Note: Descriptions are shown in the official language in which they were submitted.
1079666
1 The present invention relates to a process for
2 preparin~ both naphthenic and paraffinic lubricating oil
3 basestocks from an oil feedstock, either naphthenic or
4 paraffinic in nature.
There are two principal types of lubricating oil
6 basestocks which are commonly used for the manufacture of
7 lubricating oils. These include the paraffinic type, having
8 a viscosity index of at least about 80, and the naphthenic
9 type, having a viscosity index of less than about 80, which
are generally employed to produce low pour specialty products.
11 In the past, the high viscosity index paraffinic type lubri-
12 cating oil basestocks have been manufactured by upgrading
13 paraffinic crude oil feedstocks followed by dewaxing to
14 produce specified medium pour point products, i.e. having
pour points of between about -lO and +30F. On the other
16 hand, the naphthenic lubricating oil basestocks, employed
17 for various specialty products, have been produced by up-
18 grading distillates from naphthenic non-waxy crude oil feed-
19 stocks, to produce basestocks of very low pour points of from
about -60 to about -10F. The paraffinic lubricating oil
21 basestocks have been used for the manufacture of high quality
22 products such as motor oils, aviation oils and turbine oils,
23 while the naphthenic lubricating oil basestocks have been
24 used in less critical applications in which the viscosity
index exhibited by the basestock is not as important. The
26 naphthenic lubricating oil basestocks, which generally con-
27 tain less than about 5 weight percent paraffins, contain
28 little or no wax, and thus have a much lower pour point than
29 a similar non-dewaxed paraffinic lubricating oil basestock
having the same molecular weight. It is therefore usually
31 necessary to dewax the paraffinic lubricating oil basèstocks
32 to allow fluidity of the oil even at room temperature.
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1079~i66
Various lubricating oils, be they naphthenic or paraffinic,
are generally prepared by various techniques or processes in
order to retain specified qualities. Thus, such processes as
solvent extraction to remove aromatic, asphaltic and sulfur
compounds, solvent dewaxing, with such solvents as propane and/
or a ketone such as methyl ethyl ketone, to improve pour and
cloud points, clay contaGting for color improvement, acid
treatment to remove the aromatic unsaturated portions of the
distillate and/or hydrofinishing to reduce neutralization
number and sulfur so as to improve color and stablility, have
all been employed in the past. In addition, it has been
necessary to employ each of these techniques to upgrade both
naphthenic and paraffinic lubricating oil base-stocks, each
of which has, in the past, been exclusively derived from
either naphthenic or paraffinic crude oil base-stocks, res-
pectively.
Two of the principal methods of categorizing and quali-
fying various lubricating oil basestocks are by their viscosity
. .
index and pour point. Thus, depending upon the particular
end use contemplated, it is essential to know the specific
effect of increasing temperatures on a specific lubricating
oil, and this is most commonly done by the viscosity-temper-
ature relationship known as viscosity index. This viscosity
index system is based on two standard oils; a highly naph-
thenic oil from a Gulf Coast crude which underwent a consid-
erable decrease in viscosity with increase in temperature
was assigned a viscosity index of 0, and a highly paraffinic
oil from Pennsylvania which underwent a relatively small de-
crease in viscosity with increase in temperature was assigned
a viscosity index of 100. A method for calculating viscosity
index is given in ASTM Method D-567-53.
1~79666
Generally, oils having higher viscosity indices are
more stable in gasoline engines, and thus more desirable. As
for pour points, these are defined as that temperature 5F
above the temperature at which the oil is solid (ASTM Method
D-97-57). The pour point is most significant since it re-
presents the limit below which oil cannot flow to the engine
parts. That is, if the oil is below its pour point temper-
ature at startup, it cannot circulate and the engine will not
be lubricated. In the past, pour points of paraffinic lub-
ricating oil basestocks have been reduced by solvent dewaxingor by the use of additives known as pour depressants.
In accordance with the present invention it has now been
discovered that both high quality paraffinic lubricating oil
basestocks exhibiting relatively high viscosity indices and
medium pour points as well as desirable naphthenic lubricating
~ oil basestocks having low pour point characteristics can be
;; simultaneously prepared from hydrocarbon feedstocks. Further-
more, it has been discovered that by employing the present pro-
cess it is also possible to prepare paraffinic lubricating oil
basestocks from a naphthenic crude oil feedstock without the
need to employ the dewaxing procedures described above. In
addition, it is also possible to manufacture high quality lub-
ricating oil basestocks from low grade high sulfur heavy naph-
thenic crude oil feedstocks without the need for preliminary
hydrotreating to reduce the sulfur content of these feedstocks.
These results may be accomplished by hydrocracking a hydro-
carbon feedstock by contacting said feedstock with a hydro-
cracking catalyst at hydrocracking conditions including a tem-
perature of between about 650F and 850F, to produce a hydro-
cracked product stream, and separating both a paraffinic
~ _ 4 _
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lubricating oil basestock having a pour point of from about
-lO to ~30F and a viscosity index of above about 80, and a
naphthenic lubricating oil basestock having a pour point of
from about -60 to -10F and a viscosity index of below about
80 from said hydrocracked product stream. The naphthenic
lubricating
- 4a -
` 1079666
:
1 oil basestock comprises that portion of the hydrocracked
2 product stream having a boiling range between about 600F
3 and the initial boiling point of the hydrocracker feed,
4 while the paraffinic lubricating oil basestock comprises the
higher boiling portion of the hydrocracked product stream
6 having a boiling range largely above the initial boiling point
7 of the hydrocracker ~eed. In a preferred embodiment of the
8 present invention, where a naphthenic crude oil feedstock
9 is employed, it is unnecessary to dewax ~he paraffinic lub-
ricating oil basestock produced thereby. On the other hand,
1 when a paraffinic crude oil feedstock is employed, it is
l2 necessary to dewax the paraffinic lubricating oil basestock
13 portion separated from the hydrocracked product stream in
14 order to prepare paraffinic lubricating oil basestocks
having acceptable pour points of below at least about +30F.
l6 In another em~odiment of the present invention the
17 W stability and viscosity index of either the paraffinic or
8 naphthenic lubricating oil basestocks separated from t~e
19 hydrocracked product stream are improved by subsequent sol-
vent extraction and/or hydrogenation processes well known in
21 this art.
22 BRIEF DESCRIPTION OF THE DRAWINGS
.. . . . . . . . . . .
23 Figure l is a schematic flow diagram of the process
24 of the present invention;
Figure 2 is a schematic flow diagram of another
26 embodiment of the process of the present invention.
27 DETAILED DESCRIPTION
28 Referring to the draw~ngs, in whfch like numerals
29 refer to like portions thereof, Figure l includes a hydro-
cracker 1 to which a hydr~carbon feedstock is fed through
31 lines 2 and 3 The hydrocarbon feedstock fed to the hydro-
32 cracker l through line 2 is preferably a distillate of either
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1 a naphthenic or paraffinic crude oil feedstockO Generally,
2 any feedstock8 including mixtures of hydrocarbons or hydro-
3 carbon fractions9 the predom~nant portion of wh~ch e~hibit
4 initial boiling points above about 650F can be employed.
It is however, preferred that the raw crude oil feedstock
6 be passed through a vacuum distillation zone where one or
7 more ~acuum gas oil cuts boiling in the range of from about
8 650F t~ about 1100F are separated for subsequent feeding
9 through line 2 to hydrocracker 1D In this manner, a light
o distillate, generally boiling below about 659F, and a
bottoms fraction generally boiling above about 1100F are
l2 separated from the crude oil feedstock i~ the distillation
13 zoneD
14 The crude oil feedstocks from which the feeds to
hydrocracker 1 of the present invention are derived, as
l6 discussed above9 may be either paraffinic or naphthenic
17 crudes. Thus~ these crude oil ~eedstocks generally include
18 high sulfur, heavy naphthenic crudes containing from about
19 2 to 10 weight percent sulfur based on the weight of the
total feedstock, and preferably containing from about 2.5 to
21 6 weight percent sulfurO The specifi-c gravities of such
22 crudes r~nge from about 5 to 20 API, and preferably range
23 from about 5 to 16 API~ Preferably, these crude oil feed-
24 s~ocks have a low wax content of less than about 0.5 weight
percent based on the weight of the total feedstockO These
26 heavy naphthenic crudes are further characterized by having
27 from 0 to 10 volume percent v~latile materials boiling below
28 about 400F, 25 to 75 volume percent boiling above about
29 1,000F, 10 to 90 weight percent aromatics and from 0.05 to
1 weight percent nitrogenD The vacuum distillates boiling
31 between about 650 and 1100F (atmospheric pressure equiva-
32 lent) prepared from such heavy naphthenic crudes generally
~ 6 ~
- ~079~66
,,
1 have sulfur contents of from about l.S to 10 weight percent,
2 preferably from about 2 to 8 weight percent5 API gravitie8
3 of from about 10 to 25~ nitrogen contents of from about
~ 0.05 to 1 weight percent, aromatic~ con~ents of from about
10 to 90 percent9 and less than about 0.5 weight percent
6 waxO Typical of such heavy naphthenic crudes are Cold Lake
7 heavy crude oilg tar sands bitumen3 shale oil and the like.
8 The crude oil feedstocks from which the feeds to
9 the hydrocracker 1 may be also derived can also include
0 paraffinic crude oil feedstocks generally containing from
about 0.1 to 6 weight percent sulfur based on the weight of
12 the total feedstock and preferably containing from about 0.5
13 to 3 weight percent sulfur. The specific gravity of such
14 paraffinic crudes ranges from about 20 to 50 API, and
preferably from about 25 to 40 API. Preferably, these
l6 paraffinic crude oil feedstocka have a wax content of less
17 than about 20 weight percent based on the weightof the
18 total feedstock. Furthermore~ these paraffinic crudes are
19 characterized by having from between 5 to 40 volume percent
volatile materials boiling below 400Fg 0 to 50 volume
21 percent boiling above 1000F9 5 to 60 weight percent aroma-
22 tics and 0.001 to loO weight percent nitrogen Vacuum
23 distillates boiling between about 65~ and 1100F (atmos~
24 pheric pressure equivalent) from such paraffinic crudes
have sulfur co~tents ranging from between about 0.1 ~o 4
26 weight percent9 preferably from 0.5 to 3.0 weight percent,
27 API gravities of from 15 to 50, nitrogen contents of from
28 0.001 to loO weight percent, aromatics contents of from 5
29 to 60 weight percent~ and between about 1 and 50 weight
percent waxO Typical of such paraffinic crudes are Light
31 Arabian, Kuwait, North Louisiana and West Texas Sour.
32 While the preferred feedstocks for supply to the
~ 7 ~
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1 hydrocracker 1 are the vacuum distillates prepared from
2 e~ther naphthenic or paraffinic crude oil feed~tocks,
3 deasphalted residua can also be employed. Raw residuals,
4 such as vacuum or atmospheric distillation bottoms, cannot
generally be employed in the present process because the
6 heavy metal contents thereof rapidly deactivate the hydro-
7 cracking catalyst. Ihe present process is not9 however,
8 appreciably senstitive to the vacuum distillate boiling
9 range, so that a wide cut such as a 700 to 1100F or a
lo narrow cut9 for example a 700 to 850F cutg can be suitably
ll employed.
I2 In ~he hydrocracker 1 the feed derived from either
13 a naphthenic or paraffinic crude oil feedstock is hydro-
14 cracked under typical hydrocracking conditions, including
a temperature of between about 650 and 850F9 preferably
16 between 700 and 800F9 a hydrogen partial pressure ranging
17 from about 500 to ~0~,000 psig, preferably from between about
18 1,000 to 3,000 psig, a hydrogen gas rate generally ranging
19 from about 1~000 to 10,000 SCF H21B and preferably ranging
from about 3,000 to 6,000 SCF H2/B, and a space velocity
21 within the hydrocracking zone ranging from about 0~1 to
22 10.0 V/V/Hr ~ preferably ranging from about 0O25 to lo 5
23 V/V/Hr
24 Useful hydrocracking catalysts include (a~ metal
compounds contained on a porous non~zeo~itic support, and
26 (b) zeolite~containing catalysts hav~ng exchanged or depos-
27 ited catalytic metals. Suitable catalyst materials falling
28 within the first category are the oxides and/or sulfides of
29 Group UIB metals9 suc4 as molybdenum and/or tungsten3
pre~erably com~osited with a Group VIII metal oxide and/or
31 sulfide such as the oxides or sulfides of nickel and/or
32 cobalt~ Preferred catalysts of this type comprise sulfided
~ 8 ~
1079666
composites of molybdenum oxide and nickel oxide supported on
a porous, relatively non-cracking carrier such as activated
alumina, silica-alumina or other difficulty reducible re-
fractory oxides. When alumina or silica-alumina are employed
as supports, they may be promoted with phosphorous or phosphor-
ous-containing compounds such as phosphoric acid. The most
preferred catalyst materials of this general type contain about
2-6 weight percent nickel and about 5 to 25 weight percent
molybdenum.
As described above, zeolite-containing materials can
also be employed as the hydrocracking catalyst. These catalysts
comprise a crystalline aluminosilicate (sieve component) and a
porous, relatively inert, thermally stable inorganic adjuvant
(amorphous component). The porous adjuvant is pre~erably
alumina, silica and mixtures thereof. The crystalline alumino-
silicates employed in the preparation of these catalysts can
comprise one or more natural or synthetic zeolites. The porous
adjuvant (i.e., amorphous component) may contain metal compounds
having hydrogenation activity and, in this embodiment is similar
to those amorphous catalysts described above in connection with
group (a) catalyst types. It is noted that, alternatively,
zeolite-containing catalysts can be formed in the substantial
absence of an amorphous component. Representative examples
of particularly preferred zeolites are zeolite X, zeolite Y,
zeolite L, and faujasite. Synthetic zeolites have been gen-
erally described in U.S. Patents 2,882,244, 3,130,007 and
3,216,789. The aluminosilicate preferably contains a Group VIB
or VIII metal hydrogenation component either exchanged or de-
posited thereon. The aluminosilicate can be in the hydrogen
form, in the polyvalent metal form or in the mixed hydrogen-
10~9666
polyvalent metal form. The polyvalent metal or hydrogen form
of the aluminosilicate component can be prepared by any of
the well-known methods described in the literature. Suitably,
the exchanged polyvalent metals are transition metals and are
preferably selected from Groups VIB and VIII of the Periodic
Table. Preferred metals include nickel, molybdenum, tungsten
and the like. The most preferred metal is nickel. The amount
of nickel (or other metal) present in the aluminosilicate (as
ion-exchanged metal) can range from about 0.1 to 20% by weight
~0 based on the final aluminosilicate composition.
In addition to the ion-exchanged polyvalent metals,
the aluminosilicate may contain as non-exchanged constituents
one or more hydrogenation components comprising the transition
metals preferably selected from Group VIB and VIII of the
~ Periodic Table and their oxides and sulfides. Such hydro-
! genation components may be combined with the aluminosilicate
by any method which gives a suitable intimate admixture, such
1 as by impregnation. Examples of suitable hydrogenation metals,
for use herein, include nickel, tungsten, molybdenum, platinum,
palladium and the like, and/or the oxides and/or sulfides
thereof. Mixtures of any two or more of such components may
also be employed. Particularly preferred metals are tungsten
and nickel. ~ost preerably, the metals are used in the form
of their oxides. The total amount of hydrogenation components
present in the final aluminosilicate composition can range
from about 0.05 to 50 weight percent, preferably from about
0.1 to 25 weight percent based on the final aluminosilicate
composition. The final weight percent composition of the
crystalline component of the total catalyst will range from
about 10 to 70 weight percent and preferably from about 10 to
30 weight percent, i.e. 20 weight percent based on total
catalyst. The final weight
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1 percent composition of the amorphous component will range
2 from about 30 to 90 weight percent and preferably from about
3 70 to 90 weight percent, ite~ 80 weight percent based on
4 total catalyst
The amorphous component and the crystalline alumino-
6 silicate component of the catalyst may be brought together
7 by any suitable method, such as by mechanical mixing of the
8 particles thereby producing a particle fon~ composite that
9 is subsequently dried and calcinedO The catalyst may also ~ !
be prepared by extrusion of wet plastic mixtures of the
11 powdered components following by drying and calcinationO
2 Preferably the complete catalyst is prepared by mixing the
13 metal-exchanged zeolite component with alumina or silica-
14 stabilized alumina and extruding the mixt~re to form catalyst
pelletsO The pellets are thereafter impregnated with an
16 aqueous solution of nickel and molybdenum or tungst~n
17 materials to form the final catalystO The preferred catalyst
18 species are a nickel exchanged hydrogen faujasite admixed
19 with a major amount of alumina9 the final catalyst also con-
taining deposited thereon a minor amount of transition metal
21 hydrogenation component9 such as nickel and/or tungsten and/
22 or molybdenum metal or their oxides or sulfides.
23 Referring again to Figure 19 hydrogen is charged to
24 the hydrocracker l through lines 4, 5 and 30 The total
effluent from the hydrocracker 1 is w~thdrawn through line
26 69 and passed to a separator 79 preferably after cooling in
27 a heat exchangerO In the high pressure separator 7 the
28 gaseous phase containing substa~tial amounts of hydrogen is
29 removed and recycled through line 8 back to the hydrocracker
1 through lines 5 and 3. The liquid product from the high
31 pressure separator 7 is then passed through a depressurizing
32 zone 9, and then to distillation column lO. In distillation
1079666
1 column 109 lowboiling light ends generally having a boiling
2 point below about 600F~ and which fonm useful fuel products,
3 are separated through line 11. The rem~ining portion of the
4 product withdrawn from the hydrocracker 1 is separated into
a naphthenic and paraffinic.lubricating oil basestockO Thus,
6 a cut boiling in the range between about 600F and the
7 initial boiling point of the hydrocracker feed is withdrawn
8 t.hrough line 129 while the higher boiling range fraction
having a boiling range largely above the ~nitial boiling
point of the hydrocracker feed is withdrawn through l~ne 13.
1 The naphthenic lubricating oil basestock witbdrawn frDm l~ne
2 12 thus has a low pour point within the range of between
-60 and ~10F9 and a low viscosity index generally below about
4 80, while the paraffinic lubricating oil basestock withdrcwn
through line 13 from distillation column 10 generally has a
16 high viscosity index greater ~than about 80~ and a pour point
7 between about ~10 and +100Fo However9 where the feed to
18 hydrocracker i is derived from a paraff~nic crud~ ~ll base-
19 stock it is preferred to pass the paraffinic lubricating oil
basestock withdrawn through line 13 into a dewaxer 149 from
21 which wax is extracted through line 15, and a dewaxed paraf-
22 finic lubricating oil basestock is withdrawn through line 16.
23 This dewaxed basestock thus has a pour point of between about
24 -10 and +30F~
2s If desired, fractionation can be carried out in
26 distillation column 10 so as to produce re than one naph-
27 thenic lubricating oil basestock boiling below the boiling
28 range of the hydrocracker feed and/or more than one paraf-
29 finic lubricating oil ba~e~tock boiling in the range above
about the initial boiling point of the hydrocracker feed.
31 Alternatively, the products withdrawn through lines 12 and 13
32 of Figure l may be fraction~ted into two or more basestocks
~ 12 -
.
1079666
in other distillation equipment.
Referring now to Figure 2, both the naphthenic lub-
ricating oil basestock withdrawn from the distillation column
10 through line 12 and the paraffinic lubricating oil base-
stock withdrawn through line 13 may be passed to an extract-
ion column 17, preferably for solvent extraction with a sol-
vent which removes aromatic, asphaltic and sulfur compounds
from the lubricating oil cut in question, such as phenol,
furfural, liquid 52~ dimethyl sulfoxide, n-methyl pyrroli-
done, acetonitrile, acetophenone, dimethyl formamide and
mixtures thereof. Thus, solvent enters through line 18,
passes through line 19, and into the top of extraction
column 17, for countercurrent contact with the naphthenic
and/or paraffinic lubricating oil basestocks withdrawn from
distillation column 10. In either or both cases, the solvent
extract after contact with the paraffinic lubricating oil
basestock is withdrawn through line 20 and/or the solvent
extract after contact with the naphthenic lubricating oil
basestock is withdrawn through line 21, while the solvent
extracted naphthenic lubricating oil basestock is withdrawn
through line 22 and/or the solvent extracted paraffinic lub-
ricating oil basestock is withdrawn through line 23. The
solvent is separated from the solvent extract in extract
stripper 24, and extract is thus removed through lines 25
or 26 while the solvent is separated from the extracted naph-
- thenic and/or paraffinic lubricating oil basestock in raffin-
ate stripper 27. The solvent recovered in extract stripper
24 is recycled through lines 28 and 29, while the solvent
recovered in raffinate stripper 27 is recycled through lines
30 and 29. The thus solvent extracted naphthenic lu~ricating
oil basestock, after removal of solvent therefrom, is with-
drawn through line 31, and/or the thus solvent treated
. - 13 -
~079666
paraffinic lubricating oil basestock, after removal of solvent,
is withdrawn through line 32. Again, if the feed to hydro-
cracker 1 is derived from a naphthenic crude oil feedstock,
dewaxing is unnecessary, and the final paraffinic lubricating
oil basestock is withdrawn through line 33. If, on the other
hand, a paraffinc crude oil feedstock is employed, it is
necessary to pass the paraffinic lubricating oil basestock
through line 34 into dewaxer 35, wherein dewaxing is accomp-
i lished by using a solvent such as a low molecular weight hydro~
carbon, such as ethane, propane, propylene, butane, and thelike, ketones, such as acetone, methyl ethyl ketone, and
methyl isobutyl ketone, mixtures of such ketones with aromatic
compounds, such as benzene and toluene, or halogenated, low
molecular weight hydrocarbons, such as dichloromethane, di-
chloroethane, and mixtures thereof, from which wax is removed
, through line 36, and dewaxed paraffinic lubricating oil base-
- stock is withdrawn from line 37. Alternatively, dewaxing may
be accomplished by contacting the paraffinic basestock with
hydrogen over a suitable catalyst under conditions resulting
in selective hydrocracking or hydroisomerization of n-paraffins,
contained therein.
While the particular flow scheme described with res-
pect to Figure 2 employs solvent extraction in order to up-
grade the paraffinic and/or naphthenic lubricating oil base-
stocks withdrawn from the hydrocracker 1, it will be under-
stood that hydrogenation reactions well known to those skilled
in this art may be employed as alternatlves to or in conjunc-
tion with such solvent extraction procedures. Furthermore,
where a paraffinic crude oil feedstock is employed, the de-
waxing step described above may be alternatively employed priorto the hydrocracking step. In this manner, the entire feed
to the hydrocracker is passed through a dewaxing system
~. .
1079666
and then t~ough the above-described hydrocracking and sep-
aration stages. In addition, referring to Figure 2, the
extract from either the naphthenic lubricating oil basestock
withdrawn through line 25 and/or the paraffinic lubricating
oil basestock withdrawn through line 26 itself may be hydro-
cracked to produce low pour point specialty products, and/or
recycled to the hydrocracker l to increase product yield.
. PREFERRED EMBODIMENT
The following examples further define, describe and
10 compare methods of preparing naphthenic and paraffinic lub-
ricating oil basestocks in accordance with the present in-
vention.
Example 1
A raw distillate was separated from a heavy crude oil
from.the Cold Lake area of Alberta, the distillate having a
boiling range of from 750 F to 890 F and a pour point of -5 F.
This distillate was hydrocracked at 750F in a hydrocracking
zone containing a fixed bed of 1/16 inch extrudates of hydro-
cracking catalyst consisting of Nalco NM 502. The hydro-
cracking conditions within the hydrocracking zone aIso in-
cluded a hydrogen partial pressure of 800 psig, a hydrogen
feed rate of 1500 SCF/B, and a liquid hourly space velocity
of 0. 5 V/V/Hr. Both a naphthenic Iubricating oil basestock
having a ~oiling range of between about 650 and 750F and
a paraffinic lubricating oil basestock having a boiling range
of above 750F were separated from the hydrocracker product,
and each such product was also subjected to solvent extraction
with a solvent comprising phenol and 5.~ weight percent water
at I35F. The results, including the viscosity index and
pour points of the extracted and unextracted portions of both
the naphthenic and paraffinic lubricating oil basestocks ~hus r
1079666
produced are contained in Table I. The results demonstrated
that both naphthenic and paraffinic lubricating oil base-
stocks were simultaneously produced in a single pass hydro-
i cracking operation, and further that a 750F+ hydrocracked
product produced a paraffinic lubricating oil basestock
having a viscosity index of 79 and a pour point of -5F,
without dewaxing, after solvent extraction. In addition, the
naphthenic lubricating oil basestock having a boiling range
of from 650 to 750F thus produced had a very low pour point
of -55F, even before solvent extraction, and that further
upgrading by solvent extraction of this low pour, wax-free,
. specialty oil produced a naphthenic lubricating oil base-
stock having a pour point of -30F, and an improved viscosity
index of 60, as well as good W stability.
Example 2
An Example identical to Example 1 was carried out,
except that the temperature in the hydrocracking zone was
increased to 765F, except that in the case a naphthenic
lubricating oil basestock was separated which had a boiling
range of from 650 to 700 F, and a paraffinic lubricating oil
basestock was separated having a boiling range of above
; 700 F. The results are contained in Table II. These results
demonstrate that as the hydrocracking temperature was in-
creased, as compared to Example 1, that both the pour point
and viscosity index of both the naphthenic and paraffinic
~ lubricating oil basestocks produced in accordance with this
invention increased. However, the naphthenic basestock re-
mained lower in both pour point and viscosity index than its
paraffinic counterpart.
Example 3
'. An Example identical to Example 1 was again carried
out, but this time the hydrocracking temperature was increased
;,
- 16 - .
1079666
to 780F. The results obtained are contained in Table III.
Again with a naphthenic and paraffinic lube oil basestock
separated as in Example 2, both the pour point and viscosity
index of the naphthenic basestock remained below that of
the paraffinic basestock.
Example _
Both a naphthenic and paraffinic lubricating oil base-
stock were produced from a paraffinic crude oil feedstock
comprising an Arabian Light distillate having a boiling range
10 of between 700 and 925F. This distillate was again hydro-
cracked in a hydrocracking zone containing the same catalyst
employed in Examples 1 through 3, and employing the following
hydrocracking conditions; a temperature of 750F, a space
velocity of 1.0 V/V/Hr, a hydrogen partial pressure of 600
psig, and a hydrogen feed of 600 SCF/B. The results obtained,
! both with and without solvent extraction with a mixture of
phenol and 3% water at 140F, are contained in Table IV. In
this case a paraffinic lubricating oil basestock having a
boiling range`of above about 6500F was separated from the
hydrocrackate, and it had a pour point of +70F, without
dewaxing, and a naphthenic lubricating oil basestock having
a boiling range of between 600 and 650F was separated from
the hydrocrackate, and it had a viscosity index of 41 and a
pour point of -10 F. This example illustrates the important
ability of the process to produce a low pour point naphthenic
lubricating oil from a waxy paraffinic feedstock without the
use of dewaxing. r
- 17 -
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