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### Document

Number: 

# 84 ) ll-B-5 8

Docket Number: 

# A-88-0 2

Printed 6/12/20089:03:31 AM

Sheet 84 of 99P. 2 

# MR I 1^ 1 A-88-0 2 JWES T RESEAR ( MIDWES T RESEARC H INSTITUT E I E

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e 35 0 40 1 Harriso n Oak

s Boulevard Cary

. N.C

. 2751 3



### Date : Octobe r 27 , 198 8

(Finalize dMarc h22 , 1989 ) Subject : Researc hStudy o f Mesh-Pa dan

dFiber-Be dM1s t Eliminator s Chromiu m Electroplatin g NESHA P EP A Contrac t 68-02-3817 ; ES D Projec t 85/02 a MR I Projec t 7717- K From : Robi nBarke r To : Andre w

M . Smit h ESD/ISB/SS S (MD-13 ) (r- i |RR 

### , _. ww r 

### !**. . U . S . Environmenta l Protectio nAgenc y 8 7 IDU

I 

### o I wv i : • Researc hTriangl e Park , NC 2771 1 • •'•• - ! 

### ^ I . Introductio n ; • . i

. . . . . ... „ .-.,•, ' 

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Ther e ar e fou r type s o f mis t eliminator s commonl y use dt o contro l aci dmis t generate dfro

m industria l processes . Th e fou r type s are : (1 ) fiber-bed ; (2 ) mesh-pad ; (3 ) packed-bed ; an d(4 ) chevron-blad e mis t eliminators . M1s t eliminator s hav e bee nuse dpredominantl y a s a secondar y contro l device , calle da nentrainmen t separator , afte r we t scrubber s an d absorbers . Mis t eliminator s contro l mis t b y a combinatio no f mechanism s includin g inertia l impaction , direc t interception , an dBrownia n diffusion . Th e contro l mechanism s fo r chevron-blad e an dpacked-be dmis t eliminator s ar e inertia l impactio nan ddirec t interceptio no f th e mist . Th e contro l mechanism s fo r mesh-pa dan dfiber-be dmis t eliminator s includ e inertia l impaction , direc t interception , an dBrownia ndiffusion . However , Brownia ndiffusio ni s a principa l contro l mechanis m onl y fo r fiber-be d mis t eliminators . Perry' s Chemica l Engineerin g Handboo k state s tha t a well-designe dmis t eliminato r ca nachiev e approximatel y 10 0 percen t remova l o f particle s abov e 5 micron s (ym ) (0.2 0 thousandth ^ o f a n inch [mils] ) insiz e a s a resul t o f impactio nan dinterception . Fo r particle s les s tha n3 u

m (0.1 2 mils ) i nsize , Brownia ndiffusio ni s require dt o achiev e hig

hremova l efficiencie s (9 5 t o 9 9 percent ) o f thes e smalle r particles . Collectio nefficiencie s fo r mis t eliminator s o f an y typ e ar e dependen t upo nth e ga s velocit y throug hth e unit . A s velocit y increases , collectio no f particle s throug hinertia l impactio nincreases . Consequently , lo

w ga s velocitie s wil l resul t i n les s tha noptimum efficiency . However , highga s velocitie s ca ncaus e collecte dparticle s t o b e reentraine di nth e ga s stream , whic hma y resul t i nlowe r overal l contro l efficiency . Therefore , ga s velocitie s shoul db e maintaine dhig h enoug ht o optimiz e collectio nthroug hinertia l impactio nye t no t caus e reentrainment .



## AP. 3

Th e followin g section s presen t a mor e thoroug hdiscussio no f mesh padan dfiber-be d mis t eliminators , includin g operatin g parameter s an d practice s an

d th e applicabilit y

o f thes e device s fo r controllin g chromi c aci d mist . A

thoroug hdiscussio no f chevron-blad e mis t eliminator s i s presente d i nChapte r 4 o f the Chromiu m Electroplatin g NESHAP Backgroun d Informatio nDocument . II . Mesh-Pa d Mis t Eliminator s Mesh-pa dmis t eliminator s consis t o f layer s o f interlocke d wir e o r plasti c filament s densel y packe d betwee ntwo supportin g grids . Althoug h thei r thicknes s an

ddensit y

ma y vary , mes hpad s commonl y use d ar e 1 5 centimeter s (cm ) ( 6 inche s [in.] ) thic k wit ha mes hdensit y o f 14 4 kijog^am s pe r cubi c mete r (kg/ m ) ( 9 pound s pe r cubi c foo t [lb/f t ] . Th e pressur e dropacros s mesh-pa d unit s typicall y range s betwee n0.2 5 an

d0.6 2 kilopasca l (kPa ) ( 1 an d 2. 5 inche s o f wate r colum n [in . w.c.] ) dependin g o nth e mes hdensity . Figur e 1 present s a schemati c o f a mesh-pa dunit . Th e mos t commo napplicatio nfo r mesh-pa d mis t eliminator s i nindustr y i s a s a nentrainmen t separator t o remov e droplet s entraine di nexhaus t gase s fro m scrubbers , absorbers , distillatio n columns , refiner y

towers , an

d evaporators . Mesh-pa d materia l i s availabl e throug hsevera l manufacturer s suc ha s Kimre , Inc . an

dOtt o H . Yor k Company . Factory-assemble d unit s ca nb e purchase d from

a variet y

o f ai r pollutio ncontro l equipmen t vendors . A . Contro l Mechanis m Th e principa l contro l mechanism s fo r mesh-pa d unit s ar e inertia l impactio nan

ddirecl : interception . Thes e contro l mechanism s ar e depicte d i nFigure s 2 an

d3 . Collectio nb

y impactio ni s simpl y the resul t o f larg e particle s (abov e 3 y m [0.1 2 mils ] i ndiameter ) wit hsufficien t velocit y collidin g wit hfiber s an d adherin g t o thei r surface . Indirec t interception , particle s attemp t t o follo w th e streamlin e around th e fibers , bu t du e t o thei r siz e an drelativ e velocity , ar e intercepte d b y th e flui d laye r tha t surround s th e fibe r surface . Collecte d liqui d droplet s flow

alon g th e fiber s t o a poin t wher e adjacen t fiber s cross . Thes e crossove r point s becom e rapidl y

loade d wit hliquid , an d droplet s drai nt o th e bottom

o f th e mis t eliminato r du e t o gravity . Som e particle s ar e als o remove db y Brownia ndiffusio n(o r Brownia n motion) ; however , thi s mechanis m i s no t a majo r facto r fo r particle s large r tha n3 y

m (0.1 2 mils) . Brownia nmotio ni s th e rando m movemen t o f particle s du e t o collision s ona molecula r o r atomi c level. 1 * Th e collectio no f smal l particle s i s a resul t o f rando m motio nwhic hplace s th e particle s o na collisio npat hwit hth e fiber s (se e Figur e 4) . Becaus e th e motio ni s random , th e mes hpa dmus t hav e a hig hdensit y (surfac e area-to-volum e ratio ) t o collec t a highpercentag e o f thes e smal l particles . Typically , mes hdensitie s ar e reporte d i nterms o f bul k density , (mas s pe r volum e units ) becaus e i t i s easie r t o measur e tha nth e surfac e area-to-volum e ratio . A s th e bul k densit y increases , th e surfac e area-to-volum e rati o wil l als o increas e becaus e mor e fiber s ar e compacte d

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IMPACTIO N Figur e 2

. Intertia l impaction." *



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DIREC T INTERCEPTION Figur e 3 . Direc t interception .



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DIFFUSIO N Figur e 4 . Brownia ndiffusion .

#P. 6

int o th e same volume . Availabl e literatur e suggest s tha t Brownia n diffusio nca naccoun t fo r th e collectio no f some particle s below 3 y m (0.1 2 mils ) i nmesh-pa dmis t eliminators . B . Operatin g Parameter s an dPractice s Th e fibe r siz e i nmesh-pa dunit s ca nvar y fro m abou t 0.01 5 c

m (0.00 6 in. ) t o 0.3 8 c m (0.1 5 in.) , dependin g upo nth e application . Pad thicknes s typicall y

range s fro

m 1 0 t o 1 5 cm

( 4 t o 6 in. ) wit hpressur e drop s betwee n0.2 5 an d0.6 2 kP a ( 1 an

d2. 5 in . w.c) . Typica l bul k mes h densitie s rang e fro

m 4 8 t o 52 9 kg/ m

( 3 t o 3 3 lb/f t ) . Collectio n efficienc y

i s clos e t o 10 0 percen t fo r particle s large r tha n5 y m (0.2 0 mils ) a t ga s velocitie s betwee nJ l and30 0 meter s pe r minut e (m/min ) (3 6 an d98 4 fee t pe r minut e [ft/min]) . Efficienc y o f thes e unit s drop s of f rapidl y

fo r particle s les s tha n5 y m (0.2 0 mils ) i ndiameter . Dr . Seymou r Calver t performe dtest s o nmesh-pa dunits t o evaluat e reentrainmen t o nunit s tha t wer e installe dverticall y i nhorizonta l duct s (se e Figur e 5 ) andunit s tha t wer e installe dhorizontall y i nvertica l duct s (se e Figur e 6) . Dr . Calver t foundtha t verticall y installe dunit s had : (1 ) highe r reentrainmen t velocitie s tha nhorizontall y installe d units becaus e verticall y installe dunit s provid e bette r liqui ddrainage ; an d(2 ) les s reentrainmen t a t th e same ga s velocit y tha nwit hhorizontall y installe dunits . T o offse t th e dro pi nefficienc y whe nparticle s below 5 y m (0.2 0 mils ) ar e encountered , two mes hpads i nserie s ca nb e used . Studie s performe da t Consolidate dChemica l Industries , Divisio no f Stauffe r Chemica l i nHouston , Texas , o na sulfuri c aci dproces s showe dtha t whe n two mes hpad s i nserie s ar e used , th e overal l performanc e o f th e uni t improved . Th e mes hpad s wer e installe d downstream o f a nabsorbe r t o collec t an

y sulfuri c aci dmis t forme di nth e stac k du e t o th e releas e o f unabsorbe dsulfu r trioxide . Th e firs t mes hpadi s mad e upo f fin e filament s an

di s operate dbeyondth e floo dpoin t t o enhanc e th e scrubbin g o f th e ga s stream , increas e it s velocity , andhenc e increas e impactio no f fin e particles . (Floodpoin t i s a ter m use dt o describ e th e situatio n wher e th e ga s flo w

rat e i s hig henoug ht o hampe r liqui dflo w throug hth e padan dproduc e a buildu po f liqui d inth e pad. ) Th e secondpadi s mad e u po f standar dfilament s an doperate dbelo w

th e floodpoin t t o catc han y reentraine dparticle s fro m th e firs t pad . Floodin g inth e firs t padca n b e assiste dby

wate r spray s an

dirrigation . Optimu m ga s velocitie s a t th e Housto nfacilit y

wer e foundt o b e betwee n27 4 an d32 9 m/mi n(90 0 an

d 1,08 0 ft/min) . C . Applicabilit y

t o Chromi c Aci dMis t Contro l
Contro l equipmen t vendor s typicall y d o no t recommendth e us e o f mesh-pa dmis t eliminator s fo r controllin g chromi c aci dmis t becaus e thes e unit s ten

dt o plu g u

pwhe noperate dunde r hig hinle t loadings . Mos t mesh padunit s tha t hav e bee ninstalle donchromiu m plating tank s d o no t hav e interna l wate r spray

system s tha t clea nth e mes hpa dan dpreven t buildu p o f chromiu

m tha t may

eventuall y

caus e pluggin g o f the pad . Unit s tha t



## 3 ~P. 7

PROCES S TANK MESH-PA D MIS T ELIMINATO R

VENTILATIO N HOO D

Figur e 5 . Mesh-pa dmis t eliminato r installe d verticall y

i nhorizonta l sectio no f duct .P. 8

/ MESH-PAD MIS T

ELIMINATO R

VENTILATIO N HOO D

Figur e 6 . Mesh-pa dmis t eliminato r installe d horizontall y

invertica l sectio no f duct .

/P. 9

8
contro l chromi c aci dmis t typicall y us e a pa

d tha t i s approximatel y 1 5 c m ( 6 in. ) thick , hav e a pressur e dro po f 0. 3 kP a ( 1 in . w.c) , an d ar e installe dhorizontall y i na vertica l sectio no f duct . Tes t result s ar e availabl e fro m tw o faci1i|i| s tha t us e mesh-pa d mis t eliminator s onhar dchromiu m platin g tanks . » Tabl e 1 present s a compariso nbetwee nth e tw o unit s tested. Uni t 1 achieve d 9 4 percen t contro l an

d Uni t 2 achieve d99 + percen t control . Th e uni t tha t achieve d 99 + percen t contro l ha s thre e technica l advantage s ove r th e uni t tha t achieve d9 4 percen t control : (1 ) th e uni t i s installe d vertically i na horizonta l sectio no f duc t a s Calver t recommend s fo r bette r drainag e an d les s reentrainment ; (2 ) tw o pad s ar e use d inseries ; an d (3 ) th e uni t i s equippe dwit ha ninterna l spra y system an d removabl e cove r t o allo w fo r th e cleanin g o f th e mes hpads . Thes e tes t result s show tha t mesh-pa d mis t eliminator s ca nb e use d t o efficientl y

contro l chromi c aci dmis t fro m chromiu m electroplatin g operations . III . Fiber-Be dMis t Eliminator s Ther e ar e thre e type s o f fiber-be d mis t eliminator s use d t o contro l fin e mis*£s : (1 ) hig hefficiency ; (2 ) highvelocity ; an d (3 ) spra y catcher . Fiber-be dmis t eliminator s ar e eithe r packed - o r wound-beds , fabricate d wit hglass , ceramic , plasty , o r meta l fiber s i nbul k (loose ) o r rovin g (rope ) for m (se e Figur e 7) . Th e individua l fiber s ar e usuall y les s tha n2 5 y

m ( 1 mil ) indiameter . Figur e 7^resent s a cross sectiona l vie w

o f th e high-efficienc y typ e unit . Fiber-be d mis t eliminator s hav e bee npredominantl y use dt o contro l aci d mist s fro m sulfuric , phosphoric , an dnitri c aci d plants . Th e tw o majo r supplier s o f fiber-be dmis t eliminator s ar e Ott o H . Yor k Compan y an d Monsant o Enviro Chem . A . Contro l Mechanis m Th e predominan t contro l mechanis m fo r th e high-velocit y an d SDj**aycatche r typ e fiber-be dmis t eliminato r unit s i s inertia l impaction . Monsant o Enviro-Chem performe d pilo t scal e testin g o f fiber-be d mis t eliminator s i n1968 . Tabl e 2 present s th e contro l efficiencie s tha t thes e typ e unit s achieve d durin g testin g whe nuse d t o contro l sulfuri c aci dmist. 1 Fiber-be d mis t eliminator s ar e abl e t o remov e smalle r particle s b

y inertia l impactio ntha nmesh-pa d mis t eliminator s becaus e o f th e highe r surfac e area-to-volume ratio s (3 0 t o 15 0 time s higher ) o f fiber-be dmis t eliminators . Th e predominan t contro l mechanis m fo r th e high-efficienc y

unit s i s Brownia ndiffusio nwhich , combine d wit hinertia l impaction , ha s bee ndemonstrate d t o resul t i n10 0 percen t contro l o f sulfuri c aci dmis t particle s abov e 3 y m (0.1 ^ mjls ^ an

d 9 5 t o 9 9 percen t contro l o f particle s below 3 y m (0.1 2 mils) . • »



# ?TABL E 1 . TES T RESULT S FO RMESH-PAD MIS T ELIMINATOR S Uni t 1 Uni t 2 Plan t Plan t nam

e Locatio n Descriptio no f mesh-pa d uni t Manufacture r No . o f pads : Spacin g betwee npads , c m (in. ) Thicknes s o f pad , c

m (1n.) 7 Mes hdensity , kg/ m

(lb/ft J ) Desig npressur e drop , kP a (in . w.c ) Desig nga s velocity , m/m1 n(ft/min ) Spray washdow

nsyste m Installatio ni nduc t Tes t result s Tota l current, ampere-hour s Inle t concentration , mg/dscm (gr/dscf ) Inle t emissio nrate , kg/ h(lb/h ) Outle t concentration , mg/dscm (gr/dscf ) Outle t emissio nrate , kg/ h(mg/h ) Collectio nefficiency , percen t Norfol k Nava l Shipyar d Portsmouth , Virgini a

Ott o Yor k Compan

y 1 NA a 15.(6.0 ) NA D
0. 3 (1.0 ) 18 0 (600 ) Non e Horizonta l

3,440 c 0.60 9 (0.00026) c e 0.008 7 (0.019) c f 0.025 7 (1.12x1 0 ) c e 0.0004 5 (0.001 ) 9 4 c e c e Precisio nMachin e an d Hydraulic , In c Worthington , W . Virgini a

ChromeTech , In c 2 1 0 (4 ) 7. 6 (3.0) , 3. 8 (1.5 ) 64. 0 (4.0 ) 0.6 2 (2.5 ) 15 0 t o 20 0 (50 0 t o 700 ) Interna l syste

m Vertica l

12,160 ° 11. 4 (0.00499) dr 0.082 9 (0.183) d / . , 0.032 6 (1.0x1 0 ) df
0.0002 3 (0.00051) df 99+ d •£ >

rHot applicable . ^No t available . ^Base d o naverag e o f thre e tes t runs . Base d o naverag e o f fiv e tes t runs . ^Base d o ntota l chromiu m analysis . Base d o nhexavalen t chromiu m analysis ,

' ^ * • o1 0 p.1 1

FIBE R PACKIN G

MIST-LADE N GA S CLEA N GA S

CONCENTRI C SCREEN S

LIQUI D OU T HAL F COUPLING

LIQUI D SEA L PO T

Figur e 7 . Cross-sectiona l view o f high-efficienc y typ e fiber-be dmis t eliminator .

./&TABL E 2 . OPERATIN GCHARACTERISTIC S OF VARIOU S TYPE S O F FIBER-BE D MIS T ELIMINATOR S A S USE D O N SULFURI C ACI D PLANT S » a Highefficienc y

Highvelocit y

Spray

catche r
Controllin g mechanis m fo r mis t collectio n

diffusio n Superficia l velocity , m/m1 n(ft/min ) 4. 5 t o 1 2 (1 5 t o 40 ) Efficienc y

o nsulfuri c aci d mis t particle s large r tha n3 y m (0.1 2 mil) , percen t 10 0 Efficienc y

o nsulfuri c aci d mis t particle s smalle r tha n3 y m (0.1 2 mil) , percen t
Pressur e drop , kP a (in . w.c. ) 1. 2 t o 3. 7 (4. 7 t o 15 ) Brownia n

12 0 t o 15 0 (39 0 t o 490 ) Essentiall y 10 0 95-99 +

1. 5 t o 2. 0 ( 6 t o 8 ) Impactio n

12 0 t o 15 0 (39 0 t o 490 ) Essentiall y 10 0 90-9 8

0. 1 t o 0.2 5 (0. 4 t o 1.0 ) Impactio n

Essentiall y

15-3 0

a Result s wer e obtaine d durin g pilot-scal e testin g b y Monsant o Enviro-Chem .

^
t oP.1 3

1 2
B . Operatin g Parameter s an dPractice s
A typica l fiber-be d cylinde r i s constructe d o f tw o concentri c screen s attache dt o a to pflang e an da bottom

drai nplate , eac ho f whic h typicall y

ha s 1-in . openings . Fibe r i s packe d int o th e annula r spac e betwee nthes e screens t o for m a bedwit ha radia l thicknes s o f 5 t o 8 c m ( 2 t o 3 in.) . Th e scree nframewor k tha t contain s th e fiber , along wit h th e to pflang e an

dbotto m plat e attachments , i s typicall y referre d t o a s a fiber-be dcage . Th e cage s ar e typicall y fabricate dfro

m eithe r meta l o r fiberglass reinforce dplastic . Th e fibe r bed s ma y b e forme d int o eithe r impactio n o r Brownian-diffusio n^p e beds , dependin g o nth e siz e o f th e fibe r wit h whic hthe y

ar e packed . A

typica l impactio ncylinde r ha s a noutsid e scree ndiamete r o f 6 6 c m (2 6 in.), x a bedthicknes s o f 5 c m ( 2 in.) , an

d a n overal l lengt ho f 18 0 cm (7 2 in.) . Typica l Brownian-diffusio ncylinder s hav e anoutsid e scree ndiamete r o f 6 1 c m (2 4 in.) , a.be d thicknes s o f 8 c m ( 3 in.) , an

da noveral l lengt ho f 30 5 c m (12 0 in.) . Pressur e drop s fo r impactio nunit s rang e fro m 0.1 5 t o 2. 0 kP a (0. 5 t o 8 in . o f w.c ) an d pressur e drop s fo r Brownian-diffusio nunit s rang e fro m 1. 2 t o 3. 7 kP a ( 5 t o 1 5 in . o f w.c) . Fiber-be dmis t eliminator s ar e als o equippe d wit htw o spray nozzles . On e spra y

nozzl e i s locate da t th e to p o f th e uni t an d i s use d t o was hdow

nany larg e particulat e tha t ma y clo g th e mis t eliminator , an d th e othe r spra y

nozzl e i s locate da t th e bottom o f th e uni t an

d i s use d a s anaeroso l spra y

t o remov e an

y contaminant s tha t ca ncrystalliz e i nth e mis t eliminato r an

dcaus e pluggin g o r imprope r drainage . Fiber-be dunit s ar e no t operate d wit hvertica l upflow o f gas ; a larg e amoun t o f contactin g equipmen t (e.g . fiber-be d size , transitio n zones , etc. ) woul db e require dt o slo w th e ga s velocit y

dow nbelow th e floodin g velocit y

becaus e th e floodin g velocit y decrease s wit h bed-specifi c surfac e area . (Floodin g velocit y i s th e velocit y

o f th e ga s strea m a t whic hreentrainmen t occurs.) . Fiber-be d unit s ar e designe d fo r horizontal , concurren t gas-liqui d flow throug hth e bed . Th e ga s an d liqui dflo

w t o th e downstream

fac e o f th e be d wher e th e liqui d drain s dow n th e oute r fac e t o th e sum pan dth e cleane d ga s flow s up an d ou t th e to p o f th e unit . A s wit hmesh-pa d mis t eliminators , ga s flo w rate s wit himpaction typ e fiber-be dunit s ar e limite d onth e lo w end b y th e decreas e in efficienc y

o f inertia l impaction . ° Th e Brownian-diffusio ntyp e unit s hav e n o lowe r limit^ nga s flo w rat e becaus e mis t collectio nincrease s a s ga s flo w decreases . Thi s effec t wil l continu e unti l th e ga s flo w rat e reache s zero . Th e maximu m ga s flo

w rat e infiber-be d mis t eliminator s i s limite db

y either : (1 ) decreas e inefficienc y withincreasin g ga s flo w rate ; o r (2 ) a gas-phas e pressur e dro plimitation . Fiber-be d mis t eliminator s hav e no limitation s oninle t loading s becaus e floodin g i s no t a problem ; the y hav e operate d wit hinle t loading s u pt o 10 6 gram s pe r cubi c mete r (4 6 grain s pe r cubi c foot ) wit hno

/*-P. M

1 3 observe dreentrainment . ° Mr . Prafe l Malka no f Monsant o Enviro-Che m indicate dtha t inoperation s wher e potentia l pluggin g o f th e fiber-be d mis t eliminato r exists , th e unit s ar e operate d wit hth e wate r spra y nozzle s inth e uni t activate dt o ai d inremova l o f particulat e buildup. 1 2 Inaddition , a facilit y operatin g a fiber-be d mis t eliminato r ma y choos e t o purchas e anadditiona l fibe r cag e s o tha t i f th e monitore d pressur e dro p exceed s th e desig nrange , th e fiber-be d cag e ca nb e remove d an d replace db

y the spar e cage . Th e plugge dcag e ca nthe nb e sen t bac k t o th e manufacture r t o b e rewoun dwit hne w fibe r material . C . Applicabilit y

t o Chromi c Aci dMis t Contro l Fiber-be dmis t eliminator s wer e firs t fabricate d b y Monsant o t o ai d insulfuri c aci dmis t control . Thes e device s hav e bee nver y successfu l fo r thi s typ e application . Th e Stat e o f California , i nconjunctio nwit h th e Meta l Finishin g Associatio no f Souther nCalifornia , currentl y plan s t o tes t th e contro l efficienc y o f fiber-be dmis t eliminator s fo r controllin g chromi c aci d mis t fro m electroplatin g operation s i nth e firs t quarte r o f 1989 . IV . Reference s 1 . Fair , J . Liquid-Ga s Systems . In : Perry' s Chemica l Engineer s Handbook . 6t hEdition . Perry , R . an d Green , D. , eds . Ne w York , McGra w Hil l Boo k Company . 1984 . p.18-7 8 2 . Referenc e 1 . pp . 18-8 3 an d18-84 . 3 . Holmes , T . L. , an dChen , G . K . Desig nan d Selectio no f Spray/M1s t Eliminatio nEquipment . Chemica l Engineering . Octobe r 15 , 1984 . p . 86 . 4 . Bethea , R . M . Ai r Pollutio nContro l Technology : AnEngineerin g Analysi s Poin t o f View . Va nNostrandReinhol d Company . Ne w York , New York . 1978 . pp . 146-148 . 5 . York , 0 . H . Performanc e o f th e Wir e Mes hDemister . Reprinte d fro m Chemica l Engineerin g Progress . Bulleti n635 . Parsippany , Ne w Jersey . 1963 . p . 2 . 6 . Calvert , S. , Yung , S. , an d Leung , J . Entrainmen t Separator s fo r Scrubbers : Fina l Report . U . S . Environmenta l Protectio nAgency , Offic e o f Researc han dDevelopment , Washington , D.C . Augus t 1975 . p . 71 . 7 . Massey , 0 . D . Demister s Fo r Sulfuri c Aci d Plan t Stacks . Chemica l Engineerin g Progress . Ma y 1959 . p . 117 . 8 . Norfol k Nava l Shipyard , Norfolk , Virginia . Source Emissio nTestin g o f th e Buildin g 19 5 Platin g Sho pa t Norfol k Nava l Shipyard , Portsmouth , Virginia . Marc h11-18 , 1985 . Nava l Energy and Environmenta l Suppor t Activity , Por t Hueneme , California . NEES A 2-124 . Ma y

1985 .


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1 4 9 . Draf t Emissio nTes t Report : Precisio nMachin e an d Hydraulic , Inc , Worthington , Wes t Virginia . Pee r Consultants , Inc. , Dayton , Ohio . Prepare d fo r U . S . Environmenta l Protectio nAgency , Researc hTriangl e Park , Nort hCarolina . Septembe r 1988 . 10 . Referenc e 3 , p . 87 . 11 . Brink , J . A. , Burgrabbe , W.F. , an d Greenwell , L.E . Mis t Eliminator s fo r Sulfuri c Aci d Plants . Chemica l Engineerin g Progress . Novembe r 1968 . p . 82-85 . 12 . Contac t Report . Barker , R. , MRI , wit hMalkan , P. , Monsant o Enviro Chem . Januar y

25 , 1989 . Informatio no ndesig nan d contro l o f fiber be d mis t eliminators .



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