LUBRICANT BLENDS HAVING HIGH VISCOSITY INDICES

This invention relates to novel lubricant compositions exhibiting superior lubricant properties such as high viscosity index. More particularly, the invention relates to novel lubricant blends of high viscosity index polyalphaolefins lubricant basestock with conventional polyalphaolefins or mineral oil lubricant basestock.

Synthetic polyalphaolefins (PAO) have found wide acceptability and commercial success in the lubricant field for their superiority to mineral oil based lubricants. In terms of lubricant properties improvement, industrial research effort on synthetic lubricants has led to PAO fluids exhibiting useful viscosities over a wide range of temperature, i.e., improved viscosity index (VI), while also showing lubricity, thermal and oxidative stability and pour point equal to or better than mineral oil. These relatively new synthetic lubricants lower mechanical friction, enhancing mechanical efficiency over the full spectrum of mechanical loads from c n gears to fraction drives and do so over a wider range of ambient operating conditions than mineral oil. The PAO's are prepared by the polymerization of 1-alkenes using typically Lewis acid or Natta catalysts. Their preparation and properties are described by J. Brennan in Ind. Eng. Chem. Prod. Res. Dev. 1980, 19, pp 2-6. PAO incorporating improved lubricant properties are also described by J. A. Brennan in U.S. Patents 3,382,291, 3,742,082, and 3,769,363.

In accordance with customary practice in the lubricants art, PAO's have been blended with a variety of functional chemicals, oligoraeric and high polymers and other synthetic and mineral oil based lubricants to confer or improve upon lubricant properties necessary for applications such as engine lubricants, hydraulic fluids, gear lubricants, etc. Blends and their components are described in Kirk-Othmer Encyclopedia of Chemical Technology, third

edition, volume 14, pages 477-526. A particular goal in the formulation of blends is the enhancement of viscosity index (VI) by the addition of VI improvers which are typically high molecular weight synthetic organic molecules. While effective in improving viscosity index, these VI improvers have been found to be deficient in that their very property of high molecular weight that makes them useful as VI improvers also confers upon the blend a vunerability in shear stability during actual use applications. This deficiency dramatically negates the range of application usefulness for many VI improvers. Their usefulness is further compromised by cost since they are relatively expensive polymeric substances that may constitute a significant proportion of the final lubricant blend. Accordingly, workers in the lubricant arts continue to search for lubricant blends with high viscosity index less vulnerable to degradation by shearing forces in actual use applications while maintaining other important properties such as thermal and oxidative stability.

Recently, a novel class of PAO lubricant compositions, herein referred to as HVI-PAO, exhibiting surprisingly high viscosity indices has been obtained. These novel PAO lubricants are particularly characterized by low ratio of methyl to methylene groups, i.e., low branch ratios, as further described hereinafter. Their very unique structure provides new opportunities for the formulation of distinctly superior and novel lubricant blends.

This invention provides lubricant mixtures having surprisingly enhanced viscosity indices and comprising hydrogenated HVI-PAO having a branch ratio of less than 0.19 and a liquid lubricant taken from mineral oil, hydrogenated PAO, vinyl polymers, poly luorocarbons, polychlorofluorocarbons, polyesters, polycarbonates, silicones, polyurethanes, polyacetals, polyamides, polythiols, their co-polymers, terepolymers and mixtures thereof. Unexpectedly, when a low viscosity lubricant is hlended with a high viscosity, high VI lubricant produced from alphaolefins containing

— - —

^c 6 ^t0 ^20 ^atoms » he resulting blends have high viscosity indices and low pour points. The high viscosity index lubricant produced as a result of blending HVI-PAO and PAO has a much lower molecular weight than a conventional polymeric VI improver, thus offering the opportunity of greater shear stability.

The HVI-PAO having a branch ratio of less than 0.19 employed to prepare the blends of the present invention may be comprised of hydrogenated hydrocarbons.

In the drawings, Fig.1 is a comparison of VI vs. viscosity for blends, HVI-PAO and commercial PAO.

Fig. 2 and 3 compares VI increases of blends of HVI-PAO with PAO vs. blending with PAO.

Fig. 4 compares pour points of the blends.

Fig. 5 compares VI improvement fot stock 142(define) with PAO stock 751(define) vs. HVI-PAO.

Fig. 6 compares VI vs Viscosity for experimental blends with theoritical blending equations.

The new synthetic lubricant basestocks of the instant invention are obtained by mixing a low viscosity lubricant basestock with HVI-PAO having a very high viscosity index. The low viscosity lubricant basestock, typically with a viscosity between 1.5 to 50

2 mm /s at 100°C, can be synthetic PAO, any conventional mineral oil lube stock derived from petroleum, or other synthetic lube stock.

The high viscosity HVI-PAO lubricant basestock, typically with a viscosity of 10 to 500 mm /s at 100°C and a very high VI greater than 130, are produced from alphaolefins, 1-alkenes, of - to

C ₂₀ , either alone or in mixture, over an activated chromium on silicate catalyst. The high viscosity, high VI basestock, HVI-PAO, is further characterized by having a branch ratio of less than

0.19. When the high viscosity HVI-PAO basestock is blended with one or more lubricant basestock of low viscostiy, the resultant lubricant has an unexpectedly high viscosity index and low pore points. The high V.I. PAO lubricants, HVI-PAO, with a branch ratio less than 0.19 are better blending components than the commercially

available PAO often used to boost V.I. Also, the HVI-PAO are superior to conventional V.I. improvers such as polybutene and polyacrylates since the blend produced therefrom is of much lower molecular weight thus offering improved shear stability. Also, the

HVI-PAO is more oxidatively and hydrolytically stable than other

V.I. improvers.

The HVI-PAO lubricant blending stock of the present invention may be prepared by the oligomerization of 1-alkenes as described hereinafter, wherein the l-alkenes have 6 to 20 carbon

2 atoms to give a viscosity range of -3-100α mm /s at 100°C. The oligomers may be homopolymers or copolymers of such C ₆ -C ₂ Q

1-alkenes, or physical mixtures of homopolymers and copolymers.

They are characterized by their branch ratio of less than 0.19, pour point below -15°C, and are further characterized as having a number averaged molecular weight range from 300 to 70,000.

In the case of blends of PAO with HVT-PAO, the low viscosity basestock PAO component, or current PAO, is obtained from commercial sources such as MOBIL Chemical Co. in a viscosity range

2 of 1.5 to 50 mm /s at 100°C. The commercial material is typically prepared by the oligomerization of 1-alkene in the presence of borontrifluoride, aluminum chloride or Natta catalyst and is characterized by having a branch ratio greater than 0.19 and viscosity indices significantly lower than HVT-PAO.

Other liquid lubricants useful as blending components with HVI-PAO include lubricant grade mineral oil from petroleum, typically comprising C ₃ Q+ hydrogenated hydrocarbons. Yet other useful HVT-PAO blending components include hydrogenated polyolefins as polyisobutylene and polypropylene and the like; vinyl polymers such as polymethylmethaciylate and polyvinylchloride; polyfluorocarbons such as polytetrafluoroethylene and polychlorofluorocarbons such as polychloro luoroethylene; polyesters such as polyethyleneterephthalate and polyethyleneadipate; polycarbonates such as polybisphenol A carbonate; polyurethanes such as polyethylenesuccinolycarbamate; silicones; polyacetals such as

polyoxymethylene; polyamides such as polycaprolactam. The foregoing polymers include copolymer thereof of known composition exhibiting useful lubricant properties or conferring dispersant, anticorrosive or other properties on the blend. In all cases, blends may include other additives as described in the previously cited Kirk-Othmer reference.

Unless otherwise noted, HVI-PAO, PAO and mineral oil based lubricants discussed herein preferably refer to hydrogenated materials in keeping with the practice of lubricant preparation well known to those skilled in the art. However, unhydrogenated high viscosity HVI-PAO with low unsaturation is sufficiently stable to be used as lubricant basestock.

The following examples illustrate the application of the instant invention in the preparation of blends of high viscosity lubes with high viscosity indices by mixing HVI-PAO with conventional commercially available PAO. The samples used for blending experiment have the following viscometric properties:

Viscometric Properties

2 2

Sample Vis mm /s Vis mm /s VI

40 °C 100°C

A 5238 483.1 271

B 1205.9 128.3 212

C 1336.2 139.4 214

D 1555.4 157.6 217

EM 3002 5.22 1.75 99

EM 3004 17.07 3.92 126

Mobil SHF-61 29.53 5.64 133

Mineral Oil 21.32 4.19 97

Mobil SHF-1001 1213.04 96.33 165

Mineral Oil 18.5/22.0 4.0 95

Sample A: A Cr (1 wt%) on silica catalyst, 4 grams, calcined at

600°C with air and reduced with CO at 350°C, was mixed with 1-decene, 63 grams in a flask. The mixture was heated in an 100°C oil bath under N ₂ atmosphere for 16 hours. The lube product was obtained by filtration to remove catalyst and distilled to remove components boiling below 120°C at 0.1 mmHg. The lube product yield was 92%.

Sample B: Similar to the previous example, except 1.7 grams of catalyst and 76 grams of 1-decene were heated to 125°C. The lube yield was 86%.

Sample C: An activated Cr (1 wt%) on silica catalyst, 3 grams, calcined at 500°C with air and reduced with CO at 350°C, was packed in a stainless steel tubular reactor and heated to 119 + or 3°C. 1-Decene was fed through this reactor at 15.3 grams per hour at 1480 kPa (200 psig). Aft r about 2 hours on stream, 27.3 grams of crude product was collected. After distillation, 19 grams of lube product was obtained.

Sample D: In the same run as the previous example, 108 grams of crude product was obtained after 15.5 hours on stream. After distillation, 86 grams of lube product was obtained.

PAO samples EM3002 and EM3004 are obtained commercially from Emery Chemical Co. Mobil SHF-61 and Mobil SHF-1001 are obtained from Mobil Chemical Co. The mineral oil used in the study is a 100", solvent neutral mineral base stock, available from Mobil Oil Corporation, Product No. 71326-3.

In Tables 1-6 the results of blending experiments using the above samples are presented. In these blending experiments, the blend products were obtained by mixing proper amounts of the different feed stocks.

Examples

Examppilee 11,, ((TTaabbllee 11)) 5.6 mm ² /s PAO (Mobil SHF-61) blended with sample B E Exxaammple 2, (Table 2) 5.6 mm ² /s PAO (Mobil SHF-61) blended with sample A.

Example 3, (Table 3) 3.9 mm ² /s PAO (EM 3004) blended with sample D.

Example 4, (Table 4)1.8 mm ² /s PAO (EM 3002) blended with sample C.

Example 5, (Table 7) 100" mineral oil blended with sample C, Control Example A, (Table 5) 4 mm ² /s PAO blended with 100 mm /s PAO.

Control Example B, (Table 6) 5.6 mm ² /s PAO blended with 100 mm ² /s PAO.

Control Example C, (Table 8) Mineral oil blended with 100mm ² /s PAO (Mobil SHF-1001).

Data in Control Examples A and B were obtained from Uniroyal Chemical Co. sales brochure of Synthon PAO.

As shown in Fig.1, when the HVI-PAO were used as blending components, the resulting blends at a specific viscosity had higher VI than the new PAO synthesized directly from 1-decene over Cr/Si0 ₂ catalyst or the PAO produced over acidic BF3 or

AlCl-7 catalysts. The VI asvantages of the blends are illustrated

2 as follows, comparing the VI's of the 10mm /s oils produced from various synthetic methods or from blending: 2 10mm /s oil From VI VI Advantage

Direct synthesis by (commercial) 137 0

Direct synthesis by Cr/Si0 ₂ 163 26

Blends of PAO + HVI-PAO 2 2

5.6mm /s 128mm /s 161 24

2 2

5.6mra /s 483mπ_ /s 165 28

2 2

3.9mm /s 158mm /s 183 46

2 2

1.8mm /s 139mm /s 220 83

As shown in Fig. 2 and 3, the resulting blends in Examples 1 to 3 with one specific viscosity also had higher VI than the blends produced in the Control Examples.

The blending products in Examples 1 to 4 have excellent low temperature properties. The pour points of the blends in Examples 1 to 4 were either lower or similar than the pour points of the current commercial PAO or the blends produced in Control Examples, as shown in Fig.4.

Similarly, when a mineral lubricant as previously defined

2 with viscosity at 100°C of 4.2 mm /s and 97 VI, was blended with the high viscosity, high VI PAO (HVI-PAO), the VI of the resulting blends were improved (Example 5, Table 7). Figure 5 shows that the

VI of the blends in Example 5 is higher than the VI of the blends produced in Control Example B, when stock 142 was blended with a current commercial PAO (Table 8). For example, when 9.1 wt% of

157.6mm ² /s HVT-PAO with 217 VI is blended with mineral oil (97

VI), the resulting lube had a VI and viscosities comparable to a commercial synthetic low viscosity PAO, Mobil SHF-61:

9% HVI-PAO in Mineral Oil Mobil SHF-61 V ^@ 100°C, mm ² /s 5.95 5.6

VI 134 133

When HVI-PAO was blended with either synthetic PAO or mineral lube, the resulting blends have unexpectedly high viscosity indices and excellent low temperature properties, such as low pour points. These very hight VI blends can be used as a basestock for engine oils or hydraulic oils with little or no VI improver added.

TABLE 1

Viscosities and Pour Points of Blends 5.5 mm ² /s PAO + 128 mm ² /s HVI-PAO

Wtl of HVI-PAO V V PP in 5.6 mm ² /s PAO 40°C mm ² /s 100°C mm ² /s ι_ 1£.

100 1205.92 128.34 212

50.5 174.79 26. 52 188 -45 -43

33.3 94.01 15.43 174 -52 -52

17.0 53.92 9.60 164 -54 -53

13.0 45.85 8.35 159

9. 1 40.36 7.42 151

4.8 34.35 6.49 144

2.4 31. 59 6.06 141

1.0 30.37 5.75 133

0 29. 53 5.64 13

TABLE 2

Viscosities of Blends 5.5 mm ² /s PAO + 483.1 mm ² /s HVI-PAO

Wt% of HVI-PAO V € v ^~

2 in 5.6 mm /s PAO 40° C mm ² /s 100°C ran I 2 //s VI

100 5238.41 483.10 271

33.3 181.34 27.85 193

16.7 70.96 12.50 176

13.0 57.22 10.27 169

9.1 50.72 9.20 165

4.8 38.83 7.29 154

2.4 34.08 6.54 149

1 30.61 5.94 142

0 29.53 5.64 133

TABLE 3

Viscosities of Blends 3.9 mm ² /s PAO + 157.6 mm ² /s HVI-PAO

Wt% of HVI-PAO Vmm ² /s 6 Vmm ² /s § PP

2 in 3.9 mm /s PAO 40°C 100°C vi 1

100 1555.75 157.62 217

66.7 288.91 41. 85 201

33.3 68.73 12.82 189 -59

28. 6 56.02 10.68 184

23.1 45.19 8.82 179

16. 7 33.82 7.01 175

9.1 24.92 5.40 160 -o4

4.8 20.82 4.59 140

2.4 18.80 4.21 130

1.0 17.68 4.02 127

0.0 17.07 3.92 126 -68

TABLE 4

Viscosities of Blends 1.75 mm ² /s PAO + 139.4 mm ² /s HVI-PAO

t% of HVI-PAO V, mm /s V, mm /s PP in 1. 75 mm /s PAO 40°C . 100°C VI _°C

100 1336.18 139.38 214

50 61.03 12.96 218

33.3 26.05 6.58 225 -71 -69

9.1 7.95 2.48 148 -75 -68

4.8 6.52 2.13 137

2.4 5.83 1.92 115

1.0 5.45 1.79 96

0.0 5.22 1.75 99

TABLE 5

Viscometrics of Blends of Low Viscosity Current PAO

(PAO-4) with high viscosity current PAO (PAO-100)

°C(°F)

100 0 100 -20 (-5) 168

90 10 74 -32 (-25) 166

75 25 45 -37 (-35) 164

50 50 20 -48 (-55) 162

25 75 9 -59 (-75) 162

10 90 5.5 <-59 «-75) 150

0 100 4 -79 (-110) 123

TABLE 6

Viscometrics of Blends of Low Viscosity Current PAO-6 with High Viscosity Current PAO (PAO-100)

PAO-100 PAO-6 KV at 100°C VI wtl wt% mm /s

10 90 8.15 146

25 75 12.61 152

67 33 40.0 159

100 0 100.0 168

TABLE 7

Viscosities of Blends

100" Mineral Oil + 157.6 mmVs HVI-PAO

Wt% of HVI-PAO V β V § PP in 100" mineral oil 40° C mm ² /s 100°C mm ² /s yj_ J-

100 1555.75 157.62 217

33.3 90.48 14.23 162

9.1 31. 79 5.95 134 -20 -19

4.8 26.15 5.04 121

2.4 23.7 4.59 108

1.0 22.27 4.35 102

0.0 21.32 4.19 97

TABLE 8

Viscosities of blends 100" Mineral Oil + Mobil SHF 1001

Wt% of Stock 751 V § V g

2 in 100" mineral oil 40 C mm ² /s 100 C mm /s VI

100 1214.04 96.33 165

90 823.68 72.26 162

75 450.88 46.15 159

70 371.06 40.38 160

50 172.62 21. 87 151

30 78.25 11.8 144

0 21.32 4.19 97

It has been found that empirical blending equations such as that given in Appendix 2 of ASTM D341-77 "Viscosity-Temperature Charts for Liquid Petroleum Products" fail to predict the viscosity/VI relationship found in the novel blends reported herein. While not accurately predicting the viscometrics of the novel blends of the instant invention, the following equation reported by M.Horio, T.Fu ii and S. Onogi (J. Phys. Chem. , 68 (1964) provides the closest approximation:

log A = WglogB + W logC

where A is the blend viscosity, B and C are the dynamic viscosities of components B and C, and w. and Wg are weight fractions. Fig. 6 compares VI and viscosity for experimental blends with curves developed from known blending equations.

The following Examples serve to further illustrate the preparation and properties of HVI-PAO employed in the unique blends of the instant invention and methods of preparing the catalyst used in the preparation of HVI-PAO. By the following methods, HVI-PAO with a weight average molecular weight between 300 and 150,000; number average molecular weight between 300 and 70,000; molecular weight distribution between 1 and five can be produced with VI greater than 130 and pour point below -15°C. Preferably, the weight average molecular weight is between 330 and 90,000, number average molecular weight is between 300 and 30,000; and molecular weight distribution is between 1.01 and 3.

Example 6

Catalyst Preparation and Activation Procedure

1.9 grams of chromium (II) acetate

Cr ₂ (OCOCH ₅ ) ₄ .2H2θ (5.58 mmole) (commercially obtained) was dissolved in 50 ml of hot acetic acid. Then 50 grams of a silica

2 gel of 8-12 mesh size, a surface area of 300 m /g, and a pore

volume of 1 ml/g, also was added. Most of the solution was absorbed by the silica gel. The final mixture was mixed for half an hour on a rotavap at room temperature and dried in an open-dish at room temperature. First, the dry solid (20 g) was purged with N ₂ at 250°C in a tube furnace. The furnace temperature was then raised to 400°C for 2 hours. The temperature was then set at 600°C with dry air purging for 16 hours. At this time the catalyst was cooled down under N2 to a temperature of 300°C. Then a stream of pure CO (99.99% from Matheson) was introduced for one hour. Finally, the catalyst was cooled down to room temperature under N ₂ and ready for use.

Example 7 The catalyst prepared in Example 1 (3.2 g) was packed in a 9.5 mm (3/8") stainless steel tubular reactor inside an N ₂ blanketed dry box. The reactor under N atmosphere was then heated to 150°C by a single-zone Lindberg furnace.Pre-purified 1-hexene was pumped into the reactor at 1079 kPa (140 psi) and 20 ml/hr. The liquid effluent was collected and stripped of the unreacted starting material and the low boiling material at 0.05 mm Hg. The residual clear, colorless liquid has viscosities and VI's suitable as a lubricant base stock.

Sample Prerun

T.O.S.*, hr. 2 3.5 5.5 21.5

Lube Yield, wt% 10 41 74 31

2 Viscosity, mm /s, at

40°C 208.5 123.3 104.4 166.2

100°C 26.1 17.1 14.5 20.4

VI 159 151 142 143

*time on stream

Example 8 Similar to Example 7, a fresh catalyst sample was charged into the reactor and 1-hexene was pumped to the reactor at 1 atm and 10 ml per hour. As shown below, a lube of high viscosities and high VI's was obtained. These runs showed that at different reaction conditions, a lube product of high viscosities can be obtained. Sample A I?

T.O.S., hrs. 20 44

Temp., °C 100 50

Lube Yield, % 8.2 8.0

Viscosities, mm /s at

40°C 13170 19011

100°C 620 1048

VI 217 263

Example 9

A commercial chrome/silica catalyst which contained 1% Cr on a large-pore volume synthetic silica gel was used. The catalyst was first calcined with air at 800°C for 16 hours and reduced with CO at 300°C for 1.5 hours. Then 3.5 g of the catalyst was packed into a tubular reactor and heated to 100°C under the N ₂ atmosphere. 1-Hexene was pumped through at 28 ml per hour at 101 kPa (1 atmosphere). The products were collected and analyzed as ollows: Sample C D E _F

T.O.S., hrs. 3.5 4.5 6.5 22.5

Lube Yield, % 73 64 59 21

Viscosity, mm /s, at

40°C 2548 2429 3315 9031

100°C 102 151 197 437

VI 108 164 174 199

These runs showed that different Cr on a silica catalyst were also effective for oligomerizing olefins to lube products.

Example 10 As in Example 9, purified 1-decene was pumped through the reactor at 1830 to 2310 kPa (250 to 320 psi). The product was collected periodically and stripped of light products boiling points below 343 °C (650°F). High quality lubes with high VI were obtained (see following table).

Reaction WHSV Lube Product Properties

Temp.°C g/g/hr V at 40°C V at 100°C VI

2 2 mm /s mm /s

120 2.5 1555.4 157.6 217

135 0.6 389.4 53.0 202

150 1.2 266.8 36.2 185

166 0.6 67.7 12.3 181

197 0.5 21.6 5.1 172

Example 11

Similar catalyst was used in testing 1-hexene oligomerization at different temperature. 1-Hexene was fed at 28 cc/hr and at 1 atmosphere.

Sample H

Temperature, °C 110 200

Lube Yield, wt.% 46 3

2 Viscosities, mm /s at

40°C 3512 3760

100°C 206 47

VI 174 185

Example 12 1.5 grams of a similar catalyst as prepared in Example 9 was added to a two-neck flask under N ₂ atmosphere. Then 25 g of 1-hexene was added. The slurry was heated to 55°C under N ₂ atmosphere for 2 hours. Then some heptane solvent was added and the catalyst was removed by filtration. The solvent and unreacted starting material was stripped off to give a viscous liquid with a

61% yield. This viscous liquid had viscosities of 1536 and 51821

2 mm /s at 100°C and 40°C, respectively. This example demonstrated that the reaction can be carried out in a batch operation.

The 1-decene oligomers as described below were synthesized by reacting purified 1-decene with an activated chromium on silica catalyst. The activated catalyst was prepared by calcining chromium acetate (1 or 3% Cr) on silica gel at 500-800°C for 16 hours, followed by treating the catalyst with CO at 300-350°C for 1 hour.

1-Decene was mixed with the activated catalyst and heated to reaction temperature for 16-21 hours. The catalyst was then removed and the viscous product was distilled to remove low boiling components at 150°C and 13 Pa.

Reaction conditions and results for the lube synthesis are summarized below:

Table 9

1-decene/

Example Cr on Calcination Treatment Catalyst Lube

NO. Silica Temp. Temp. Ratio Yld

13 3wt% 700°C 350°C 40 90%

14 3 700 350 40 90

15 1 500 350 45 86

16 1 600 350 16 92

Branch Ratios and Lube Properties of Examples 13-16 Alpha Olefin Oligomers

Table 10

Example Branch CH ₃ ^V 40° ^{C V} 100° ^C VI

No. Ratios CH ₂

13 0.14 150.5 22.8 181

14 0.15 301.4 40.1 186

15 0.16 1205.9 128.3 212

16 0.15 5238.0 483.1 271

Example 17

A commercial Cr on silica catalyst which contains 1% Cr on a large pore volume synthetic silica gel is used. The catalyst is first calcined with air at 700°C for 16 hours and reduced wth CD at 350°C for one to two hours. 1.0 part by weight of the activated catalyst is added to 1-decene of 200 parts by weight in a suitable reactor and heated to 185°C. 1-Decene is continuously fed to the reator at 2-3.5 parts/minute and 0.5 parts by weight of catalyst is added for every 100 parts of 1-decene feed. After 1200 parts of 1-decene and 6 parts of catalyst are charged, the slurry is stirred for 8 hours. The catalyst is filtered and light product boiled below 150°C § 13 Pa (0.1mm Hg) is stripped. The residual product is hydrogenated with a Ni on Kieselguhr catalyst at 200°C. The finished product has a viscosity at 100°C of 18.5 mm /s, VI of 165 and pour point of -55°C.

Example 18

Similar as in Example 17, except reaction temperature is

125 °C. The finished product has a viscosity at 100°C of 145

2 mm /s, VI of 214, pour point of -40°C.

Example 19 Similar as in Example 17, except reaction temperature is

100°C. The finished product has a viscosity at 100°C of 298

2 mm /s, VI of 246 and pour point of -32°C.

The final lube products in Example 17 and 19 contain the following amounts of dimer and trimer and isomeric distribution

(distr.).

Example 17 18 19

Vmm ² /s @100°C 18.5 145 298

VI 165 214 246

Pour Point, °C -55°C -40°C -32 wt% dimer 0.01 0.01 0.027 wt% isomeric distr. dimer n-eicosane 51% 28% 73%

9-methylnonacosane 49% 72% 27% wt% timer 5.53 0.79 0.27 wt% isomeric distr. trimer

11-octyldocosane 55 48 44

9-methy1,11-octyl- heneicosane 35 49 40 others 10 13 16

The following table summarizes the molecular weights and distributions of Examples 16 to 18. Examples 16 17 18

V @100°C, mm ² /s 18.5 145 298

VI 165 214 246 number-averaged

Hiolecular weights, MW _n 1670 2062 5990 weight-averaged molecular weights, MW 2420 4411 13290 molecular weight distribution, MWD 1.45 2.14 2.22

Under similar conditions, HVI-PAO product with viscosity as

2 2 low as 3 mm /s and as high as 1000 mm /s with VI between 130 and

280, can be produced.

Although the present invention has been described with preferred embodiments, it is to be understood that modifications and variations may be resorced to, without departing from the spirit and scope of this invention, as those skilled in the art will readily understand. Such modifications and variations are considered to be within the purview and scope of the appended claims.