US2220307A - Lubricating oils and method of producing same - Google Patents

Description

1940- J. M. WHITELEY, JR, EFAL 2,220,307

LUBRICATING' OILS AND METHOD OF PRODUCING SAME Filed Dec. 7, 1937 2 Sheets-Sheet 1 1940- J; M. WHITELEY, JR., arm. ,307

LUBRICATING OILS AND METHOD OF PRODUCING SAME Filed Dec. 7,,1937 2 Sheets-Sheet 2 i H .Dl-ISOBUTYAENE. mm 4 2 .BORON 0 OR 122 Patented Nov 5, 1940 LUBBICATING OILS AND DIETHOD 0! PRO- DUGING SAME James M. Whiteley, Jr., Elizabeth, and Jeffrey H. Bartlett, Cranford, N. 1., assignors to Standard Oil Development Company, a corporation of- Delaware Application December I, 1937, Serial No. 178,440 8 Claims. (01. 196-10) This invention relates to novel lubricating oils and novel methods of preparing same. Broadly the invention comprises preparing lubricating oils by feeding a normallygaseous olefin, particularly isobutylene, into a normally liquid reactive hydrocarbon diluent particularly of the oleflnic type, having from 6 to 24 carbon atoms, .into which liquid a Friedel-Crafts type catalyst, such as boron fluoride or aluminum- 10 chloride, has been dispersed as uniformly as pos-- sible, i. e. by solution or suspension, the reaction being carried out at approximately 0150- F.,

preferably 40-80 F., wherebya substantial proportion of the normally gaseous olefin polymerizes while'another substantial proportion thereof reacts or condenses with the normally reactive hydrocarbon diluent to produce large yields of lubricating oil having high viscosity index (low change of viscosity with change in temperature) and having a Saybolt viscosity of from about 40 seconds to 400 seconds at 210 F. and preferably from 40 to 200 seconds at 210 F.

Heretofore many processes have been proposed for polymerization of olefins or for reacting olefins with other materials to make various types of products and also many processes have been proposed specifically for making lubricating oils.

However, most of these prior art processes have either been attended with various operating difliculties or have not been practicalfrom an economical point of view or do not produce the desired type of lubricating oil. For instance, it'is known that isobutylene, for example, can be polymerized at very low temperature, e. g. from -10 C. to 50 C. or lower, to substantially solid polymers having a molecular weight greater than 1000 or 2000 and possibly as high as 100,000 or more,

using boron fluoride as catalyst; and it is also known that isobutylene can be readily poly- 40 merized to dimer, trimer and other low molecular weight polymers by reacting at somewhat elevated temperatures, e. g. 100-300 or 400 F. (about 40-200 0.). It is also known that lubricating oils are produced by passing oleflns such as ethylene, propylene, butylenes and amylenes into a hydrocarbon liquid such as petroleum ether containing aluminum chloride suspended therein. Compared to the last mentioned process, the present invention has a great advantage in producing a substantially larger yield of product of the desired viscosity range and besides makes an oil having substantiallyimproved properties. For instance, by feeding isobutylene into a solution of boron fluoride in di-isobutylene at temperatures between about 30 and F. according to the present invention, oils are produced having, Saybolt viscosity limits between about 35 or-40 up to 200 or 300 seconds at 210 F., whereas by using the same temperature range but reversing the order of adding ingredients, namely by feed- 5 I ing boron fluoride into a solution of isobutylene in di-isobutylene, products are made which have an extremely wide range of viscosity, some of the products averaging a Saybolt viscosity of 600 or 700 seconds at 210 F., some averaging 3000 sec- 10 onds at 210 F., and some covering limits as wide as 42 seconds for the lowest boiling constituents and 14,000 seconds at 210 F. for the highest boiling fractions.

The preferred procedure of the present inven- 15 tion has the advantage that in, order to produce an oil having a certain desired viscosity at' 210 F. and a certain desired viscosity index, an oil is produced having a higher flash than is obtained 'when'the process is carried out under conditions 9) resulting in the producthaving a wide range of viscosity. In other words, the products having a relatively narrow viscosity range as produced by the preferred process of the present invention, have higher flash points than the wide viscosity range oils produced by other processes.

In carrying out the reaction (polymerization and/or condensation) of oleflns such as iso-,

butylene with a reactive liquid hydrocarbon diluent such as di-isobutylene in the presence of a a catalyst such as boron fluoride, a primary feature of the invention is the particular order of combining the raw materials because it has been found, for example, that feeding isobutylene into a solution of boron fluoride in di-isobutylene gives surprisingly better results than feeding boron fluoride into a solution of isobutylenein di-isobutylene even though substantially the same reaction conditions and proportions of materials are used in bothcases. A still further advantage of this process lies in the ease of controlling the reaction as compared to the considerable fluctuations in temperatures when the catalyst is added to the solution of isobutylene in di-isobutylene.

The normally gaseous olefin which is the 1211- 5 mary reactant according to the present invention is preferably isobutylen'e although other oleflns such as ethylene, propylene, normal butylenes and amylenes may be' used. Isoolefins such as isobutylene or iso-amylene apparently are peculiarly 5 adapted to produce the desired combination-of polymerization and co-polymerization. They lead to larger yilds and superiorproducts than-are obtained with other normally gaseous oleflns. Although from an economical point of view it may 5 be preferred to use the isobutylene (or other normally gaseous oleflns) in the gaseous state, it-is possible to use them also in a liquid state by using a sufficient amount of pressure under the temperature of operation. Also, instead of using any particular single olefln, it is possible to use mixtures of several normally gaseous olefins or one or more of these oleflns mixed with an inert diluent such as one or more of the normally gaseous paraifins having from 1 to 5 carbon atoms, such as methane, butane, etc. or other inert gases such as nitrogen or hydrogen.

. It is preferred to use di-isobutylene, tri-iso-' butylene or other polymers thereof up through the hexamer, because they are apparently peculiarly adapted to react with the isobutylene or present invention is not entirely understood, it v is believed that having the catalyst such as boron fluoride dissolved or suspended in this reactive hydrocarbon liquid diluent before adding the isobutylene, accomplishes simultaneously several advantageous results including that it permits close temperature control and thereby makes possible the production of an oil having a relatively narrow viscosity spread, and-it facilitates the desired polymerization of the iso-butylene to the lubricating oil type of product rather than to either low polymers such as dimer and trimer or the very much higher substantially solid polymers such as those havingmolecular weights from several thousand up to 100,000. It also permits carrying out the reaction at temperatures such as 60 F. without the use of pressure (if, on the other hand, boron fluoride were to be fed into a solution of isobutylene in di-isobutylene at 60 F., the reaction chamber would have to be kept under a sufficient pressure to keep the isobutylene in the liquid phase). The lower polymers, especially dimer, trimer, etc. of isobutylene have been found to be especially good solvents for boron fluoride, approximately 1.0% by weight being soluble as compared to about 0.1% by weight soluble in a saturated hydrocarbon such as iso-octane at atmospheric pressure.

. Boron fluoride is the preferred catalyst for the reactions involved in the present invention because it actually dissolves to a suitable extent in the di-isobutylene or other reaction liquid being used as diluent, instead of merely being suspended therein in a flnely divided solid condition. However, other Friedel-Crafts type catalysts may be used such as aluminum chloride, titanium tetrachloride or modified catalysts'such as boron fluoride dissolved in water or in acids such as sulfuric, phosphoric, etc.

The process may be carried out in-separate batches but is preferably carried out in a continuous process as will be described more fully later. In any case, when the polymerization and condensation or co-polymerization have been carried out to the desired extent for which a reaction time varying from a few minutes to 4 or 10 hours may be used, the product is preferably treated first to separate the catalyst such as by water washing or by distilling off the boron fluoride at a temperature of 200 F., or lower ifpartial vacuum is used, and then the product is subjected to distillation or fractionation in order to remove any light polymers or unreacted raw material having not more than 24 carbon atoms or having a molecular weight not more than about 300 or 325, or in other words, itis desired to recycle any product having a viscosity less than about 40 seconds Saybolt at 210 F. This separation may be effected by distilling or fractionating at a temperature of about 400-500 F.

at atmospheric pressure with steam or'by using a temperature up to about 300 F. at 5 mm. pressure. i

The residual product having a viscosity greater than 40 seconds Saybolt at 210 F. may, if desired, be separated by fractionation into a light lubricating oil blending stock having a viscosity of 40 to 100 seconds Saybolt at 210 F.- and a heavy lubricating oil blending stock having a viscosity of 100 to 200 seconds Saybolt at 210 F. Although even somewhat higher viscosity products such as those having.a Saybolt viscosity of up to 400 to'500 seconds at 210 F. may be used in motor oils by blending them with considerably lower viscosity stocks, it is preferred to regulate the operating conditions so that relatively little product will be made outside the.

limits of 40 and 200 seconds Saybolt at 210 F. In carrying out the reaction, the temperature is preferably controlled within relatively narrow limits and this may be done by several methods' one is by controlling the rate of the addition of the normally gaseous olefin and the other is by the use of cooling means, such as cooling coils (either inside or outside the reaction vessel), or the desired reaction temperature may be maintained by using some liquefied, normally gaseous material (either one of the reactants or some inert diluent) in the liquid .phase by maintaining the reaction vessel under suitable elevated pressure and then releasing some of the pressure if and when desired to coolthe reaction liquid, thecooling being effected by absorption of the latent heat of evaporation of the liquefied, normally gaseous material.

Various types of equipment may be-used in carrying out this invention, but for the sake of illustration suitable equipment will be described for carrying out the process, either by batch or continuously.

In the accompanying drawings,

Fig. 1 is a diagrammatic sketch of suitable equipment for batch operation which may, if desired, also be used for continuous operation.

Fig. 2 illustrates an improved and more detailed layout for a continuous cyclic process.

Referringto Fig. .1, boron fluoride is fed in through inlet and admixed with di-isobutylene being fed in through inlet, 2 and the resulting solution passing through pipe 3 is met by isobutylene being fed in through inlet 4. The remay also be removed by water washing the product leaving the cooling coil 6, .or traces of boron fluoride may be washed from the product leaving v 2,21 20,30: still a. The residue in $11 a which is maintained at a suitable temperature, such as about 200 F., passes through line I! into another still or fractionating column l3 maintained'at about 400 or 500' F. at atmospheric pressure or up to 300 F. under vacuum mm.'pressure). .From here, any unreacted ,di-isobutylene, together with light polymers having a Saybolt viscosity less than about 40 seconds at 210 F., is taken off overhead through line l4 and, if desired, may be recirculated through line l5 into original diisobutylene inlet 2. .The bottoms taken of! from still l3 constitute the lubricating oil product having a Saybolt viscosity above 40 seconds at 210 F. and, if desired, may be further fractionated by suitable equipment not shown into light and heavy lubricating oil blending stocks.

Referring to Fig. 2, which represents a continuouscyclic process in which only a portion of the product is drawn off and separated. while the remaining portion of the product is recycled, boron fluoride is fed from a suitable source l8 through line I, which is preferably provided with a suitable pressure controlling device, such as mercury seal ll, traps l8 and I9 and meter 20, into the upper part of coiled line 6v and the reactive hydrocarbon liquid diluent, such as diisobutylene, is fed from a suitable source 2| through inlet 2 into the upper part of the same coiled line 8. through the coiled line 6 descends through line 22 through pump 23 and is met by isobutylene being fed from a suitable source 24 through line 4, which is preferably provided with calcium chloride drier 25, caustic soda drier 26, safety valve 21, pressure gauge 28 and manometer 29. The isobutylene from line 4 meets the solution of boron fluoride in di-isobutylenecoming through line 22 and the reaction starts in line 5, the reaction liquid then passing upward into the coiled line 6 which is being cooled by a suitable bath mixture 30 such as alcohol to which solid carbon dioxide is added. The temperature of the liquids at various stages throughout this cyclic equipment may be observed by having the thermometers 3|, 32 and 33 placed at proper points in the equipment as indicated. Part of the reaction products being discharged from overflow 34 pass through line 35 into a suitable washing chamber 36 into which water is fed through line 31 and from which some boron fluoride catalyst escapes through line 38 and may be recycled into line la for reuse. Any excess boron fluoride that is forced through the mercury of seal l1 into line la, joints the recovered boron'fluoride from line 38. The washed lubricating oil product is dischargedthrough line 38 and may, if de-- sired, be further treated, as by fractionation, etc., by suitable equipment not shown. Any low molecular weight polymers below lubricating oil in boiling range and 'viscosity may be recovered I from the product and returned to diluent supply cycling is carried out at the proper rate and thetank 2| and to the system through line 2.

In operating this cyclic equipment shown in Fig. 2 and described hereinabove, when the reraw materials are fed at the proper rate and the desired equilibrium has been established, the temperature difference between any of the three thermometers 3|, 32 and 33 should not exceed The bulk of the liquid rising Also the temperature to be used will vary somewhat according to the raw material being used; for example, with plant isobutylene (a crude commercial stock of isobutylene) which generall'y contains small amounts of normal butenes as well as 'a small amount of butanes, it is best to use a -reaction temperature of. about 40 F. whereas with a specially refractio'nated isobutylene, in other words, a practically pure isobutylene, the reaction temperature should be some what higher, e. g. about'65 1". Commercial supplies of isobutylene may be obtained by separation (by distillation or absorption, etc.) from the socalled 04 cut 'from petroleum refineries. The

separation of it may be obtained by cracking diisobutylene (readily prepared from a C4 cut by,

treating with sulfuric acid) or bydehydrating iso-butyl or tertiary butyl alcohol or may also be prepared by dehydrogenation of iso-butane.

In addition 'to the reactive hydrocarbon diluents mentioned previously, one may also use a cracked -wax distillate boiling below the range of hydrocarbons having a Saybolt viscosity below 40 seconds at 210 F. I Another suitable stock is alight polymer oil obtained by the polymerization' of isobutylene up. to a Saybolt viscosity of 63 seconds at 100 F. which is only slightly heavier than a mineral seal oil stock.

The proportion of the raw materials may vary considerably according to the nature of the materials used, the reaction conditions such as temsome circumstances, however, to use considerablylarger amounts, e; g. up to 5 or 10% or more, particularly with'some of the other less effective catalysts and when other reaction conditions are varied so as to-require larger amounts of catalyst.

If the isobutylene is fed in at a high or fast rate, the yield of oil of the desired boiling range, e. g. 40 to 200 seconds Saybolt'viscosityat 210 F.,

decreases and also the viscosity at 100 F. is increased whereas if the rate of addition of isobutylene is slow, a more uniform product is produced, i. e. having a narrower viscosity'range (from the low to high boiling constituents) and the yield of oil is increased due to much greater co-polymerization. The slow rate of adding isobutylene is preferred. This means that in the continuous recycling process a high rate of circulation of the BFadi-isobutylene solution should be used, and a relatively small proportion of isobutylene compound to the amount of circulated material should be fed into the system.

Agitation also is a factor .to be considered in that good agitation tends to cause more copolymerization and produces a product having a narrower viscosity spread. In the'continu'ous system this agitation is obtained by a high rate of flow through the coil.

Some examples of detailed operating ,condi-. tions and products are given in the following experimental data which are submitted for illustration only and not intended to limit the invention specifically thereto.

TABLE I treated polymer, namely 230 F., is reduced to 120 F. in the treated polymer. Likewise, the and overhead points were all reduced in-the treated polymer.

Apparently, in carrying out the presentinvention, particularly in the continuous recycling process, a number'of various reactions tend to come to equilibrium and the exact nature of this equilibrium will depend upon the operating conditions, such as the temperature, proportions 01.

Comparison of inert and reactive diluents Tm D t f g 2; Oil boiling asbove 450 F. with U011 ran Inna m I No. isobutylene Tune m Yield vis./210 F, v. I.

. Hour: "F. -Perunt 1 250 gm. n-beptane 548 4 05 32 85 53 2 250 gm. 63 vis./100 F. polymer 585 4 4B 92 53 The above Table I shows that-under identical reaction conditions (e. g. time and temperature) in the same apparatus and using substantially identical proportions of materials (diluent and isobutylene), the reactive diluent, namely, the 63 vis. at 100 F. polymer. resulted in a-yield of 48% or oil boiling above 450 F. with steam, which is about 50% greater yield than the 32% yield obtained with the normal heptane inert diluent. Also the reactive diluent produced an oil having slightly higher viscosity (92 seconds at 210 F, compared to hr the inert diluent).

It is believedthat a number of diflerent reactions are involved inthe mechanism of the present invention and that these reactions cannot be summed up in any simple chemical equation .in-

volving merely the polymerization of isobutylene ing of a reactive hydrocarbon liquid diluent such as the light isobutylene polymer oil referred to 3 hmn's at Eject of isobutylene feed rate and reaction time TABLI II on-yield, viscosity and V. I.

Cracking eflect of BF; on light isobutylene" V 1 Oil boiling 8333:0450 F. with a Ifobutylene' Tl I niectedme, r time en -"2a are v. ,2.- F

c en een s. to? F- .onisobusecs. Saybolt I tylene vis./ r...

- 11.0 1 as 43 so B 111.2 1 184 45 72 Percent overhead g i 2g g 2g 10.8 -6- 124 ea 10 13.8 a 2a (9a) 16'. 'zao $1 1 3 1 12 g 318 soc 3 Temperature in above runs 3H0 I". 395 m The above Table III shows that with low isoabove, namely, having a Sayboltviscosity of 63 seconds at 100 F. In these tests a sample ofthe untreated oil is compared with a sample or the same 011 after treatment with boron fluoride materials, rate of feed, etc. It is believed that stitue'nts 01' the reactive liquid hydrocarbon diluent to slightly higher boiling constituents but not high enough to produce the desired lubricating oils, e. g. polymerization of di-isobutylene to tetra-isobutylene;

3. Co-polymerization isobutylene;

4. Co-polymeriz'atioh of isobutylene with tetraisobutylene; v

5. Cracking of some'of the constituents of the reactive hydrocarbon liquid diluent; and

6. Cracking and/or polymerization of at least some or the products of that cracking.

of isobutylene with. di-

The data given in the following Table III show' how the yield, the viscosity at 210 F., and the viscosity index vary with the feed rate of isobutylene and the reaction time. These tests were all carried out at 35-40 F., using boron fluoride as catalyst dissolved in the light isobutylene polymeroil having a Saybolt viscosity-o1 63 seconds at 100 F. as the reactive diluent. 1

Test: III

The above table shows'that when the light polymer oil is treated with. boron fluoride at 40 R, a substantial cracking occurs as indicated by the i'act that the initial boiling P int of the unwith increasing isobutylene feed rate (note the yields-in tests 5, 8, 'l and}, for example). It

is also apparent that the viscosity at 210 1'. increases (irom 43 to 77 in tests 5 and 8) in direct proportion to the isobutylene feed rate. On the other hand, the V. I. (viscosity index) varies from about -80 in these tests', the exact value apparently being dependent upon the time as well as the isobutylene feed rate, the highest V. I. values being obtained in tests 6 and 7 when the reaction time was one hour and in tests 9 and 10 when the reaction time was six hours.

The following Table IV gives the data from different tests in which the total amount 0! isobutylene added during each or the tests was equivalent, although the rate of addition was varied. These tests were all made under the same general conditions as those in Table III, two of them, namely tests 8 and 9, being the same data as that shown in Table III.

. not vary greatly (only from 77-66) between yield batch experiments areshown in Table V in'which approximately V4 part by weight of refractionated isobutylene was passed into one part by weight of reactive diluent containing suspended aluminum chloride for three hours.

Tun: V Tests using aluminum chloride as catalyst T t Reactive diluent lsobutyl Time Temp No. wt one (gms.) hours" F. on theisovim/21ml" Kind (gms.) butylene 10...-. Di-isobutylene 1000 27s a 00 110 00.0 13 i7 c cnisobutyiene polymer 1000 287 3 20 123 v 50.8 62

=TABLE IV Efiect of isobutylene feed rate and time when same total amount of isobutylene is used Oil boiling above 450 F. with steam Isobutylene Test rate mlloogm. Time, No. diluent/hr. hours Yield, percent based Via/210 F. v I on isobuty- Saybolt secs.

lane

Temperature in above runs 36-40 F.

In test 16 the temperature was 60 F. and the diluent was di-isobutylene.

In test 17 the temperature was 20 F. and the diluent was tetra-isobutylene (Cm-C20 polymer), containing about ,5 part of aluminum chloride suspended therein. The high yields, 119 and 123%, (based on the isobutylene used) are an indication of a large amount of co-polymerization and/or condensation.

The following Table VI shows the operating conditions used and results obtained in some TABLE VI Tests in continuous recycling apparatus Ratioiso- 6 Tm Circulation Isobutylene butylene gfffg Limghtrojggz g Yield based No Temp. rate. liters] feed rate (cod rateto product Via/210 F. 0y eaddod isobutylene onisobutylhr. (gm./hr.) circulation stream (gm. 1 one; percent 1'8 OF r .18 1o 42 1000 24 7.7 4a 3200 3.2 a2

10.... 10 42 2000 48 as 53' 0400 3.2 41 20... so 140 1325 0.5 14.7 01 I 4000 3.2 02 21... so 10 663 0.0 14.2 07 2030 2.2 00 40 14.0 000 4.1 0.5 66 21:10 4.2 40 2a.... '40 70 000 0.0 12.1 30 2730 4.2 04 24.... 0 42 000 15.4 v 14.2 1m 2130 42 75 of isobutylene per gms. of diluent per hour) the V. I. remains substantially the same (between 7346) and the viscosity at 210 F. does In the above Table VIthe circulation rate means the rate' at which the fluid is pumped through at line 5 and the cooling coil 6 in Figure 2. The per cent oil in stream refers to the per cent of oil recovered irom the washed oily product coming from line 39. The viscosity at a 1 tests using the continuous recycling process illustrated in, Figure 2 of the drawings. 0

. 210- F. refers to the oil in the previous column in the table. The recycle added is the amount of light distillate which is recycled into the diluent feed line 2 in Figure 2 of the drawings. This recycle represents dimer and other low molecular weight polymers of isobutylene which come off by the steam distillation referred to from the product obtainedin line 3.9. k

- From the above Table it is noted that as the temperature is decreased from 70 to 40, the yield is progressively increased. Also, it is noted, particularly comparing tests 22, 23 and 24, that the yield and'viscosity at 210 F. are both increased as the circulation rate is decreased, the amount of isobutylene and recycle being both constant.

For the sake of calling attention to the fact TABLE VII Study of heavy bottoms from tests 18 and 22 Tw Bottoms Vis./lF. Vis./210'F.

30% bottoms (525 F.

33 o bottoms (530 F.

The rcentages oi bottoms shown are based on the total amount of oil is t after steam distiliationat 450 F. A

Although the lower boiling constituents of both oils had approximatelythe same viscosity (because both oils were free from lighter constituents) by steam distillation at 450 F., yet the bottoms obtainedjfrom test 18 had a Saybolt viscosity of only 157 seconds compared to 269 seconds at 210 F. 'for the bottoms obtained in test 22. Therefore, inasmuch as in practice oil having a 210 F. viscosity less than 40 seconds would be removed, then the viscosity spread of the lubricating oil produced in test 18 would be 117 (157 minus 40) whereas the corresponding lubricating oil from test 22 would 'have a viscosity spread of 229 (269 minus 40).

The 33% bottoms obtained in test 22 shown above as having aviscosity of 269 seconds at 210 F. had an average molecular weight of 691 whereas a fraction having a viscosity of about 40 seconds at 210 F. has a. molecular weight of about 330 to 350. I

By successive batch precipitations of the high molecular weight fractions from polymer oil bottoms with benzol-acetone mixtures, or by prov pane precipitation, fairly good yields of low visvia/210 F. bottoms, and 72% of 85 via/210 F.'

oil from a 134 .vis./210F. bottoms. Precipitation of 1.6% of heavy oil from the 134 via/210 F. bottoms lowered the viscosity to 118 via/210 F.

It is not intended that this invention be limited to any of the specific examples given nor by any theories advanced as to the operation of the invention, but only by the appended claims in which it is intended to claim all novelty inherent in the invention as broadly as the prior art permits.

We claim:

1. The process of preparing lubricating oils which comprises dispersing a Friedel-Crafts type catalyst in a liquid consisting of a reactive aliphatic hydrocarbon liquid diluent having 01efinic groups and less than 25 carbon atoms, and then contacting therewith a normally gaseous olefln at a temperature between the approximate limits of 0 and 150 F.

2. The process of preparing lubricating oils comprising dispersing a Friedel crafts type .catalystin an isobutylene polymer comprising 2 to 6 monomers, and then feeding thereinto isobutylene at a temperature between the approximate limits of 0 and 150 F.

- 3. The process of preparing lubricating oils which comprises dissolving boronfluoride in an isobutylene polymer serving as reactive catalyst solvent having from 8 to 24 carbon atoms and .then feeding isobutylene into the resulting solution at a temperature between the approximate limits of and F.

4. The process according to claim 3 in which between about and 10 parts by weight of isobutylene are used to one partof the isobutylene polymer feed.

5. The process according to claim 3 in which lower boiling constituents are separated from the which comprises dissolving boron fluoride into a cracked wax liquid substantially free of aromatic hydrocarbons having about 10 to 24 carbon atoms per molecule and then feeding isobutylene into the resulting solution at a temperature between the approximate limits of 0 and F.

8. A hydrocarbon lubricating oil having it Saybolt viscosity above 40 seconds. at 210' F. and a viscosity index above 30 obtained by dispersing a Friedel-Crafts type catalyst in a liquid consisting of a reactive aliphatic hydrocarbon diluent having oleflnic groups and less than 25 tween the approximate limits of 0 F. and 150 F.

JAMES M. WHITELE'Y, JR. JEFFREY H. BARTLETT.

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