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GASOLI NE RANGE ETHER SYNTHESI S FROM LI GHT NAPHTHA PRODUCTS OF
FLUI D CATALYTI C CRACKI NG OF FI SCHER- TROPSCHWAX.
W
J . Reagan
Amoco Oi l Company
Naperv i l l e, I l l i noi s 60566
Keywords: Fi scher - Tropsch wax, Fl ui d Cat al yti c Cr acki ng. Et her Synthesi s
The Fl ui d Catal yti c Cr acki ng of Fi scher- Tropsch wax ( Czof par aff i ns) produces
two to f our t i mes the concent r ati on of r eacti ve i so- ol ef i ns ( i sobut yl ene,
i soarnyl enes, i sohexenes) t han obser ved f romconvent i onal gas oi l f eedst ocks.
Met hanol reacts wi t h these ol ef i ns t o f orm the corr espondi ng t er t i ar y al kyl
methyl ethers: MTBE. TAME and MTHE' s. These etheri f i cati on r eact i ons ar e
ml dl y exotherm c and equi l i br i um l i m t ed. The r eact i on t emper at ure and t he
ol ef i n mol ecul ar st r uct ur e are i mport ant var i abl es f or maxi mum ether yi el ds.
The base napht ha research oct ane number i ncr eases by 2- 4 number s af t er t he
et heri f i cat i on react i on.
on ether yi el ds because of hydr ogenati on of r eacti ve ol efi ns t o par af f i ns.
The cat al yti c cr acki ng of Fi scher- Tr opsch wax pr ovi des a non-convent i onal
SOUKCe of ol ef i ns f or et her synt hesi s that can suppl ement exi st i ng and
dw ndl i ng petr ol eumsuppl i es .
I NTRODUCTI ON
Fi scher- Tropsch (F-T) synt hesi s t echnol ogy (1) pr oduces l i qui d hydrocarbons
f r om synt hesi s gas ( hydrogen and carbon monoxi de) deri ved f r omt he
gas i f i cat i on of coal O r ef orm ng of nat ur al gas.
consi st s of a br oad r ange of nor mal par aff i ns (C-C,+ and a smal l quant i t y
of oxygenates and ol ef i ns. The di st i l l ate f r act i on, C+ i s an excel l ent
qual i t y f uel . The l argest pr oduct f racti on. C, 8+ i s pr i mar i l y wax and is
usel ess as a t r anspor t at i on f uel .
convent i onal petr ol eum processes, such
as
hydr otr eat i ng, r efor m ng and
cat al yt i c cracki ng to produce convent i onal gasol i ne and di st i l l ate
f uel s .
2 )
Fl ui d Catal yt i c cr acki ng and hydr ocracki ng st udi es have been r epor t ed by
Mobi l ( 3 ) and UOP. 4 ) Heavy wax C,,+) f r act i ons have also been t r eat ed
wi t h hydroi someri zati on and hydr ocracki ng processes at Exxon. ( 5 )
Hydr odewaxi ng and cat al yt i c cr acki ng t r eatment s of heavy wax f r omsl urr y F- T
processi ng are al so repor t ed by Mobi l . ( 6 )
I n
addi t i on, pure component
cr acki ng st udi es (decanol , decanal ) over the i nter medi ate
-
pore zeol i t e
HZSM- 5 have been r epor t ed.
( 7 )
exam ned i n some detai l by Woj ci echowski Over l arge- pore f auj asi t e
(zeol i te
Y)
and over HZSM- 5 zeol i t e cat al yst s. ( 8. 9) Government al
r egul at i ons, most r ecent l y i n t he Cl ean Ai r Act Amendment s of
November , 1 9 9 0 . have r esul t ed i n the phaseout of l ead addi t i ves, l ower i ng
of t he Rei d vapor pl ; essure of gasol i ne and i n some geographi cal ar eas, t he
mandat ed use of oxygenat es.
pr oduced and used
as
gasol i ne bl endi ng component s. (10) Recent st udi es of
methyl t ert i ary but yl et her ( MTBE) and t ert i ary amyl methyl et her ( TAME)
suggest t hat t hese compounds may r educe automat i ve car bon monoxi de
em ssi ons, have hi gh bl endi ng gasol i ne oct ane r at i ngs, R+M/ 2, ( MTBE-108,
TAME- 102) and have l o w Rei d Vapor pr essure. These et her s are pr oduced
commerci al l y by t he ether i f i cat i on of t he appr opr i ate ol ef i n by methanol
( MTBE, i sobutyl ene; TAME, i soamyl enes). ( 11. 12) There i s l ess i nf ormati on i n
the open l i t eratur e about t he et her i f i cat i on r eact i ons of C, ol ef i ns that
are al so pr esent i n s i gni f i cant quanti t i es i n f l ui d cat al yt i c Cr acki ng
product napht has.
f r om C,-C, r eact i ve i so-ol efi ns i n napht has. One r eport
(14)
pr ovi des some
i nf ormati on about t he r eact i on of C, i so- ol efi ns w t h methanol t o pr oduce
the hi gher et her s, MTHE' s, methyl t ert i ary hexyl et her s. MTBE has attracted
the most att ent i on i n recent year s.
coul d reach 25%par year by 1995.
( 15. 16)
There i s e gr owi ng need f or
al t er nat i ve sour ces of ol efi ns f or ether synt heses as demand f ar t hese
materi al s escal ates beyond t he capaci t y of conventi onal petr ol eumP KOC~SS ~S.
There ar e no r eport ed st udi es of t he cat al yti c cracki ng processi ng of F-T
l i qui ds t o pr oduce C,- C8 ol ef i ns as f eedst ocks f or t he synt hesi s
of
gasol i ne
range
ethers .
EXPERI MENTAL
The f eedst ock OK t hi s wor k i s a sampl e of r eact or wax f r oma commer ci al
f i xed bed F- T uni t operated by Sasol , L i m t ed.
char acteri zat i on of t hi s f eedstock i s avai l abl e i n other st udi es. ( 4) The
smal l scal e (1 gramof f eed,
3-5 gr ams of cat al yst ) cat al yti c cr acki ng t est s
wer e perf ormed on a M cro Act i vi t y Test uni t ( MAT) si m l ar i n desi gn t o the
uni t descr i bed i n ASTM procedur e.
09907- 86. Thi s test uni t
i s
equi pped f or
detai l ed anal yses of gas and l i qui d pr oduct s and cake yi el ds.
pl ant t est s were conduct ed i n
a
c i rcul at i ng cat al ys t uni t s t m i l n r o i
desi gn descr i bed by ARCO. Thi s uni t operates wi Lh
2
to 3 ki l ogr ams < i
The presence of hydrogen has a det r i ment al ef f ect
The F- T l i qui d pr oduct
These pr oduct s ar e f urt her t r eat ed by
The cat al yt i c cracki ng of F- T l i qui ds was
Sever al t ypes of et her s are now commer ci al l y
The Et her ol process (13) produces a m xed et her product
The gr owt h r ate f ar i t s pr oduct i on
The anal yti cal
The pi l ot
337
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catal yst and f eed rat es of 10- 30 gr ams/ m nut e.
exper i ment s were Car r i ed out i n a convent i onal hi gh pressure m cro- r eact or.
Tht ee FCC catal yst s,
cont ai ni ng zeol i t e
Y,
zeol i t e Beta and zeol i t e HSZM- 5
arb t he pri mary catal ysts f or t he FCC st udi es, The Y zeol i t e cat a l ys t i s an.
Ul crastabl e Y f auj as i t e ( USY) zeol i t e cat al yst taken fr om one of Amoco s
commerc i al FCC uni t s. The HZSM- 5 cat al yst
is
a commer ci al sampl e pr oduced by
I ncer cat Gor p. The Beta s ampl e was prepar ed i n our l abor at ory by spray
dr yi ng a commer ci al l y avai l abl e Beta zeol i t e and a convent i onal si l i ca-
al um na matr i x. Two commer ci al i on exchange r esi n cat al yst s, Rohmand
Haas' s Amber l yst 15 and Bayer ' s K 2 6 3 4 , were used i n t he et her s ynt hesi s
The et her synt hesi s
KU115.
RESULTS AND DI SCUSSI ON.
A. Cat al yt i c Cr acki ng Test s
I ni t i a l catal yt i c Cracki ng runs wi t h t he smal l scal e test systemprovi de
some i nsi ght s i nt o the cat al yt i c cracki ng behavi or of the wax f eedst ock.
The
i ni t i al choi ce of f l ui d c at a l yt i c c r ac ki ng
( FCC) catal yst and pr ocess
condi t i ons f ocuses on compar i sons wi t h convent i onai gas oi l , t he usual
f eedst ock t o commerc i al FCC uni t s. At t hese condi t i ons. (970' F r eacti on
t emperat ure,
3 cata l ys t
to
oi l wei ght r ati o), t he wax feedst ock readi l y
COnVeKt S
( 8 5 +
conver si on) t o hi gh yi el ds of C,- gas ( hi gh i n propyl ene and
C, ol ef i ns) and napht ha (C -430' F). A Summar y of t hi s compari son is
presented i n Tabl e
I .
The conversi on l evel i s def i ned by convent i on
as
t he
sum of t he pr oduct s: napht ha, gas and coke, Thi s hi gh cat al yt i c cracki ng
conver si on l evel
f or t he wax f eedst ock agr ees wi t h the publ i shed Mobi l dat a
3 . 6 ) on F- T wax cr acki ng. I n addi t i on. hi st ori cal pur e component
hydrocarbon cr acki ng studi es
( 17) suggest t hat l ong chai n paraf f i ns cr ack at
much gr eater Kate5 than t he short er chai n paraf f i ns.
t he wax f eedst ock wi l l be an i mport ant par amet er when commer ci al heat
bal anced Operat i ons are eval uat ed.
wax product napht ha r esul t s f r om t he hi gher concentr at i ons of l ow octane
number paraf f i ns compared t o t he gasol i ne f r om t he mor e ar omat i c gas oi l
f eedst ocks. The oct ane number s i n the Tabl e I are est i mat ed resul t s f rom
detai l ed naphtha anal yses by gas chromat ogr aphy and cor r el ati ons wi t h oct ane
engi ne t est s. The t arget of t hese st udi es i s to opt i m ze the yi el ds of
br anched ol ef i n i nter medi ates ( i sobut yl ene and i soamyl enes) f or et her
synt hesi s . Three FCC catal yst s, cont ai ni ng zeol i t e
Y,
zeol i t e Beta, and
zeol i t e HZSH- 5,
wer e test ed f or
wax C O ~ V ~ K S ~ O ~
nd product sel ect i vi t y as a
ser i es of b l ends wi t h an i ner t sol i d. Tabl e I1 pr esent s t he det ai l ed
pr oduct d i st r i but i ons f or t he t hr ee catal ysts at a s i m l ar conver s i on l evel
of about 8 3 .
of the desi r abl e ol e f i ns, However . th i s OCCUKS at t he expense of napht ha
pr oduct .
pr opyl ene. These scr eeni ng t est r esul t s show t hat FCC catal yst vari at i ons
can provi de f or w del y di f f erent pr oduct di st r i but i ons.
8. Pi l ot P l ant Cata l yt i c Cracki ng Test s .
Some i ni t i a l wax cat al yt i c cr ack i ng screeni ng t ests on the pi l ot pl ant uni t
ar e pr esent ed i n Tabl e 111.
t he pi l ot pl ant agree wi t h the smal l
scal e
test resul t s .
cat al yst convert s
a
great er f r act i on of the wax f eedstock to l i ght ol e f i ns,
i ncl udi ng propyl ene, i sobut yl ene and i soamyl enes. t han the
Y
zeol i t e
cat a l ys t .
napht ha yi el d f or t he Bet a zeol i t e cat al yst compar ed to t he st andard Y
zeol i t e cat a l ys t .
s i m l ar to the Beta zeol i t e.
Hi gh yi el ds of the t argec l i ght ol ef i ns ar e
produced but t he napht ha yi el d i s much l ower t han the Y zeol i t e cat a l ys t .
Thi s t rade- of f of l i ght ol ef i n and napht ha yi el ds can be adj ust ed by t he
amount of t he HZSM- 5 addi t i ve.
pl ant Catal yti c cr acki ng r uns were combi ned and di st i l l ed ( ASTMKethod
0 - 2 8 9 2 ) to pr oduce l i ght napht ha (QOO F) f r acti ons f or t he ether i f i cati on
studi es .
The l ow coke yi el d of
The r el at i vel y l ow oct ane number of t he
Bot h t he Bet a and HZSH- 5 cat al yst s produce much hi gher yi el ds
I n addi t i on, t he HZSH- 5 cat al yst pr oduces ver y hi gh yi el ds of
The hi gh conver si ons of the wax f eedstock i n
The Beta zeol i t e
The hi gher ol ef i n y i e l ds are off set by a s i gni f i cant l y l ower
The t est r esul t s for t he HZSH- 5 cat al yst m xture are
The total l i qui d products f romsever al p i l ot
C . Et her Synt hesi s.
Si nce the r eact i on of i sobut yl ene and methanol to f orm MTBE i s wel l known,
thi s st udy wi l l f ocus on t he producti on of TAME and KTHE ethers f r om the
l i ght napht ha pr oducts of the pi l ot pl ant wax cracki ng st udi es.
f i xed bed uni t was used f or t hese et her i f i cat i on st udi es. The i ni t i a l t est
runs i nvol ve the r eact i on of 2-Kethyl - 2- but ene wi t h methanol to pr oduce
TAKE.
i soamyl ene to TAME: mol es TAME out/ mol es i soamyl ene i n*100) .
condi t i ons are: vari abl e t emperatures, 200
PSIC
uni t pr essure, 0 . 6 6 WHSV
(ol ef i n) and 1. 2 mol rat i o of met hanol / ol ef i n.
i s Amber l yst 15,
a
commerci al ether i f i cat i on cat al yst The r eact i on
t empcr aLure is
R
m a j o r f actor I n L hf s eLher i Cl cnLi on
re.wt. Ion.
A smal l .
Tabl e I V shows t he compar i son of TAME yi el ds ( conver si on of
The test
The cat al yst f or t hese r uns
TIIV a l ~ i ~ r , ,
338
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c
I
I
r i se i n TAME yi el d at 150 F and t he decl i ne at 200' F suggest s t hat
equi l i br i uml i m t at i ons exi st at t hese t emper at ur es and r eact i on condi t i ons .
The maxi mumyi el ds of et her s wi l l occur at t hese equi l i br i umcondi t i ons.
Tabl e V pr esent s t he det ai l ed composi t i on of the l i ght napht ha sampl es f r om
t he Pi l ot pl ant wax cat al yt i c cr acki ng KUnS.
sampl es, f eeds 8 and
C ,
are hi gher f r om the pi l ot pl ant wax cat al yt i c
cr acki ng runs t han t he l i ght naphtha sampl e. f eed " A".
Use Of hi gh ol ef i n sel ecti ve FCC cat al yst s, Beta and HZSM- 5.
i n the pi l ot
pl ant r uns, Nos. 940- 01, 02 and 941- 01. The same
Y
zeol i t e cata l ys t w a s used
i n the r uns f or f eed "A" and
"C"
,
r esul t s f r om the l ower conver si on l evel . The reacti ve i soamyl enes, 2-
Methyl - 2-butene and 2- Met hyl - 1- but ene f or TAME synt hesi s and the r eact i ve C,
i so- ol ef i ns. 2- Methyl - 1- pent ene. 2- Met hyl - 2- pent ene. 2. 3- Di met hyl - 1- but ene.
and Ci s and t r ans 3- Met hyl - 2- pent ene f or MTHE synt hesi s ar e t he i mpor t ant
components . Thi s l i ght napht ha. f eed "A" sampl e and met hanol are t he
f eedst ock f or a seri es of ether i f i cat i on r uns at the same pr ocess condi t i ons
f or t he 2-Hethyl-2-butene/methanol t es ts . Due to the l i m ted avai l abi l i t y
of t he napht ha, onl y t wo r eact i on t emperatures ar e avai l abl e.
t he conversi on of t he vari ous C and C, i so- ol ef i ns to t hei r r espect i ve
met hyl et her s, Tabl e VI . shows t hat r eact i on t emper at ure
i s
a maj or f actor
i n the et her i f i cat i on r eact i on. The decrease
i n conver si on
w t h the
i ncrease i n the car bon number of the i so-ol efi n agr ees wi t h ot her l i t eratur e
ether i f i cat i on s tudi es .
( 18. 20)
The r eact i on pr oduct s f r omt hese r uns have
a s i gni f i cant yel l ow col or, especi al l y at the hi gher r eact i on t emper at ur e of
150F.
tests . I t i s l i kel y that pol ymer i zat i on of o l ef i ns to
C,,+
hydr ocar bon
"col or bodi es" i s responsi bl e f or the col or ed pr oduct . The col or of t he
et her product coul d be a si gni f i cant pr oduct qual i t y i ssue.
pr esent s t he r esul t s of the et heri f i cat i on r uns wi t h t he "B" and "C"
l i ght
napht has at 15OF. I n t hese r uns, both Amber l yst 15 and another CO~e r Ci a l
et her i f i cat i on cat al yst , gayer' s K2634 ar e under st udy.
The
Bayer catal yst
cont ai ns a nobl e met al i n addi t i on to t he str ong aci d f unct i onal i t y.
nobl e metal i s avai l abl e f ar o l ef i n i somer i zat i on and di ol ef i n sat urat i on,
i n the pr esence of hydrogen.
pr evi ous set of r uns,
200
P S I G , 2. 9 gr ams of cat al yst , met hanol 1. 37 g/ hr ,
napht ha, 5 . 5 g/hr ar e t he same except t hat onl y one r eact i on t emper at ure.
150'F. i s avai l abl e. The i so- ol ef i n conver si on r esul t s are si m l ar for bot h
catal yst s and the t hree f eedstocks. i n the absence of hydrogen gas i n t he
r eact or. The cal cul ated r esearch octane val ues f or t he products of t hese
ether i f i cat i on r uns ar e 2- 4 number s hi gher t han t he st art i ng l i ght napht ha
Feedst ocks, Tabl e
VI I I .
As expect ed, t hi s oct ane i ncrease depends, t o some
ext ent upon t he concent r at i ons of t he ether s i n the pr oduct.
octane number s f or t he m xed ether l i ght napht ha f r act i ons ar e al so shown i n
Tabl e VI I I . There i s a f ai r agreement wi t h the cal cul ated ( by
G C
oct ane
numbers . When hydr ogen gas i s pres ent , Run No. 034- 1, Tabl e VI I I , t here i s
a maj or l oss of i so- ol ef i n conver s i on. These react i on condi t i ons resul t i n
the hydr ogenat i on of bot h react i ve i so- ol ef i ns and l i near o l ef i ns . Thi s i s
an undesi r abl e r esul t si nce bot h t he pr oducti on of ethers and t he octane
number of t he pr oduct decr eases si gni f i cant l y. The r un wi t h added hydrogen
gas, 034- 1, has a l ower r esear ch oct ane r ati ng ( 79. 5) t han t he f eedstock
( 84. 6) or t he r un wi t h no added hydr ogen, 034- 3, ( 8 5 . 8 ) . Thi s octane l oss
i s due t o t he conver si on of hi gh oct ane val ue ol ef i ns to l ow oct ane val ue
para f f i ns .
ether i f i cat i on products i n the pr esence of hydr ogen gas.
These et her i f i cat i on r uns cl ear l y demonst r ate t hat t he l i ght napht ha
f ract i ons f r om the cat al yt i c cracki ng of Fi scher- Tropsch wax ar e excel l ent
ether synt hesi s feedst ocks.
ACKNOWLEDGEMENT
Thi s work
was
suppor t ed by t he U S . Depar t ment of Ener gy. Pi t t sbur gh Ener gy
Technol ogy Cent er . Pi t t sbur gh. Pennsyl vani a under Cont r act No. DE- AC22-
91PC90057. D. Kovach and R. Br own per f or med t he exper i mental wor k.
3 .
Newbur y pr ovi ded the
GC
napht ha anal yses.
REFERENCES
The i so- ol ef i n content s of the
Thi s i s due to t he
The hi gh i so- ol ef i n cont ent of f eed
C
A s ummar y of
Thi s cal or i s not present f or t he pur e component 2- Met hyl butene-:
Tabl e V I 1
The
The nom nal r eact i on condi t i ons f r omt he
Bl endi ng
There i s a si gni f i cant i mpr ovement i n the col or of t he
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2 .
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29-150. 1985
Convers ion,
w t X
P l O h l S t l .
r t X :
c
c.
C
430.F
43O.Ft
Coke
I r ob t y l cnc
I . O ~ l C C I
Naphtha, u r n
MOW
Gas
o i l UI)I
61.6 88.1
2.6 1.8
11.6 31.4
6.9 15.9
36.2 36.8
38.4 11.9
4 3 2.2
1.3 4.5
2.3 5.8
90.4 85.8
79.8 77.6
T M LE I1
U T IEST RESILIS--UTALIST
oDIpARIso*S
AT mLIF
Z e o l i t e Befa
042
85.3
C a t a l y s t
1
Z e o l i t e Y
u r n
Y O.
c onv e r s i on . U t % 83.0
le01 t c HLsn-5
055
85 . 8
Product Y i e l d s , Ut :
c;
c
C
C
C
;
C,.430 F
430.F
Coke
0.6
7.4
0.8
13.2
3.7
11.7
3.6
41.7
17.0
0.3
l s o b t y l e n c
l r o a m y l m e s
G-430.F
57.0
85.2
16.2
ON
K W
340
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1ABLE 111
P l l O l pu*T m s
Feed IO: 92-0490-01A 93-0024-011
reed
A*
reed
B
Pilot P l a n t
939-01. +
02
v40-01. 02
m NOS. 4 us7 CDt.l St 941-01
conversion = 93.6% 8etalHZSU-5
C a t a l y s t
convers ions = 90.96%
r o t a l P a r a f f i n s w t X 6.69 8.44
T o t a l I r o - p . r a f f l n 9 U t 42.71 17.64
To t a l A r m t i c 9 wtX 1.74 2.62
T o t a l NsPhthems W t X 3.96 5.55
T ot al o l c f i m YtX 44.51 64.47
~ e a c t i v e r o - o le f in r
wtX
93-0024-01C
Feed
C
939-04
4
SY Cstalyst
C m e r . i M 3%
4.32
22.88
0.35
3.16
68.6
1.25
4.26
C6's
2 , 3 - d i m t h y l h t c n c
2-mthyL.l.pnrcne
Z-nrthyl-2-pntene
S - m t h y L - t r a n s - 2 - p n t e m
I - r e t hy l - v i s -Z -pn t em
2.15
.67
0.8 0 . n 0.97
2.35
2.49 3.02
4.01 5.27 5.46
2.49 3.13 3.29
3.98 5.48 5.35
1.76
5.64
341
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6/6
I so -o le f in C 1Z'F
2~Wethyl-l-bUtene 85.4
2-nrthyl -Z-brtme
2P.P
2.3 Dimethyl-l-butene
56.5
2-Wethyl - l -pntme
65.9
2-Methyl.Z-pnttne 20.7
3-Wethyl-ci~-Z-penCene 21.7
cs
C6
3-Wethy l - t rans-Z -penfene
20.8
150'6
G
8P.P
65.5
83.4
87.5
48 6
38.6
2P.8
i r o -o le f in
c-ent
2-Methy1-l-butcne
2-Methy1-2.butane 65.5 62.2 M.2 42.9 38.2 61.2
89 9 b0.2 87.1 77.2 78.1 87.7
200.F-
Naphtha
Reaction
T a p .F
Catalyst
Feed
A
F e d B
Feed
C
P2-04P-OlA
92-0024-01A PI-0024-01C
150 150
50 150 150
50
lnberlyrt 15 Ir he r ly st 15 12634 12634 12634
K2634
No
H2 H2 H2
No
H2
TLBLE V I 1 1
2.3.0Incthyl-l-butene
C6'r
2-nechyl- l -pmtme
2-Methy1-2-pentenc
3-Mefhyl -Ci s-2-pntene
3-nc~hy l - t ranr -Z-pntenc
...
eed
A
-0-01A
15586-024-2 125.F
15586-024-6 15UF
15586-024-8 150.F
Feed
P3-0026-01A
15586-031-2 150.F
05586-033-1 150.F
15586-033-3 150.6
...
83 . 4 ... ...
87.5 85.5 84.1 72.2 78.6 86.P
48 6
56.1 62.7 44.2 31.5 51.5
38.6 31.0 43.4 23.8 7.3
25.8
2P.B
32.2 43.7 25.P 20.7
33.3
...
93-0024-OlC
15586-034-1 1W F
RV no.
Feed A
G O - O l A
15586-024-2
15586-024-6
15586-024-8
Feed
15586-031-2
15586-033-3
Feed C
ps-ooi4-OIA
05586-033.1
OCtllM
Nlnber
80.P2
w r l y r t 15 80 . OP
83.76
w r 1 y r t
15
83.88
I * O .
P araf fi ns pa raf f in s A ~ m t i ~ s aphthenes O l ef i ns OxyeCnateS V n t n o ~ n s
6 689
42.712
1.736 3.956 44.507
0.071 0.33
7.806
40.230
1.W5 4.474
33.762
11.406 0.34
6 463
40.42P
2.247 4.576
29.671
16.294 0.32
6.337 4 0 . 4 M
2.263
4.586 2'9.58
16 436 0 . 3 3
m.437
17.617 2.623
5 . 5 4 ~ 64.472
0.17 1.11
7.381
1 7 . ~ 0 3 . 6~ 1
6.583
41.716
22.44s 0 .844
7.417
17.989
3.647 6 424
41.847 21.815 0.821
8.205 1 7 . M
3.62 6.512
45 889
17.277 0.83
84.56
95.9
ayer
H2 12634 m.47
88.P
Keyer no H2 12634 85.78
95 9
...
*CBlC l.ted
342