acatalyti c incinerato r i a used , temperatur e monitorin g device s shal l be-installe di n th e ga s strea m immediatel y before an dafter th e catalys t bed

. (2 ) A flow indicato r

tha t provide s a recor do f ven t strea mflow t o th e incinerato r

a t leas t onc e ever

y hou r fo r eac h affecte dfacility

. Th e flow indicato r shal l b e installe din di e ven t strea m fro meac h affecte dfacilit

y a t apoin t closes t t o th e inle t

o f eac h incinerato r an dbefore bein g joine dwit h an y othe r \en t stream

. (b ) Th e owne r

o r operato r o f a n affecte dfacilit

y tha t use s aflar

e t o seek to comply wit

h { 60.702(b ) shal l install , calibrate , maintai n an doperat e accordin g to manufacturer' s specification s th e followin g equipment : (1 ) A hea t sensin g d : ice

. suc h e s a ultra-viole t

beamsense : o r thermocouple , a t

tiie pi.o t ligh t t o indicat e continuou s presenc e o f aflame. (2 ) A flow indicato r

tha t provide s a recor do f ven t strea mflow to th e Rare a t leas t onc e every hou r

fo r eac h affecte d facility

. Th e flow indicato r shal l b e installe di n th e ven t

strea mfro

meac h affecte dfacilit

y a t apoin t closes t t o th e flare an dbefore bein g joine dwit h an y othe r ven t stream

. (c ) Th e owne r

o r operato r o f a n affecte dfacilit

y tha t use s aboile r

o r proces s heate r

t o see k to comply wit

h S 60.702(a ) shal l install , calibrate , maintain , an doperat e accordin g t o di e manufacturer' s specification s th e followin g equipment : (1 ) A flow indicato r

tiiat provide s a recor do f ven t strea mflow t o di e boile r o r proces s heate r

a t leas t onc e every hou r fo r eac h affecte dfacility

. Th e flow indicato r shal l b e installe di n th e ven t strea mfro meac h affecte dfacilit

y a t a poin t closes t t o th e inle t

o f eac h boile r o r proces s heate r

an dbefor e bein g joine dwith an y othe r

ven t stream

. (2) A temperatur e monitorin g devic e in th e firebo x equippe dwith a continuou s recorde r

an dhavin g a

n accurac y of

± 1 percen t

of th e temperatur e bein g measure dexpresse d i n degree s Celsiu s o r

±0.5°C , whicheve r i s greater , fo

r boiler s o r

proces s heater s o f les s tha n 4

4 M W (15 0 millio n Btu/hr ) desig n hea t

inpu t capacity

. (3 ) Monito r

an drecor ddi e period s o

f operatio n o

f th e boile r

o r proces s heate r i f th e desig n hea t

inpu t capacit y o

f th e boile r o r proces s heate r

i s 4 4 M W (15 0 millio n Btu/hr ) o r

greater

. Tb e record s mus t b e readil y availabl e fo

r inspection

. (d) Th e owne r

o r operato r o f a n affecte dfacilit

y tha t seek s t o demonstrat e complianc e with th e TR E inde x valu e limi t

specifie dunde r S 60.702(c ) shal l install , calibrate , maintain , an doperat e accordin g t o manufacturer' s specification s th e followin g equipmen t

unles s alternativ e monitorin g procedure s o r requirement s ar e approve dfo

r tha t facilit y b y di e Administrator

. (1 ) Wher e a n absorbe r

i s th e fina

l recovery devic e in th e recovery system : (i ) A scrubbin g liqui dtemperatur e monitorin g devic e havin g a n accurac y o f ± 1 percen t

o f th e temperatur e bein g monitore dexpresse di n degree s Celsiu s o r ±0. 5 *C , whicheve r

i s greater , an da specifi c gravity monitorin g devic e havin g a n accurac y o

f ±0.0 2 specifi c gravity uni t

eac h equippe dwith a continuou s recorder , o r (ii ) A n organi c monitorin g devic e use d t o indicat e th e concentratio n leve l o i organi c compound s exitin g di e recovery devic e base do n adetectio n principl e suc h a s infra-red , photoianization , o r therma l conductivity , eac h equippe d with acontinuou s recorder

. (2) Wher e acondense r

i s th e fina

l recovery devic e in th e recovery system : (i) A condense T exi t

(produc t side ) temperatur e monitorin g devic e equippe d witi i acontinuou s recorde r an dhavin g a n accurac y o

f ± 1 percen t

o f th e temperatur e bein g monitore dexpresse d i n degree s Celsiu s o r

±0. 5 °C

. whicheve r

i s greater , o r (ii ) A n organi c monitorin g devic e ust d t o indicat e th e concentratio n leve l o f organi c compound s exitin g th e reco \cr y devic e base don adetectio n principl e suc h a s infra-red , photcionizalion , o r therma l conductivity , eac h equippe d witi i acontinuou s recorder

. (3 ) Wher e acarbo n adsorbe r i s th * fina l recovery devic e uni t

in th e recovery system : (i ) A n integratin g stea mflow monitorin g devic e havin g an accur-.ic y o f ±1 0 percent , an dacarbo n be d temperatur e monitorin g devic e havin g a n accurac y o

f ± 1 percen t

o f th e temperatur e bein g monitore dexp : esse d i n degree s Celsiu s o r

±0. 5 °C

. whicheve r

i s greater , both equippe d wit h acontinuou s recorder , o r (ii ) A n organi c monitorin g devic e use d t o indicat e di e concentratio n leve l o f organi c compound s exitin g th e recovery devic e baae don adetectio n principl e suc h a s infra-red , photoionization , o r therma l conductivity , eac h equippe d with acontinuou s recorder

. (e ) A n owne r o r operato r o f a n affecte dfacilit

y seekin g to demonsttut e complianc e wit

h th e standard s specifie d unde r § 60.702 wit

h contro l device s othe r tiian incinerator , boiler , proces s heater , o r flare: o r recovery device s othe r tha n an absorber , condenser , o r carbo n adsorbe r

shal l provid e t o th e Administrato r

informatio n describin g th e operatio n o

f di e contro l devic e o r recovery devic e an dth e proces s parameter(s ) tha t

woul dindicat e proper operatio n an dmaintenanc e o f th e device

. Th e Administrato r ma y reques t further informatio n an dwil l specif y appropriat e monitorin g procedure s o t requirements

. §60.70 4 Tes t method s an d procedures

. (a ) Fo r th e purpos e o

f demonstratin g complianc e with 9 60.702 , al l affecte d facilitie s shal l b e run a t

ful l operatin g condition s an dflow ra!e s durin g an y performanc e test

. (b ) Th e followin g method s in appendi x A to thi s part , excep t a s provide dunde r

9 60.8(b) , shal l b e use d a s referenc e method s to determin e complianc e wit

h th e emissio n limi t

o rpercen treductio n efficienc y specifie d

unde r § 60.702(a)
. (1 ) Metho d 1 o r IA , a s appropriate , fo r selectio n o f

th e samplin g sites
. Th e contro l devic e inle tsamplin g sit e fo r determinatio n o f

ven tstrea m mola r compositio n o r TO C (les s methan e an d ethane ) reductio n efficienc y shal l b e prio r to th e inle to f

th e contro l devic e an d afte r th e recover y system . (2 ) Metho d 2
. 2A , 2C , o r 2D , a s appropriate , fo r determinatio n o f th e ga s volumetri c flow rates . (3 ) Th e emissio n rat e correctio n factor , integrate d samplin g an d analysi s procedur e o f

Metho d 3 shal l b e use d t o determin e th e oxyge n concentratio n (%02 d ) fo r th e purpose s o f

determinin g complianc e wit h th e 2 0 ppm v limit
. Th e samplin g sit e shal l b e th e sam e a s tha t o f th e TO C sample s an d th e sample s shal l b e take n durin g th e sam e tim e tha t th e TO C sample s ar e taken . Th e TO C concentratio n correcte d t o 3 percen tO j (C J shal l b e compute d usin g th e followin g equation :

17. 9

Cc=Croc = 20.9-%0i d Where : C , =Cortcentratio

n o f TOC correcte

d t o 3 percen tOi
. dr y basis , pp

m b y volume . CT.<-=Concentratio n o

f TO C (minu s methan e an d ethane) , dr

y basis , pp

m by volume . %iht— Concentration o f Oj
. dr y basis , percen

t b y volume . (4) Metho d 1 8 t o determin e th e concentratio n o f

TO C i n th e contro l devic e outle tan d th e concentratio n o f TO C i n th e inle twhe n th e reductio n efficienc y o f

di e contro l devic e i s t o b e determined
. (i ) Th e samplin g tim e fo r eac h run sha d b e 1 hou r i n whic h eithe r a n integrate d sampl e o r fou r gra b sample s shal l b e taken . I

f gra b samplin g i s use d the n th e sample s shal l b e take n a t15
- minut e intervals
. (ii ) Th e emissio n reductio n (R ) o f TO C (minu s methan e an d ethane ) shal l b e determine d usin g th e followin g equation :

Ei-E
. X10 O

where : R= Emission reduction , percen tby weight
. E,=Mas o rat

e o f TO C enterin g th e contro l device , k g TOC/hr
. E„-Mao o rat

e o f TOC discharge

d t o th e atmosphere , k

g TOC/hr
. (iii ) Th e mas s rate s o f

TO C (Et

. E„ ) shal l b e compute d usin g tiie followin g equations : n E,=K 8 ( X CMi ) Q

i i = *

*%=K* ( 2 C*H» > Q o i= *
where : Croc=Concentration o

f sampl e componen

t "j " o f di e ga s strea

m a tdi e inle tan d outle to f th e contro l device , respectively , dr y basis , pp

m by volume . M„ . Mo=Molecula r weighto f sampl e componen

t"j " o f the ga s strea

m a tth e inle tan d outleto f th e contro l device , respectively , g/g-mol e (lb/lb-mole)
. Qi
. Q 0 =Flo w rat

e o f ga o strea m a tth e inle t and outleto

f the contro

l device , respectively , dscm/mi n (dscf/min)
. Ka=2.49 0 X 10-."(l/pm)(g-mole/scm)(kg / g)(min/hr) , wher

e standar d temperatur

e fo r (g-mole/scm ) i

o 20* C (iv ) Th e TO C concentratio n (Croc) i s th e su m o f

di e individua l component s en d shal l b e compute d fo r eac h run usin g th e followin g equation :

n Cro c = X C

j 1= 1
where : CTOC=Concentratio

n o f TOC (minu

s methan e an d ethane) , dr

y basis , pp

m b y volume . C,=Concentratio n o

f oampl e componen

t"j"
. dr y basis , pp

m b y volume . n=Numbe r o

f component

s in th e sample . (5 ) Whe n a boile r o r proces s heate r wit h a desig n hea tinpu tcapacit y o f 4 4 M W (15 0 millio n Btu/hour ) o r greate r i o use d t o see k t o compl y wit h g 60.702(a)
. th e requiremen tfo r a n initia l performanc e tes ti s waived , i n accordanc e wit h g 60.8(b)
. However , th e Administrato r reserve s th e optio n t o requir e testin g a tsuc h othe r time s a s ma y b e required , a s provide d fo r i n sectio n 11 4 o f

th e Ac t (c ) Whe n a flar e i o use d t o see k t o compl y wit h g 60.702(b) , th e flar e shal l compl y wit h th e requirement s o f g 60.16
. (d ) Th e followin g tes tmethod o i n appendi x A t o thi s part , excep ts o provide d unde r 0 60.8(b) , shal l b e use d a o referenc e metiiod s fo r determinin g di e ne theatin g valu e o f th s ga o combuste d t o determin e complianc e unde r 8 60.702(b ) an d fo r determinin g tiie proces s ven tstrea m TR E inde x valu e t o determin e complianc e unde r § 60.702(c)
. (l)(i ) Metho d 1 o r IA , a s appropriate , fo r selectio n o f

th e samplin g site
. Th e samplin g sit e fo r th e ven tstrea m mola r compositio n determinatio n an d flow rat e prescribe d i n g 60.704(d)(2 ) an d (d)(3 ) shal l be , excep tfo r th e situation s outline d i n paragrap h (d)(1)(H ) o f this section , prio r t o th e inle to f an y contro l device , prio r t o an y post-reacto r dilutio n o f th e strea m wit h air , an d prio r t o an y post-reacto r introductio n o f halogenate d compound s int o di e proces s ven tstream . N o travers e sit e selectio n metho d i s neede d fo r vent s smalle r tha n 4 inche s i n diameter
. (ii ) I f an y ga s strea m othe r tha n th e reactor ven tstrea m i s normall y conducte d throug h th e final recover y device : (A ) Th e samplin g sit e fo r ven tstrea m flow rat e an d mola r compositio n shal l b e prio r t o th e final recover y devic e an d prio r t o th e poin ta twhic h an y nonreacto r strea m o r strea m from a nonaffecte d reacto r i s introduced
. (B ) Th e efficienc y o f

th e final recover y devic e i s determine d b y measurin g th e TO C concentratio n usin g Metho d 1 8 a t th e inle tt o th e final recover y devic e afte r th e introductio n o f al l ven tstream s an d a tth e outle to f

th e final recover y device
. (C ) Th e efficienc y o f

th e final recover y devic e shal l b e applie d t o th e TO C concentratio n measure d prio r t o th e final recover y devic e an d prio r t o th e introductio n o f

an y nonreacto r strea m o r strea m fro m a nonaffecte d reacto r t o determin e th e concentratio n o f TO C i n th e reacto r ven tstrea m fro m th e final recover y device
. Thi s concentratio n o f TO C i o the n use d t o perfor m th e calculation s outline d i n g 60.704(d ) (4 ) an d (5)
. (2 ) Th e mola r compositio n o f th e ven t strea m shal l b e determine d a s follows : (i ) Metho d 1 8 t o measur e the . concentratio n o f

TO C includin g thos e containin g halogens . (ii ) AST M D1946-7 7 t o measur e th e concentratio n o f

carbo n monoxid e an d hydrogen . (iii ) Metho d 4 t o measur e di e conten t o f wate r vapor . (3 ) Th e volumetri c flow rat e shal l b e determine d usin g Metho d 2 , 2A , 2C , o r 2D
. a s appropriate
. (•> ) Th e ne theatin g valu e o f Ui e ven t strea m shal l b e calculate d usin g th e followin g equation :

M T =K , ( 2 C.H, )

| = 1

where :

### Federa l Registe r /

Vol

. 55 , N a126 /

Friday , Jun e 29 , 1990 /

Propose dRule s 2697 5

--Ne t heatin g valu e o

f di e sample

. M] / sent , wher e th e net

enthalp y pe r

mol e o f ven t streami s base do n combustio n a t 2 5

" C an d76 0 m mHg

. bo t m e standar d temperatur e fo

r determining-th e volume correspondin g to on e mol e i s 2 0 *C , a s i n th e definitio n o

f Q , (ven t streamflo

w rate)

.
1
pp m 

### M

J Constant

. 1.74OM0- r

f \( moi e \( \ wher e standar dtemperature fo r ( mo! e ] i»20°C

.

C , = Concrr.tratio n o n awe t basi s o f compoun dj r

n ppm
. a s measure dfo

r organic s b y Metho d1 8 an dmeasure dfo r hydroge n an dcarbo n monoxid e b y AST M D1946-7 7 a s indicate din 8 60.704(d)(2)

. H,=N'e t hea t o f combustio n o

f compoun dj , kca!/g-mole , base do n combustio n a t 25
° C an d70 0 tri mHg

. Th e heat s o

f combustio n o

f ven t strea mcomponent s woul db e require dto b e determine d using AST M D2332-7 8 i

f publishe d value s ar e no t

availabl e o r

canno t b e calculated

. (5 ) Th e emissio n rat e o f TO C i n th e ven t strea mshal l b e calculate dusin g th e followin g equation : E - » c

- K

- U CM1Q

. 1= 1
where : E roc =Emissior

. rat e o

f TO C i n ih e sample , kg/h r Ki = Constant , 2.49

4 x 10"«(l/ppm)(g-mole/ scrn)fkg/g)(rr.in/hr) , wher e standar d temperatur e fo

r (g-moie/scm ) i s 2

0 ° C C,=Concentratio n on adr y basi s o f compoun dJ

. i n pp ma * aiea«uze db y Metho d1 8 a s indicate din { 60.704(d)(2) M j = Molecula

r weight o f sampl e J , g/g-mol e Q , = Ven t

strea mfla

w rat e (scm/min ) a t

a standar dtemperatur e o

f 2 0 * C (8 ) Th e tota l ven t

strea m concentratio n (b y volume ) o f compound s containin g halogen s (ppmv

. b y compound ) shal l b e summe dfromth e individua l concentration s o f compound s containin g halogen s whic h \ve: e

measure db y Metiio d18

. (e ) Fo r purpose s o f

complyin g with

. { f 60.702tc) , th e owne r

o r operato r o f a facilit y affecte db y thi s subpar t shal l calculat e th e TR E inde x valu e o f th e ven t strea musin g th e equatio n fo r incineratio n i n paragrap h (e)(1 ) o f thi s sectio n fo r

halogenate dven t

streams

. Th e owne r

o r operato r o f a n affected : facilit y wit h anonhalogenate dven t strea mshal l determin e th e TR E inde x valu e b y calculatin g value s usin g bot h th e incinerato r

equatio n i n paragrap h (e)(1 ) o f thi asectio n an dth e flar e equatio n i n paragrap h (e)(2 ) o f thi s sectio n an dselectin g tile lowe r o f th e tw o values

. (1 ) Th e equatio n fo r

calculatin g th s TR E inde x valu e o f

aven t strea m controlle db y a n incinerato r i s s s follows :

TR E = (a+bfQJ a "+c(CW+-l(qjlH T ) + etQ.r* , mr) a "**flYJ'-- ) ETO C

(i ) wher e fo r

aven t strea mflo w rat e (scm/min ) a t

astandar dtemperatur e o f 2 0 ° C tha t

i s greate r

tha n o r equa l t o 14. 2 scm/min : TRE-TR E inde x value

. Q.= = Veir t strea mflo w rat e (scm/min ) a t a stmid.-ir dtemperature o

f 2 0 "C

. H t = Vent strea mne t

heatin g valu e (MJ/scm)

. wher e th e ne t

enthalp y per

mol e o f ven t strea mi s base do n combustio n a t 25 * C an d76 0 m mHg , bu t th e standar d temperatur e for

determinin g di e volume correspondin g t o on e mol e i s 2 0 * C a * i n th e definitio n o

f Q , V

. = Q

. fo r al l vent strea mcategorie s liste d in Tabl e 1 excep t

fo r Categor y E ven t stream s wher e Y , = (Q. ) (Hr)/3.9

. E 10 C = Hourly emission s o f TO C reporte din kg/hr

. a , b , e , d , e
. an df

ar e coefficients

. Th e se t o f coefficient s tha t

appl y t o a ven t strea mca n b e obtaine dfro mTabl e 1

. BILUH 6 COO E 6M0-M- MP.2 5



### 2697 6 Federa l Register /

Vol

. 55 , No

. 12 6 /

Friday , Jun e 29.199 0 /

Propose dRule s

TABL E 1

. REACTO R PROCESSE S NSP S TR E COEFFICIENT S FO R VEN T STREAM S CONTROLLE D B Y A N INCINERATO R

DESIG N CATEGORY Al

. FO R HALOGENATE D PROCES S VEN T STREAMS

. I F 0 < NE T HEATIN G VALU E (MJ/scm ) < 3.5 : Q , • Ven tStrea m Flo w rat e (scm/min ) 14. 2 < 0 . < 18. 8 < 0 ? - 69 9 140 0 210 0 280 0 « s 

### ° s Q$ Q s O s 18. 8 69 9 140 0 210 0 280 0 350 0 19.6555 9

20.4884 8 40.8333 8 61.1782 8 81.5231 8 101.6660 8 0.2794 8

0.2794 8 0.3037 2 0.3188 7 0.3300 7 0.3390 2 0.7668 3

0.3092 9 0.3092 9 0.3092 9 0.3092 9 0.3092 9 -0.1317 3

-0.1317 3 -0.1317 3 -0.1317 3 -0.1317 3 -0.1317 3 0.0104 4 0.0104 4 0.0147 7 0.0180 9 0.0208 8 0.0233 5

DESIG N CATEGOR Y A2 . FO

R HALOGENATE D PROCES S VEN T STREAMS . I F NE T HEATING VALU E > 3. 5 MJ/scm :
Q . • Ven t Strea

m Flo w rat e (scm/min ) 14. 2 < Q , < 18. 8 18. 8 < Q f < 69 9 69 9 < Q , < 140 0 140 0 < Q , < 210 0 280 0 < Q J < 350 0 19.3120 3

20.1449 1 40.1462 5 60.1475 9 80.1489 2 100.1502 6 0.2709 9

0.2709 9 0.2944 9 0.3091 7 0.3200 3 0.3287 2 -0.2050 0

-0.2525 5 -0.2525 5 -0.2525 5 -0.2525 5 -0.2525 5 0.0104 4 0.0104 4 0.0147 7 0.0180 9 0.0208 8 0.0233 5

DESIG N CATEGOR Y B . FO

R NONHALOGENATE D PROCES S VEN T STREAMS . I F 0 < NE T HEATING VALU E (MJ/scm ) < 0.48 :

Ven t Strea

m Flo w rat e (scm/min ) 14. 2 < Q s < 134 0 134 0 " < 0 . < 269 0 269 0 < 0 , < 404 0 8.8431 2 17.5526 7 26.2572 1 0.1069 6

0.1162 3 0.1220 3 0.0918 8

0.0918 8 0.0918 8 -0.1725 2

-0.1725 2 -0.1725 2 0.0104 4 0.0147 7 0.0180 9

DESIG N CATEGORY C . FO

R NONHALOGENATE D PROCES S VEN T STREAMS . I F 0.4 8 < NE T HEATIN

G VALU E (MJ/scm ) < 1.9 :

Q « • Ven t Strea

m Flo w rat e (scm/min ) 14. 2 < Q , < 134 0 134 0 < Q , < 269 0 269 0 < Q , < 404 0 9.5678 3 18.9920 9 28.4163 5 0.0618 7

0.0672 3 0.070S 8 0.3230 3

0.3230 3 0.3230 3 -0.1631 6

-0.1631 6 -0.1631 6 0.0104 4 0.0147 7 0.0180 9

DESIG N CATEGOR Y D . FO

R NONHALOGENATE D PROCES S VEN T STREAMS . I F 1. 9 < NE T HEATIN G VALU E (MJ/scm ) < 3.6 :

Ven t Strea

m Flo w rat e (scm/min ) 14. 2 < Q , < 118 0 118 0 < Q I < 237 0 237 0 < Q ! < 355 0 6.8761 2 13.6086 6 20.3412 0 0.0703 6

0.0764 6 0.0802 8 0.0266 9

0.0266 9 0.0266 9 0.0104 4 0.0147 7 0.0180 9

DESIG N CATEGOR Y E . FO

R NONHALOGENATE D PROCES S VEN T STREAMS , I F NE T HEATING VALU E > 3. 6 MJ/scm :

Y , • Dilutio n Flo

w rat e (scVmln ) • (Q, ) (H T )/3. 6 14. 2 « Y . < 118 0 118 0 « Y " < 237 0 237 0 « Y , < 355 0 6.8761 2 13.6086 6 20.3412 0 -0.0073 0 -0.0073 0 -0.0073 0 0.0224 9

0.0244 5 0.0256 6 0.0104 4

0.0147 7 0.0180 9

WUJN O COO t MW-fO- C

### Federa l Registe r /

Vol

. 55 , No

. 12

6 / Friday , Jun e 29 , 1990 / Propose dRule s 2G97 7
(ii ) Fo r a ven tstrea m flow rat e (scm / min ) a ta standar d temperatur e o f 2 0 * C tha ti s les s tha n 14. 2 scm/min : TR E = TR E inde x value . Q , = 14. 2 scm/min
. H T = (FLOW

) (HVAL)/11 2 wher e di e following input

s ar e used : FLO W = Ven tstea m flow rat

e (scm/min) , at a standar d temperatur

e o f 29 0 * C HVA

L - Ven tstrea m netheatin g value (MJ

/ scm) , wher

e the netenthalpy pe

r mole o f ventstrea m i s base d o n combustion a t25 * C an d 78 0 m m Hg , bu tui e standar

d temperatur

e fo r determinin

g the volume correspondin

g to on e mole i s 2

0 * C a s i n definition o

f Q , Y , —14.2 scm/mi n fo

r al l ventstreams excep tfo r Categor y E ventstreams , wher e Y , - (14.2)(Hr)/3.6
. Ero c - Hourl y emission s o

f TO C reporte

d in kg/hr
. a . b , c , d. e , an d f

ar e coefficients
. Th e se to f

coefficient s tha tappl y t o a ven tstrea m ca n b e obtaine d from Tabl e 1
. (2 ) Th e equatio n fo r calculatin g di e TR E inde x valu e o f

a ven tstrea m controlle d b y a flare i s a s follows :

TR E : Ero c (

a (QJ+ b (Q."+ r (Q.)(Hr)-i- d (ErocJ+e )

where : TR E = TR E inde x value . Ero c = Hourl y emissio n rat

e o f TO C reporte d i n kg/hr
. Q , = Ven tstrea m flow rat

e (scm/min ) a

ta standar d temperatur

e o f 2 0 "C
. H

T * > Ven tstrea m netheating valu e (M] / scm)
. wher

e the ne tenthalpy pe

r mole o f offga s i tbase d o

n combustion a

t2 5 " C and 76 0 m m Hg , bu tthe standar

d temperatur

e fo r determinin

g the volume corresponding t

o on e mole i s 2

0 " C a s in definition o

f Q,
. a , b , c d , e , and f ar e coefficients
. Th e se to f coefficient s tha tappl y t o a ven tstrea m ca n b e obtaine d from Tabl e 2
.

TABL E 2.—REACTO R PROCESSE S NSP S TR E COEFFICIENT S FO R VEN T STREAM S CONTROLLE D B Y A FLAR E

Hr<11.2MJ/scm.

. H T >11. 2 MJ/scm. , 2.2 5 0.30 9 0.28 8

0.061 9 -0.18 3

-0.004 3 -0.008 1

-0.003 4 2.0 8

2.0 8

(f ) Eac h owne r o r operato r o f a n affecte d facilit y seekin g t o compl y wit h § 60.700(c)(2 ) o r § 60.702(c ) shal l recalculat e th e TR

E inde x valu e fo r th e affecte d facilit y wheneve r proces s change s ar e made . Example s o f proces s change s includ e change s i n productio n capacity , feedstoc k type , o r catalys t type , o r wheneve r ther e i s replacement , removal , o r additio n o f recover y equipment
. Th e TR

E inde x valu e shal l b e recalculate d base d o n tes tdata , o r o n bes tengineerin g estimate s o f th e effect s o f th e chang e o n th e recover y system . (1 ) Wher e th e recalculate d TR E inde x valu e i s les s tha n o r equa l t o 1.0 , th e owne r o r operato r shal l notif y th e Administrato r withi n 1 wee k o f th e recalculatio n an d shal l conduc ta performanc e tes taccordin g t o th e method s an d procedure s require d b y S 60.70 4 i n orde r t o determin e complianc e wit h 8 80.702(a)
. Performanc e test s mus tb e conducte d a s soo n a s possibl e afte r di e proces s chang e bu tn o late r tha n 18 0 day s fro m di e tim e o f

th e proces s change . (2 ) Wher e th e initia l TR E inde x valu e i s greater tha n 8. 0 an d th e recalculate d TRE inde x valu e i s les s tha n o r equa l t o 8. 0 bu tgreater tha n 1.0 , th e owne r o r operato r shal l conduc ta performanc e tes ti n accordanc e wit h § 60. 8 an d S 60.70 4 an d shal l compl y wit h { 60.703 , § 60.704 , an d 8 60.705
. Performanc e test s mus tb e conducte d a s soo n a s possibl e afte r th e proces s chang e bu tn o late r tha n 18 0 day s fro m th e tim e o f th e proces s change . (g ) An y owne r o r operato r subjec tt o th e provision s o f

thi s subpar tseekin g t o demonstrat e complianc e witi i S 60.700(c)(4 ) shal l us e Metho d 2 , 2A , 2C , o r 2 D o f appendi x A t o par t60 , a s appropriate , fo r determinatio n o f volumetri c flow rate . § 60.70 5 Reportin g an d recordkeepin g requirements

. (a ) Eac h owne r o r operato r subjec tt o S 60.70 2 shal l notif

y th e Administrato r o f th e specifi c provision s o f 9 60.70 2 ( 5 60.70 2 (a) , (b)
. o r (c) ) wit h whic h th e owne r o r operato r ha s electe d t o comply . Notificatio n shal l b e submitte d wit h th e notificatio n o f initia l start-u p require d b y $ 60.7(a)(3)
. I f a n owne r o r operato r elect s a ta late r dat e t o us e a n alternativ e provisio n o f § 60.70 2 witi i whic h h e o r sh e wil l comply , the n th e Administrato r shal l b e notifie d b y th e owne r o r operato r 9 0 day s befor e implementin g a chang e and , upo n implementin g di e change , a performanc e tes tshal l b e performe d a s specifie d b y S 60.70 4 withi n 18 0 days . (b ) Eac h owne r o r operato r subjec tt o th e provision s o f

thi s subpar tshal l kee p a n up-to-date , readil y accessibl e recor d o f th e followin g dat a measure d durin g eac h performanc e test , an d als o includ e th e followin g dat a i n th e repor to f th e initia l performanc e tes trequire d unde r 8 60.8
. Wher e a boile r o r proces s heate r wit h a desig n hea tinpu tcapacit y o f 4 4 M W (15 0 millio n Bru/hour ) o r greate r i s use d t o compl y wit h S 60.702(a) , a repor t containin g performanc e tes tdat a nee d no tb e submitted , bu ta repor tcontainin g th e informatio n i n S 60.705(b)(2)(i ) i s required
. Th e sam e dat a specifie d i n thi a sectio n shal l b e submitte d i n th e report s o f al l subsequentl y require d performanc e test s wher e eithe r th e emissio n contro l efficienc y o f a contro l device , outle tconcentratio n o f TOC , o r di e TR E inde x valu e o f

a ven tstrea m from a recover y syste m i s determined
. (1 ) Wher e a n owne r o r operato r subjec tt o th e provision s o f tiiis subpar t seek s t o demonstrat e complianc e wit h 8 60.702(a ) throug h us e o f eithe r a therma l o r catalyti c incinerato r (i ) Th e averag e firebo x temperatur e o f th e incinerato r (o r th e averag e temperatur e upstrea m an d downstrea m o f th e catalys tbe d fo r a catalyti c incinerator) , measure d a tleas tever y 1 5 minute s an d average d ove r th e sam e tim e perio d o f

th e performanc e testing , an d (ii ) Th e percen treductio n o f TO C determine d a s specifie d i n 8 60.704(b j achieve d b y th e incinerator , o r th e

### 2697 8 Federa l Registe r /

Vol

. 55

. No

. 12 6 /

Friday , Jun e 29 , 199 0 / Propose dRule s
concentratio n of

TO C (ppmv
. b y compound

) determine

d a s specifie d in 8 60.704(b) atth e outletof di e contro l devic e o n a dr

y basi s corrected t

o 3 percentoxygen . (2 ) Wher e a n owne r o r operato r subjectt o the provision s o

f thi s subpar

t seek s t o demonstrat

e compliance wit

h 8 60.702(a ) throug h us e o f a boile r o r proces s heate r (i ) A descriptio n o

f th e locatio n a

t whic h the ventstrea

m i s introduced int

o th e boile r o

r proces s heater , an

d (ii ) Th e average combustio n temperatur

e o f the boile r o

r proces s heate r wit

h a design heatinpu

tcapacit y o f less tha n 4 4 M W (15 0 million Btu/hr

) measure d atleas tevery 1 5 minute s and average d ove r the sam e tim e period o f th e performanc

e testing
. (3 ) Wher e a n owne r o r operator subjectt o di e provision s o

f thi s subpar

t seek s t o demonstrat

e complianc e wit

h 8 60.702(b) throug

h us e o f a smokeles s flare , flar e design (i.e. , steam-assisted , air-assiste d o

r non-assisted) , al l visibl e emissio n readings , heatcontent determinations , flo w rat

e measurements , an d exi tvelocit y determinations mad

e durin g th e performanc

e tes tcontinuou s record s o f th e flar e pilotflam

e monitoring , an

d record s o f al l period s o

f operation s durin g whic h di e pilotflam

e i s absent . (4 ) Wher e a n owner o r operator subjectt o di e provision s o

f thi s subpar

t seek s t o demonstrat

e compliance wit

h 8 60.702(c) : (i) Wher e a n absorber i s th e fina

l recover y devic e i n the recover

y system , the exi tspecifi c gravit

y (o r alternative paramete r whic h i s a measur

e o f th e degre e o f absorbing liqui d saturation , i f approved by the Administrator) , and average exi ttemperatur

e o f the absorbing liquid , measured atleas t ever y 15 minutes an

d averaged ove r di e sam e time perio d o

f di e performanc

e testin g (bot

h measured whil e di e vent strea m i s normall

y route d and constituted) , o

r (ii) Wher e a condense r i s di e fina

l recover y devic e i n di e recover

y system , the average exi t(produc

tside ) temperatur

e measured a

tleas tever

y 15 minutes and average d ove r th e sam e tim e period o f th e performanc

e testin g whil e the ven tstrea

m i s route

d an d constitute d normally , o

r (iii ) Wher e a carbon adsorber i s di e fina l recover y devic e i n the recover

y system , th

e tota l stea m mas s flow measured atleas tever

y 1 5 minute s and average d ove r di e same time perio d o f th e performanc

e tes t(ful l carbo n be d cycle) , temperatur

e o f the carbon be d afte r regeneratio n (an

d withi n 1 5 minute s o f completio n o

f any coolin g cycle(s)) , an

d duratio n o f th e carbon bed steaming cycl e (al l measured whil e the

ven tstrea m f a route d and constitute d normally) , o r (iv) A s a n alternativ e t

o 8 60.70 5 (bpjti l (bJHJC

m o r [hmm. th e concentratio n leve l o

r reading indicate d b y th e organics monitorin g devic e a tth e oude tof th e absorber , condenser , or carbon adsorber, measured a tleas t ever y 1 5 minutes and average d ove r th e same tim e perio d o f di e performanc

e testin g whil e the ven tstrea m i s normall

y route d and constituted
. (v) Al l measurement

s and calculation s performe d t o determin

e the TR E inde x valu e o f the vent.stream . (c ) Eac h owne r o r operato r subjectt

o th e provision s of

thi s subpar

tshal l kee p up-to-date , readil y accessibl e continuou s record s ofth e equipmen t operating parameter

s specifie d t

o b e monitore d unde r 8 60.70 3 (a ) and (c ) a s wel l a s up-to-date , readil y accessibl e records o f period s o f operatio n durin

g which th e parameter boundarie s establishe d durin

g di e mos trecent performanc

e tes tar e exceeded . The Administrato r ma

y a tan y tim e requir e a repor to f tiiese data . Wher e a combustio n devic e i s use d t o compl y wit h 8 60.702(a) , period s o

f operation durin g which the parameter boundarie s establishe d durin

g th e mos trecent performanc

e test s ar e exceede d ar

e define d a s follows : (1 ) Fo r therma l incinerators , al l 3-hou

r period s o f operatio n durin

g whic h the average combustio n temperatur e wa s mor e tha n 2 8 X (50 °F

) belo w di e averag e combustio n temperatur e durin g the mos trecentperformanc e tes tat whic h complianc e wit

h 8 60.702(a

) wa s determined
. (2 ) Fo r catalyti c incinerators , al l 3
- hou r period s o

f operatio n durin

g whic h di e averag e temperatur

e o f th e vent strea m immediately befor

e the catalys t be d i s mor

e tha n 2 8 " C (5 0 °F ) belo w the averag e temperatur

e o f the ven tstrea

m durin g di e mos trecen tperformanc e tes t a twhich complianc e wit

h 8 60.702(a

) wa s determined
. Th e owne r or operato r als o shal l recor

d all 3-hou

r period s o

f operatio n durin

g whic h the average temperatur

e difference acros s the catalys tbe d i s les s tha

n 8 0 percen to f th e averag e temperatur

e difference o

f the devic e durin

g th e mos trecent performanc

e tes ta twhic h compliance wit h 8 60.702(a

) wa s determined
. (3) Al l 3-hou

r period s o

f operatio n durin g whic h di e averag e combustio n temperatur

e wa s mor

e tha n 2 8 * C (5 0 °F ) belo w the average combustio n temperatur

e durin g di e mos trecen

t performanc

e tes ta twhich compliance wit h 8 66702(a ) wa s determined fo r boiler s o r proces s heaters wit

h a design hea tinpu

tcapacit y of less tha n 44 M W (150 millio n Btu/hr)
. (4 ) Fo r boiler s o r proces s heaters , wheneve r ther

e i s a change i n the locatio n a twhic h th e ven tstrea

m i s introduced int

o th e flame xnrr

e a s require d unde r 8 60.702(a)
. (d) Eac h owne r o r operato r subjectt o th e provision s o

f thi s subpar

tshal l kee p u p t o date , readily accessibl e continuou s records o f di e indicatio n o

f flow specifie d unde

r 8 60.703(a)(2) , 8 60.703(b)(2

) and 8 60.703(c)(1)
. a s wel l a s up-to-date , readil y accessibl e records o f all period s whe n the ventstrea m i s diverte d fro

m the contro

l devic e o r has n o flow rate . (e ) Eac h owne r or operator subjec tt o the provision s o

f tins subpar

twh o use s a boile r o r proces s heate r witi i a design hea tinpu tcapacit y o f 4 4 M W o r greater t o comply with 8 60.702(a

) shall keep a

n up-to-date , readily accessibl e recor d o f all period s o

f operatio n o

f the boile r o

r proces s heater . (Examples o f suc h record s coul d includ e records o f stea m use , fue l use , o r monitorin

g dat a collecte d pursuan

tt o other Stat

e o r Federa l regulator

y requirements. ) (f ) Eac h owne r or operato r subjectt o th e provision s o

f thi s subpar

tshall keep up-to-date , readil y accessibl e continuou s record s o

f di e flar e pilot flam e monitorin

g specifie d unde

r 8 60.703(b) , a s wel l a s up-to-date , readil y accessibl e records o f al l periods o f operation s in whic

h th e pilo tflame i s absen t (g ) Eac h owne r o r operator subjec

tt o th e provision s o

f thi s subpar

tshal l keep up-to-date , readily accessibl e continuou s record s o

f di e equipmen

t operating parameter

s specifie d t

o b e monitore d unde r 8 60.703(d)
. a s wel l a s up-to-date , readil y accessibl e records o f period s o f operation durin

g whic h th e parameter boundarie s establishe d durin g the mostrecentperformanc e tes t ar e exceeded . The Administrato r ma y a t an y tim e requir

e a repor to f tiiese data . Wher e a n owne r o r operato r seek s t

o compl y wit h 6 60.702(c) , period s o

f operatio n durin

g whic h di e paramete

r boundarie s establishe d durin g the mos t recentperformanc

e tes tor e exceede d ar e defined a s follows : (1 ) Wher e a n absorbe r i s di e fina

l recover y devic e i n a recover

y system . an d wher e a n organic compoun

d monitorin g devic e i s notused : (i ) All 3-hou

r period s o

f operation durin g which th e average absorbing liquid temperatur

e wa s mor

e tiian 1 1 *

C (2 0 *F ) abov e di e averag e absorbing liqui d temperatur

e durin g the most recen tperfonnance tes to

r (ii ) Al l 3-hou

r period s of

operatio n durin g which th e average absorbing

# I

Federa l Risgista g /

Vol

. 55 , No

. 12 0 /

Friday , Jun e 29 , 199 0 / Propose dRule s 2697 9 liqui dspecifi c gravity wa s mor e tha n 0. 1 uni t above , o r more tha n 0. 1 uni t

below , th e averag e absorbin g liqui dspecifi c gravity durin g th e mos t

recen t performanc e tes t

(unles s monitorin g o

f a n alternativ e parameter , whic h i s a measur e o f th e degre e o

f absorbin g liqui dsaturation , i s approve db y di e Administrator , in whic h cas e h e wil l defin e appropriat e paramete r boundarie s an dperiod s o f operatio n durin g whic h the y ar e exceeded)

. (2 ) Wher e acondense r

i s th e fina

l recovery devic e in asystem , an dwher e a n organi c compoun dmonitorin g devic e i s no t used , al l 3-hou

r period s o f operatio n durin g whic h th e averag e exi t (produc t side ) condense r

operatin g temperatur e wa s more tha n 8 ° C (1 1 *F ) abov e th e averag e exi t

(produc t side ) operatin g temperatur e durin g th e mos t recen t performanc e test

. (3 ) Wher e acarbo n adsorbe r i s th e final recovery devic e i n asystem , an d wher e a n organi c compoun dmonitorin g devic e i s no t

used : (i ) Al l carbo n be dregeneratio n cycle s durin g whic h di e tota l mas s stea mflow wa s more tha n 1 0 percen t belo w di e tota l mas s stea mflow durin g th e mos t recen t performanc e test , o r (ii ) All carbo n be dregeneratio n cycle s durin g whic h th e temperatur e o f di e carbo n be dafter

regeneratio n [an dafter completio n o

f an y coolin g cycle(s) ] wa s mor e tiian 1 0 percen t

greate r tha n th e carbo n be dtemperatur e (i n degree s Celsius ) durin g th e mos t

recen t performanc e tes t (4 ) Wher e a n absorber , condenser , o r carbo n adsorbe r

i s di e fina

l recovery devic e i n th e recovery syste man d wher e an organi c monitorin g devic e i s used , al l 3-hou

r period s o f operatio n durin g whic h th e averag e organi c compoun dconcentratio n leve l o r readin g o f organi c compound s i n di e exhaus t gase s i s more tiian 2

0 percen t greate r tha n th e exhaus t

ga s organi c compeun dconcentratio n leve l o r readin g measure db y th e monitorin g devic e durin g di e mos t

recen t performanc e test

. (h) Eac h owne r

o r operato r o f a n affecte dfacilit

y subjec t t o th e provision s o f thi s subpar t

an dseekin g t o demonstrat e complianc e witi i § 60.702(c ) shal l kee p up-to-date , readil y accessibl e record s of : (1 ) An y change s in productio n capacity , feedstoc k

type , o r catalys t type , o r cf an y replacement , remova l o r additio n o f recovery equipmen t

o r reactors ; (2 ) An y recalculatio n o

f tiie TR E inde x valu e performe dpursuan t t o § 60.704(f) ; an d (3 ) Th e result s of an y performanc e tes t performe dpursuan t

t o th e method s an d procedure s require db y g 60.704(d)

. (i ) Eac h owne r

o r operato r o f a n affecte dfacilit

y tha t seek s t o compl y with th e requirement s o

f thi s subpar t

b y complyin g with di e flow rat e cutof f i n g 60.700(c)(4) shal l kee p up-to-date , readil y accessibl e record s t o indicat e tha t th e strea mflow rat e i s les s tha n 0.01 1 scm/mi n an do

f an y chang e i n equipmen t

o r proces s operatio n tha t increase s th e operatin g ven t strea mflow rate , includin g ameasuremen t o f th e ne w ven t strea mflow rate

. (j ) Eac h owne r

o r operato r o f a n affecte dfacilit

y tha t seek s t o compl y with th e requirement s o

f tiiis subpar t

b y complyin g with th e desig n productio n capacit y provisio n i n g 60.700(c)(3 ) shal l kee p up-to-date , readil y accessibl e record s o f an y chang e i n equipmen t o r proces s operatio n tha t

increase s th e desig n productio n capacit y o f th e proces s uni t

in.whic h th e affecte d facilit y i s located

. (k ) Eac h owne r

an doperato r

subjec t t o th e provision s o

f thi s subpar t

i s exemp t fro mth e quarterl y reportin g requirement s containe di n § 60.7(c ) o f th e Genera l Provisions

. (I ) Eac h owne r

o r operato r tiiat seek s t o compl y with di e requirement s o f thi s subpar t b y complyin g with th e requirement s o

f g 60.70 0 (c)(2) , (c)(3)

. o r (c)(4 ) o r g 60.70 2 shal l submi t

t o th e Administrato r

semiannua l report s o

f th e followin g recorde dinformation

. Th e initia l repor t

shal l b e submitte dwithi n 8 month s afte r

th e initia l start-u p date

. (1 ) Exceedance s o

f monitore d parameter s recorde dunde r § 60.705 (c ) an d(g)

. (2 ) Al l period s recorde dunde r I 60.705(d ) whe n di e ven t

strea mi s diverte dfro

mth e contro l devic e o r

ha s n o flow rate

. (3 ) Al l period s recorde dunde r § 60.705(e) whe n di e boile r o r proces s heate r wa s no t operating. (4 ) Al l period s recorde dunde r § 60.705(f ) i n whic h th e pilo t

flame o f di e flare wa s absen t (5 ) An y chang e i n equipmen t o r proces s operatio n tiiat

increase s th e operatin g ven t

strea mflow rat e abov e th e lo w flow exemptio n leve l i n § 60.700(c)(4) , includin g ameasuremen t o f di e ne w ven t

strea mflow rate , a s recorde dunde r

§ 60.705(i)

. Thes e mus t b e reporte da s soo n a s possibl e after di e chang e an dn o late r

tha n 18 0 day s after th e change

. A performanc e tes t mus t b e complete dwithi n th e sam e tim e perio d t o verif y di e recalculate dflo w valu e an d t o obtai n th e ven t

strea mcharacteristic s o f heatin g valu e an dEroc

- Th e performanc e tes t

i s subjec t t o th e requirement s o

f g 60. 8 o f di e Genera l Provisions

. Unles s th e facilit y qualifie s fo r a n exemptio n unde r

th e lo w capacit y exemptio n statu s i n g 60.700(c)(3) , th e facilit y mus t begi n complianc e wit

h th e requirement s se t

fort h in g 60.702

. (6 ) An y chang e i n equipmen t o r proces s operation , a s recorde dunde r g 60.705(j) , tha t

increase s th e desig n productio n capacity abov e th e lo w capacit y exemptio n leve l i n § 60.700(c)(3 ) an dth e ne w capacity resultin g fro

mth e chang e fo

r th e reacto r proces s uni t

containin g th e affecte d facility

. Thes e mus t

b e reporte da s soo n a s possibl e after

di e chang e an dn o late r tha n 18 0 day s after

th e change

. A performanc e tes t

mus t b e complete d withi n th e sam e time perio dt o obtai n di e ven t strea mflow rate , heatin g value , an dEroc

- Th e performanc e tes t i s subjec t t o th e requirement s o

f g 60. 8 o f th e Genera l Provisions

. Unles s th e facilit y qualifie s fo

r a n exemptio n unde r th e flow exemptio n in g 60.700(c)(4) , th e facilit y mus t begi n complianc e wit

h th e requirement s se t

fort h i n g 60.702

. (7 ) Any recalculation o

f th e TR E inde x value , a s recorde dunde r

§ 60.702(h)

. (m ) Th e requirement s o

f § 60.705(1 ) remai n i n forc e unti l an dunles s EPA , in delegatin g enforcemen t

authority to a Stat e unde r

sectio n 111(c ) o

f th e Act , approve s reportin g requirement s o r an alternativ e mean s o

f complianc e surveillanc e adopte db y suc h State

. I n dia t even t affecte dsource s witiii n th e Stat e wil l b e relieve do

f th e obligatio n t o compl y witi i g 60.705(i) , provide ddiat the y compl y with th e requirement s establishe db y th e State

. (n ) Eac h owne r

o r operato r tha t seek s t o demonstrat e complianc e wit h g 60.700(c)(3 ) mus t

submi t t o th e Administrato r

a n initia l report

detailin g di e desig n productio n capacit y o f th e proces s uni t (o ) Eac h owne r

o r operato r dia t seek s t o demonstrat e complianc e with g 60.700(c)(4) mus t

submi t t o di e Administrato r

a n initia l report

includin g aflow rat e measuremen t

usin g th e tes t method s specifie di n g 60.704

. (p ) Th e Administrato r

wil l specif

y appropriat e reportin g an drecordkeepin g requirement s wher e th e owne r o r operato r o f an affecte dfacilit

y complie s with th e standard s specifie dunde r § 60.70 2 othe r than a s provide dunde r § 60.70 3 (a) , (b) , (c) , an d(d)

. § 60.70 3 ftoconotructtsn. (a ) Fo r purpose s o

f thi s subpar t

"fixe d capita l cos t

o f di e ne w components. " a s use di n g 60.15 , include s th e fixe d capita l cos t

o f al l depreciabl e component s whic h ar e o r

wil l b e replace dpursuan t

t o al l continuou s program s o

f componen t

replacemen t

### 2698 0 Federa l Registe r /

Vol

. 55 , Ne

. 12 6 /

Friday

. Jan e 29 , 1990 /

Propose dRule s
which ar e commenced withi n an

y 2-yea r perio d followin g Jun

e 29,1990
. Fo

r purpose s o

f thi s paragraph , "commenced " mean s thatan - owne r a r operato r ha s undertake

n a com*inuou

# progra m o f componen

treplacemen

to r tha ta n owne r or operator ha s entere d int o a contractua

l obligatio n t o undertak e and complete , withi n a reasonabl e time , a continuou s progra m o f componen

treplacemen t §60.70 7 CtMmical s affecte d b y subpar t RRR

.

Chemica l nam e
Acetaldehyde.

. Aceti c aad. - Aceti c anhydrid e Aceton e . Aceton e cyanohydrin.

. Acetylen e

_ Acryli c aci d — Acrytonitrite Adipi c acid.

. Adipofiitiilo

. Alcohols , C-1 1 o r lower , mixture * Alcohotoa , C-1 2 o r higher , mixture*

. Alcohols , C-1 2 o r higher , unmixed.. - Ally l chlorid e _... . Amylene...

. Amytenes , mixed.

. Anilin e Benzen e Benzenesulfoni c aci d

__ Benzenesulfoni c aci d C, 0 >.-atky t de rivatives , aodki m salts

. Benzy l chlorid e Bispheno l A Brometon e 1.3-Butadien e .

__. . Butadien e an d buten e traction s .- . n-Butan e 1.4-Butanediol.

. Butanes , mixed..

. 1-Buten e 2-Buten e Butenes

. mixed..

. n-Buty l acetate..
. Buty l acrylate..

. n-Buty t alcoho l

_ sec-Buty l alcoho l ten-Buty l alcoho l Butyloenzy

t phthalate.

. tert-Buty l hydroperoxide.

. 2-Butyne-1.4«*o l ButyraldehydT

. Butyri c anhydrid e Caproiacta m Carbo n disulfid e Carbo n tetrachlorid e Crttoroaceti c aci d Chlorobenxen e Chlorodif luoromethane..

. Chlufuf(ovm

_- ... . p-Chlofonrtrobenzen * Citri c aci d Cumen e Cumen e hydroperoxide.

. Cyanuri c chlorid e Cyctohexan e Cydohexane , oxkfesd...

. CASNa '
75-07- 0 64-10- 7 108-24- 7 67-64- 1 75-66- 5 74-86- 2 76-10- 7 107-19- 1 124-04- 6 T11-68- 3

107-05- 1 513-35- 8 62-53- 3 71-43- 2 98-11- 3 66081-61- 2 100-44- 7 80-05- 7 76-08- 4 106-96- 0
106-87- 6 110-63- 4
106-96- 6 25167-67- 3 123-86- 4 141-32- 2 71-36- 3 78-93- 2 75-65- 0 85-86- 7 75-61- 2 110-65- 6 123-72- 6 106-31- 0 105-60- 2 75-15- 0 56-23- 5 76-11- 6 108-60- 7 75-»5- 6 67-66- 3 100-00- 5 77-92- 6 98-82- 8 60-15- 6 108-77- 0 110-62- 0 66512-15- 2 Che n ricar nam e

Cyclohexano t Cydohexanon o Cydohoxanon e oxsno> » Cydohaxen e Cyclopropan e - Diaceton e alcoho l 1,4-OtcrttorooutBn e 3,4-Dichloro-t-buten a Dichlorodifluoromethano..

. Dichlorodimethytstlan e Dichlorofluoroniethan e Oiethanolamin a Diethylbonzon o ,.._.._.. _ Diethylen e glycol Di-isodecy t phthalat e Dimethy l terephthalat e 2,4-(an d 2,6HJtnitrotoluene

_ Dtocty t phthalate.

. Dodocono*.

. Dodecylbenzewe.

. wo wlinear — Dodecytbenzeneaultonl c acid Dodecytbenzenesulfoni c sodiu m set t Epichlorohydrt n Ethano l EthanolartWn*.

. Ethy l acetate Ethy l acrylate.

. Ethylbenzene.

. Ethy l chloride.

. Ethylen e . acid

.

Ethylen e dibromide Ethylen e dichlorid e .... . Ethylen e glycol.

. Ethylen e glyco l monbuty l ethe r Ethylen e glyco l monethy l ethe r ace tate
. Ethylen e glyco l monomethy l ethe r — Ethylen e oxid e

_ 2-Ethylhexy l alcoho l (2-Ethylhexy Q amin e 6-Ethy M ,2,3.4-tetrahydr o 9.10-entra cenedkme

. Formaldehyd e Glycerol—-..-........»

. - n-Heptane.._

_»__._.

_ Heptane s (mixed ) Hexamethylen e diamine.
- Hexamethyten e diamin e adipate Hexamethylenetetramin e Hexan e - Isobutane...

. Isobutano l

_ Isobutylen e laobytyraldehyd e I i Isopropanol — Ketsn e Linea r alcohol* , ethoxylated , mixed Linea r alcohols , ethoxylated , an d sulfated , sodiu m salt , mixed

. Linea r afcytbenzen e — Malei c anhydrid e Mesity l oxid e CA S NO. 1

10&-93- 0 108>-94- 1 100-64- 1 t10-83- 6 75-16- 4 123-42- 2 110-57- 6 64037-54- 3 75-71- 6 75-78- 5 75-43- 4 111-42- 2 25340-17- 4

Methanol.

. Methylamin e - ar-Methytbenzenediamine.

. Methy l chlorid e Methylen e chlorid e Methy l ethy l keton e Methy l isobuty l keton e Methy l methacrylat

e - m-46- »

26761-40- 0 120-61- 6 121-14- 2 606-20- 2 117-61- 7 25376-22- 7 27176-87- 0 25155-30- 0
106-66- 6 64-17- 6 141-43- 5 U1-78- 6 140-66- 6 100-41- 4 75-00- 3 74-85- 1 106-93- 4 107-06- 2 107-21- 1 111-76- 2 H1-15- 9
109-66- 4 75-21- 6 104-76- 7 104-75- 6 15547-17- 6
50-00- 0 56-61- 6 142-82- 5 124-06- 4 3323-63- 3 100-97- 0 110-54- 3 75-26- 6 78-63- 1 115-11- 7 78-84- 2 78-76- 4 78-79- 6 67-63- 0 463-51- 4

123-01- 3 106-31- 6 141-79- 7 67-56- 1 74-39- 5 25376-45- 8 74-87- 3 75-09- 2 78-93- 3 106-10- 1 60-62- 6 Chemica l nam e

1 -Methyl-2-pynoltiJono..

. Methy l tert-buty l ethe r

_ Naphthalen e
1-Nonen e Nony i alcohol.

. Nonytpbono J Nonylphenol

. ethoxylate d Octen e Oil-soluabl e petroleu m sulfonate , calciu m sal t Pentaerythrito i 3-Pentenenitril e Pentenes , mixe d

_ Perchchkxoethyten e 1-Phenytethy i hydroperoxide

. Phenytpropan e

_

_ Phthali c anhydride

. Proplonaldohyde.

. Propy l alcohoL— , CA S No. '

Propylen e glycol.

. Propylen e oxide

. Sorbito l Styrene

. Terephthali c aci d .- — Tetraethy t lea d - Tetrahydrofura n .'.
—— Tetr a (methy l ethyf ) lead.

. Tetramethy l lea d - - Toluen e „ ._ _ Toluen».2.4-dnvnin e Tokjene-2,4-(and , 2.6HMsocyanat e (80/2 0 mixture)

. i t T t t-TficntofO*jMn6yw>M*>«>»<-R—~»~.> H *.

. 1, 1 ^-Tnchtoi*o*Vittna > .„„..„.—..«....«« , TrrcNoroethy(«n « TncMorofluoconwthsn o — *

.... . 1. 1 A-Trichloro- 1 A2-trtlluoroethane..

. Triethanolejnine.- * ..—....— . Trlethylon o glycol—.—_...--—.—-

. Viny l acetat e

_ _ Vmy l chlorid e _.. . Vinyliden e chlorid e m-Xylen e o-Xylen e p-Xylene.

. Xylene s (mixed) - 672-50- 4 61-20- 3 68-95- 3 27215-95- 8 143-08-0 8 25154-52- 3 9016-45- 6 25377-63- 7

115-77- 6 4635-67- 4 109-67- 1 127-16- 4 106-95- 2 3071-32- 7 103-65- 1 75-44- 5 65-44- 6 74-66- 6 123-36- 6 71-23- 6 115-07- 1 57-65- 6 75-56- 9 50-70- 4 100-42- 5 100-21- 0 76-00- 2 109-69- 9 75-74- 1 106-66- 3 95-60- 7 26471-62- 5 71-56- 6 7640- 5 79-01- 6 75-69- 4 76-13- 1 102-71- 6 112-27- 6 108-05- 4 75-01- 4 75-35- 4 106-36- 3 95-47- 6 106-42- 3 1330-20- 7
'CA S number s refe r t o th e Chemica l Abstract * Registr y number s assigne d t o specifi c chemicals , isomers , o r mixture * o f chemicals

. Som e ieofner s o r mixture s tha t ar e covere d b y th e standard s d o no t hav e CA S number s assigne d t o them

. Th e standard s appl y to a l o f th e chemical s listed , whethe r CA S number s hav e bee n assigne d o r no t

860.70 8 Delegatio n o f authority

. (a ) I n delegatin g implementation an d enforcemen

tauthorit y t o a State unde

r sectio n 111(c

) o f di e Act, the authorities containe d i

n paragrap

h (b ) o f thi s sectio n shal l b e retained b y the Administrato r an

d no ttransferre

d t o a State
. (b ) Authoritie s whic

h wil l no tb e delegate d t

o States : i 60.703(e)
. [F R Do c 90-1426 6 File d 6-28-90 : 6:4 5 am j BILUN O COO

f 4M0-6O-

W