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# OAR Box 1828
Prepped by Ollie Stewart



### Document

Number: 

# 300 ) IV-A-1 0

Docket Number: 

# A-83-2 7

Printed 11/12/200811:12:59AM Sheet 300of 325P. 2 

# A-83-2 7

IV-A-1 0

PRODUCTIO N

O F VER YLOW-SULFURRESIDUA L FUE L OIL S

Prepare dby : Davi dWhit e an

dEdwar dMorett i Radia nCorporatio n P.O . Box130 0 Researc hTriangl e Park , NC 2770 9

Prepare dfor : Fre dPorte r Standard s Developmen t Branc h Emission s Standard s andEngineerin g Branc h Offic e o f Ai r Qualit y

Plannin g an

dStandard s U.S . Environmenta l Protectio nAgenc y Researc hTriangl e Park , N C 2771 1

Apri l 10 , 198 7PRODUCTIO N O F VER YLOW-SULFURRESIDUAL FUE L OIL S

SUMMARY
Thi s study

briefl y review s petroleu

m refinin g technologie s an dsuppl y dat a associate dwit hproductio no f ver y low-sulfu r residua l oil s (VLSRO , define da s residua l oil s containin g 0. 3 percen t sulfu r o r less) . O f speci fi c interes t i s th e us e o f residuu m hydrodesulfurizatio n(RHDS ) technolog y t o produc e VLSRO . Informatio nreviewe di nth e stud y include s bot hpublishe d literatur e an

dtelephon e conversation s wit hoi l company personne l an

d desulfurizatio ntechnolog y vendors . Th e primar y conclusion s tha t emerg e ar e a s follows :

• Mos t U.S . petroleu

m refinerie s ar e designe dt o maximiz e th e produc tio no f "highvalue " petroleu m product s suc ha s transportatio n fuels , distillat e oils , an dpetrochemica l feedstocks . A s a result , a substantia l portio no f th e lowe r valu e product s suc ha s residua l oi l i s "upgraded " t o thes e highe r value dproduct s rathe r tha nsol d a s residua l fue l oil . A s a result, th e U.S . import s abou t one-hal f o f it s tota l residua l oi l suppl y fro m othe r countries . Mor e importantly , oyer

three-fourth s o f th e U.S . suppl y o f VLSR O 1 s imported .

• VLSR O ca nb e produce db y eithe r RHD S o f high-sulfu r residuu m o r distillatio no f yery

low-sulfu r crud e oil . Becaus e o f th e high sulfur , nitrogen , an

dmetal s content s inmos t residuums , RHDS . require s substantia l amount s o f hydroge nan dcatalyst . Th e leas t cos t approac hfo r producin g VLSR O depend s o nth e cos t premiu m fo r very low-sulfu r crud e oil s relativ e t o th e processin g cos t fo r desulfurizin g highe r sulfu r residuum .

• Currently , i t i s cheape r fo r U.S . refineries t o produc e VLSR O throug hdistillatio no f ver y low-sulfu r crud e oil s tha nb y RHD SP. 4

o f residuu

m produce dfro

m medium - an

d high-sulfu r crud e oils . A s a result , mos t existin g RHD S capacit y inth e U.S . i s currentl y bein g use d t o produc e highvalu e product s suc ha s gasolin e an ddiese l fuels .

t ^lery few foreig nrefinerie s exportin g VLSR O t o th e U.S . hav e RHD S capacity . A s a result , mos t VLSR O importe dint o th e U.S . i s produce d b

y distillatio no f ver y low-sulfu r crud e oils . Two majo r exception s ar e refinerie s inVenezuel a an dth e Virgi nIslands ; thes e tw o location s accounte d fo r roughl y 2 0 percen t o f th e tota l U.S . suppl y o f VLSR O in1985 .

t Th e us e o f distillatio nt o produc e mos t VLSR O reflect s curren t suppl y an d deman d economic s inth e worl doi l market . I f crud e oi l sulfu r premium s wer e t o increas e o r supplie s o f ver y low-sulfu r crud e oil s wer e t o b e constraine db y resourc e limitations , politica l actions , or

othe r factors , th e economic s o f RHD S woul dimprove .

• Give nthes e uncertainties , i t 1 s difficul t t o predic t th e exten t o f RHD S tha t wil l occu r i nth e future . However , i t i s expecte dtha t distillatio no f very

low-sulfu r crud e oil s wil l continu e t o represen t a significan t percentag e o f VLSR O productio nfo r th e foreseeabl e future .

RESIDUA L OI L REFININGOPERATION S

Residua l fue l oi l 1 s produce dfro m th e heavy , high-boiling-poin t (650°F+ ) fractio n(know na s "atmospheri c residuum" ) obtaine ddurin g atmospheri c distillatio no f crud e oi l (Figur e 1) . Atmospheri c residuu m ca n be furthe r separate d usin g vacuu m distillatio nint o vacuu m ga s oi l (VGO , boilin g poin t 650-1000°F ) andvacuu m residuu m (boilin g poin t 1000°F+) . Th e long-chai nhydrocarbon s i nthes e fraction s contai na significan t percentag e o f th e sulfur , nitrogen , an dmetal s (primaril y

nicke l an

dvanadium ) foundin crud e oil . Sulfu r dat a fo r severa l selecte dcrud e oil s an dassociate dP. 5

Crud e Oi l " Gase s

_ 

### T)atloIIIst o

Q
.

. C o E <. A Napth a

Kerosen e

_

Ga s Oi l

_ Sulfu r Recovery

Hydrotreatin g ••LP G

'—• » — * » Reformin g
Hydrotreatin g

Hydrotreating * m.
• —»>



# r ^

• ~ N |Atmospherl c Residuu m •'acuumDistillation Vacuu m fc

Ga s Oi l " "

•Hydrotreating * Catalyti c Crackin g easonn e Blendin g —•» •Gasoline



# V 1 | Vacuu m Residuu m •Hydrotreating * Therma l Crackin g Distillat e Blendin g --

Je t Fue l

—•Distillat e Oi l

1—•» Residua l Blendin g —•» » Residua l Oi l

—• » T o Napth a Hydrotreatin g ••Cok e

'optiona l dependin g o n feedstoc k an d produc

t quality
.



### FIGUR E 1 . SIMPLIFIE D FLO W DIAGRA M O F U.S . PETROLEU

M REFINERYP. 6

TABL E 1 . WEIGH T PERCEN T SULFURI N SELECTE D CRUD E OIL S AN D ASSOCIATE D DISTILLATIO N

FRACTION S

•

Low-Sulfu r Domesti c So . Louisian a Coasta l Texa s Low-Sulfu r Imported Algeri a Angol a Canad a (Alberta ) Denmar k (Nort hSea ) Indonesi a (Sumatra ) Nigeri a Norwa y (Nort hSea ) Zair e Othe r Importe d Crude s Mexic o Saud i Arabi a (light ) Saud i Arabi a (heavy ) Venezuel a Crud e 

### Oi l

0.1 4 0.2 0

0.1 0 0.1 7 0.1 5 0.2 0 0.1 2 0.1 4 0.1 0 0.1 2

1.4 0 1.9 0 2.8 0 2.5 0 

### At

m Resi d

0.3 1 0.3 0

0.2 5 0.2 3 0.3 3 0.4 0 0.1 8 0.3 0 0.3 0 0.1 8

2.5 5 3.2 0 4.5 0 2.9 0 

### VG

O

0.2 4 0.2 4

0.1 7 0.1 8 0.2 5 0.2 9 0.1 4 0.2 5 0.2 6 0.1 3

1.9 0 2.4 5 3.0 0 2.2 5 

### Va

c Resi d

0.3 1 0.6 0

0.3 0 0.3 0 0.5 4 0.6 0 0.2 3 0.5 2 0.5 0 0.2 2

3.6 0 4.1 0 5.5 0 3.3 0 Fue l



### Oi l

0.3 5 0.3 7

0.2 5 0.2 3 0.4 0 0.4 0 0.2 0 0.3 4 0.4 0 0.1 8

2.6 5 3.2 0 4.1 0 2.5 5
Source : Referenc e 1
residuu m fraction s ar e presente dinTabl e 1 ; crud e oil s tha t ar e relativel y lo w i nsulfu r conten t ar e emphasized . Not e tha t sulfu r i s significantl y mor e concentrate di nvacuu m residuu m tha ni nth e somewha t lighte r VGO . Th e "fue l oil " colum

ni s a blendo f processe dresiduu m products . Dependin g o nth e gravit y an d compositio no f a give nresiduu m fraction , th e desire dproducts , and th e require dproduc t quality , i t ma y b e necessar y t o hydrotrea t th e residuu m t o remov e sulfur , nitrogen , an d metal s before furthe r refining . Th e technolog y an d processin g requirement s associate d wit hhydrotreatmen t o f residuu m ar e discusse dlater . Followin g hydrotreatment , vacuu m ga s oi l i s generall y

sen t t o a catalyti c crackin g uni t wher e i t i s heate dinth e presenc e o f a catalys t t o conver t th e larg e VG O molecule s int o lighter , lowe r boilin g poin t product s suc ha s gasolin e an

d distillat e oil . Vacuu m residuu m ca nals o be cataly ticall y cracked , bu t i s mor e expensiv e t o proces s du e t o it s lowe r hydroge nP. 7

content , highe r leve l o f Impurities , an dhighe r boilin g temperature . Becaus e o f thi s highe r cost , vacuu m residuu m i s mor e frequentl y

processe d usin g therma l cracking . Therma l crackin g involve s th e us e o f hig h temperatur e an

dpressur e t o produc e eithe r a mixtur e o f lighte r product s an d heavy , hydrogen-deficien t cok e (know na s "coking" ) o r a lowe r viscosit y residua l oi l (know

na s "visbreaking") . Dependin g onresiduu

m qualit y an dth e processin g capabilitie s o f a give nrefinery , low-sulfu r residua l oi l ca nb e produce d1 ) directl y fro m low-sulfu r crud e oils , 2 ) b y blendin g wit hga s oil s o r distillate s t o reduc e sulfu r concentration s an dimprov e physica l propertie s (e.g. , viscosity) , o r 3 ) b y hydrotreatin g high-sulfu r residuum . Th e relativ e economic s an dus e o f thes e differen t approache s ar e discusse dlater .
RESIDUA L OI L SUPPL YAN D DEMAND
Reflectin g th e relativ e availabilit y an deconomi c valu e o f variou s fuels , productio no f petroleu m product s i nth e U.S . ha s graduall y shifte d fro m distillat e an

dresidua l oil s use db y industr y

an delectri c utilitie s t o lighte r product s suc ha s transportatio nfuel s an dpetrochemica l feedstocks . A s a result , mos t U.S . refinerie s hav e Installe dsignifican t refinin g capacit y t o conver t residuu

m t o thes e lighter , highe r value dproducts . Th e imbalanc e betwee nresiduu m suppl y an dresidua l oi l productio n provide s anestimat e o f th e percentag e o f residuu m upgrade dt o thes e lighte r products . A s show

nI nTabl e 2 , crud e oil s processe db y U.S . refinerie s 1n 198 4 containe danaverag e o f 16. 3 percen t atmospheri c residuu m an d0.9 6 percen t sulfur ; fo r 198 8 thes e value s ar e projecte dt o Increas e t o 17. 0 percen t residuu

m an d1.0 6 percen t sulfur . However , a s show ni nTabl e 3 , residua l oi l accounte dfo r onl y 6. 0 percen t o f tota l refiner y product s in 198 4 an di s projecte dt o declin e t o around5. 5 percen t b y 1988 . Thes e figure s sugges t tha t onl y abou t one-thir do f th e tota l residuu m suppl y i s ultimatel y

sol da s residua l oi l (base don6 percen t RO divide db y 1 7 percen t residuum) . Th e declin e i nresidua l oi l productio nbetwee n198 4 an d198 8 reflect s th e highe r retur nonrefiner y investmen t associate dwit hproductio n o f lighter , highe r valu e petroleu m products . Th e projecte dintens e pric eP. 8

TABL E 2 . AVERAG E COMPOSITIO N O F CRUD E OI L PROCESSE D BYU.S . REFINERIE S

Crud e Characteristi c Tota l Quantit y(MB/CD) a Specifi c Gravit y(°API ) % Residuu

m Avg
. % Sulfu r % < 0.5 % S % 0.5-1.0 % S % > 1.0 % S Actua l 198 4 11,64 2 32. 6 16. 3 0.9 6 50. 5 16. 8 32. 9 Projecte d 198 8 12,42 0 31. 7 17. 0 1.0 6 46. 2 16. 1 37. 6

a millio nbarrel s pe r calende r da y Referenc e 3 , pp . 30-31 .

TABL E 3 . PRODUCTIO N

O F RESIDUA L OI L BYU.S . REFINERIE S

Characteristic s
Tota l Refiner yProduct s (MB/CD )
Tota l Residua l 01 1 (MB/CD ) % < 0.3 % Sulfu r R O % 0. 3 - 1.0 % Sulfu r R O % 1. 0 - 2.0 % Sulfu r R O % > 2.0 % Sulfu r R O Actua l 198 4 13,92 0 

### 83 4 5. 2 22. 5 36. 5 35. 9 Projecte d 198 8 14,49 9 

### 79 9 4. 5 24. 7 40. 9 29. 9
Referenc e 3 , pp . 33-35 .P. 9

competitio nbetwee nnatura l ga s an d residua l oi l a s a boile r fue l wil l als o contribut e t o reduce dresidua l oi l deman dan d resul t i nfurthe r upgradin g o f residuu m t o lighte r products . Als o not e fro m Tabl e 3 tha t VLSR O represents onl y abou t 5 percen t o f tota l U.S . residua l oi l production . I n1985 , residua l oi l represente d7. 6 percen t o f tota l U.S . petroleu m 2 consumption . Difference s betwee ndomesti c residua l oi l suppl y an d demand historicall y

hav e bee nsatisfie db y import s fro

m foreig nrefineries . A s show ninTabl e 4 , 198 5 residua l oi l import s accounte dfo r roughl y 4 3 percen t o f U.S . consumptio nafte r adjustmen t fo r residua l oi l export s (believe dt o be primaril y

highinsulfu r content) . Fo r VLSRO , import s accounte dfo r almos t 7 6 percen t o f th e total .

TABL E 4 . SUPPL YO F RESIDUAL OI L BYSULFURCONTENT , 198 5

VOLUM E (ThousandBarrels ) Domesti c Importe dTota l
< 0.3 % Sulfu r 0.3-1.0 % Sulfu r
> 1.0 % Sulfu r Tota l

a include s 72,06 0 thousan dbarrel s o f unknow nsulfu r conten t exporte dt o othe r countries . Referenc e 2 , pp . 55-56 .
RESIDUU M HYDRODESULFURIZATIO N

TECHNOLOG Y
Residuu m hydrodesulfurizatio n(RHDS ) i s use dt o desulfuriz e an d upgrad e residuu m fo r us e a s a feedstoc k i nproducin g transportatio nfuel s an d distillat e oil s a s wel l a s t o produc e low-sulfu r residua l oil . RHD S involve s mixin g atmospheri c o r vacuu m residuu m wit hhydroge nan

d heatin g in th e presenc e o f a catalyst . Sulfu r an d nitroge nar e converte dt o H 2 S an d NH- . Exces s hydroge ni s remove dina high-pressur e separato r whil e H-S , NH~ , an d non-condensabl e hydrocarbo ngase s ar e remove di na low-pressur e 24,78 7 82,96 9 214,24 1 321,997 a 78,20 1

36,16 6 71,91 7 186,28 4 102,98 8

119,13 5 286,15 8 508,281 aP.1 0

separator . A

portio no f th e metal s remove ddurin g hydrotreatmen t adher e t o th e catalys t an

d reduc e it s effectiveness . Severa l commercia l RHD S techno logie s ar e summarize d inTabl e 5 . Not e tha t inadditio nt o desulfurization , par t o f th e hydroge n1 s consume d throug hpartia l conversio no f th e residuu m t o lighte r product s suc ha s distillates . RHD S technolog y

ca nreduc e th e sulfu r conten t o f residuu m b y u pt o 9 5 percen t and produc e residua l oil s o f 0. 3 percen t sulfu r andbelow . However , inactua l operation , severa l factor s influenc e th e economic s o f RHD S processes . Thes e factor s includ e catalys t life , hydroge nconsumption , an d residuu m quality . Catalys t lif e i s substantiall y shortene da s metal s conten t increases . Fo r example , on e poundo f catalys t ca nremov e 9 0 percen t o f th e sulfu r fro

m roughl y

2 7 barrel s o f feedstoc k containin g 2 5 pp m metals ; t o achiev e th e sam

e sulfu r remova l fro

m a 10 0 pp

m metal s conten t feedstock , 4 onl y 4. 5 barrel s ca nb e processe dpe r poundo f catalyst . Ona relativ e basis , thi s four-fol d Increas e 1nmetal s conten t cause s a six-fol ddecreas e i ncatalys t life . Deactivatio no f th e catalys t ca nb e overcom e b y increasin g be d temperatur e o r hydroge nconsumption , bu t result s 1nhighe r overal l proces s cost . Becaus e o f it s lowe r hydroge nconten t an dhighe r sulfu r an

d metal s content , desulfurizin g vacuu m residuu

m generall y

cost s mor e tha ndesulfurizatio no f atmospheri c residuum . T o produc e 0.3-1. 0 percen t sulfu r fue l oil s fro m atmospheri c residuum , 345-77 5 standar dcubi c fee t (scf ) o f hydroge npe r barre l o f residuu m ar e required , whil e vacuu m residuu m require s 870-115 0 sc f t o accomplis hth e same task . I naggregate , hydroge nan

d catalys t cost s typicall y accoun t fo r 65-7 5 percen t o f th e tota l
cos t o f RHDS. 4 Th e approximat e cos t o f RHD S pe r barre l o f produc t 1 s summarize din Tabl e 6 fo r severa l differen t crud e oil s an dresidua l oi l produc t qualities . Becaus e o f uncertaintie s i nrelativ e inflatio nrate s fo r variou s desulfurizatio ncos t components , thes e tota l cost s ar e take ndirectl y fro m 4 th e 197 9 repor t i nwhic hthe y appeare d an

dhav e no t bee nescalate dt o 1986 . Fo r a 0. 3 percen t sulfu r product , cost s fo r desulfurizatio nrang e fro m $3.14-4.5 3 pe r barrel . Not e tha t a t sulfu r level s inth e desulfurize d produc t o f 0. 8 percen t an d above , th e cos t o f desulfurizatio ni s roughl y proportionat e t o th e initia l sulfu r conten t o f th e crud e oil . A t level s o fTABL E 5 . RESIDUU M HYDRODESULFURIZATIO N PROCESSE S

Process/Develope r Principle s o f Operatio n Conversio n (X ) Maximu

m Reporte d Sulfu r Remova l IX) Comment s

LC-f1n1ng / Luimnu s Cres t Inc
.

RC D Unlbon / UO P Inc .

RD S an d VRD S hydrotreating / Chevro nResearc h Corporatio n Residuu m an d hydroge nar e 50-8 5 fedt o a n expande d be d o f catalyst . Fo r efficien t contact , th e be d I s maintaine d Inturbulenc e b y liqui dflow . Effluen t 1 s separate d a t lo

w pressure . Fee d an d hydroge npas s 30-6 0 throug htw o fixe d bed s o f catalys t i

nseries . Firs t be daccomplishe s demetallzatlon s secondbe d accomplishe s hydrodesulfurization . On e pas s operatio no f hydroge n30-6 0 and fee d throug ha fixe d be d o f catalyst . Moderat e temperatur e an

d pressur e maintained . Grade d catalys t use d t o maintai nconsisten t qualit y fo r differen t fee d stocks . 9 0

9 5

91 Produc t qualit y I s maintaine d b y Intermitten t additio nan d withdrawa l o f catalyst . Sulfu r conten t o f produc t fue l oi l I s nominall y

I X(b y weight) , whic hca n b e blende dwit hcutte r stock s t o produc e LSR0 . Proces s ca n trea t atmospheri c o r vacuum

residuum . Catalys t quantit y determine s amoun t o f sulfu r removal .

Proces s ca n trea t atmospher e o r vacuum

residuum . Thirtee n unit s operating , on e indesign .

Resldflnlng / Exxo nResearc h an dEngineerin g Fee d an d pre-heate d hydroge n ga s ar e fe

d t o a fixe d be d o f catalyst . Effluen t passe s throug hseparator s operatin g a t successivel y

lowe r temperatures . Hydroge nga s I s recovere d an

d recycled . 5 0 N . Av . Proces s ca n trea t atmospher e o r vacuu m residuum . Tw o unit s hav e bee nInstalled .

Percentag e o f residuu m converte d t o ga s oil s an d lighte r product . 2 Sulfu r remova l number s ar e base d o n th e highes t remova l value s presente d Inth e reference dliterature . Reference : Hydrocarbo nProcessing . Volume 65 . No . 9 . September . 1986 . pp . 87.90 .P.1 2

TABL E 6 . RHD S COS T FO RRESIDUAL OI L FROM SELECTE D FEEDSTOCK S (1979S/BBL )

Feedstoc k

Cuet a E . Venezuel a Kuwai t Khafj i Col d Lak e Sulfu r (% ) 2.1 2 2.3 8 3.8 0 4.3 6 4.5 5 Metal s

(ppm ) 

### 292 27 4 6 0 11 8 23 6 Percen t Sulfu r

1. 6 0. 8 0.9 1 1.1 7 1.8 0 2.2 0 2.5 2 2.2 8

2.4 5 2.4 9 2.8 5 3.4 2 inProduc t

0. 3 3.9 1 3.9 3 3.1 4 3.6 0 4.5 3 R

O 0. 1 5.2 8 5.7 1 3.5 1 4.1 1 5.8 4
Referenc e 4 , p . 110 .
0. 3 percen t sulfu r an

d below , th e Initia l metal s conten t 1 s dominan t in determinin g th e cos t o f desulfurization . A numbe r o f domesti c refineries Installe dRHD S capacit y durin g th e lat e 1970 s an d earl y 1980 s (Tabl e 7) . A t tha t time , crud e oil s fro m Algeria , Nigeria , an

d Indonesi a (generall y containin g les s tha n0. 3 percen t sulfur ) wer e sellin g a t $4- 6 pe r barre l mor e tha ncrude s fro m Saud i Arabia , Mexico , an dIran(generall y

containin g 1 t o 3 percen t sulfur) . Als o durin g thi s period , residua l oil s containin g les s tha non e percen t sulfu r wholesale dfo r a naverag e o f $5.4 0 pe r barre l mor e tha nresidua l oil s containin g i nexces s c o f on e percen t sulfur . Unde r thes e conditions , RHD S a t $3- 5 pe r barre l appeare deconomicall y

attractive , thu s resultin g i nconstructio no f th e capacit y show n1nTabl e 7 . B y Septembe r o f 1986 , however , th e differentia l 1ncrud e oi l price s fro m th e abov e countrie s had decline dt o $2- 3 pe r barre l whil e th e pric e differentia l fo r residua l oil s abov e an d below on e percen t sulfu r had decrease dt o roughl y

$1.5 0 pe r barrel . Inlin e wit hthes e pric e change s an dth e abov e estimate s o f desulfurizatio ncosts , th e economi c attractive nes s o f RHD S ha s significantl y declined . Recen t telephon e contact s wit hth e companie s liste di nTabl e 7 foundtha t severa l o f th e RHD S unit s hav e bee n converte dt o desulfurizatio no f ga s oil s whil e other s ar e use dsolel y t o produc e feedstock s fo r upgradin g t o lighte r products . Fo r example , Phillip s

1 1P.1 3

TABL E 7 . RESIDUU

M HYDRODESULFURIZATIO N

CAPACIT Y

Company Chevro nUS A Chevro nUS A
Exxon , US A Phillip s Phillip s Valer o Refl n TOTA L 

### 1n

g Locatio n

E l Segundo , CA Pascagoula , M S Baytown , T X Borger , T X Sweeny , T X Corpu s Chr1st1 , T X RHD S Capacit y (bpsd) a 24,00 0 96,00 0 71,000 50,00 0 75,00 0 54,00 0 370,00 0

a barrel s pe r strea

m da y (barrel s pe r da y

whe noperatin g a t ful l capacity) . Referenc e 12 , pp . 100-115 .
Petroleu m Company' s Borger , Texa s an dSweeny , Texa s refinerie s hav e th e capacit y t o desulfuriz e 50,00 0 bp dan d75,00 0 bp

do f residuum , respectively ; however , al l o f th e desulfurize dproduc t 1 s sen t t o a catalyti c cracke r fo r fractionatio nt o lighte r products . ' Exxo nha s converte dIt s 71,00 0 bp d o RHD S uni t i n Baytown , Texas , t o desulfurizatio no f ga s oils . Similarly , Chevron' s El Segundo , Californi a refiner y ha s converte dmos t o f It s desulfurizatio ncapacit y t o desulfurizatio no f ga s oi l fo r productio no f 9 low-sulfu r diese l fuels . Chevro ndoe s produc e an dmarke t low-sulfu r residua l oil s o f 0.25-0. 5 percen t sulfu r a t fou r o f It s refineries , bu t use s disti1 1 a t tha nRHD S
AVAILABILIT YO F VLSR O

, Supplie s o f VLSR O an d RHD S capacit y

i n 198 5 base don th e poin t o f refinin g ar e show

ni n Tabl e 8 ; foreig ncountrie s ar e liste di n descendin g orde r o f impor t volumes . O f th e tota l domesti c VLSR O supply , 7 6 percen t wa s imported . O f th e remainin g 2 4 percen t produce din th e U.S. , 4 2 percen t wa s

12 g low-sulfu r diese l fuels
. Chevro n doe s produc e an d marke t low-sulfu r residua l oil s o f 0.25-0. 5 percen t sulfu r a t fou r o f It s refineries , b i distillatio n o f low-sulfu r oil s (primaril y fro m Indonesi a an d Africa ) rathe r 1P.1 4

TABL E 8 . U.S . SUPPL YO F VERYLO W SULFURRESIDUAL OI L B YLOCATION

O F REFININGAN D RHD S CAPACITY , 198 5

REFININ GLOCATION ( DOMESTI C PADD C I (Eas t Coast ) PADD I I (Midwest ) PAD D II I (Gul f Coast ) PAD D I V (Rock y Mountains ) PAD D V (Wes t Coast ) Subtota l
IMPORTE D Algeri a Virgi nIsland s Brazi l Nigeri a Netherland s Antille s Venezuel a Canad a Bahama s Mexic o d Wester nEurop e -Othe r OPE C Othe r Wester nHemispher e Othe r Easter nHemispher e Subtota l TOTAL BREAKOU T BASE D ON

RHD S CAPACIT Y Domesti c wit hRHD S Capacit y Import s wit hRHD S Capacit y Domesti c withou t RHD S Capacit y Import s withou t RHD S Capacit y VOLUME a Thousand Barrels )
1,48 7 2,72 7 8,84 8 1,20 2 10,52 3 24,78 7
19,79 4 10,52 9 4,96 1 4,14 5 4,14 0 3,98 9 3,54 0 3,22 4 2,82 2 2,50 0 1,30 2 6,77 5 10,48 0 78,20 1 102,98 8
19,37 1 23,38 0 5,41 6 54,82 1 RHD S CAPACITY 6 (bpsd )



### 0 0 346,00 0 

### 0 24,00 0 370,00 0


### 0 130,00 0 

### 0 0 0 200,40 0 3,60 0 

### 0 5,00 0 52,00 0 

### 0 0 0 391,00 0
•*•••« • 761,00 0
370,00 0 391,00 0 

### 0 0

a b
c d Referenc e 2 , pp . 55-56 . Referenc e 3 , Appendi xC . Petroleu m Administratio nfo r Defens e District , geographi c division s o f U.S . use d b

y DO E fo r petroleu

m accountin g purposes . Unite d Kingdom , Spain , Norway , Netherlands .

1 3P.1 5

produce donth e Wes t Coas t (PADD V ) an d3 6 percen t inth e Gul f Coas t state s (PADD III) . Bot ho f thes e PADD s hav e significan t RHD S capacity ; bu t a s discusse dabove , muc ho f thi s capacit y ha s bee nconverte dt o processin g lighte r products . O f th e foreig nsupply , 7 0 percen t come fro m countrie s tha t d o no t hav e an y RHD S capacit y

an dthu s bas e productio nonrefinin g o f low-sulfu r crud e oils . O f th e remainin g 3 0 percent , onl y th e Virgi nIslands , Venezuela , an d wester nEurop e hav e significan t RHD S capacity . Becaus e o f th e relativel y high(2- 3 percent ) sulfu r conten t o f Venezuela natmospheri c residuum , 1 t 1 s likel y tha t remova l o f sulfu r b y RHD S approache s 9 0 percent . Dat a onth e sulfu r contents o f crud e oil s processe dinth e Virgi nIsland s an dwester n Europ e wa s no t found . Thus , althoug hprecis e quantitativ e dat a ar e no t availabl e detailin g th e metho db

y whic hdomesti c VLSR O supplie s ar e currentl y produced , availabl e dat a onbot hth e geographi c distributio nan deconomic s o f VLSR O refinin g sugges t tha t th e majorit y o f curren t suppl y

come s fro

m distillatio n o f yery low-sulfu r crud e oils . RHD S ma y b e Involve dI nth e productio no f roughl y 2 0 percen t o f th e tota l domesti c suppl y o f VLSRO , bu t th e percentag e o f sulfu r remova l durin g RHD S 1 s uncertain .

1 4REFERENCE S

1 . Beyaert , Bruce , Chevro nUSA , Sa nFrancisco , California , telephon e conversatio nwit hE

d Moretti , Radia nCorporation , Januar y 14 , 1987 . 2 . Energy

Informatio nAdministration , Petroleu m Suppl y Annua l 1985 . Washington , DC , DOE/EIA-0340(85)/1 , Ma y 22 , 1986 . 3 . Nationa l Petroleu m Council , U.S . Petroleu m Refining . Octobe r 1986 , pp . 26-36 , Appendi xC . 4 . Comley , E.A. , Keen , R.T. , an d Tyndall , M.F. , (Catalyti c Inc.) , Technolog y

Assessmen t Repor t fo r Industria l Boile r ADDHcations : Oi l Cleaning . U.S . EPA , Researc hTriangl e Park , NC , EPA-600/7-79-178b , Novembe r 1979 . 5 . Energy

Informatio nAdministration , Monthl y Energy Review . Washington , DC , D0E/EIA-0035(86/9) , Septembe r 1986 . 6 . Davis , Ed , Phillip s Petroleu m Co. , Borger , Texas , telephon e conversatio nwit hE

d Moretti , Radia nCorporation , Januar y 6 , 1987 . 7 . Earnest , Neil , Phillip s Petroleu m Co. , Sweeny , Texas , telephon e conversatio nwit hE

d Moretti , Radia nCorporation , Januar y 6 , 1987 . 8 . Reid , Frank , Exxo nCorporation , Baytown , Texas , telephon e conversatio n wit hE d Moretti , Radia nCorporation , Januar y 6 , 1987 . 9 . Bredehofte , Ron , Chevro nCorporation , E l Segundo , California , telephon e conversatio nwit hE

d Moretti , Radia nCorporation , Januar y 12 , 1987 . 10 . Houde , Ed , UO P Inc. , telephon e conversatio nwit hE d Moretti , Radia n Corporation , Januar y 6 , 1987 . 11 . va nDriesen , Roger , Lummus-Cres t Inc. , telephon e conversatio nwit hE d Moretti , Radia nCorporation , Januar y 6 , 1987 . 12 . Oi l an

d Ga s Journal . Vol . 84 , No . 12 , Marc h24 , 1986 , pp . 100-115 . 13 . Whittington , Lou , M.W . Kellog g Co. , telephon e conversatio nwit hE d Moretti , Radia nCorporation , Januar y 5 , 1987 . 14 . Bruch , Herber t W. , Nationa l Petroleu m Refiner s Association * telephon e conversatio nwit hE

d Moretti , Radia nCorporation , Decembe r 3 , 1986 .



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