P. 1 

# OAR Box 1123 Prepped by Ollie Stewart



## Document

Number: 

# 168 ) ll-B- 2 Docket Number: 

# A-84-4 4

Printed 4/16/20082:49:56

PM Sheet 168ofl 78P. 2



### R.JLS.05 0 Septembe r11 , 198

4 

# DRAFT - " JL-H.-2-

MEMORANDU

M TO : Docke t A-80-20 A FROM : Jeffre yL . Shumake r SUBJECT : Sweetening Cos t Factor s Purpos e .Develo p capita l an

d operating cos t factor s fo r estimating sweetening uni t cost s fo r a rang e o f wel l hea d ga s compositions . Summaryo f Factor s Smal l Larg e Facilitie s Facilitie s (DEA ; (Sulfinol ; <10 0 LT/D ) >10 0 LT/D ) $0.5 1 Componen t Capita l Cos t Unit s ,of , Facto r $0,06 4 Annualize d Capita l Cos t Operating an

d Maintenance : Regeneratio n Hea t Pumping Cos t Labo r Maintenanc e Supplie s Chemical s Tota l Operating an

d Maintenance : 

### $127,000/yea r+ $0.302 4 0 

### _^ Tota l Annualize d Cost :

$127,000/yea. r + $0.366 4 OR .

$0,25 7 $0.016 7 $127,00 0 $0.0 1 $0.018 7 $0.6 1 SCF D Acid ; 

### Ga s

$0,06 9 /yea r pe r SCF D Aci d Ga s $0,15 8 /yea r pe r SCF D Aci d Ga s $0,01 2 /yea r pe r SCF D Aci d Ga s i 

### $127,00 0 /yea r $0.01Z . /yea r pe r SCF D Aci d Ga s $0.018 7 /yea r pe r SCF D Aci d Ga s $0.2' H /yea r pe r SCF D Aci d Ga s

/yea r pe r SCF D Aci d Ga s 

## $0 .

# c p p 

### Docke t A-80-20 A

Pag e Two Septembe r 11 , 198 4 j,-.- ^ —= f Approac hBasi s fo r Smal l Facilit y (<10 0 LT/D ) Factor s Smal l facilitie s o f th e typ e likel y t o hav e advers e economi c impact s generall y

hav e a smal l percentag e o f aci dga s i nth e wel l hea dga s stream . A s a result , th e amin e sweetenin g processe s ar e commonl y use dfo r facilitie s o f thi s type . Fo r th e purpos e o f generatin g cos t factor s th e diethanolamin e proces s i s considered . Installe dcapita l cos t an doperatin g cos t factor s wher e develope d base doninformatio nlearne di ncontactin g 4 sweetenin g uni t desig nfirm s (Attachment s 1 throug h7) . Capita l Cos t Facto r Basis : $4000/GP M o f DE A circulatio ninstalle dcapita l cos t in mi d198 4 dollar s (Se e Attachmen t 1) . Othe r factor s ar e fro m Attachmen t 2 . Panita l rn*t

- $ 400 0 

### v

Ga 1 S 

### ° 1 > n

### y 1 bSo 1 

### ' n

### v

105.1 4 l b 

### uapita i ^ osz



### Gal/mi n x

### 8. 6 l bSol' n x

### 0.3 5 l bDEA x

### l bmol e DEA l bmol e DEA

l bmol e Day x

### 0. 5 l bmol e aci dga s 37 9 SC F x

### 2 4 x6 0 mi n Capita l Cos t = $0.51/SCF DAci dGa s (mi d198 4 dollars ) Annualize dCapita l Cos t Assumin g 2 0 yea r lif e an d1 0 percen t interes t rat e = $0.51/SCF Dx.1124 6 = $0.064/yea r pe r SCF DAci dGas . Operatin g Cost s 1 . Regeneratio nHeat : Basi s 95 0 BTU/Ga l DE A approximat e reboile r hea t dut y (Se e Attachmen t 2 , pg . 15-21) . Als o assume a valu e o f $3.3 5 pe r MMBT Uo f natura l ga s t o fir e th e reboile r (highen do f EAB' s pric e range) , an

dan8 0 percen t boile r efficiency . 95 0 BTU. Ga l Sol' n. . l bSol' n. . 105.1 4 1 b Hea t Cos t Ga l Sol' n A 

### 8. 6 l bSol" n A



### 0.3 5 l bDEA

A 

### l bmol e DEA l bmol e DEA

l bmol e _1

_ $3.3 5 35 0 Day s x

### 0. 5 l bmol e Aci dGa s x

### 37 9 SC F x

### .8 0 x

### MMBT Ux

### yea r

= $0.257/yea r pe r SCF DAci dGa sP. 4 ir f " T



## Docke t A-80-20 A Pag e Thre e Septembe r 11 , 198 4 2 . Pumpin g Cost : Th e pumping cos t i s a functio no f th e GP M o f amin e circulate dandth e pressur e p f the ga s inth e contacto r (i.e. , th e ga s wel l pressur e minu s transmit!o ntemperature) . Th e highe r th e pressur e th e highe r th e energ y

requiremen t andthu s the cost . Normall y contactor s ar e no t ru

nabov e 100 0 PSI . Wel l pressure s highe r tha nthi s generall y are le t downprio r t o sweetening . Lowe r pressure s wil l incu r lowe r pumping costs . Thus , i t i s assume dtha t th e contacto r operate s a t 100 0 PS I pressure . Furthe r i t i s assume dtha t a pum pefficienc y

o f 7 0 percen t i s achieved . Usin g th e hydrauli c horsepowe r equatio n (Perry' s 5t hEd. , pg . 6-3) , anassume denergy cos t o f $0.05/KWH , and othe r appropriat e factor s th e pumping cos t i s a s follows : Pumoin a Cos t = Hp100 0 PS I Ga l Sol' n Pumping Los t 17 

## i 4 PS 

## I-Ga l Sol'n/mi nx

## 1 x

## 8. 6 l bSol' n

l bSoT n 0.3 5 l bDE

A Day 2 4 x6 0 mi n .745 7 K

W $0.0 5 105.1 4 l bDE

A lbmol e 0.7 0 H p x

## KW H x

## l bDEA

x

## 37 9 SC F 840 0 h r yea r l..0167/yea

r pe r SCF DAci dGa s 3 . Operatin g andMaintenanc e Labor : On e perso npe r shif t fo r al l cases ; $14.50/h r labo r rat e = $127,000/year . 4 . Maintenanc e Supplies : Base don2 percen t o f capita l cos t

= $0.51/SCF Dx0.0 2 = $0.01/yea r pe r SCF DAci dGa s 5 . Replacemen t Chemicals : Base don-\>2 5 percen t pe r yea r replacemen t rat e anda DEA cos t o f $7.50/Ga l a 5 0 GP M amin e uni t incur s anannua l replacemen t cost s o f $7300/yea r i n198 4 dollar s (Attachmen t 1) . $730 0 1 Ga l Sol' nl bSoT n105.1 4 lb yea r x

## 5 0 Ga l Sol'n/mi nx

## 8. 6 l bSol' nx

## 0.3 5 lbDE A x

## l bmol e DE

A l bmol e DEA

lbmol e x

## 0. 5 l bmol e Aci dGa s x

## 37 9 SC F x 

## 2 4 x^mi n = 

## $0-0187/yea r pe r SCF D Aci dGa sP. 5 r|M"! i •- •



### Docke t A-80-20 A Pag e Fou r Septembe r 11 , 198 4 J'J' ^ Basi s fo r Larg e Facilit y Factor s Larg e plant s (>10 0 LT/ D sulfu r feed ) generall y emplo y a sweetenin g technolog y

tha t require s highe r capita l investmen t tha nth e DE A proces s bu t whic hha s lowe r operatin g cost s pe r uni t volume o f ga s treated . System s usin g sulfino l a s th e absorben t ar e commo ni nthi s large r siz e rang e andthi s proces s i s selecte da s th e basi s fo r estimatin g cost s fo r sulfu r fee drate s greate r tha n10 0 LT/D . Th e sulfino l process , lik e othe r processe s commonl y employe di nlarge r plants , i s a proprietar y proces s distribute dunde r licensin g agreements . Consequently , les s informatio ni s availabl e onthi s proces s inpubli c literatur e an dth e developmen t o f genera l cos t factor s involve s a highe r degre e o f approximatio nthanwa s neede dfo r th e DE A proces s factor s discusse dpreviously . Th e followin g assumption s ar e made : t Th e sulfino l solutio ni s 3 3 percen t solfolane , 33. 3 percen t di-isopropano l amine , an d3 3 percen t water . • Th e aci dga s picku prat e i s 10. 5 SCF/gallo nsolutio n(the midpoin t o f th e rang e i

nAttachmen t 2) . • Th e reboile r hea t dut y i s 113 5 Btu/gallo nleansolutio n(the midpoin t o f th e rang e i nAttachmen t 2) . • Solutio ndensit y i s 9. 1 lb/gallon ; averag e MW T o f solvent s i s 126.7 . • Th e capita l cos t o f th e sulfino l proces s i s 2 0 percen t highe r tha n th e DEA proces s capita l cost . Wit hthes e assumptions , th e cos t factor s canbe calculate da s follows : Capita l Cos t $0.51/SCF D x1. 2 = $0.61/pe r SCF D Aci dGa s Annualize dCapita l Cost : $.61/SCF D x.1124 6 = $0.069/yea r pe r SCF D Aci dGa sP. 6 -f i nn'! 1



## Docke t A-80-20 A Pag e Five Septembe r 11 , 198 4 Operating Cost s 1 . Regeneratio nHeat :

113 5 Bt uGa l SoT n1 $3,^ 5 350_Dav s Ga l SoT nA



## 10. 5 SC F Aci dGa s x

## .8 0 MMBt u x

## yea r

= $0.158/yea r pe r SCF DAci dGa s 2 . Pumping Cost : J B , . 100 0 PS I „ Ga l SoT n.745 7 K W 171 4 PSI-Ga l Sol'n/mi nx

## 1 x

## 10. 5 SC F x

## Hp - 

## ~

x

## W " x

## 2 4 x D 

## 6 ^ mi nx

## ^T^

= »^2/yea r pe r SCF DAci dGa s 3 . Operating an

dMaintenanc e Labor : (Sam e a s fo r DEA ) $127,000/yea r 4 . Maintenanc e Supplies :

$0.6 1 x.0 2 = $0.012/yea r pe r SCF DAci dGa s 5 . Replacemen t Chemicals : (Sam e a s fo r DEA ) $0.0187/yea r pe r SCF DAci dGa s JLS:d w Attachment s (7 )P. 7

•• r-irjj i 

### ATTACHMEN T 1 

# RADIA N

TELEPHON C CAL L RECOft O Qloco-11 * Cal l Oouctoln g tell Fatte n Callin g 

### Jeffre yL . Shumaker , Radia n Patto n Calla * 

### Ken t Carlisle , Ortlof f rtojM t *> . 231-059-0 6 NSS-0NSH0R E NATURA L GA S PRODUCTIO N Oa w 

### 8/10/8 4 an d 8/24/8 4 Tia t

Activit y Activit y 

### (915 ) 699-325 8 PUtilt K "l(" '

CtMTf l Sukjac t SWEETENIN G COS

TESTIMATE S FO

R SMAL L PLANTS TOPIC S DISCUSSE D AN O ACTIO N TAKE N 

### • Dominan t paramete r i s mole s o f aci dga s processe d- The y (Ortloff ) us e thi s approac hfo r quic kanalyses . • $4000/GP M

amin e circulatio ni s a goodinstalle dcapita l cost s facto r i n 198 4 dollars . • 0. 5 mole s aci dgas/mol e amin e maximum . ^0.3 5 facto r recommended . • Fue l consumption : 1 l bsteam/mi npe r GP M circulation ; 8 0 percen t efficien t boiler ; 100 0 BTU/l bstea m o r 15,00 0 BTU/h r pe r mol e aci dga s remove d eac hhour . • Pumpin g cost s - Dependen t upo nga s pressur e inth e contacto r - us e standar dhorsepowe r equation ; strippe r i s a t 1 atmosphere ; contacto r pressure s rang e fro

m <50 0 t o 100 0 PSI—i f >100 0 pressur e usuall y le t dow nt o 100 0 PSI . Us e 100 0 l bassumption . • Solven t replacemen t - -^25 percen t pe r yea r solven t replacement . Som e example s follow : 40 0 GP M uni t - $340,00 0 initia l solven t cost , $85,000/yea r replacemen t solven t lost ; 5 0 GP M , 390 0 gallon s capacit y - $29,00 0 initia l solven t cost , $7300/yea r replacemen t solven t cost . Solven t cost s abou t $7.5 0 pe r gallo nin198 4 dollars . • Operatin g labo r - Some companie s wil l no t leav e on e operato r alon e i na sou r ga s processin g facility ; proces s wil l no t nee dmor e tha n1 . • Operatin g cost s o r a t leas t hea t an dpumping cos t factor s ar e appropriat e irrespectiv e o f size . • Th e capita l cos t facto r i s appropriat e fo r smal l facilitie s ( 5 LT/D) , bu t wil l become les s appropriat e fo r smalle r andsmalle r facilit y sizes- - i.e. , becaus e o f th e los s o f econom y o f scale . • I f he wer e estimatin g th e cost s quickly , he woul dus e th e abov e factors . • Th e contacto r i s no t a dominan t capita l cos t component . I t run s ^1 0 t o 1 5 percen t o f th e tota l cost . Th e hea t exchanger s an dpum pmak e u

pa larg e fractio no f th e capita l cost . Thes e vary i ncos t onl y

wit hthe GP M o f amin e solution .P.8

• • " • r| IFJ 1 ' ! 1 ' " '

TELEPHONECA U RECOR D Olncoala t Cal l Oout«ola s Cal l rttao nCallla i Ftrto nCallad Ptojac tMo . Ptojoc t 

### H^<m ~ 0/YS/fO<Z-&m Dat a 

### < ? \il&Y Itam

Activit y Activit y 

## 4 . T <£? ? 3Z£T B Canata l Subjac t 

### CUH£-CK./*XJ



## ^u)e<Lr^>Jf ^ (?os r Fftcro^ s TOPIC S DISCUSSE D ANO ACTIO N TAKE N PUCrlbotlar .



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b^-aoi e b.£ A ' ^(Cg . Uj> , fcA4-sS <U» A Mg . ,<>o£/£.&vrH> . T"Hrg

_OHr.AP><£J2

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### Q.« ^ 

## gs~^ » vAmg $ A^^ > 

## nis , cx./€»r ~ PVWS , TH^- I

## frfeVcg.. u KI6H^Jg . CoejzoS'Q*- 1 

### gA-TEL-g, . ("so 1 

### ^
- O PCAQiLU c v/ S <2rfg-v/gQ*-e-r ~



# 1 Mors . Tx-v r

rx-g - 2^^~o Ng » >a.UPm J A^SJM^'Q M 

### H ^ o "S v M J

### g,yr ff-<» ~ /CO O LT

1 O- r^lA^VS , (-<'nEt_ Y uJQuq ^ KA\j g SUL.-^O L

### u ^ I

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- rvu .P. 9 *VrT^<K^«e-V^ T £- • rf |"!|P|tlPr T 

# fori, Baco n&Mm 3ncorporalr & Engineer s - Constructor s



### Augus t 8 , 198 4 

## Radia n Corporatio n P . 0 . Bo x 130 0 Researc h Triangl e Park , N C 2770 9 Attn : Mr . Jef f Schumake r Dea r Sir : Attache d yo u wil l fin d a copyo f th e Ga s Treatin g Sectio n fromNGPS AEngineerin g Dat a Boo k a s wa s discusse d today . Yo u wil l als o fin

d a cop yo f Proces s Desig n o f variou s type s o f Sulfu r Remova l Processe s fo r you r files . I regre t tha t I coul d no t ?r- e o f furthe r servic e a t thi s time . Sincerely , FORD , BACON& DAVIS , INCORPORATE D Texa s Divisio n L . L . Patterson , P . E . Principa l Proces s Enginee r JGJ10/LL P

P.O . Bo x3820 9 • Dallas , Texa s 75238-020 9 • (214 ) 238-650 0 • Tele x79-248 8

220 1 Nort h Centra l Expressway• Richardson , Texa s 7508 0P.1 0



# c

c

L 2 . Dingman , J . C , an dLeBas , C . L. , Oil Ga s J.,6 2 (No .

5) , 75-7 7 (1964) . b . 3 . Hales , G . E. , "Molecular Sieve s inCryogeni c Plants
Operatin g Experience s an dGuidelines" , Natura l Ga s Processor s Association , Regiona l Meeting , Ne w Or
leans , Louisiana , Januar y 21,1974 . a, b , c . Mole sieve. 4 . Jacoby , Robt . H. , "Calculatio nof Methano l Require
ment s t o Preven t

Formatio nof

Ga s Hydrates" , Gas , Feb . 1955 , p . 114 . Methanol. 5 . Kessock , Jr. , A. , an dFris , J . P. , "Ho w Kenov aPlan t Drie s Fee dGas" , Hydrocarbo n Processin g and Petro leum Refiner , 44 , No . 4 , p p 123-12 4 (1965) . c . Mole sieve. 6 . Kraychy , P . N . an dMasuda , A. , "Molecula r Sieve s Dehydrat e High-Aci dGa s a t Pin e Creek" , Oil an d Ga s Journal , Augus t

8 , 1966 . a , c . Mole sieve. 7 . Loomer , J . A. , an dWelch , J . W. , Proceeding s Ga s Conditionin g Conferenc e 1961 , 71-80 , Th e Universit y of Oklahoma , a , c , d . Glycol. 8 . McCarthy , E . L. , Boyd , W . L. , an dReid , L . S. , Petro leu m Transaction s AIME , 189 , 24 1 (1950) . b . Water Content. 9 . McLeod , H . 0. , an dCampbell , J . M. , J . Petro . Technol. , 13 , 590-94 (1961) . b . Hydrate equilibrium. 10 . Patterson , E . O. , Jr. , "Ge t Lo w Dew Point s wit hSoli d Desiccants" , Oil & Ga s Journal , March , 1969 . a , c . Solid desiccants. 11 . Perry , C . R. , Oil Ga s J. , 5 8 (No . 32) , 71-7 4 (1960) . a, c . Glycol. 12 . Polderman , L . D. , Oil Ga s J. , 54 (No . 5) , 198-19 9 (1955) . b . Glycol. 13 . Russell , T . H. , Oil Ga s J. , 6 0 (No . 45) , 94-9 9 (1962) . c . Glycol. 14 . Scauzillo , F . R. , J . Petrol . Techno. , 13 , 697-70 2 (1961) . b . Glycol. 15 . Swerdloff

, W. , Proceeding s Gas Conditionin g Confer enc e 1969 , A-l-A-25 , Th e Universit y of Oklahoma , a, c , d . Glycol, solid

desiccants. 16 . Weyemuller , G . H. , Harlan , J . D. , an dRoberts , Darrel , "Molecula r

Sieve s Kee p Heliu mPlan t o nStream" , Chemical Processing , Novembe r 1966 . c , d . Mole sieve. 17 . Worley , M

. S. , Proceeding s Gas Conditionin g Confer enc e 1967 , H-l-H-15 , Th e Universit y of Oklahoma , a , c . Glycol. 18 . Wunder , J . W . J. , "Ho w t o Desig naNatura l Ga s Drier" , Oi

l & Gas Journal , Augus t 6 , 1962 , pag e 137 . a . Solid bed dehydration. 19 . Young , Jr. , Phili p L. , "Molecula r Siev e Adsorptio ni n LNGPlan t

Pre-Purification" , Presente da t th e Distri
butio nConferenc e America nGa s Association , Hous
ton , Texa s (Ma

y 6-9,1968) . a, c , d . 20 . Campbell , J . M. , "Ga s Conditionin g an d Processing" , Thir dEditio n1974 . 21 . Weibe , R. , an dGaddy , V . L. , J . Am . Chem . Soc . (1941) , Vol . 63 , 475 . CO-rH.O. 22 . Selleck , F . T. , Carmichael , L . T. , an dSage , B . H. , Ind . Eng . Chem . (1952) , Vol . 44 , 2219 . H : S-H,0. 23 . Hall , G . D. , an dPolderman , L . D. , Chem . En e 5 4 (No . 10) , 52-5 8 (1960) . TEG.



## Ga s treatin g Ther e ar e man y method s tha t ma y b e employe d t o remov e aci dgase s (primaril y H 2 S an dC0 2 ) fro m natura l gas . Th e method s ma y b e broadl y categor ize da s thos e dependin g o nchemica l reaction , physi
ca l solution , o r

adsorption . Processe s employin g eac hof thes e method s ar e describe dan dagenera l bibliograph y i s included . 

### Safety precaution s Hydroge nsulfid e i s ahighl y toxi c gas , rapidl y causin g deat hwhe ninhale di nhig hconcentrations . Eve na t lo w concentrations , irritatio nof th e eyes , nos e an dthroa t

ar e possible . Thes e point s illustrat e th e hazar do f

varyin g concentrations : 1 . Threshol dlimi t

value , (TLV) , fo r

prolonge d exposure : 1 0 ppm * 2 . Sligh t

symptom s afte r

severa l hour s exposure : 70-15 0 pp m 3 . Maximu mconcentration s tha t ca nb e inhale d fo r on e hou r

withou t seriou s effects : 170-30 0 pp m 4 . Dangerou s afte r

exposur e of

3 0 minute s t o on e hour : 400-70 0 pp m 5 . Fata l i n3 0 minutes : 70 0 pp man dabov e * 1.0 grain/10 0 sc f

i s equivalen t

t o 17. 1 pp mb y weight , o r

15. 9 pp mb y volume . Th e greates t

dange r fro mth e inhalatio nof Ho S i s fro mit s acut e effects ; i t i s no t cumulativ e i naction . Hydroge nsulfid e i s aflammabl e gas . I nconcen tration s o f

4. 3 t o 46. 0 vo l %i nair , i t explode s upo n ignition . Th e vapor s ar e heavie r tha nai r

an dma y trave l considerabl e distanc e t o asourc e of ignitio n an dflas hback . Anyon e engage di nth e desig no r operatio nof

a facilit y i nwhic hH 2 S i s presen t shoul dconsul t

som e sourc e of

informatio no nsafet y precaution s t o b e taken . On e suc hsourc e i s th e Manufacturin g Chem
ist s Association , Manua l Shee t SD-36 . GENERA L CONSIDERATION S Ther e ar e man y variable s involve di nga s treat ing . Thi s make s th e precis e definitio no f are aof applicatio nof

agive nproces s ver y difficult . Som e of th e factor s t o b e considere di nmakin g aproces s selectio nare : 1 . Typ e an dconcentratio nof impuritie s in . th e sou r gas . 2 . Specification s fo r

th e residu e gas . 3 . Specification s fo r

th e aci dgas . 4 . Temperatur e an dpressur e a t whic hth e sou r ga s i s availabl e an da t whic hth e swee t

ga s mus t b e delivered . 5 . Volum e of

ga s t o b e processed . 6 . Hydrocarbo ncompositio nof th e gas . 7 . Selectivit y of

aci dga s remova l required . 1 5
- 1 9 Rev. 197 6" I P.1 1

8 . Capita l cost s an doperatin g costs . 9 . H 2 S t o CO; , rati o i nth e sou r gas . Gase s wit hhig hH L . S t o CO. , ratio s ar e les s cor rosiv e tha nthos e havin g lo w H 2 S t o CO * ratios . I n general , ahig hH 2 S-to-C0 2 rati o ga s wil l permi t highe r acid-ga s concentratio ni nth e absorbin g solu
tion . Carbo nstee l ma y b e satisfactor y fo r muc hof th e equipmen t

i nan y process . However , recommen dation s fo r

material s o f

constructio nar e bes t

handle d o na nindividua l uni t basi s b y th e contracto r o r supplier . Al l gas-sweetenin g unit s shoul dhav e agoo dinle t separator . A continuou s introductio nof on e pp mof foreig nmateria l enterin g a100-MMscf dplan t repre sent s a naccumulatio nof 1 ton/yr . Contactin g tower s shoul db e equippe dwit hdifferentia l pressur e gauge s t o ai di ndetectin g floodin g and/o r foaming . Th e absorbe r shoul dhav e amis t

extracto r

abov e th e to p tra y and/o r

a nefficien t

separato r

i nth e exi t

ga s line . Reboile r heatin g element s shoul dalway s b e submerged . Ther e shoul db e adequat e spac e allowanc e fo r vapo r flow , an di f stea mi s employe da s th e heatin g medium , i t shoul d alway s b e saturated—neve r superheated . I nsolutio nhea t exchangers , th e acid-ga s ric hsolutio nshoul db e o nth e tub e sid e inupflow . A flas htan k

betwee nth e absorbe r an dth e hea t exchange r

wil l reduc e erosio nan dals o minimiz e hydrocarbo nconten t

i nth e aci dgas . Valve s fo r pressur e let-dow nar e subjec t t o sever e service . Stainles s tri mwit hstellit e facin g i s commonl y used . Wher e applicabl e asolutio nreclaime r shoul db e considered . Th e reclaime r wil l normall y handl e 2 % t o 3%o f th e tota l solutio ncirculation . Solutio nfil
tratio nshoul dals o b e provided . Commo ndesig n filtratio nrange s fro m5 % o f circulatio nt o ful l stream . I nsom e cases , activate dcarbo ntreatmen t o f asid e strea mi s use dt o adsor b impurities . Activate dcarbo ncanno t replac e areclaime r

fo r remova l of

degradatio nproducts . Wher e aseparat e activate dcarbo nuni t

i s provided , i t

shoul db e lo
cate ddownstrea mof

th e filter . Her e ar e som e operatin g precaution s whic hexperienc e ha s prove nt o b e goo dpractice : 1 . Al l equipmen t

shoul db e cleane dafte r installatio n an dbefor e initia l operation . Thi s cleanin g may b e don e b y circulatin g aho t

1 % t o 2 % b y weigh t

solutio nof

lo w chlorid e conten t sod aash . 2 . Wher e wate r

make-u p i s used , i t

shoul dcom e fro m stea mcondensat e o r

deionize dwater . 3 . D o no t us e soap-base dlubricants . 4 . A short-ter m(second s t o minutes ) increas e indiffer
entia l pressur e acros s th e contacto r ca nindicat e foaming . A gradua l increas e indifferentia l pressur e ove r alon g perio do f tim e may indicat e foulin g of tray s o r packing . 5 . If foamin g i s though t

t o b e occurring , chec k

fo r entr y o r condensatio nof

liqui dhydrocarbons , an dru nlaborator y test s wit han dwithou t

foaminhibitors . Neve r

ad dafoam inhibito r t o th e plan t

solutio nwithou t

prio r testin g inth e laboratory . 6 . If areclaime r

and/o r filte r i s provided , operat e i t fro mth e da y th e plan t

i s started . Chang e o r

cleanfilter s a s required . 7 . Lea nsolutio nt o contacto r an dstrippe r

overhea d condense r

outle t temperature s shoul db e kep t a s lo w a s possibl e t o minimiz e solutio nan dwate r losses . Lea nsolu
tio ntemperature s shoul db e 10°-15 " abov e enterin g ga s temperatur e t o minimiz e hydrocarbo ncondensatio nwhic h ma y caus e foaming . 8 . Monito r

corrosio nrate s wit hcoupon s o r resistanc e probes . 9 . Lea nan dric hsolution s shoul db e analyze droutinel y fo r absorben t

concentratio nan daci dga s loading . 10 . Housekeeping , particularl y packin g glan dleaks , i s amajo r facto r i ncontrollin g chemica l losses . Chemicall y reactin g processe s Thes e processe s ar e base do nreversibl e chemica l reac tions . Th e absorben t

react s wit hCO , an dH. S inth e con tacto r withth e directio nof

reactio nbein g reverse db y hig h temperatur e and/o r

lo w pressur e inth e stripper . Fig . 15
- 25 Alist s approximat e guideline s fo r anumbe r

of chemi
call y reactin g processes , eac hof whic hwil l b e discusse d below . Fig . 15-25 B give s asummar y of proces s capabilities . Fig . 15-2 6 depict s th e proces s flow o f atypica l chemica l absorptio nprocess . Fig . 15-2 8 i s atabl e of

physical propertie s of

gas-treatin g chemicals . Figs . 15-29 throug h15-3 2 sho w vapo r pressure s a t variou s temperatures , an dfreezin g point s an dspecifi c gravit y fo r

som e of th e treatin g chemicals . AMIN EPROCESSE S Monoethanolamine , conventiona l Diethanolamine , SNPA-DE A an dhigh-loadin g DE A processe s wil l b e con sidere dhere . Th e ethanolamin e processe s ar e particularl y applicabl e whe naci dga s partia l pressure s ar e lo w and/o r lo w level s o f aci dga s ar e desire dinth e residu e gas . Unit s employin g ME

A hav e bee nsuccessfull y designe d inth e 50-100 psi g operatin g range ; however , car e shoul d b e use dinth e desig nof

DE Aplant s fo r

lo w pressur e ga s sweetening . Th e actua l CO , picku p ha s bee nreporte dt o b e lowe r tha nexpected . I nfact , ahig hH, S selectivit y ha s bee nreporte dwhic hindicate s th e proces s ma y b e rat e limitin g (18) . Becaus e o f

th e wate r

conten t o f th e circulatin g solu
tion , thes e processe s ar e wel l suite dfo r gase s ric hin heavie r hydrocarbons . Th e aqueou s amin e processe s hav e ver y littl e selectivit y fo r H, S o r CO, , excep t

a s noted . Th e DE Aprocesse s ar e particularl y applicabl e whe nth e ga s strea mcontain s carbony l sulfid e whic hreact s irreversibl y wit hMEA . Th e SNPA-DE Aproces s (33 ) i s patente dinCanad aan d possibl y othe r

countries , excludin g th e U . S . Th e paten t cover s arang e o f

loadin g fro m0. 9 t o 1. 3 mole s o f DEA / mol e of aci dgas . Thi s proces s i s use dfo r hig hpressure , hig haci dga s conten t

stream s havin g arelativel y hig h rati o o f H,S/CO, . Fo r MEAunits , tota l aci dga s pick-u p i s normall y lim
ite dt o 0.3 3 t o 0.3 5 mole s o f aci dgas/mol e o f

MEA . Th e concentratio nof

MEAi s generall y hel di nth e 1 5 t o 1 8 

# c

e 

# e

Rev . 197 6 1 5 -2 0MI"" " P.1 2 

# c FIG . 15-2 5 A Approximat e guideline s fo r sweetenin g processes' 1 '



# c

c


# c ME A DE A SNPA-DEA< 9 > Econamine(DGA ) Sulfino l Aci d gas pickup , scf/ga l @ 100°f . norma l range' 2 1 3. 1 t o 4. 3 3. 8 t o 5. 0 6. 7 t o 7. 8 4. 7 t o 6. 6 4 t o 1 7 Aci d gas pickup , mols/mo l amine , norma l range 13 1 0.3 3 t o 0.4 0 0.3 5 t o 0.6 5 0.7 2 t o 1.02 0.2 5 t o 0. 3 N.A . Lea n solutio n residua l aci d gas , mol/mo l amine , norma l range 14 1

.. . 0.12 + 0.08 ±0.08 ±0.10 + N.A . Ric h solutio n aci d gas loading , mol/mo l amine , norma l range' 3 ' —0.4 5 t o 0.5 2 0.4 3 t o 0.7 3 0. 8 t o 1. 1 0.3 5 t o 0.4 0 N.A . Solutio n concentration , wt . V norma l rang e 1 5 t o 2 5 2 5 t o 3 5 2 5 t o 3 0 5 0 t o 7 0 3 components.Vane s Approx . reboile rhea t duty . Btu/ga l lea n solution'5 1 1.00 0 t o 1.20 0 90 0 t o 1,00 0 90 0 t o 1.00 0 1,10 0 t o 1.30 0 55 0 t o 1.72 0 Stea m heate d reboile rtub e bundle , approx . averag e hea t flux , Q/ A= M Btu/hr-ft

2 ' 6 1 9 t o 1 0 9 t

o 1 0 9 t

o 10 9 t

o 10 9 t

o 10 Direc t fire d reboile rfir e tube , averag e hea t flux , Q/ A= M Btu/hr-ft 2 ' 6 ' 8 t o 1 0 8 t o 1 0 8 t o 1 0 8 t o 1 0 . 8 t o 1 0 Reclaimer , stea m bundl e o rfir e tube , averag e heat flux , Q/ A= M Btu/hr-ft ? < « 6 t o 8 N.A' " N.A.l' l 6 t o 8 N.A . Reboile rtemp. , norma l operatin g range , "F M 22 5 t o 26 0 23 0 t o 25 0 23 0 t o 25 0 25 0 t o 26 0 23 0 t o 28 0 Heat s of reaction;""'approximate : Btu/l b H 2 S 55 0 t o 670"° > 50 0 t o 600" " 51 1 67 4 Var ywit h loading . Btu/lbC0 2 62 0 t o 70 0 58 0 t o 65 0 65 3 85 0 Var ywit h loading . N.A.—no t applicabl e o rno t availabl e NOTES : 1 . Thes e dat a alon e shoul d no t b e use d fo rspecifi cdesig n purposes . Man ydesig n factor s mus t b e considere d fo ractua l plan t design . 2 . Dependen t upo n aci d gas partia l pressure s an d solutio n concentrations . 3 . Dependen t upo n aci d gas partia l pressure s an d corrosivenes s o fsolution . 4 . Varie s wit h strippe roverhea d reflu xratio . Lo wresidua l aci d ga

s content s requir e more strippe rtray s and/o rhighe rreflu xratio s yieldin g large rreboile rduties . 5 . Varie s wit h strippe roverhea d reflu xratios , ric h solutio n fee d temperatur e t o stnppe ran d reboile rtemperature . 6 . Maximu m poin t hea t flu xcan reac h 20.00 0 t o 25.00 0 Btu/hr-ft 2 a t highes t flam e temperatur e a t th e inle t of a direc t fire d fir e tube . Th e mos t satisfactorydesig n o l fir e tub e heatin g element s employ s a zon e byzon e calculatio n base d o n therma l efficienc ydesire d an d limitin g th e maximu m tub e wal l temperatur e a s require d b yth e solutio n t o preven t therma l degradation . Th e averag e hea t flux . Q/A , i s a resul t o fthes e calculations . 7 . Reclaimer s ar e no t use d i n DE Asystems . Activate d carbo n filter s ar e use d t o remov e degradatio n product . 8 . Reboile rtemperature s ar e dependen t o n solutio n cone , flare/ven t lin e bac k pressur e and/o rresidua l CO ? conten t required . I t i s goo d practic e t o operat e th e reboile ra

t a s lowa temperatur e a

s possible . 9 . Canadia n an d Foreig n Patente d DE AProcess . 10 . B . L . Cryne s an d R . N . Maddox . Oi l Ga s J. , p . 65-67 . Dec . 1 5 (1969) . Th e heat s ofreactio n ten d t o varywit h aci d gas loadin g an d solutio n concentration . 11 . J . I . Lee . F D . Otto , an d A . E . Mather . Can . GP AResearc h Seminar . Nov . 1972 . Th e heat s ofreactio n ten d t o var ywit h aci d gas loadin g an d solutio n concentration . FIG . 15-25 B wt. % ran^ e to limi tcorrosion . DE A concentration s up t o Summar y o f

proces s capabilitie s ('3 5 wt%jar e acceptable . Normall y Equilibriu msolubilit ydat aan d applicatio nfo rH £ an d capabl eo f R«m.ve > CO , i n ME A an d DE A solution s ar egive ni nreference s Meetin g Mercap - 4 3 an d 4 4 Va , Groi n ta n 8, Selectiv e s p £ $!°! , Ab»rb. d solutionDegrade d b y uFo rbot h prwMMse s contactors m d stripper s typicall y

hav e1 8 t o 2 2 trays . ME A unit s shoul d hav eareclaimer . M °"° . References: 11.14,15,24,25,26.33,34x45,46,47, and 51. ethanolamin e Ye s Partia l N o Yes (COS . CO, . CS, ) Diethanolamin e Yes Partia l N o Som e (COS , CO, , CS, ) Sulfino l Ye s Ye

s Yes 3 Som e (CO, . CS, ) Exampl e Proble m Diglycolomin e Ye s Portia l N o Ye s (COS . CO, . CS, ) » * i * ,^„»,» . , . . nnn • • . . Seiexo i Ye

s Sligh tYes3 N o A natura l ga s strea mo f 5 0 MMscf d a t90 0 psi gi s t o b e Ho tPot-Benfiel d Yes1 No 2 N o N o sweetened . Th esourga s contain s 0.50%JH2 S an d 2.0 % C0 2 . Fluo rSolventNo 4 N o N o N o Th e rich amin eleave s th econtacto ra t140° F (60°C) . Strettor d Ye s Partia l Ye

s Ye

s (HC N vi a thiocyanate ) Solutio n Iro n Spong e Ye s Partia l Ye

s — Mo l Siev eYe

s Ye s Yes

3 —Assumin gidea l gases , th epartia l pressur eofH^ S i nth e 1 . Hi-pur e version . SOU rga s wil l b e 2 . Hydrolize s CO S onl y Q 0Q 5 x 91

_y (760/1 4 7 ) _23 7 m mH g J . Som e selectivit

y is exhibite d b y thes e processes . 4 . Ca n b e metwit

h specia l desig n features . Th e partia l pressur e o f CO o i s ) - '• groi n H,S/100sc f 0.0 2 X 91 5 X (760/14.7 ) = 94 6 m m H g 15-2 1 Rev . 1976 . 198 1P.1 3

Th e rati o o f

aci dga s partia l pressur e i s R v= (237/946 ) = 0.2 5 Th e equilibriu mcompositio nof th e H2 S i nth e amin e ca nthe nb e rea dfromth e know nvalu e of R v(0.25 ) an dth e H 2 S partia l pressur e of

23 7 mmHg . Fro mFig . 15-3 5 w e rea dth e equilibriu mconcentratio nof H 2 S t o b e 0.0 9 mole s ofH, S pe r

mol e of MEA . Fro mFig . 15-3 9 usin g th e 23 7 mm H g o f H;, S partia l pressur e i nth e sou r ga s an dth e equili
briu mconcentratio nof

0.0 9 mol s of

H^ S pe r mol e of MEA w e rea da nRLvalu e of

0.17 . R L= (mol s H 2 S/mol e MEA/mol s COj/mol e MEA ) Mol s COjmole ME A = (0.09/0.17 ) = 0.5 3 Th e equilibriu maci dga s concentratio nof th e ME A solutio na t

th e estimate d140° Ftemperatur e leavin g th e absorbe r wil l b e 0.0 9 mol e H, S + 0.5 3 mol e C0 2= 0.6 2 mol e aci dga s total/mol e ME A DIGLYCOLAMIN

E PROCES S Thi s proces s use s Diglycolamin e (DGA ) bran do f 2-(2
- aminoethoxy ) ethano l i naqueou s solutio na s th e sweeten in g agent . Th e proces s ca nb e use dsuccessfull y for treatin g natura l o r

refiner y ga s stream s containin g carbony l sulfid e and/o r carbo ndisulfide . Asolutio nconcentratio nof 5 0 t o 7 0 wt % DG

A i s use dt o permi t

highe r aci dga s remova l pe r gallo no f solution . DG A ha s a nadvantag e fo r

plant s operatin g i ncol dcli
mate s wher e freezin g o f th e solutio ncoul doccur . Areclaime r shoul db e provided . References: 17, 32, and 18. HO T CARBONAT E PROCESSE S Thi s proces s wa s develope da t th e U . S . Burea u o f Mine s an demploy s a naqueou s solutio no f potas siu mcarbonate . Th e absorbe r an dregenerato r

bot h operat e a t

elevate dtemperature s i nth e neighborhoo d of 230 ° t o 240°F . Th e proces s canno t b e use do nga s stream s containin g onl y H 2 S . I t als o encounter s difficult y i nattemptin g t o trea t ga s t o 0.2 5 grain s o f HgS/lO O scf

, th e norma l specification . Th e mos t

popular.o f

th e carbonat e processe s ar e thos e containin g a nactivator . Thes e proprietar y processe s are : 1 . Benfield : Severa l activators . 2 . Girdler : Alkanolamin e activators . 3 . Catacarb : Alkanolamin e and/o r borat e acti
vators . 4 . Giammarco-Vetrocoke : Arseni c an dothe r activators . I ngeneral , plant s ar e constructe dof carbo nsteel , with stainles s stee l bein g use da t critica l points . Becaus e th e circulatin g solutio ni s aconcentrate dsal t solution , car e mus t b e take nt o avoi dcol dspot s i nline s an dequipment . References: 2, 5, 23, and

50. STRETFOR D PROCES S Thi s proces s wa s develope db y th e Nort hWester n Ga s Boar dan dClayto nCompan y Ltd . o f England . I t utilize s aquinon e solutio nt o conver t th e H.. S t o sul
fur . Th e proces s i s selectiv e fo r H. S an dca nreduc e th e H 2 S conten t

wel l belo w th e pipelin e specification . 

### Physical-solven t processe s Thes e processe s ar e base do nphysica l absorptio n an doperat e i nmuc hth e sam e wa y tha t th e oi l ab
sorbe r i nanatura l ga s plan t does . I ngeneral , a physica l solven t

proces s shoul db e considere dwhen : 1 . Th e partia l pressur e of th e aci dga s i nth e fee d i s 5 0 ps i o r

higher . 2 . Th e concentratio no f heav y hydrocarbon s i n th e fee dga s i s low . 3. . Whe nonl y bul k

remova l o f

th e aci dga s i s desired . 4 . Whe nth e solven t

i s abl e t o d o asatisfactor y dehydratio na s wel l a s aci dga s removal . 5 . Whe nselectiv e H 2 S remova l i s desired . Th e absorbe r

employe di s aconventiona l traye d o r packe dtower . Regeneratio ni s accomplishe db y usin g on e o r

mor e of thes e techniques : 1 . Multi-stag e flashin g t o lowe r pressures . 2 . Relativel y lo w temperatur e strippin g wit ha n iner t gas . 3 . Heatin g an dstrippin g wit hth e solven t vapor . Physical-solven t

processe s employe di nth e nat ura l ga s industr y includ e th e Fluo r Solven t Process , th e Selexo l Process , th e Sulfino l Process , an dth e Rectiso l Process . I ngeneral , al l th e physical-solven t processe s hav e th e limitatio no f

ahig haffinit y fo r

heav y hydro
carbons . Fig . 15-2 7 i s atypica l proces s flow diagra m fo r remova l of

bot hC0 2an dH 2 S . FLUO RSOLVEN T Thi s proces s i s patente db y th e Fluo r Corporatio nan d i s base do nth e us e o f

anhydrou s propylen e carbonate . Th e temperatur e o f

th e leansolutio nt o th e absorbe r i s usuall y wel l belo w ambient , an dsom e metho do f refrigeratin g th e solven t i s usuall y necessary . References: 8, 9, 13, 19, 37, and 38. SELEXO L Thi s proces s use s th e dimethylethe r o f polyethylen e glyco l a s asolvent . I t

ca nb e use dfo r

obtainin g ver y lo w partia l pressure s of

aci dga s b y addin g di-isopropanolamine . Th e proces s i s license db y th e Allie dChemica l Corp . Th e temperatur e of

th e leansolutio nt o th e absorbe r i s approxi
matel y ambient . Withth e us e of

thi s solven t

i t i s possibl e t o achiev e pipelin e specificatio nresidu e ga s wit hrespec t t o H.S , whil e rejectin g a s muc ha s 85 % o f th e CO . presen t

inth e origina l sou r

ga3 . References: 28, 31, 39, iO, and 55. SULFINO LPROCES S Th e Sulfino l solven t

consist s o f

sulfolan e (tetrahydro
thiophen e dioxide ) di-isopropanolamine , an dwate r inpro portion s varie dt o sui t

th e application . Th e proces s ca nb e designe dt o mee t

awid e rang e of

produc t specifications . Bul k CO , remova l i s achieve dwit hminima l hea t require
men t an dwithou t

refrigeration . 

# c

c

c 

# e

Rev. 1976 . 198 1 15-2 2P. M 

# c Remova

l o f H.S , COS , mercaptans , an dorgani c sulfide s t o mee t pipelin e specification s i s achieve dove r awid e rang e of operatin g conditions . Th e proces s i s license db y Shel l Developmen t

Company . References: 20, 21, and 27. RECTISO LPROCES S Thi s proces s use s methano l a s asolvent , an dwa s devel
ope dby th e Germa nLurg i Co . an dLinde A . G . Becaus e o f th e vapo r

pressur e o f

methanol , th e proces s i s normall y applie da t

lo w temperature s of

-3 0 t o -100° Ffor

th e Recti
so l solution . I t

ha s bee napplie dfo

r th e purificatio nof natura l ga s for

LN Gproduction . Th e proces s i s bes t suite d wher e ther e ar e limite dquantitie s of ethan e an dheavie r components . Fig . 15-2 8 i s atabl e of physica l propertie s of gas treatin g chemicals . Figs . 15-2 9 throug h15-3 2 sho w vapo r pressure s a t

variou s temperatures , an dfreezin g 

# c point s an dspecifi c gravit y fo r som e of

th e treatin g chemicals . 

### Dr y be d processe s

IRON-SPONG EPROCES S Thi s proces s utilize s ahydrate diro noxide , impregnate d o nwoo dchips , whic hreact s onl y withH.S . I t find s appli
catio nonl y o ngase s wit hlo w concentration s of H.S . I n batch-proces s operations , th e iro nsulfid e ca nb e regener ate dafe w time s withair . I naddition , th e chip s mus t periodicall y b e replaced . Car e mus i b e take ndurin g re chargin g t o preven t

ai r pollutio nand/o r

fir e becaus e th e spen t iro nsulfid e o nwoo dchip s ca nignit e spontaneously . Successfu l treatin g require s controlle dga s temperatur e an dwate r

conten t of th e bed . Referenc e 5 6 (copie s avail
abl e fro mConnelly , Inc. , 315 4 Sout hCaliforni aAvenue , Chicago , 111 . 60608 ) discusse s thi s process . 

### FIG . 15-2 6 Typica l ga < sweetenin g b y chemica l reactio n Sweet Ga s 

# / O w

Contacto r 

# 7\ " (p) Coole

r Optiona l equipmen t 

# c Sou r ga t 

# az D "B— <&- %

Fue l 

# 7 ox

I flas h tan k

. Aci d ga s

Courtes y Fis h Engineerin g & Construction , Inc . FIG . 15-2 7 Typica l ga s sweetenin g b y physica l absorptio n 

# c

Sou r ga s 

# e H, S on d strippin g ga s 

## > Coole r I i f* /

* r H l v % T LJ •i

• 

# t Solven t recover y

•Strippin g ga s

Courtes y fis h Engineerin g & Construction , Inc .

Rev . 198 1 15-2 3 Rev . 197 6P.1 5

Formul a
Molecula rWt . leilin g po m 9 76 0 m m Hg , "I. Frteiin g point , 'I. . Critica l constant ! failure, psia . Temperature , °F . . Densit y9 20'C . gm/c < Wtight , lb/ge t Sptcifi c gro«it

y2O°C./20°C . Specifi c hoo

t 9 U'F . ITU7lb/" F Therma l conductivity. ITU/hr . FT' , "F./ft. . (a ! W f.... letln t hto t sfvoportiation . ITU/l b Noo t o frooctien . ITU/l b o

ftci d Co i H. S CO . Viuoiity , c

p

Itfractiv t indti . « „ 6I°F . fin k point , COC

. 'I HOCiHahM i
61. M JM. 9 so t

I Oi l 1.41 9 M° F 1.017 9 060 0 9 U' F o.i « IS S O 7* 0 m m M g

74. 1 9 M° F

I4S1 9 20 0 FIG . 15-2 8

Physica l propertie s o t ga s treatin g chemical s Trielheeol - —eiweeelomie e (HOCJH.I.H H
10 5 1 4 SU I M. 4 474.7 117 1 IM S 10 1 9 M* F I09I9(10/20'C ) OU O 011 7 2 M 9 7 ) m m H f

3W< 3 6I° F (a t 90 % ot . solution ) l.477 o 21 0 (HOClHall K
I4II 9 UO (Oecempoies) 7 7 3 IS S 957. 7 1.12 4 ? 3 7 9 U° F III M 0.7 0 21 0 9 7U

mn -40 0 -43 0 101 1 9 6I' F lit 95 % wl . solution ) I.4IS 2 16 S oiGircouuuNc e H(0C)H.),«H > I0S.I 4 43 0 •s S47.l l 75 4 4 l.0SI@U° F 1.1 2 9 U' F 1.057 1 0.57 1 0.12 1 119.1 4 9 7U m -47 4 -IS O 4 0 aU' F

1.459 1 2 U Witeprepaael emiii e (H0C>H.),M H
113.1 9 479 7 10 7 4 544 1 22» I W9 M' C 0.9J9 ( 3 45' C >20' C 0.4 9 9 10' C "1* 9 U S 9 (?|m m H

g

17 0 9 M° F I t l 9 I U' F 1 6 9 llf l 1454 2 9 I U'F . 2S S SCUXOl * Oimolhylothe

r o fpolytthylm o llycol . 2 M S U -2 0

1.0) 1 9 77' F I. U 9 77 V 0.4 9 9 4 1 ° F 0.lla?7» F -19 0 9 77' F -IU<a77 V S J a 77' F

10 4 Propylen e Corbonow C.H.CO i
102.09 447 - 5 4 4

I.20S7 1.20 3 0.33 ! 0.1 2 @ (?)' f 20 1 ( 3 760 m m M

g

1.6 7 9 100' F 19.4 c i 9 —40* F 1.7 9 C l <§ > I00' f 0.12 7 c i <3 2I0" F 1.420 9 270 

# c

(

Formul a

•oilin g poin t 9 74

0 m m Hg , °F . frtuin g point , °f. (ritko l conifont i Frtlluro , pti o . . . Ttrnporaturo , ' F Oomil y9 20'C , gm/e c Wtight , lb/ga l Specifi c gravit

y20'C./20' C Spocific hta frp

U'F . ITU/lb/" F Thormo t conductivity. ITU/hr . FT . - F./ft . (SlU' F lattn l hoo

t sfvaporisation , ITU/l b IHiyWue i Glyco l HOC,HaO H
12.07 317. 0 1. 6 111 4 2 701. 4 9 2 1 9 6I° F I.IIS S 055 2 0.144 ( 3 60° F 14 4 ( 3 7* 0 m m H

g Glyco l

H0(CjMa0)i H
106.1 2 472. 6 17. 6 476. 0 766. 4 9) 1 9 Wl I II M 0 53 5 014 4 9 U' F 2) 2 9 7* 0 m m H g Triethy W

Otyco l HO(CiH.0|i M IS O 1 7 $49 ) 19. 0 479 2 12 1 •3 4 9 U' F 1.125 4 0.49 2 0 1)9 9 U' F 17 9 9 76 0 mmHg Glyco l

H0(C,Ha0|a H
1941 2 621. 1 20 1 376 ) I I * 9 3 4 9 U' F U4 I 051 0 14 1 9 76 0 m m H g SulfoUno

® C.H.S0 )
1201 7 S4 S 11.7 767 ) 101) 1 10.62 ) 9 )0' t /W C 1.261 0) 6 9 30°C 0.11 4 9 I00° F 22S 7 9 2I2' F MOHMM I CHIO H
12.04 141 1 -143 1 1153 9 46 4 0.791 7 0.590 (S'-I0"C | 0.124 47 4 9 7* 0 m m H

g 

# c

c

Viicoiity . c

p .. .

lofracHvs indei , > * U'F . Floi h point , COC

. *F . 20. 9 9 U' F

1431 4 2* 0 3 5 7 9 U' F

1.447 2 29 0 47. 9 9 U' F

1455 9 11 0 « 0 0 9 U' F

1.459 5 IS O 1 0 3 9 U' F 4. 1 9 I22' f J. S 9 JU' f 1. 4 9101' F 0.4 7 9 192" F 1.41 1 9 UT IS O O. t9 U' F

1.121 6 S I 

# e

Rev . 197 6 15-2 4P.1 6 , , - -, r ,

( a FIG . 15-2 9 Vapo r pressure s o fga s treatin g chemical s 1,000



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nea l :o . 10 0 15 0 20 0 

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15-2 5 Rev . 197 6P.1 7

a E

a 5 > FIG . 15-3 0 Freezin g point s o faqueou s amin e solution s 9 0 8 0 7 0 6 0 5 0 4 0 3 0 2 0 1 0 0 - 1 0 - 2 0 - 3 0 - 4 0 - 5 0 FIG . 15-3 1 Specifi cgravit yo f aqueou s glyco l solution s

ef f 1 er s 1 _ o n C h 1_ _ e m 1 — ic a 1 C 1 _ 

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2 0 4 0 6 0 8 0 10 0 FIG . 15-3 2 Specifi cgravit yo faqueou s amin e solution s
1.1 4

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11.11 . 2 0 4 0 6 0 8 0 10 0

Glycol , wt %

2 0 4 0 6 0

Amine , wt % 8 0 10 0 MOLECULA RSIEV E Molecular-siev e processe s ar e bein g use dfo r remova l o f sulfu r compound s fro mnatura l ga s stream s (se e Fig . 15-33) . Th e grad e of

molecular

sieve s t o b e use di s selecte d o nth e basi s of

th e operatin g conditions . Hydroge nsulfid e ca nb e remove dt o mee t 0.2 5 grains/10 0 sc f

specificatio n wit hselectiv e remova l o f H.S . Th e siev e be dca nb e de
signe dt o dehydrat e an dsweete nsimultaneously . I ngeneral , th e concentration s of aci dga s ar e suc htha t cycl e time s ar e inth e orde r o f 2 hours . T o operat e properl y th e sieve s mus t

b e hel da t

atemperatur e clos e t o 600°F . fo r alon g enoug hperio do f tim e t o remov e al l adsorbe d materials . Exac t

arrangemen t

o f th e regeneratio ncycl e depend s upo nproces s conditions . Th e proble mo f

CO S formatio ndurin g processin g ac cordin g t o th e reactio nof H, S + C0,=.C0 S + H. O ha s bee nextensivel y studied . Th e molecular siev e ca ncat alyz e th e reaction ; however , ne w molecula r siev e product s hav e bee ndevelope dt o retar dsignificantl y CO S forma
tion . Th e centra l zon e i nth e regeneratio ncycl e i s mos t favorabl e t o CO S formation . Operatio nof

adsorben t

plant s i s quit e simple , bu t de
sig ni s complex . Manufacturer s mus t b e consulte dfo r potentia l applications . Refe r t o ga s dryin g an dliqui d sweetenin g section s fo r

additiona l details . References: 12, JH, JK), .5.J , 57. 5M, 5!l. Cll and til. 

# c


# e

Rev . 197 6 1 5 - 2 6P.1 8 

# c FIG . 15-3 3 Typica l COj-rk h natura l ga s treate r 9 0 MMscf d 20 0 MMscf d 6 % CO , 10-10 0 g rHi S 7 I b HjO'MMsc f 11 0 MMscf d 

# J^\ Molecula r siev e Adsorbin g Molecula r siev e regeneratin g 

# w

Courtes y Daviso n Chemica l 1 0 MMscf d Liqui d sweetenin g an d dehydratio n process

10 0 MMscf d 67 . CO , 0.2 5 g rH, S Bon e dry 10 0 MMscf d Ni l CO , 0.2 5 g rH, S 7 I b H,0/MMsc f 20 0 MMscf d 3 % CO , 0.2 5 g rH, S 3 I b H, 0 MMscf



# c

c

C Equilibriu m dat a fo r

amine-sou r ga s system s On e o f th e peculiaritie s of

amin e treatin g system s i s th e interactiv e effect s o f on e aci dga s constituen t wit h amin e upo nth e equilibriu mpartia l pressur e of th e othe r constituent . Th e mos t

commonl y encountere dsou r ga s constituent s ar e H, S an dCO, . Th e capacit y o f agive n amin e fo r

eithe r on e of th e aci dga s constituent s alon e i s muc hgreate r

tha nwhe nth e tw o occu r together . Jone s e t a l (63 ) hav e presente ddat at o confirmth e inter
activ e effec t

of H, S an dCO , inmonoethanolamin e solu
tions . More recently , Le e e t a l (64 ) hav e presente dsimila r dat afo r diethanolamin e solutions . Thes e dat aprovid e th e basi s fo r predictin g th e equilibriu mconcentratio nof ME A an dDE A solution s whe nincontac t wit hsou r

gase s con tainin g bothH, S an dCO, . McCoy an dMaddo x hav e plotte dth e dat ao f Jone s e t a l fo r ME A innomograp hformfo r eas e o f use . Th e McCoy an dMaddo x chart s ar e show ninFigs . 15-3 4 t o 15-41 . Th e Lee , e t al , chart s fo r

DE A ar e show ninFigs . 15-42 t o 15-49 . Neithe r th e dat ao nME A no r

th e dat ao nDE Acove r al l possibl e temperature s tha t migh t b e encountere dina n amin e treatin g unit . Consequently , som e techniqu e i s neede dfo r

interpolatin g acid-ga s partia l pressure s an d equilibriu mconcentration s t o temperature s intermediat e betwee nthos e show ni nth e equilibriu mdat acharts . Ap
proximat e value s a t

othe r temperature s ma y b e calculate d base do nth e assumptio ntha t vapo r pressur e i s afunctio n of temperatur e onl y an dfollow s th e rule :

lnP <, ~ - 

### ( D Where : P " - pur e componen t

vapo r pressur e T = absolut e temperatur e Fo r reactin g systems , wher e th e amoun t of on e compo nen t reacte daffect s th e amoun t o f anothe r componen t

tha t canreact , thi s i s onl y a napproximation . However , i t pro vide s th e bes t

rul e availabl e fo r

interpolatio nbetwee n temperature s o neithe r

th e McCoy an dMaddo x o r th e Le e e t al charts . • Applyin g Equatio n1 t o th e interpolatio nbetwee ntw o temperature s t o determin e partia l pressur e fo r agive n aci dga s loadin g i nth e amin e yields :

lnP ° = l nP ° + Where : 

## yr, T, ;



## yr, T, / I n- ^ (2 )

1 = th e lowe r

temperatur e 2 = th e highe r

temperatur e i = atemperatur e intermediat e betwee n1 an d2 a t whic hth e partia l pressur e of th e particula r

aci d ga s ove r th e amin e solutio ni s desire d Example : A2. 0 NDE Asolutio ncontain s 0. 2 mol e H S/DE Aan d 0. 4 mole CO/DEA . a . Wha t wil l b e th e equilibriu mpartia l pressure s o f CO , an dH. S ove r

thi s solutio na t

50°C ? Fro mFigur e 15-4

4 ppC O =4. 2 psi a Fro mFigur e 15-42 ppH. S = 2. 8 psia . b . Wha t wil l b e th e equilibriu mpartia l pressure s o f H. S an dCO , ove r

th e solutio na t

100°C ? Fro mFigur e 15-45 ppCO , = 47 psi a Fro mFigur e 15-4 3 pp H S = 1 5 psia . 1 5 - 2 7 Rev . 197 6P.1 9

c . Wha t wil l b e th e equilibriu mpartia l pressure s of H. S an dCO , ove r

th e DEA solutio na t

t = 60°C ? Interpolatio nfo r

temperature s intermediat e betwee n50 ° an d100° C make s us e of th e fac t tha t th e lo g of th e vapo r

pressur e of

amateria l varie s in
versel y wit habsolut e temperature . Assumin g tha t th e vapo r

pressur e o f

a naci dga s constituen t ove r th e DE A solutio nplot s a s astraigh t lin e whe nlo g vapo r pressur e i s plotte dagains t th e reciproca l o f th e absolut e temperatur e give s ris e t o th e followin g interpolatio nequation :

l nPPT= 1 " PP

TM +

Fo r CO , a t 60° C l npp C Q= l n42 +

= 1.976 1 PP C Q= 7. 2 psi a Fo r H, S a t 60 ° C

l nppH. S = ln2. 8 +

= 1.405 6 PP Hg = 4. 1 psi a 

### 1

32 3 1 1 t + 27 3 

### 1 32 3 37 3



### 1 32 3 1 1 33 3 1 32 3 37 3



### 1 32 3 1 1 33 3 1 32 3 37 3 . /

P P\ 

### '"(-PPT ;

I n 4 7 4. 2

l n 1 5 2. 8 3 . Ballard , D. , Hydrocarbo nProcessing , 44 (No . 4) , 131
- 13 8 (1965) . c , d . Silica gel. Alumina. 4 . Beck , J . E. , "Operationa l Problem s inCO Removal a t th e Mitchel l Plant, " Proc . Ga s Cond . Conf. 1960,129
- 40 . MEA, DEA. 5 . Benson , H . E. ; Field , J . H. ; Haynes , W . P. : "Improve d Proces s fo r

CO , Absorptio nUse s Ho t Carbonat e Solu
tions, " Chemica l Engineerin g Progress , 52 , p p 433- 8 (Oct. , 1956) . HKC. 6 . Benson . H . E . an dParrish , R . W. , "Hi-Pur e Proces s Remove s CO/H,S" , Hyd . Proc . p . 81 . (Apri l 1974) . Benfield HKC. 7 . Boston , F . C , "Adsorptio nProces s Use s Multistaging" , Hyd . Proc . an d Pet . Ref . 43 , No . 8 , pp . 141-14 5 (Aug
us t 1964) . a . Solid

bed. 8 . Buckingham , P . A. , "Fluo r Solven t Proces s Demon
strate dinEPN GPlant" , NGA ARegiona l Meeting , Odessa , Texas , Ma

y 1961 . Fluor. 9 . Buckingham , P . A. , Hydrocarbo nProcessin g an d Petroleu mRefiner , 43 , No . 4 , p 11 3 (April 1964) . Fluor. 10 . Comeaux , R . V. , Hydrocarbo nProcessing , 4 1 (No . 5) , 141-14 3 (1962) . d . MEA corrosion. 11 . Connors , J . S. , Oi l Ga s J. , 5 6 (No . 9) , 100-11 0 (1958) . a , c , d . MEA. 12 . Conviser , S . A. , "Molecula r Sieve s Use dt o Remov e Mercaptan s fro mNatura l Gas" , Oi l an d Ga s Journal , pp . 130-13 3 (Dec . 6,1965) . c . Mol sieve 13 . Cook , T . P . an dR . N . Tennyson , Chem . Eng . Progr. , 65 , No . 11 , 61-64 , (Novembe r 1969) . Fluor. 14 . Dailey , L . W. , Oi l Ga s J. , p . 13 6 (Ma y 4 , 1970) . a , c . • SNPA-DEA. 15 . Dingman , J . C , Hydrocarbo nProcessing , 4 2 (No . 9) , 189-19 1 (1963) . b . MEA. 16 . Dingman , J . C ; Allen , D . L. ; Moore , T . F. , Hydrocar
bo nProcessing , 45 , (No . 9) 28 5 (1966) . a, c , d . MEA corrosion. 

# c

BIBLIOGRAPHY-GA S TREATIN G Subjec t i s indicate db y cod e followin g reference . a—desig n b—physical an dchemica l propertie s c —operatio n d—corrosio nan dmaterial s of constructio n HKC— -hot

potassiu mcarbonat e Fluor—propylene carbonat e Selexol—polyglycol ethe r General— considers man y processe s 1 . Allensandria , A . B . an dJaggard , Norton , "Refiner s Repor t Ne w Case s of

Stainles s Stee l Failure, " Petrol . Refine r 39 , No . 5 , 151-15 6 (1960) . c , d . 2 . Allie dChemical Corp. , Solva y Proces s Division : "Th e Ho t Potassiu mCarbonat e Proces s fo r Aci dGa s Ab
sorption, " Technica l Servic e Repor tNo . 6.6 1 (Marc h 30 , 1961) . HKC. 17 . Dingman , J . C . an dMoore , T . F. , "Compar e DG Aan d ME ASweetenin g Methods" , Hydrocarbo nProc . 47 , No . 7,138-14 0 (1960) . MEA, DGA. 18 . Donnelly , R . F . an dD . R . Henderson , Can . NGP A Thir d Quarterl y Meeting , Calgary , Sept . 13 , 1974 . DEA. 19 . Do w Chemical Company , The , "Propylen e Carbonat e fo r Natura l Ga s Purification" , For mNo . 164-86 , Sep
tembe r 1960 . Fluor. 20 . Dunn , C . L. ; Freitas , E . R. ; Goodenbour , J . W. ; Hen
derson , H . T. , an dPapadopoulos , M . N. , "Ne w Pilo t Plan t Dat ao nSulfino l Process" , Hydrocarbo nProc
essin g an d Petroleu mRefiner , Vol . 43 , No . 3 , p p 150
- 154 , Marc h1964 . Sulfinol. 21 . Dunn , C . L. , Freitas , E . R. , Hill , E.'S. , an dSheeler . J . E . R. , "Sulfino l Process" , Oil an d Ga s Journal , March , 1965 , p p 89-92 . Sulfinol. 

# L



# < r

Rev . 197 6 15-2 8P.2 0



# c

c

C 22 . Ebdon , J . Fred , "Tw o E l Pas o Natura l Plants" , Ga s

45 , No . 6 , 52-5 8 (1969) . DGA. 23 . Eickmeyer , A . G. , "Catalyti c Removal of CO." , Chem
ica l Engineerin g Progress , 58 , #4 , p p 89-9 1 (April , 1962) . HKC, Catacarb. 24 . Ellis , G . C ; Leachman , G . S. ; Formaina , R . E. ; Hazel
ton , R . F. ; Smith , W . C , Proceeding s Ga s Condition
in g Conferenc e 1963 , B-l-B-19 , Th e Universit y of Oklahoma , b . MEA. 25 . Fitzgerald , K . J. , an dRichardson , J . A. , Hydrocarbo n Processing , 4 5 (No . 7) , 125 (1966) . a , b , c . MEA. 26 . Fitzgerald , K . J . an dRichardson , J . A. , Oi l Ga s J , 64 (No . 43) , 11 0 (1966) . a, b , c . MEA. 27 . Goar , B . G. , "Sulfino l Proces s Ha s Severa l Ke y Ad
vantages" , Oil an dGa s Journal , Jun e 30 , 1969 , p 117
- 120 . Sulfinol. 28 . Greene , P . A . an dKutsher , G . S. , "Carbo nDioxid e Remova l an dRecovery—Ne w Polyglyco l Ethe r Proc
esses" , Proceeding s o f

th e Ga s Conditionin g Confer
ence , Universit y o f

Oklahom aExtensio nDivision , Norman , Oklahom a(1965) . Selexol. 29 . Gustafson , K . J. , an dHealey , Jr. , M . J. , "Remova l o f Hydroge nSulfid e fro mNatura l Gas/Carbo nDioxid e Mixture s wit hMolecula r Sieves" , Presente da t

th e 18thAnnua l Ga s Conditionin g Conference , Norman , Oklahom a(Apri l 3 , 1968) . a , b , c . Mol sieve. 30 . Harris , T . B. , an dVictory , R . M. , "Recen t Molecular Siev e Product s an dProces s Development s inNatura l Ga s Processing" , Presente da t th e 20thAnnua l Ga s Conditionin g Conference , Universit y of Oklahoma , Norman , Oklahom a(Apri l 1 , 1970) . a , b , c . Mol sieve . 31 . Hegwer , A . M. , an dHarris , R . A. , "Selexo l Solve s Hig h H,S/CO , Problem" , Hydrocarbo nProcessing , Volum e 49 , No . 4 , Apri l 1970 , p 103 . Selexol. 32 . Holder , Howar dL. , "Diglycolamin e —A Promisin g Ne w Acid-Ga s Remover" , Oi l Ga s J. , 64 , No . 18 , 83
- 8 6 (1966) . DGA. 33 . Jean-Pierre , R. , an dGuillo , R. , Canadia nPatent , 651 , 379 . a, c . SNPA, DEA. 34 . Jones , J . H. ; Froning , H . R. ; an dClaytor , E . E. , Jr. , J . Chem . Eng . Data , 4 (No . 1) , 85-9 2 (1959) . b . MEA. 35 . Katz , Donal dL. , "Handboo k of Natura l Ga s Engineer
ing" , McGraw-Hil l Book Co. , Inc . (1959) . a , b , c , d . General. 36 . Kohl , Arthu r

L . an dReisenfeld , Fre dC , "Ga s Purifi
cation" , McGraw-Hil l Book Co. , Inc . (1960 ) (Chemical Engineerin g Series) . General. 37 . Kohl , A . L . an dP . A . Buckingham , Petroleu mRefiner , 39 , No . 5 , p 19 3 (May 1960) . Fluor. 38 . Kohl , A . L . an dF . E . Miller , U . S . Paten t 2926751 , Marc h1 , 1960 . Fluor. 39 . Kutsher , G . S . an dSmith , G . A. , "CO , Remova l an d Recovery—Pegasol- A Solven t Process" , Proceeding s of th e Ga s Conditionin g Conference , Universit y o f Oklahom aExtensio nDivision , Norman , Oklahom a (1966) . Selexol. 40 . Kutsher , G . S. ; Smith , G . A. ; Greene , P . A. , "Sou r Ga s Scrubbing—Allie dChemica l Solven t Process" , Pro
ceeding s o f

th e Forty-Sixt hNGP AAnnua l Conven
tion , Marc h14-16 , 1967 , Houston , Texas . Selexol. 41 . Lang , France s L . an dMason , J . F. , Jr. , "Corrosio ni n Amin e Ga s Treatin g Solutions" , Corrosio n14 , No . 2 , 105 + -108 + (1958) . d . Amine. 42 . Leachman , Georg e S . an dEllis , Garlan dC , "Trouble
Fre e Ethanolamin e Gas-Treatin g Plants" , Oi l Ga s J . 50 , No . 30 , 84-8 8 (1961) . Amine. 43 . Lee , J . I. , Otto , F . D. , an dMather , A . E. , "Th e Solu
bilit y of Mixture s of

CO , an dH S inDE A Solutions" , Canadia nJ . Chem . Eng. , 52 , p . 125 (1974) . b . DEA. 44 . Maddox , R . N. , "Ga s an dLiqui dSweetening" , J . M . Campbel l Petroleu mSeries , a , b . General. 45 . Maddox , R . N. , an dBurns , M . D. , Oi l Ga s J. , 6 5 (No . 33) , 131-13 3 (1967) : Ibid. , 6 5 (No . 34) , 83-8 5 (1967) : Ibid. , 6 5 (No . 35) , 116-11 7 (1967) . a, c . General. 46 . Maddox , R . N. , an dBurns , M . D. , Oi l Ga s J. , 6 5 (No . 38) , 112-12 1 (1967) : Ibid , 6 5 (No . 40) , 110-11 1 (1967) . a, c . General. 47 . Maddox , R . N. , Proceeding s 49t hNGP AAnnua l Con
vention , 93-103 , Marc h17-19 , 1970 , Denver , a, c . General. 48 . Mason , J . R. , an dGriffith , T . E. , "MEA-DG ASwitc h Save s Steam" , Oil Ga s J . 67 , No . 23,67-6 9 (1969) . DGA. 49 . Moore , Kennet hL. , "Corrosio nProblem s inaRefiner y Diethanolamin e System" , Corrosio n16 , No . 10 , 503 + - 506 + (1960) . c , d . Amine. 50 . Mottley , J . R. , an dFincher , D . R. , "Inhibitio no f Monoethano l Amin e Solutions" , Material s Protectio n 2 , No . 8 , 26-3 0 (1963) . c , d . HKC. 51 . Muhlbauer , H . G. , an dMonaghan , P . R. , Oi l Ga s J. , 5 5 (No . 52) , 139-14 5 (1957) . b . MEA, Amine equil. 52 . Perry , C . R. , Proceedings , th e Ga s Conditionin g Con
ferenc e 1967 , C-l-C-15 , Th e Universit y of Oklahoma , a , c . MEA. 53 . Polderman , L . D. , an dSteele , A . B. , Oi l Ga s J. , 5 4 (No . 65) , 206-21 4 (1956) . b , c . MEA. 54 . Schoofs , J . R. , "Molecula r Sieve s fo r

Natura l Ga s Sweetening" , Addres s a t Wester nGa s Processor s an d Oi l Refiner s Association , Anaheim , Californi a(Octo
be r 6 , 1966) . b , c . Mol

sieve. 55 . Sweeney , Joh nL. , an dBrooks , Geral dE. , "Selexo l a t For t Stockton" , Proceeding s o f th e Ga s Conditionin g Conference , Universit y o f Oklahom aExtensio nDivi
sion , Norman , Oklahom a(1970) . Selexol. 56 . Taylor , D . K. , "Ho w t o Desulfuriz e Natura l Gas" , Oi l an dGa s Journal , Nov.-Dec . (1956) . Iron Sponge. 57 . Thomas , T . L. , an dClark , E . L. , "Molecular Sieve s Reduc e Economi c Operationa l Problems" , Oi l an dGa s Journal , 65 , No . 12 , p p 112-11 5 (1967) . c . Mol sieve. 58 . Thomas , T . L. , an dClark , E . L. , "Molecula r Siev e Proces s Development s an dThei r Impac t o nth e Natu
ra l Ga s Industry" , Reprinte dfro mProceeding s fo r Forty-Sixt hAnnua l Conventio no f th e Natura l Ga s Processor s Association , c . Mol sieve. 59 . Thomas , T . L. , "Molecular Sieve s inPetroleu man d 15-2 9 Rev . 197 6P.2 1

Natura l Ga s Processing" , Adapte dfro mapape r pre sente da t th e Sixt hWorl dPetroleu mCongress , Frank
furt/Main , c . Mol

sieve. 60 . Turnock , P . H . an dGustafson , K . J. , "Advance s in Molecula r Siev e Technolog y fo r

Natura l Ga s Sweeten
ing" , Proc . Ga s Cond . Conf. , Univ . of Otolahoma , 1972 . b . Mol sieve. 61 . Young , Jr. , Phili p L. , "Molecula r Siev e Adsorptio ni n LN GPlan t

Pre-Purification" , Presente da t th e Distri
butio nConferenc e America nGa s Association , Hous
ton , Texa s (May 6-9 , 1968) . a , c , d . Mol sieve. 62 . Zapffe , Fred , "Sou r

Ga s Treating : A Desig nProblem" , Proc . Ga s Cond . Conf. , Univ . o f Oklahoma , 1969 . a . General. 63 . Jones , J . H. ; Froning , H . R. ; an dClaytor , E . E. , Jr. : Chem . Eng . Data , 4 , p . 8 5 (Jan . 1959) . 64 . Lee , J . I. : Otto , F . D. ; an dMather , A . E. : Ga s Proc
essing/Canada , p . 26 , March-April , 1973 . 65 . Lee , J . I. ; Otto , F . D. ; an d.Mather , A. E. : "Solubilit y o f CO , inAqueou s DE A Solution s a t Hig hPressures" , J . Chem . Eng . Dat a17 , 46 5 (1972) . b . 66 . Lee , J . I. ; Otto . F . D. ; an dMather , A . E. : "CO . an dH S i n2.5 NME A Solution" , Can . J . Chem . Eng . 52 , 80 3 (1974) . b . 67 . Isaacs , E . E. ; Otto , F . D. ; an dMather , A . E. : "Solubil
it y of Aci dGase s inAqueou s DIP A Solutions" , 68th Annua l AICh Emeeting , Lo s Angeles , Nov . 16-20,1974 . b . HmS, CO,. 

# c

Fig . 15-3 4 Hydroge n Sulfid e an d Carbo n Dioxid e Partia l Pressure s Ove r 1 5 wt % Monoethanolamin e Solution s Containin g Hydroge n Sulfid e

an d Carbo n Dioxid e a t 40°C .

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_R . N . Maddox , Oklahom a Slat e Universit y



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# c

C

Gasolin e an d LP-gas treatin g Mos tgasolin e an d LP-ga s stream s contai n sulfu r i n variou s forms . Thos e tha tar e especiall y objec tionabl e ar e hydroge n sulfide , mercaptan s an d ele menta l sulfur . Gasolin e containin g hydroge n sulfid e ha s a n objectionabl e odo ran d i s corrosive . Mercap tan s giv e aver y objectionabl e odo rt o th e gasolin e an d elementa l sulfu rmake s th e gasolin e ver y cor rosive . A produc tcontainin g th e objectionabl e ele ment s ca n b e treate d t o remov e th e hydroge n sulfid e an d elementa l sulfu ran d t o eithe rremov e th e mer captan s o rconver tthe m t o les s objectionabl e com pounds . Hydroge n sulfid e remova l Hydroge n sulfid e ca n b e remove d fro m LP-ga s an d gasolin e b y liquid-liqui d contactin g processe s usin g acausti csolutio n o rethanolamines . Th e ethanolamin e processe s ar e describe d i n th e gas treatin g sectio n earlie ri n thi s chapter . I n thi s ap plication , precaution s mus tb e take n t o minimiz e th e introductio n o f

hydrocarbon s int o th e regeneratio n sectio n o f

th e amin e unit . Sulfu rremova l Elementa l sulfu ri s remove d fro m th e gasolin e b y contactin g i twit h apolysulfid e was h solution . A sulfid e solutio n i s mad e u p b y usin g th e followin g amount s o f

chemical s pe r1,00 0 gallon s o f water : 1,000 l b o f

causti c(NaOH) , 80 0 l b o f commercia l Na-j S an d 2 0 l b o f

sulfur . Th e flak e sodiu m sulfid e (Na^S ) i s melte d i n ava tb y us e o f astea m lance . Add"th e sulfu rto th e melte d Na 2 S . Th e sulfu rmus t b e completel y dissolve d i n th e liqui d sulfide , an d 

# c the n thi s mixtur e i s adde d t o th e 10 % (1,00 0 ga l wate ran d 1,000 l b NaOH ) causti csolution . (Pro tectiv e clothin g an d goggle s shoul d b e wor n whe n handlin g thes e chemicals) . Mercapta n treatin g Mercaptan s ar e converte d t o disulfide s o rre move d fro m gasolin e b y severa l method s t o provid e asatisfactor y product . Th e metho d o rcombinatio n o f method s tha tca n b e use d depend s o n th e mercapta n conten tof

th e produc tt o b e treate d an d th e specifi catio n tha tmus tb e met . Regenerativ e causti cproces s Th e regenerativ e causti cmetho d o f removin g methy l an d ethy l mercaptan s fro m LP-ga s o rbutan e employ s countercurren tcontactin g o f th e liquid s wit h 10 % sodiu m hydroxid e solutio n i n apacke d column . Th e causti ci s regenerate d i n astrippin g colum n b y th e additio n o f ope n stea m o rb y stea m internall y generate d b y acolum n heatin g element . A condense rma y b e use d t o condens e wate rvapor s tha tg o overhea d wit h th e liberate d mercapta n vapors . Th e condensat e i s returne d t o th e strippin g colum n t o maintai n causti cconcentration . A n LP ga s strea m containin g 0.03 % mercapta n sulfu rca n b e treate d docto rswee twit h volum e ratio s o f hydro carbo n t o causti ca s lo wa s 3 3 t o 1 . Approximatel y si x pound s o f

proces s stea m pe rgallo n o f causti car e require d fo rregeneration . Th e followin g ratio s ma y b e mor e desirabl e becaus e o f plan teconomics : L b steam/ga l NaO H 4 5 6 7 8 1 0 1 2 14. 5 17 £ZL Ga l hydrocarbon /

\_ _ ga l NaO H 1 5 2 5 3 3 3 9 4 3 5 0 5 5 6 0 6 2 

# C

Rev . 198 1 15-3 8P.3 0 

# c

c



# c

c Highl y corrosiv e condition s tha tca n exis ti n a uni tfo rthi s proces s ar e minimize d b y materia l se lectio n o rb y carefu l attentio n t o operatin g conditions . Th e latte ri s don e b y minimizin g th e contaminatio n o f th e regenerativ e causti csyste m wit h sodiu m sul fid e an d b y operatin g th e reactifyin g colum n a tlo w pressur e an d temperature . Th e maximu m desire d stea m temperatur e t o th e kettl e elemen ti s 260°F . Th e sulfid e contaminatio n i s controlle d b y causti c washin g th e LP-ga s ahea d o f th e mercapta n ab sorbe ran d b y blowdow n o f th e circulatin g solution . A maximu m Naj S conten to f 0.2 % i s suggested . Th e diamete ro f

th e mercapta n absorber , alon g wit h othe rliquid-liqui d treaters , i s base d upo n th e hydrocarbo n throughput . A typica l desig n use s flo w rate s o f 10-1 5 gpm/s q f

to f cross-sectiona l areafo r acolum n packe d wit h 1 % in . raschi g rings . Othe r towe rpacking s ma y b e use d and , if so , th e abov e throughpu twoul d b e changed. . Th e packe d heigh t i s normall y abou t3 0 ft , broke n u p int o tw o o rthre e packe d bed s t o optimiz e dispersio n o f th e hydro carbo n phas e A n additiona l 8-1 0 f to f colum n heigh t i s require d fo rdistributio n an d settlin g areas . Mero xproces s A varian tof

. th e regenerative causti cproces s ha s bee n develope d by UOPProces s Division . Sou rproduc ti s treate d with causti ccontainin g Mero xcatalys tt o extrac tth e mer captans . Th e Mero

x solutio n i s regenerate d by mixing with ai ran d oxidizing . Disulfide s an d exces s ai rar e remove d overhead . Existin g extractio n equipmen twit h stea m re generatio n can b e adapte d to th e Mero x process . Causti c was h A causti cwas h ma y b e use d t o remov e hydroge n sulfid e o rmethy l an d ethy l mercaptan s fro m gaso line . Equa l volume s o f gasolin e an d recirculate d causti car e mixe d b y mean s o f apum p an d discharge d t o acausti csettlin g tan kwher e th e liquid s separate . Th e siz e o f

th e tan krequire d i s base d o n th e reten tio n tim e necessar y fo rcomplet e separatio n o f th e gasoline-causti cemulsion . Th e retentio n tim e varie s fro m on e an d ahal f

hour s fo rheav y gasoline s t o three-fourth s o f

a n hou rfo rpropane . Sinc e th e separatin g tan ki s one-thir d ful l of causti csolution , th e gasolin e retentio n tim e i s base d o n two-third s o f th e tan kvolume . SOU D POTASSIUM HYDROXID E TREATMEN T Soli d potassium hydroxid e may b e used to remove small amounts o f

sulfu rcompounds from liquid propane and LP ga s streams . Th e reactio n fo rthi s proces s is : H, S + 2KO H • K. S + 2H. O Theoretical consumptio n o f KO H i s 3.2 9 lb/l b o f H2S . Actual consumptio n ha s been reported to be abou t 4.4 5 lb/lb , representin g a n efficiency o f 74%. Althoug h wate ri s forme d a s areactio n product , i ti s necessar y t o ad d smal l quantitie s of wate rt o th e be d i n orde rfo rth e reactio n t o progres s properly . Thi s treatin g metho d i s normall y applie d t o dr y propan e stream s containin g smal l amount s o f hydro ge n sulfid e an d mercapta n contaminant . Th e produc t t o th e treate rmeet s cobal tbromid e specification , a s doe s th e treate d stream . Th e wate radde d plu s tha t forme d i s apparentl y hel d b y th e chemica l an d settle s t o th e botto m o f th e vesse l a s asolution . Thi s aqueou s solutio n shoul d b e draine d fro m th e vesse l daily . Th e require d wate radditio n i s abou ton e quar t fo r20,00 0 gal , bu tma y var y dependin g upo n th e H. S content . A mixtur e of methano l an d wate rca n b e adde d i n winte rt o avoi d freezing . A n effectiv e mixin g devic e mus tb e installe d downstrea m o f th e poin to f wate radditio n t o insur e tha ti ti s dissolve d i n th e propane . Otherwise , th e wate ri s ineffective . Poo rmixin g i s evidence d b y alo wsolid s conten to f th e draine d solution . Constructio n o f

th e soli d causti ctreate ri s ver y simple—requirin g onl y avesse l wit h th e necessar y interna l support s fo rth e caustic , an d th e variou s nozzle s fo rth e fluids . Lo wpropan e velocit y (1. 5 ft/mi n superficia l velocity ) i s use d i n orde rtha t th e reactio n product s ca n settl e an d b e draine d off . A thighe rvelocitie s i tbecome s necessar y t o sto p th e flo wfo rafe wminute s t o permi tsettling . N o regeneratio n i s required . N o utilitie s ar e required . Walnut-size d KO H i s recommended . A scree n shoul d b e place d ove rth e outle tlin e t o preven t carry-ove rof

causti ci n cas e o f

flashin g of

propan e o n startup . Methano l o rCO , in th e liqui d fee d strea m wil l caus e additional causti cconsumption . CO, , react s with KO

H an d consume s approximatel y th e sam e amoun to f KO H a s doe s H.S . I f i n sufficien tquantities , th e combine d H.S , CO.., and methano l can dictat e considerin g anothe rproces s be caus e of shorte rbe

d lif e and cos to f

KO H replacement . Molecular-sieve s treatin g proces s Propane , butan e an d mixe d LP-ga s stream s ca n b e treate d t o mee tGP A specification s fo rdryness , volatil e sulfu ran d corrosio n wit h molecula rsieve s i n aon e ste p process . Mos tunit s trea tpropan e o r butan e stream s bu tth e proces s principle s ar e th e sam e fo rmixe d LP-ga s stream s an d ma y b e extende d t o selecte d natura l gasolin e streams .

PROCES S DESCRIPTIO N A typica l proces s flowshee tfo ratw o be d syste m appear s i n Fig . 15-33 . Whil e on e be d i s o n adsorp tio n (treating ) th e secon d be d i s regenerated . A typica l proces s cycl e consist s of : 1 - Treating—Liqui d fee d passe s (eithe rupflo w o rdownflow ) throug h on e be d of typ e 13 X molecula r sieve . Sufficien tfee d pressur e i s use d t o maintai n liqui d phas e flow . Propan e treater s usuall y operat e a t20 0 t o 25 0 psi g wit h butan e treater s a t10 0 to 15 0 psig . Th e molecula rsiev e selectivel y remove s firs t wate ran d the n sulfu rcompounds . Th e amoun to f molec ula rsiev e require d depend s primaril y o n quantit y an d typ e o f sulfu rcompound s presen ti n th e fee d stream . 15-3 9 Rev . 1977 . 1979 . 198 1P.3 1

Fo r stream s containin g les s tha n1 5 grains/10 0 sc f sulfu r compound s th e treate r i s abou t

th e sam e siz e a s th e alumin adehydrato r require ddownstrea m fro macausti c scrubber . 2 . Drain—Afte r

treatin g (t o 2

4 hours ) th e bed s ar e switched . Liqui di s draine ddownflo w fromth e be dtake nof

f treatin g usin g aga s pa dwit h1 0 t o 2 0 ps i drivin g force . Draine dliqui dma y b e sen t to swee t produc t storag e if

downflo w treatin g i s use do r recycle d t o feedif upflo w treatin g i s used . 3 . Depressurize—Sinc e heatin g ga s i s usuall y a t alowe r pressur e tha nth e treatin g step , i t i s neces sar y t o depressuriz e th e vesse l t o th e heatin g ga s pressure . Thi s i s don e th e sam e tim e th e heatin g ste p i s starte dan dwil l therefor e usuall y b e i nth e sam e flow directio na s heating . Be dliftin g ma y occcu r if upflo w depressurizatio ni s to o rapid . Down
flow depressurizatio ni s preferre da t rate s of

5 0 psi/minut e o r

less . Durin g th e depressur e ste p liqui d hel du p o nth e be dflashes . Th e vesse l an dexi t line s ma y becom e noticeabl y cold . 4 . Heat— A swee t

ga s a t moderat e pressure s i s use dt o regenerat e th e molecula r siev e i nth e opposit e flo w directio na s treating . Temperatur e an dflo w rat e depen do nth e quantitie s o f wate r an dsulfu r

com pound s t o b e removed , th e hydrocarbo nstrea mtreate d an dth e qualit y o f

th e regeneratio ngas . Typica l oper atin g range s are : pressur e 5 0 t o 20 0 psig , temperatur e 550° t o 650 ° F. , flo w rat e 4 0 t o 8 0 scf/l b molecula r sieve . Change s i nan y o f

th e regeneratio nvariable s ca nsig
nificantl y affec t

th e performanc e o f

th e treater . Efflu
en t regeneratio nga s i s coole dan dreturne dt o aga s system . 5 . Repressurize—Thi s ste p i s require dafte r heat
in g if liqui dproduc t

i s use dfo r

cooling , bu t

woul d follo w th e coolin g ste p if ambien t temperatur e purg e ga s i s used . Repressurizin g wit hproduc t liqui d actuall y occur s a s th e firs t par t of th e coolin g step . A slipstrea mof

produc t liqui dt o b e use dfo r

coolin g i s slowl y ble dint o th e ho t molecula r

siev e be dan da s th e liqui dflashes , th e vesse l repressure s t o th e prod
uc t pressure . A repressur e rat e of les s tha n5 0 psi / minut e i s preferred . 6 . Coo l an dfill—Produc t liqui dfro mth e on strea mtreate r

i s normall y use dfo r coolin g i nth e sam e flo w directio na s treating . Coolin g i s accom plishe da s th e liqui dflashe s o ncontac t wit hth e ho t vesse l an dmolecula r

sieve , an dcontinue s a s aliqui d leve l begin s t o buil di nth e botto mof th e vessel . Ef

fluen t coolin g vapo r

i s condense di nacoole r befor e blendin g int o th e produc t stream . Whe nth e treatin g directio ni s downflo w th e entir e vesse l mus t b e fille dwit hliqui dprio r t o switchin g t o driv e al l ga s fro mvoi dspace s t o insur e n o channelin g fro mtw o phas e flow . Typica l liqui dcoolin g rate s ar e 3 t o 6 gpm , 1000 l b of

molecula r

sieve . Ambien t temperatur e purg e ga s ca nals o b e use d fo r coolin g afte r

whic hproduc t

liqui di s ble dint o th e be dt o repressur e an dfill . Whe nth e coo l an d fil l ste p i s complet e th e bed s ar e switche dan dtreat in g i s starte do nth e coole dbed . DESIG N CONSIDERATION S Tw o be dsystem s ar e mos t commo nfo r

LP-ga s f treatin g bu t

three , fou r

o r multipl e be doperatio ni s als o possible . Inle t

an doutle t

nozzle s shoul db e equippe dwit hbaffl e plate s o r equivalen t

distribu
tors . T o preven t

los s of molecula r

siev e durin g a n upse t condition , nozzle s shoul db e covere dwit ha fin e mes hscreen . Three-wa y valve s ma y resul t i n investmen t

economie s bu t

tw o wa y valve s ar e pre ferre dt o minimiz e leakag e problems . Molecula r

siev e typ e 13 X ca nlas t fro m3 t o 6 year s i ntreatin g service . Usefu l lif e an doptimu m performanc e ar e enhance db y prope r choic e of

re generatio ncondition s an dguardin g agains t thes e proble mareas : A " 1 . Durin g start-ups , shu t down s an dturna round s car e shoul db e take nt o avoi dcarryove r bump s of absorbe r

oil , glyco l o r

excessiv e amount s o f

water . Asimpl e by-pas s lin e i s especiall y usefu l durin g start-ups . 2 . If corrosio ninhibitor s ar e injecte dupstrea m o r absorbe r

oi l carryove r

i s suspected , coalescer s and/o r alaye r of activate dcarbo no nth e inle t en d of th e be dshoul db e added . 3 . Iro nsulfid e an diro nflak e carryove r ma y b e eliminate db y addin g afilte r o nth e fee dinle t

line . 4 . Sulfu r

compound s loade do ntyp e 13 X ma y reac t vi ath e Clau s reactio nwhe nexpose dt o ai r f durin g unloading . Th e be dshoul db e thoroughl y I regenerate dan dals o purge dwit hiner t ga s prio r

t o dumping . 5 . Molecula r

siev e unloade ddurin g maintenanc e turnaround s shoul db e store di nairtigh t container s i f re-us e i s planned . 6 . Minimiz e glycol , amin e o r absorbe r

oi l i nth e purg e ga s whic hcoul dcaus e molecula r siev e de
gradation . MOLECULA RSIEV E TREATIN G FEATURE S 1 . Unit s ma y b e designe dfo r flowrate s fro monl y afe w GP M t o hundred s of GPM . 2 . Unit s ma y operat e efficientl y a t throughput s wel l belo w th e desig nconditio ni f ther e i s adecreas e i nrequirements . 3 . Reduce s tota l sulfu r conten t

b y removin g hydroge nsulfide , mercaptan s an dothe r organi c sul
fu r compound s i nth e sam e adsorbe r vessel . 

# c

uc t 4 . Wil l produc e copper-strip , docto r swee t prod
5 . Wil l dr y t o zer o o r trac e wate r

level s i nth e ^ ~ sam e ste p withou t

additiona l equipment .

Rev . 1976 . 1977 , 198 1 15-4 0P.3 2
,..,.,.. . 

# c

c



# c

c 6 . Non-corrosiv e proces s minimize s maintenanc e costs , downtim e an ddisposa l problems . 7 . Sulfu r

compound s remove db y purg e ga s ma y b e burne dwithi nfue l system . Carbony l sulfid e remova l A s concer nfor

minimizin g tota l sulfu r emission s ha s increased , ther e ha s bee nagrowt hof interes t i nremovin g carbony l sulfid e (COS ) fro mpropan e an dLP Gstreams . I t can , of course , b e remove dsacrificiall y b y MEA . I nrecen t year s severa l alternativ e processe s hav e bee nproposed . Mick 1 ha s reporte dsuccessfu l us e of acombinatio nof potassiu mhydroxid e an dmethy l alcohol . Thi s proces s i s als o sacrificial . Th e Malaprop 2

- 3 4 proces s use s Diglycol
amin e bu t

require s unspecifie dmodification s i nth e proc es s flow . Th e ADIP S proces s utilize s diisopropanolamine . Molecula r

sieve s ca nals o b e use dfor removin g COS . Th e Malaprop , ADI Pan dmol e siev e processe s ar e regenerative . 1 . Mick , M . B. , "TVea

t Propan e for

CO S Removal, " Hy
drocarbo nProcessing , p . 137 , July , 1976 . 2 . McClure , G . P . an dD . C . Morrow , "Malapro p Proces s Remove s COS, " Hydrocarbo nProcessing , p . 231 , Jan . 1979 . 3 . McClure , G . P . an dD . C . Morrow , "Amin e Proces s Re
move s CO S fro mPropan e Economically, " Th e Oi l an d Ga s Journal , p . 107 , Jul y 2 , 1979 . 4 . Weber, S . an dG . McClure , "Ne w Amin e Proces s for FC C Desulfurize s Ligh t

Liqui dStreams, " Th e Oi l an dGa s Journal , p . 161 , Jun e 8 , 1981 . 5 . Klein , J . P. , "Development s i nSulfino l an dADI PProc
esse s Increas e Uses, " Oi l an dGa s International , September , 1970 . Perc o soli d coppe rchlorid e sweetenin g proces s Th e coppe r

chlorid e sweetenin g proces s i s use dfo r sweetenin g gasolin e blendin g stocks . I t i s acontin
uou s proces s i nwhic hth e mercapta nsulfu r i nth e gasolin e i s converte dt o disulfide s i nareactio nwit h coppe r chloride . Th e coppe r

chlorid e reagen t

i s impregnate di na stationar y be do f

fuller s earth . A s manufactured , thi s materia l contain s approximatel y 16 % wate r bu t lose s it s reactivit y belo w 7% . T o restor e thi s reactivity , wate r shoul db e adde db y (a ) injectin g asmal l quan tit y of stea mint o th e gasolin e fee dstrea mt o th e treater , o r

(b ) bubblin g asidestrea mo f gasolin e throug hasmal l po t

containin g wate r

an dreturnin g i t t o th e mai nstream . Abov e 30% . th e coppe r chlorid e tend s t o g o int o solutio nan dthu s b e extracte dfro m th e fuller s earth . If

th e gasolin e fee dstrea mi s wate r saturated , i t

wil l b e necessar y t o hea t i t t o preven t th e formatio nof

fre e wate r

whic hwoul dten dt o dissolv e coppe r

chlorid e fro mth e fuller s earth . An y hydroge nsulfid e i nth e gasolin e mus t b e remove db y acausti c was hbefor e contac t wit hth e conversio nbed . I nth e sweetenin g reactio nmercaptan s ar e oxi
dize dt o th e disulfide ; 

### (1 ) 4RS H + 4CuCL 2RSSR + 4CuCl + 4HC 1 Th e cuprou s chlorid e i s reactivate dsimultaneousl y b y addin g ai r

t o th e inle t

gasolin e stream : (2 ) 4 CuC l + 4 HC I + O.. 4 CuC L+ 2H.. 0

Standar d soli d coppe rreagen t tower s Charg e Rat e bbl/do y 18 7 42 4 75 2 1177 150 0 Tewe r >iu , f t 2 X1 0 3 X1 0 4 X1 0 5 X1 0 5 X1 2 Be d ve l c u f t 21. 9 49. 5 88. 0 137. 5 176. 5 Reagen t I b 109 0 247 5 440 0 687 0 883 0 Th e standar dbe ddept hi s 7 f t wit hamaximu m o f 9 f t an daminimu mof

4 f t if standar dtower s ar e no t used .

Th e charg e rat e i s base do ntw o volume s of gaso line/volum e of

reagent/hour . If

th e mercapta ncon ten t of th e gasolin e i s low , thes e charg e rate s ca nb e exceeded . Ai r i s adde dt o th e sou r

charg e b y mean s of

adif
fusin g dis c a t

th e rat e of

1 c u f t of ai r (STP)/bb l of charg e pe r

0.01 % mercapta nsulfur . I f th e mercapta nconten t of th e gasolin e i s high , th e operatin g pressur e mus t b e increase dt o hol dth e additiona l ai r

i nsolution . Th e rat e of

ai r injectio nshoul db e maintaine da s nea r t o thi s figur e a s practica l sinc e insufficien t ai r wil l preven t

complet e reactivatio no f th e reagen t

an d exces s ai r

ma y resul t

i nairbindin g of

th e treate r vessel ; a nextremel y hazardou s condition .

Genera l note s Ther e ar e man y license dprocesse s fo r produc t treating . Informatio no nbot

hprocesse s an dsupplier s i s availabl e in Hydrocarbo nProcessin g specia l issues : Septembe r eve n years—"Refinin g Handbook " an dApri l oddyears—"Ga s Processin g Handbook" . 15-4 1 Rev . 1976 . 1977 . 198 1P.3 3

Mixin g Very goo d mixin g of

gasolin e and treatin g solution s i s accomplishe d by mean s o f alo wefficienc y (40% ) centrifu ga l pump . The gasolin e strea m and solutio n recycl e stream joi n jus tahead o f

th e pum p in equa l volume s an

d are dis charge d to th e solutio n settlin g tank . The siz e o f amixin g pum p i s based on fourtime s th e gasolin e flowrate . San d tower s Sand tower s are usuall y placed downstream of aliquid was h o f gasolin e o rLP-ga s t o remov e an y entraine d wate r o rsolution . Th e gasolin e flow s downwar d through th e tower . Th e desig n o f

th e towe ri s base d o

n aspac e velocity o f 4 volume s o f

gasoline/volum e o f

sand/hour . Distributio n header s Distributio n headers shoul d be provided i n vessel s used fo rliquid-liquid contacting .

TREATIN G SELECTIO N A s aguid e i

n th e selectio n o f

th e method of

treatin g to b e used , th e followin g characteristic s o f each are given : 1 . Regenerativ e causti c a . Handl e larg e volum e o f hydrocarbon . b . Primarily fo rremovin g methyl and ethy l mercaptans . c . Capable o f

producin g a"docto rsweet " product. d . Reduces th e total sulfu rconten to f treate d produc t 2 . Perc o soli d coppe rchlorid e proces s a. Ca n trea tgasolin e stream s with relativel y hig h mer captan content . b . Suite d fo rsmal l flo wrate . c . Sulfu rconten tno treduced . d . Wate rconten tmus tbe onl y tha tof saturation . e . Hydroge n sulfid e mus tb e remove d ahead o f contac t with th e bed . f . I f th e produc

ti s fractionate d afte rtreating , th e over head produc

twil l b e essentiall y sulfur-free . g . Exces s regeneratio n oxyge n may caus e corrosio n downstrea m o f

bed . Gasolin e wit h components tha t may b e affecte d by oxygen , such a s olefins , shoul d no tb e treate d in thi s process . 3 . Causti cwas h a . Us e asingl e was h o rtw o o rthre e washe s in series . b . Bes tsuite d fo rstream s with lowmercapta n content . c . Primarily fo rremovin g hydroge n sulfid e o rmethy l and ethy l mercaptans . d . Disposin g o f

spen tcausti ci s amajorconsideration . e . Relativel y hig h causti cconsumptio n pe r1,00 0 gal o f gasoline . 4 . Soli d potassiu m hydroxid e treatmen t a. Lo winstallatio n and operatin g costs . b . Act s a s adesiccan ta s wel l a s removin g th e sulfu r compounds . 5 . Molecula rsieve s treatin g a. Ca n handle larg e o rsmall stream s wit h equa l facility . b . Reduce s total sulfu rconten tby removin g hydrogen sulfide , mercaptans , o rothe rorgani csulfu rin th e sam e adsorbervessel . c . Wil l produc e copper-strip , docto rswee tproduct . d . Will dr

y in th e sam e ste p withou tadditional equip ment . e . Require s tha tplan tfuel suppl y b e made slightl y sou rf by us e of thi s stream to stri p sulfu rcompounds from V th e molecularsieve . 6 . Meroxtreatin g a . Ca n handle larg e orsmal l stream s with equa l facility . b . Eliminate proble

m o f disposal o f

spen tphenoli ccaustic . c . Producti s swee twhe n i tleave s unit ; no holdin g pe riod i s required . d . Add s proble

m o f sulfu rcompounds fro

m regenerate d ai rleavin g th e regenerator . LP-ga s dehydratio n I ti s usuall y necessar y t o dehydrat e LP-ga s (es - y ^ peciall y propane ) followin g treatin g t o preven tth « formatio n of

hydrate s a s th e LP-ga s i s cooled . Hy drate s ca n form i n propane , fo rinstance , a t42°F . Normally , asoli d desiccan tdehydrator , simila rt o th e typ e discusse d i n th e ga s dehydratio n section , i s employe d t o dehydrat e LP-gas . Desiccant s whic h ar e suitabl e fo rdryin g natura l ga s ar e generall y als o satisfactor y fo rdryin g LP-gas , excep ttha tunsat urate d compounds , suc h a s propylene , ar e polymerize d b y desiccant s whic h contai n alarg e proportio n o f silica . LP-ga s mixture s whic h contai n appreciabl e quan titie s of suc h material s shoul d b e carefull y studie d t o f determin e th e mos tsuitabl e desiccant . I tma y b e f necessar y t o purg e th e desiccan tbe d wit h natura l ^ - ga s befor e regeneratio n wit h LP-ga s (containin g onl y saturate d compounds ) o rgas . Olefi n polymerizatio n ca n b e avoide d b y usin g molecula rsiev e Typ e 3 A whic h selectivel y adsorb s water , only . Regeneratio n of

th e water-saturate d desiccan tbe d i s usuall y accomplishe d b y withdrawin g asmal l vol um e o f LP-ga s fro m th e inle tstrea m an d passin g i t throug h avaporize rt o superhea ti tbefor e i tenter s th e desiccan tbed . Th e water-bearin g LP-ga s vapo r fro m th e be d i s coole d i n ahea texchang e t o condens e th e wate ran d the n flow s int o awater-LP-ga s sepa rator . Th e LP-ga s phas e i s returne d t o th e inle tLP - S ga s strea m downstrea m o f aback-pressur e valv e v _ whic h provide s th e pressur e differentia l require d t o prope l th e regeneran tLP-ga s throug h th e circuit . Th e hea tloa d include s th e hea to f desorptio n o f th e water , th e hea to f desorptio n o f

th e adsorbe d hydroarbon s (usuall y assume d t o b e equa l t o th e hea to f desorptio n of

th e water) , sensibl e hea tt o brin g th e wate rvapor , desiccant , an d stee l vesse l u p t o temperature , an d atmospheri chea tloss . A s i n th e cas e o f th e ga s dehydrator , th e tota l hea tloa d i s se t a ttwic e th e calculate d hea tloa d t o compensat e fo r variatio n i n th e rat e of hea texchang e durin g th e heatin g period . Th e tota l quantit y o f

LP-ga s require d fo rregen eratio n i s establishe d b y dividin g th e tota l hea tloa d b y th e sensibl e hea tof th e vaporize d LP-gas . Fo ra n 

# e

Rev . 1976 , 1977 , 198 1 15-4 2FIQURE 2

C0 2 ABSORBE R 

### GIftMMflRCO-VETROCOK E PROCES S AI ROU T CO 2 OU T •

SOLUTION

PUH P AI R BLOUE R URTE R CIRCULATIO N

PUM PFIOUR E 3 

## TYPICA L GAS SWEETENIN

GB YPHYSICA

L ABSORPTIO

N 

# r 2 

# ^* H 2 8 AND

STRIPPING0R 8 

# X

POWE R RECOVER Y TURBIN E 

### I I I I 

# f SOLVEN T RECOVERY

8TAIPPIN 0 OR SP.3 6

.,,,, • -, ,



### PROCES S DESIG

NO F VARIOU S TYPE S O F SULFU R REMOVAL PROCESSE S

By Leo n L . Patterso n Principa l Proces s Enginee r

FORD , BACO

N& DAVIS , INCORPORATE D Texa s Divisio n Dallas , Texa s

Jun e 198 3



# 4fbro , Baco nA^avis . 3ncorporalp oP.3 7

„ f ;,, - 

### Pag e 1

PROCES S DESIG

NO F VARIOU S TYPE S O F SULFU R REMOV E PROCESSE S

Prio r t o th e 1960's , th e easies t an d mos t economica l wayt o handl e sou r ga s wa s t o "plug th e well " becaus e th e pric e o f ga s wa s i n th e 15C/MC F range . A s th e deman d increase d b

ybot h industryan d th e public , th e ga s reserve s decreased . I n orde r t o kee p up wit h th e demand, ; deepe r well s hav e bee n drille d whic h hav e produce d mor e sou r ga s whic h ha s t o b e processed . Presently , associate d ga s fro mwell s i n Wyoming and othe r state s contain s a s muc h a s 42 % hydroge n sulfid e an d 29 % carbon 1 

### dioxide . A s th e valu e o f the crud e oi l increased , treating o f thi s ga s wa s required , no t fo r th e ga s itsel f bu t fo r th e crud e oi l production . Thi s increase d volume o f sou r o.a< s an d the highe r cos t o f energ yhav e place d he w emphasi s o n th e treating processes . Aci d ga s remova l mayb e require d fo r a numbe r o f reasons : 1 . Specificatio n o f Ga s (Almos t al l o f th e sale s ga s contract s limi t the amoun t o f hydroge n sulfid e t o n o mor e than 0.2 5 grai n pe r 10 0 cubi c fee t o f gas. ) 2 . Specification s o f Liqui d Product s (LPG ha s limitation s o n hydroge n sulfid e an d organi c sulfu r content. ) 3 . Wate r saturate d ga s containing hydroge n sulfid e an d carbo n dioxid e ca n b e corrosiv e t o carbo n steel . 4 . Safet y& Environmenta l Protectio n (Hydroge n sulfid e i s a dangerous-toxi c gas ; i.e. , 70 0 ppmi n ai r i s considere d fata l i n exposure s o f 3 0 minute s o r less. ) 5 . Carbo n dioxide , a n inert , lower s th e hea t conten t o f th e gas . (Almos t al l ga s contract s ar e mad e o n a BT U content. ) 6 . Carbo n dioxid e can caus e problem s a t cryogeni c plan t temperatures .



# 4foro, Baco n&3tovie . 3ncorporalr oP.3 8
Pag e 2

Astudyshoul d b e mad e t o determin e th e proces s fo r th e specifi c applica
tion . Question s tha t nee d t o b e answere d include : 1 . Wha t impuritie s wil l ther e be ? 2 . Wha t i s th e volum e o f ga s t o b e processed ? 3 . Wha t i s th e en d use—fo r ga s o r liquids ? 4 . Wha t chemica l o r physica l proces s wil l b e used ? 5 . Wha t ar e th e cause s o f degradation ? 6 . Ca n i t mee t th e require d ga s specification ? 7 . Ca n i t mee t th e require d specificatio n o f th e aci d gas ? 8 . I s selectiv e hydroge n sulfid e remova l a viabl e solution ? 9 . I s reclaimin g required ? 10 . Wha t ar e th e hea t an d energ yrequirement s fo r th e process ? 11 . Wha t royalt yi s required ? Th e processe s that shoul d b e considere d are : 1 . Ho t Carbonat e Processe s (Figur e 1 ) . Employ s a n aqueou s solutio n o f potassiu mcarbonate . Th e absorbe r an d regenerato r bot h ar e a t elevate d temperatures . A . Proprietar yprocesse s include : (1 ) Benfiel d - severa l activator s (2 ) Girdle r - alkanolamin e activator s (3 ) Catacar b - alkanolamin e and/o r borat e activator s (4 ) Giammarco-Vetrocok e (Figur e 2 ) - arseni c an d othe r activator s B . Th e advantage s o f th e hot carbonat e processe s are : (1 ) Continuou s circulatin g syste memployin g a n inexpensiv e chemical . (2 ) Iso-therma l syste mwher e bot h absorptio n an d desorptio n o f th e aci d gase s ar e nearl ya t unifor mhig h temperature , therefor e n o heat exchang e equipmen t i s require d i n th e flui d circulatin g system . (3 ) Th e desorptio n o f strippin g i s accomplishe d wit h a smalle r stea mrat e tha n require d fo r a n amin e plant . 

## ,iford, .Baco nA^tovis , 3ncorporalr oP.3 9 Pag e 3

C . Th e disadvantage s o f th e ho t carbonat e processe s are : (1 ) Furthe r treatmen t i s require d b ya conventiona l amin e syste m t o economicall yproduc e pipelin e specificatio n product . (2 ) Th e unit s ar e pron e t o corrosio n a s wit h othe r aci d ga s remova l processes . (3 ) Problem s ar e encountere d i n suspende d solid s an d foamin g a s wit h othe r processes . Physica l Processe s (Figur e 3 ) that ar e availabl e include : A . Fluo r Solven t - use s anhydrou s propylen e carbonate . (1 ) Th e temperatur e o f th e solutio n i s wel l belo wambient , whic h require s refrigeration . B . Selexo l - use s dimethylethe r o f polyethylen e glyco l a s a solvent . (1 ) Absorption-remova l o f sou r ga s fractio n i n fee d ga s i n a conventiona l countercurren t absorptio n column . (2 ) Th e solven t i s regenerate d bya serie s o f flashe s an d possibl ya stripper . ( Avariet yo f strippin g ga s include s air , nitrogen , combustio n gas , o r steam. ) C . Sulfino l Proces s - use s Sulfolan e (Tetrahydrothiophen e dioxide) , Di-isopropanolamin e (DIPA ) an d water , o r Methyldiethanolamin e (MDEA ) i n th e plac e o f DIPA . (1 ) Bul k remova l o f carbo n dioxid e i s achieve d wit h minima l hea t requirement s an d wit h n o refrigeration . (2 ) Remova l o f H S , COS , mercaptan s an d othe r organi c sulfu r compound s i s accomplishe d t o mee t pipelin e specifications . (3 ) Th e flo wschem e i s simila r t o a n amin e system . D . Rectiso l Proces s - use s methano l a s th e solven t applie d at extremel ylo wtemperatures , i.e. , -30° F t o -100°F .



## 4foro, Baco n&3Javis , incorporate dP.4 0 I ! VJl'J Pag e 4

Thes e physica l absorptio n processe s operat e i n a comparabl e wa y a s oi l absorption . The yshoul d b e considere d when : (1 ) Th e partia l pressur e o f th e aci d ga s i n th e fee d i s abov e 5 0 psi . (2 ) Th e concentratio n o f heav yhydrocarbon s i s low , a s th e physica l absorptio n als o pick s u p heav yhydrocarbons . 

### (3 ) Whe n bul k H S remova l i s desired . Dehydratio n o f th e treate d ga s i s not require d i n th e Rectiso l o r Selexo l processes . Slurrisweet Proces s Remove s smal l amount s o f hydroge n sulfid e (u p t o 10 0 grains/10 0 cubi c feet) , wit h th e spen t solutio n t o b e dispose d o f a' s waste . Preliminar ytest s indicat e th e spent solutio n •. / b e a ver ygoo d fertilizer . Iro n Spong e Proces s Utilize s a hydrate d iro n oxid e whic h i s impregnate d o n woo d chips . A . Thi s syste mca n b e regenerate d a fe wtime s wit h air . B . Car e must b e exerte d i n th e disposa l o f th e spen t chip s a s th e iro n sulfid e i s pyrophoric . Dr yBe d Proces s Molecula r sieve s ar e bein g use d fo r remova l o f sulfu r compounds . A . Th e operatio n o f adsorbent plant s i s quit e simpl e bu t th e desig n i s ver ycomplex . Manufacturer s mus t b e consulte d fo r potentia l applications . Amin e Typ e Unit s - Chemica l Absorptio n Mine s tha t ma yb e use d are : MEA , DEA , MDE Aan d DGA . Thes e ar e th e mos t commo n type s o f units . Th e specifi c desig n detail s fo r a typica l amin e proces s ar e a s follows .



# .ford, Baco nd^avie , incorporatedP.4 1 lf|l'I V 

### Pag e 5 Prio r t o an

ytyp e o f gas-liqui d contact , whethe r i t i s a sour ga s treatmen t process , ga s dehydration , o r a natura l ga s liquid s extractio n unit , a n effectiv e inle t ga s separato r mus t b e designe d t o remov e entraine d droplet s o r slug s o f liqui d prio r t o enterin g th e system . Typica l contaminant s i n the natura l ga s ar e liqui d hydrocarbons , sal t water , sands , wel l treating chemicals , pipelin e treatin g chemicals , an d compresso r oils . Thes e contaminant s can caus e a numbe r o f operationa l problem s onc e theyge t int o th e sweetening system . Thes e problem s mayinclud e foaming , equipmen t fouling , an d hig h corrosio n rates , whic h resul t i n solven t los s an d difficult yi n meeting swee t ga s specifications . Ther e ar e fou r majo r type s o f separator s available : vertical , horizonta l singl e tube , horizonta l doubl e tube , an d spherical . Th e advantag e o f the vertica l separato r i s th e capabilit yo f handling greate r slug s o f liqui d withou t carryove r t o the ga s outlet . Som e o f the disadvantage s o f th e vertica l separato r ar e tha t i t i s mor e difficul t an d expensiv e t o fabricat e an d shi p i n ski d mounte d assemblies . I t take s a large r diamete r separato r than a horizonta l separator . Spherica l separator s ar e inexpensiv e an d compact . Theydo , however , hav e limite d surg e spac e an d liqui d settling . Th e locatio n an d actio n o f th e liqui d leve l contro l i s ver ycritical . Th e horizonta l separato r ha s severa l advantage s ove r the vertica l separator . I t i s easie r t o ski d mount , les s pipin g i s required , an d a smalle r diamete r i s require d fo r a give n ga s capacity . I t ha s a large r interfac e are a betwee n the liqui d an d ga s phases , whic h aid s i n separation . However , the liqui d leve l contro l placemen t i s mor e critica l an d th e surg e spac e i s somewha t limited . The doubl e tub e ha s a sligh t advantag e ove r the singl e tube bu t obviousl yi s mor e expensive .



# 4ford , Baco nditovie , incorporate dP.4 2 

### Pag e 6
Th e ga s capacit yo f the oil-ga s separator s ha s bee n designe d fo r man y year s b yth e us e o f th e Souders-Brow n equation :

Where : V 

# .£

V = A= Q = G K P 

### L - P 

### G The n A 

# = 2 v Superficia l ga s velocit ybase d o n tota l cross-sectiona l are a o f vessel , ft/se c Cross-sectiona l are a o f separator , sq.ft . Ga s flo wrat e a t operating conditions , ft 3 

### /se c Densit yo f liqui d a t operating conditions , lb/ft 3 

### Densit yo f ga s a t operating conditions , lb/ft 3 

### Imperica l facto r Fo r vertica l separators : 5 fee t high - K 1 0 fee t high - K 0.1 2 t o 0.2 4 (avg . 0.167 ) 0.1 8 t o 0.3 5 (avg . 0.21 ) Fo r horizonta l separators : 1 0 fee t lon

g - K Othe r length s - K = 0.4 0 t o 0.5 0 (avg . 0.45 )

" 0.4 5 * , '• « Fo r spherica l separators : K = 0.3 5

DESIG NO F AMIN E SYSTEM S (Figur e 4 an d Figur e 5 ) Th e absorptio n an d desorptio n o f H S an d C O ar e comple x mas s transfe r and chemica l reactions . The H S an d C O reac t wit h th e amin e wit h the following reactions : Primar yan d SecondaryAmine s RR'N H + RR'NCOO " RR'N H + 

## co 2 

### + H 2 

### 0 H 2 

### S - •

- •

- * • 

### RR'NCOO ~ RR'N H + RR'N H * 2 + + H HC O ~ + HS ~ (Fast )

(Slow ) (Ver yfast ) 

# ,1/ord , Baco n&"5>avi$

. incorporate dP.4 3 irpii!'! ' :• ! 

### Pag e 7 Tertiar y Amine s

R 2 

### NR « R 2 

### NR ' R 2 

### NR ' + + + C0 ? 

## co 2 

### H 2 

### S + H 2 

### 0 -• •



### -> •

- • 

### No reactio n R NHR , + 

### + HC O " + - R NHR ' + H S (Slow ) (Ver yti

1 

### Th e tertiaryamine s canno t reac t directl ywit h C O t o for mcarba
2 i 

### mates . Th e C0 2 

### mus t firs t reac t wit h water , the n combin e wit h th e amin e vi a th e aci d bas e reaction . T o sa yi t i n anothe r way , th e rat e o f reactio n o f C O wit h amine s i s slowe r than th e rat e o f reactio n an d transfe r o f H S . Significan t difference s ar e experience d i n th e rat e o f absorptio n o f C O from 1 

### on e typ e o f amin e t o another . Tertiaryamine s exhibi t th e greates t selectivit yfo r H S ; al l amine s showsome selectivity . Selectivit yincrease s wit h decreasing temperatur e an d decreasing pressure . Th e desig n o f an amin e gas . treating plan t include s determining th e solven t circulatio n rate , reboile r hea t duty , an d towe r diameters . Th e amin e circulatio n rat e i s determine d b ya n iterative calculatio n o f hea t an d materia l balance s aroun d th e absorber , base d o n a n estimate d :approach t o equilibriu

mo f the aci d ga s i n th e ric h solven t a t th e botto mof ] th e absorbe r an

d th e temperatur e o f th e exiting swee t ga s strea ma t the top . T o preven t hydrocarbo n condensation , the lea n solven t temperatur e shoul d b e aroun

d 10° F warme r than th e fee d ga s temperature . Th e produc t ga s temperatur e i s assume d t o b e th e same a s the temperatur e o f the lean solvent . Severa l article s contai n equilibri a dat a o n the solubilit yo f H S , (1 2 3 ) C0„ , an d H S-CO mixture s i n ME Aan d DEA . ' ' The us e o f the's e data , 2 2 2 ( 3 4 ) a s wel l a s the hea t o f reactio n o f H S an d C0 0 

### ' , enabl e a rigorou s determinatio n o f th o require d strengt h an d circulatio n rates .



# .iford. Baco n&"$avie, incorporate dP.4 4

- M r j,, r . , — > 

### Pag e 8 Compute r program s hav e bee n develope d fo r a rigorou s solutio n t o amin e design . Some o f thes e program s are : Simulatio n Science , ChemShare , TSWEET , AMSIM , a s wel l a s Oklahom a Stat e University . Absorber-Contacto r

. Overal l tra

yefficiencywil l b e abou t 2 5 t o 40% ; therefore , 1 6 t o 2 0 actua l tray s ar e generall yused . Some o f the aforementione d compute r program s mode l the absorbe r wit h th e us e o f Murphre e TrayEfficiency . Afte r contac t i n the absorber , th e ric h amin e solutio n passe s int o a hydrocarbo n flas h tank . Th e functio n o f th e flas h tan k i s t o remove mos t o f th e dissolve d hydrocarbons . Dat a o n the solubilit yo f methan e an d ethan e i n aqueou s ME Aan d DE Asolutions , eithe r fre e o f aci d ga s o r wit h H S an d C O , wer e reporte d b yLawso n an

d Garst . Becaus e o f the molecula r structure , DE Aha s th e poores t affinit yfo r hydrocarbons . Th e nex t leve l i s ME Aan d DIPA , wit h DG

Ahaving th e stronges t affinit yfo r hydrocarbons . Aconservativ e approac h woul d b e t o us e hydrocarbo n solubilitie s i n wate r a t variou s temperature s an d pressures . Aslipstrea

mo f lea

n amin e t o a smal l packe d scrubbe r wil l reabsorb th e aci d gase s flashe d ou t o f solutio n wit h the hydrocarbo n vapors . A residenc e time o f approximatel y3 t o 4 minute s i s require d fo r thi s flas h tank . Some o f the flas h tank s hav e a wei r provide d t o enabl e periodica l remova l o f liqui d hydrocarbon s tha t mayb e entraine d wit h the ric h amin e solution . Th e ric h amin e passe s fro mth e flas h tan

k through lean-ric h amin e hea t exchangers . Solutio n hea t exchange r corrosio n problem s occu r whe n aci d gase s ar e liberate d a t th e ho t unit . Genera l practic e i s no t t o prehea t th e ric h amin e solven t abov e 190°F . Thes e exchanger s shoul d hav e impingemen t baffle s a t shel l entr ynozzle s t o minimiz e tube erosio n an d corrosion .



## ,iford , Baco n&3>avis . incorporate dP.4 5 

### ?ag e 9
Thes e exchanger s shoul d b e stacke d verticall ywit h ric h amin e solutio n passing through the tube s an d enterin g th e lowe r par t o f the botto mexchange r i n orde r tha t the liberate d gase s wil l b e remove d i n i • ' 

### upwar d flo wo f amin e solution . Th e maximu mvelocit yt o minimiz e corrosio n i n th e tube s i s 2 ft/sec . Regenerato r (Stripper ) Th e strippe r i s eithe r a tra yo r packe d colum

n wit h approximatel y2 0 tray s o r th e packing equivalent . T o reduc e amin e vaporizatio n lo|ss , ther e i s generall ya was h sectio n a t th e top o f th e vesse l wit h an ajdditiona l fou r t o si x trays . Th e preheated , ric h amin e enter s nea r th e top o f th e vesse l an

d flow s dow

n countercurren t t o a ga s strea mconsisting o f steam , H S and C O . Th e reboile r generate s th e steam , whic h reduce s th e partia l pressur e o f H S an

d C O i n th e ga s strengthening th e driving forc e o f the 

# i aci d gase s fro

mthe amin e solution . Th e overhea d ga s passe s throug h a condense r t o recove r wate r an d th e smal l amoun t o f amin e whic h i s vaporize d i n th e regenerator . Th e reboile r hea t dut yinclude s th e sensibl e hea t require d t o rais e th e temperature s o f th e ric h amin e feed , th e reflux , an d the make--u

p wate r t o th e temperatur e o f the reboiler , the hea t o f reactio n t o break the chemica l bond s betwee n the aci d ga s an d the amin e a s wel l a s the , hea t o f vaporizatio n o f wate r t o produc e a stripping vapor—steam . The reflu x rati o (mole s o f stea mt o mole s o f aci d ga s i n th e overhea d gas , u p strea m o f the condenser ) range s fro m1. 5 t o 4 t o 1 ratio , depending upon the require d purit yo f the lea n amine . Afiltratio n scheme o f mechanica l an d activate d carbo n filter s i s importan t i n maintaining goo d solutio n control . Mechanica l filter s (cartridg e o r precoat ) remove particulat e material , whil e the carbo n filte r remove s th e chemica l contaminants , i.e. , entraine d hydrocarbon s an d surfac e activ e compounds .



# .iford, Baco n&"3>avi$

, incorporate dP.4 6 

### Pag e 1 0
Filter s ar e locate d i n the ric h lin e i n some plants ; i n other , plant s theyar e locate d o n th e lean line . Locating th e filter s i n th e (ric h lin e u p strea mo f th e lean/ric h exchange r wil l protec t bot h the hea t exchange r and th e strippe r frompluggin g b yreducing th e erosion/corrosio n irat e i n th e exchanger . However , i n term s o f safety , i t i s fa r mor e hazardou s t o locat e th e filter s i n th e ric h lin e than the lean line . Th e mechanica l filte r shoul d b e locate d i n fron t o f th e carbo n filte r a s th e carbo n filte r woul d plu g considerabl yfaste r du e t o soli d material . A1 0 . t o 2 0 micro n mechanica l filte r shoul d b e adequat e fo r particulat e removal . Circulatio n rate s through the mechanica l filte r varie s b ypreferenc e fro

m 5 % t o ful l flow . Circulatio n rate s ar e simila r fo r the carbo n filter . Th e carbo n filte r shoul d b e change d whe n a high pressur e dro p exist s acros s the be d a s wit h th e mechanica l filter , o r whe n a colo r compariso n ca n b e mad e betwee n a sampl e take n fro mfilte r effluen t an d a sampl e run through a fres h carbo n filte r i n the lab . A n increas e i n foaming tendenc y wil l als o requir e a filte r change . Asid e strea

mreclaime r operatio n fo r ME Ao r DG A(usuall y0.5 % t o 3 % o f circulate d volume ) i s use d t o effec t the separatio n o f th e amin e fro m it s hea t stabl e salts . Th e flowi s controlle d b yhea t inpu t rat e an d a leve l controller . Initiall ythe reclaime r boiling temperatur e rise s a s th e concentratio n increases . Temperatur e cutoff s i n the ME Aar e i n the 280°t o 300° F rang e t o preven t carryover . Ahig h shutdow

n temperatur e contro l i s desirabl e t o preven t carryove r wit h subsequen t foaming . Some companie s reques t a mean s o f injecting causti c sod a t o the reclaimer . Astud ymad e b

ythe Societ e National e El f Aquitain e o f (7 ) Franc e indicate s tha t the causti c soda react s i n an irreversibl e way , firs t wit h th e stronges t acids , the n i f i t i s i n excess , wit h H S an d C O t o for msodiu msulfid e an

d carbonate . Th e hea t flu

x o n a stea

mreclaime r shoul d b e betwee n 6 t o 8 MBTU/hr.ft J 

### . Th e hea t flu x o n a stea

mheate d reboile r shoul d b e betwee n 9 t o 1 0 MBTU/hr.ft 2 

### . Th e norma l reboile r temperatur e fo r ME Ai s 22 5 t o 260°F , fo r DE Ai t i s 23 0 t o 250°F , an d fo r DG

Ai t wil l rang e fro m25 0 t o 260°F . 

## .ifard. Baco n&"^avi6. incorporate dP.4 7 

### Pag e 1 1

MATERIAL S O F CONSTRUCTION(Figur e 6 ) Absorber-Contacto r Typ e 30 4 o r 41 0 stainles s stee l tray s ar e recommende d t o preven t sticking o f th e valves . Th e vesse l shoul d b e constructe d wit h 1/8 " corrosio n allowanc e carbo n steel . Th e maximu

mvelocit yo f the lean-ric h exchange r shoul d b e limite d t o 2. 0 ft/sec . Preferenc e o f 30 4 stainles s stee l tube s ha s bee n indicate d b y some contractor s o r operatin g companies . I f the pressur e brea k (contro l valve ) i s a t th e stripper , thi s mayno t b e justified . Carbo n stee l wit h a corrosio n allowanc e o f 1/4 " ha s bee n use d satisfactorily . Chahgin g t o stainles s stee l tube s ha s increase d the lif e approximatel ydouble . I f carbo n stee l i s used , stres s relieving the bundl e i s necessary . Reboile r tube s o f carbo n stee l hav e bee n use d successfull ywit h a corrosio n allowanc e o f 1/4 " o n th e shell , wit h a stres s relieve d bundl e an d shell . D o no t excee d 350° F o n th e stea mside . Overhea d condenser s hav e bee n constructe d wit h carbo n stee l wit h n o apparen t disadvantage . A smal l amoun t o f amin e i n th e overhea d condensat e wil l provid e corrosio n inhibition . Experienc e o f goo d operator s ha s show n tha t abou t 0.5 % amin e i n th e condensat e i s a happymedium . Allowabl e velocitie s i n the pipin g systemshoul d b e limite d t o 3 ft/sec . Contro l valve s shoul d hav e velocitie s betwee n 1 5 an d 2 0 ft/sec . Regenerato r (Stripper ) Typ e 30 4 stainles s stee l tray s shoul d b e use d i n the regenerator . The corrosio n proble mi n thi s towe r appear s t o b e mor e sever e than tha t i n the absorbe r discusse d earlier . Th e vesse l shoul d b e constructe d ou t o f carbo n stee l wit h 1/4 " corrosio n allowance . The reflu x dru mshoul d b e stres s relieved . Corrosio n i s high her e a s atteste d b ythe nee d fo r the 1/4 " corrosio n allowance .



## /ord , Baco nd^tovis , incorporatedP.4 8 

### Pag e 1 2

CONCLUSIO

N Th e prope r selectio n o f th e proces s fo r aci d ga s remova l is]necessar y t o reduc e th e excessiv e costs , expenses , an d headache s w e ,have al l \ experience d i n th e past . Mor e innovativ e processe s mus t b e develope d t o | I - J 

### b e abl e t o efficientl yproces s th e verysour ga s produce d fro mth e deepe r formation s an

d th e associate d ga s fromthe oi l well s i n Wyoming .



## .iford. Baco n&3tovis . incorporate dP.4 9 •«V-»rrr'-' " " Pag e 1 3

REFERENCE S 1 . Lee , Ott o an d Mather , "Solubilitie s o f Aci d Gase s i n Amin e Treating Solutions" , CNGPA , Novembe r 30 , 1973 . Ibid , "Solubilit yo f Aci d Ga s i n ME ASolutions" , CNGPA , Novembe r 29 , 1974 . Ibid , "Solubilit yo f H S an d C O i n Aqueou s ME ASolution" , Canadia n Journa l o f Chemica l Engineering , Vol . 52 , Decembe r 1974 . 2 . Lawson , J.D , an d A.W . Garst , "Ga s Sweetenin g Data ; Equilibriu m Solubilit yo f H S an d C O i n Aqueou s ME Aan d Aqueou s DE ASolutions" , Journa l o f Chemica l Engineerin g Data , Vol . 21 , No . 1 , 1976 . 3 . Ga s Processor s Supplier s Association , Engineerin g Dat a Book , GPSA , Tulsa , Oklahoma , 1981 . 4 . Kohl , A.L . an d F.C . Riesenfeld , Ga s Purification , 3r d Edition , Gul f Publishin g Company , Houston , Texas , 1979 . 5 . Lawson , J.D . an d A.W . Garst , Journa l o f Chemica l an d Engineerin g Data , Vol . 21 , No . 1 , pp . 30-32 , 1976 . 6 . McKetta , J.J. , e t al. , Petroleu m Refiner , variou s volumes , 1951 , 1958 , 1961 , 1962 . 7 . Blanc , C , M . Grail , G . Demarais , Societ yNational e El f Aquita'ine , Lacq , Franc , "Th e Par t Playe d b yDegradatio n Product s i n th e Corrosio n o f Ga s Sweetenin g Plant s Usin g DE Aan d MDEA" , Proceedin g of
Ga s Conditionin g Conference , 1982 , Th e Universit yo f Oklahoma . SUGGESTE D REDIN G "Lease-Ga s Sweetening" , 1-11 , Th e Oi l an d Ga s Journal , Augus t 14 , 196 7 Ma y13 , 1968 .



## ,iford , Baco n&3tovis . incorporate dP.5 0



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OF AMINE SOLUTION ) $ PE RSCF DACI DGA S ,0.48 0 ANNUALIZE DCAPITAL COST .2 0 YEA REQUIP . LIFE. : 107 . INT . RATE;CRF= . 11246 ) $/Y RPERSCF DACI D6A S 0.05 4 REGENERATION

HEAT f/Y RPERSCF DACI DGAS 0.24 0 PUMPIN GCOS T W RPERSCF DACI D6A S 0.01 6 LABORCOS T (IMAN/SHIFT , 3SHIFTS/DAY , 365DAYS/YR ; 114.5 0 PERHOUR ! $/Y R12700 0 MAINTENANC E SUPPLIE S (27 . OF CAPITAL COST ) W RPERSCF DACI DGA S 0.00 1 CEMICAL COS T (BASEDQ

N 25 % PE RYEA RREPLACEMENT ) W RPERSCF DACI DGA S 0.01 8jr,i'|'T" ,

CAS E 

### GP A 

### 1 2 SULFUR LT/ D 

### 1 5 5 ACI D 

### GA S XH2 S 0.1 3 

### 0. 5 0. 2 FACTO R CAPITA L COS T it) 10187 5 12734 4 31836 0 FACTO R CAPITA L COS T 

### (WR ) 1146 1 1432 6 35BI 6 FACTO R

HEA T COS T 

### !WR ) 5093 8 6367 2 15913 0 FACTO R PUMPIN G COS T 

### !WR ) 339 6 424 5 1061 2 FACTO R FACTO R LABO R MAINTENANC E COS T 

### (WR ) 12700 0 12700 0 12700 0 SUPPLIE S

($/YR ) 

### 21 2 26 5 663 FACTO R CHEMICAL S COS T 

### (WR ) 382 0 477 5 1193 9 FACTO R

TOTAL 

### O& M 

### (WR ) 18536 6 19995 8 30939 4 FACTO R

, TOTAL COS T 

### ; (WR ) 19682 7 21428 4 ' 34520 9



### 1 0 1 1 1 2 

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### 0. 8 0. 5 0. 2 7959 0 2546B S 63672 0 895 4

2865 2 7163 1 3979 5 12734 4 31836 0 265 3

349 0 2122 4 12700 0 12700 0 12700 0 

### 16

6 53 1 132 7 298 5

955 1 2387 7 17259 8

27291 5 49178 8 18155 2

30156 7 56341 9



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28652 4 313360 0 127344 0 21224 0

8489 6 12700 0 12700 0 1326 5

530 6 23877 0

9550 3 377437 5

15S615 0 449118 5

187267 4

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95503 0 233770 0 924663 8

1471850 0 • 3660575 0 1103746 3

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