CA1079666A - Simultaneous production of lube oil and low pour products - Google Patents

Abstract

ABSTRACT OF DISCLOSURE

A process for the simultaneous preparation of both naphthenic and paraffinic lubricating oil basestocks is disclosed, including hydrocracking a hydrocarbon feedstock, comprising either a naph-thenic or paraffinic crude oil, in the presence of a hydrocracking catalyst, at a temperature of from about 650 to 850°F, and separating both a paraffinic lubricating oil basestock and a naphthenic lubri-cating oil basestock for use in low pour specialty products from the hydrocracked product produced thereby.

Description

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.

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 _ 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.

.. . . . . . . . . . .
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.

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 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 ~

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 ~

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 -- 10 -- .

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 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 -.

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 ~. .

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 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 - .

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 1~)796~;6 + I`~1 0 U~
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Claims (13)

THE EMBODIMENTS OF THE INVENTION IN WHICH AN EXCLUSIVE
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:

1. A process for the simultaneous preparation of naphthenic and paraffinic lubricating oil basestocks com-prising hydrocracking a hydrocarbon feedstock by contacting said feedstock with a hydrocracking catalyst under hydro-cracking conditions including a temperature of about 650 F
to 850°F to produce a hydrocracked product stream, separating a paraffinic lubricating oil basestock fraction and a naph-thenic lubricating oil basestock fraction from said product stream, said paraffinic lubricating oil basestock having a pour point of from about -10 to +30 F., a Viscosity Index above about 80 and a boiling range largely above the initial boiling point of said hydrocarbon feedstock and said naph-thenic lubricating oil basestock having a pour point of from between about -60 to 10°F., a Viscosity Index of below about 80 and a boiling range between about 600°F and the initial boiling point of said hydrocarbon feedstock.

2. The process of claim 1 wherein said hydrocarbon feedstock boils above about 700 F.

3. The process of claim 1 wherein aromatics, as-phaltic, and sulfur compounds are removed from said paraf-finic lubricating oil basestocks by contacting said basestock with a solvent selected from the group consisting of phenol, furfural, liquid SO2, dimethyl sulfoxide, n-methyl pyrroli-done, acetonitrile, acetophenone, dimethyl formamide and mixtures thereof.

4. The process of claim 1 wherein aromatics, as-phaltic, and sulfur compounds are removed from said naphthen-ic lubricating oil basestock by contacting said basestock with a solvent selected from the group consisting of phenol, furfural, liquid SO2, dimethyl sulfoxide, n-methyl pyrroli-done, acetonitrile, acetophenone, dimethyl formamide and mixtures thereof.

5. The process of claim 1 wherein aromatic, as-phaltic, and sulfur compounds are removed from both said par-affinic and naphthenic lubricating oil basestocks by contac-ting said basestocks with a solvent selected from the group consisting of phenol, furfural, liquid SO2, dimethyl sulfox-ide, n-methyl pyrrolidone, acetonitrile, acetophenone, di-methyl formamide, and mixtures thereof.

6. The process of claim 1 wherein said hydrocarbon feedstock is derived from a crude oil feedstock selected from the group consisting of naphthenic and paraffinic crude oil feedstocks.

7. The process of claim 1 wherein said hydrocar-bon feedstock is prepared by the vacuum distillation of a crude oil feedstock selected from the group consisting of naphthenic and paraffinic crude oil feedstocks, said vacuum distillation carried out in order to produce a hydrocarbon feedstock boiling in the range between about 650 and 1100°F.

8. The process of claim 1 wherein said hydro-cracking conditions include a hydrogen pressure of from about 1000 to 3000 psig.

9. The process of claim 1 wherein said hydro-cracking catalyst is selected from the group consisting of a Group VIB metal supported on a porous carrier and a crystal-line alumino silicate zeolite-containing catalyst.

10. A process for the simultaneous preparation of both naphthenic and paraffinic lubricating oil basestocks comprising vacuum distilling a crude oil feedstock selected from the group consisting of naphthenic and paraffinic crude oil feedstocks to obtain at least one distillate cut boiling in the range of from about 650 to 1100°F., hydrocracking said distillate feedstock by contacting said feedstock with a hydrocracking catalyst under hydrocracking conditions in-cluding a temperature of about 650 to 850°F., a hydrogen partial pressure of between about 500 to 10,000 psig, a space velocity of between about 0.1 and 10 V/V/Hr. and a hydrogen feed rate of between about 1000-10,000 SCF/B to produce a hydrocracked product stream, separating at least a paraffinic lubricating oil basestock fraction and a naph-thenic lubricating oil basestock fraction from said product stream, said paraffinic lubricating oil basestock having a pour point of from between about -10 to +30°F., a Viscosity Index above about 80 and a boiling range largely above the initial boiling point of said distillate cut, and said naph-thenic lubricating oil basestock having a pour point of from between about -60 to -10°F., a Viscosity Index of below about 80 and a boiling range between about 600°F. and the initial boiling point of said distillate cut.

11. The process of claim 10 wherein said paraf-finic lubricating oil basestock is dewaxed by contacting said basestock with a solvent selected from the group con-sisting of acetone, methyl ethyl ketone, methyl isobutyl ketone, dichloromethane, dichloroethane, ethane, propane, butane, propylene, and mixtures of a ketone selected from the group consisting of acetone, methyl ethyl ketone and methyl isobutyl ketone and an aromatic compound selected from the group consisting of benzene and toluene.

12. The process of claim 10 wherein the UV
stability and color of said paraffinic lubricating oil basestock is improved by hydrogenation.

13. The process of claim 10 wherein the UV
stability and color of said naphthenic lubricating oil basestock is improved by hydrogenation.