JPH07150186A - Raw material for synthetic lubricating oil and its preparation - Google Patents

Abstract

PURPOSE: To obtain a synthetic lubricating oil stock containing a specific type oligomer and having excellent viscosity and, in some case, a low flow point, by incorporating a specific type compound therein.

CONSTITUTION: A synthetic lubricating oil stock, which contains an oligomer obtained from an olefin composition comprising a 10-24C linear olefin, further comprises an alkyl-substituted biphenyl, diphenyl ether or an anisole of formula I or II (wherein R¹ represents a group of formula III or IV; R^2-7 independently represent H or a 1-24C alkyl provided that one or more thereof independently represent a 10-24C alkyl; R¹¹ represents 1-10C alkyl; R¹² represents a 10-24C alkyl; and R^13-14 independently represent H or a 1-10C alkyl).

COPYRIGHT: (C)1995,JPO

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a synthetic lubricating oil raw material, and more particularly to a synthetic lubricating oil raw material having an excellent viscosity. Some of these synthetic lube feedstocks also exhibit low pour points.

[0002]

2. Description of the Related Art Synthetic lubricating oils produced from man-made raw material oils have a uniform molecular structure and, in turn, show clear characteristics that can be tailored to specific applications. on the other hand,
Mineral oil feedstock is produced from crude oil and is a complex mixture of naturally occurring hydrocarbons. The more uniform synthetic lubricating oil generally results in superior properties. For example, synthetic lubricating oils exhibit excellent thermal stability. As automobile engines are miniaturized to save weight and fuel, such engines will operate at higher temperatures, resulting in the need for more heat stable oils. Lubricants produced from synthetic feedstocks exhibit properties such as excellent oxidative / thermal stability, very low volatility and good viscosity index over a wide range of temperatures,
These provide a better lubrication effect, allow longer oil change intervals, and reduce oil loss due to vaporization during the change.

Synthetic feedstocks are those that oligomerize internal olefin monomers and α-olefin monomers to form a mixture of dimers, trimers, tetramers and pentamers while minimizing the amount of relatively highly polymerized oligomers. Can be manufactured by. The unsaturated oligomer product is then hydrogenated to improve its oxidative stability with little change in other properties. The resulting synthetic feedstock exhibits a uniform structure of isoparaffinic hydrocarbons similar to high quality paraffinic mineral feedstocks, but has the above-mentioned excellent properties because of its higher homogeneity.

Synthetic feedstocks are produced in a wide range of viscosities. Generally, feedstocks are classified by viscosity at 100 ° C., measured in centistokes (cSt).
A feedstock having a viscosity of 4 cSt or less is generally referred to as a "low viscosity" feedstock, and a feedstock having a viscosity of 40 to 100 cSt is generally referred to as a "high viscosity" feedstock. A feedstock having a viscosity of 4-8 cSt is called a "medium viscosity" feedstock. Low viscosity feedstocks are generally recommended for use at low temperatures. Feedstocks for use at higher temperatures, such as motor oils, automatic transmission oils, turbine lubricants and other industrial lubricants, are generally those obtained with higher viscosity, eg medium viscosity feedstocks (ie 4-8 cS).
t) is required. High-viscosity feedstocks are used as gear oils and blending feedstocks.

The viscosity of the feedstock is usually determined by the chain length of the oligomer molecules formed during the oligomerization reaction. The degree of oligomerization is influenced by the catalyst used in the oligomerization reaction and the reaction conditions. The carbon chain length of the monomer starting material also directly affects the properties of the oligomer product. Fluids made from short chain monomers tend to have low pour points and moderately low viscosity indices,
Fluids made from long chain monomers tend to have moderately low pour points and higher viscosity indices. Oligomers made from long chain monomers are generally more suitable for use as medium viscosity synthetic lubricating oil feedstocks than those made from short chain monomers.

A known method of oligomerizing long chain olefins to produce a synthetic lubricating oil feedstock is US Pat. No. 4,40.
0,565, 4,420,646, 4,42
As described in Nos. 0,647 and 4,434,308, the olefin is contacted with boron trifluoride together with a reaction promoter at a reaction temperature sufficient to cause its oligomerization. However, boron trifluoride gas (BF ₃ ) is a lung irritant, and inhaling this gas or fumes formed by hydration of this gas with atmospheric moisture should preferably be avoided. Will be presented. Moreover, the disposal / neutralization of BF ₃ is of environmental concern. Thus, a process for oligomerizing long chain olefins using a non-hazardous and non-environmental catalyst would be a significant improvement in the art.

“Preparation of High-Vi” by Kuliev et al.
scosity Synthetic Lubricants Using an Aluminosilic
ate Catalyst ”(Institute of Petrochemical Process
es of the Academy of Sciences of the Azerbaidzhan
SSR, Azer. Neft. Khoz., 1983, No.4, p.40-43)
USSR consisting of those Azerbaijan bentonite activated by sulfuric acid and hydrochloric acid, using an acid clay does not cause environmental destruction without risk, by oligomerizing long-chain (C ₉ ~C ₁₄₎ olefins, synthetic lubricating Attempted to produce oil. Kuliev et al., "It is not possible to produce viscous or highly viscous oils by olefin polymerization over aluminosilicate catalysts", and "Redistribution of hydrogen reactions is based on aromatic hydrocarbon, coke and paraffinic systems. It takes precedence over the formation of hydrocarbons. " On the other hand, U.S. Pat. No. 4,531,014 discloses the use of bentonite from Wyoming, USA to oligomerize short chain olefins.
Similar to that of Kuliev et al., It is not possible to obtain a product that is rich in dimers, trimers and tetramers and poor in disproportionation reaction products.

Our previous application (Japanese Patent Application No. 3-859)
52) discloses that synthetic lubricating oil feedstocks can be produced in good yields by oligomerizing long chain olefins using a specific acidic montmorillonite clay catalyst. Contains up to 20% by weight of water, 3 to 30
Almost all associated hydrogen redistribution by-products are formed by using acidic calcium-montmorillonite clay showing residual acidity up to mg KOH / g (by titration to phenolphthalein end point) and having a surface area of 300 m ² / g or more. It has been found that long-chain olefins can be converted to dimers, trimers and tetramers at high rates without.
In addition to being excellent catalysts, these clays are not dangerous and do not cause environmental damage.

The viscosity (and in some cases the pour point) of the feedstock produced in this way depends on the amount of large amounts of long-chain linear olefins and small amounts of certain aromatic compounds such as anisole, diphenyl ether and / or biphenyl ( That is, it can be improved by co-reacting (at a molar ratio of about 3: 1 or more). Mixtures of the resulting oligomers with alkylated anisole, alkylated diphenyl ethers and / or alkylated biphenyls have excellent viscosities and, in the case of alkylated diphenyl ethers and alkylated biphenyls, pour points found in feedstocks consisting only of olefin oligomers. Shows a significantly lower pour point. The inclusion of ether linkages (in the case of anisole and diphenyl ether) also acts to increase the additive solubility of the resulting feedstock. The oligomers and alkylated anisole, alkylated diphenyl ethers and / or alkylated biphenyls can be hydrogenated (alkanes and alkylated dicyclohexyl ethers and / or alkylated bicyclohexyls) to increase their oxidative stability. US Patent No. 4,
No. 480,142 is a process for making alkylated polycyclic aromatic hydrocarbons by contacting an aromatic compound with an α-olefin at an olefin: aromatic compound molar ratio of up to 2.5: 1. Is disclosed. Acidic montmorillonite clay is used as the catalyst for this reaction.

[0010]

One embodiment of the invention is a synthetic lubricating oil feedstock consisting of an oligomer prepared from an olefin composition comprising a linear olefin having 10 to 24 carbon atoms, the formula comprising:

[Chemical 10] (In the formula, R ¹ is the formula

[Chemical 11] A group represented by; R ² , R ³ , R ⁴ , R ⁵ ,
At least one of R ⁶ and R ⁷ is 10 to 24.
R is an alkyl group having 1 to 10 carbon atoms; R is H or an alkyl group having 1 to 24 carbon atoms; R ¹¹ is an alkyl group having 1 to 10 carbon atoms; ¹² is an alkyl group having 10 to 24 carbon atoms; R ¹³ and R ¹⁴ are each an alkyl group having up to 10 carbon atoms), the alkyl-substituted biphenyl, diphenyl ether or A synthetic lubricating oil feedstock further comprising anisole is provided.

Embodiments of the present invention also include formula (A)

[Chemical 12] (In the formula, R ¹ is the formula

[Chemical 13] , And formula (B)

[Chemical 14] (In the formula, R ¹ is the formula

[Chemical 15] Or formula (C)

[Chemical 16] And R ^{2 to} R ⁷ and R ^{11 to} R ¹⁴ have the same meanings as defined above, further providing such a composition comprising an alkyl-substituted aromatic or cycloaliphatic compound. .

The linear olefin can consist of α-olefins, internal olefins or mixtures thereof.

In another embodiment, the olefin composition comprises the linear olefin and up to 20% by weight of propylene or 1,3-diisopropenylbenzene or α-methylstyrene.

Alternatively, the olefin composition may comprise the linear olefin and a vinylidene olefin having 10 to 24 carbon atoms (eg 5 to 40% by weight).

The present invention also includes the formula

[Chemical 17] (In the formula, R ¹ is the formula

[Chemical 18] R ^{2 to} R ⁷ have the same meaning as defined above if at least one of them is hydrogen; R ¹¹ has 1 to 10 carbon atoms. An alkyl group; R ¹² is hydrogen; R ¹³ and R
¹⁴ are each hydrogen or an alkyl group having 1 to 10 carbon atoms) by contacting the olefin composition with an acidic montmorillonite clay in the presence of an alkyl-substituted biphenyl, diphenyl ether or anisole. A method for producing a synthetic lubricating oil raw material as described above is provided.

Optionally, the clay may be Lewis acid activated.

The alkylated oligomerization product of this reaction can be fully or partially hydrogenated.

Our previous application (Japanese Patent Application No. 3-859)
52) shows that a synthetic lubricating oil feedstock can be produced in good yield by oligomerizing a long chain linear olefin using a specific acidic montmorillonite clay catalyst. Improves viscosity (and possibly pour point) of these feedstocks when the starting material is a mixture of large amounts of long chain linear olefins and small amounts of certain aromatic compounds such as anisole, diphenyl ether and / or biphenyl I found that I could do it. As used herein, the phrase "diphenyl ether and / or biphenyl" means that the mixture is (1) diphenyl ether only, (2) biphenyl only, or (3) both diphenyl ether and biphenyl (ratio of 1:99 to 99: 1). In) is included. Those using "and / or" in connection with the other components of the mixtures described herein also include either (or in the case of three or more any) components, or both (or three or more). Should also be construed as indicating the presence of some or all of the components).

The starting material used to produce the feedstock of the present invention comprises a mixture of long chain linear olefins and a specified aromatic compound in a molar ratio of 3: 1 or greater. Co-reacting a large amount of linear olefin feed with a small amount of anisole, diphenyl ether and / or biphenyl gives a mixture of olefin oligomer and alkylated anisole, alkylated diphenyl ether and / or alkylated biphenyl. Preferably, the resulting feed oil is
It contains from 1 to 50% by weight of alkylated diphenyl ether and / or alkylated biphenyl. More preferably,
The resulting feedstock contains 5 to 25% by weight of alkylated diphenyl ether and / or alkylated biphenyl. Then, optionally, the double bond present in the oligomer and the alkylated diphenyl ether and / or the alkylated biphenyl contained in the mixture is hydrogenated, and the reduced oligomer and the alkylated dicyclohexyl ether and / or
Alternatively, a mixture with alkylated bicyclohexyl may be obtained. Preferably, the resulting feedstock contains 1 to 50% by weight of alkylated dicyclohexyl ether and / or alkylated bicyclohexyl. More preferably, the resulting feedstock contains 5 to 25% by weight of alkylated dicyclohexyl ether and / or alkylated bicyclohexyl. Optionally, one skilled in the art may also use hydrogenation conditions that reduce only the oligomer to obtain a mixture of reduced oligomer and alkylated diphenyl ether and / or alkylated biphenyl. Those skilled in the art will also use hydrogenation conditions to reduce a portion of the oligomer and the alkylated diphenyl ether and / or alkylated biphenyl,
Reduced oligomer, alkylated diphenyl ether and /
Alternatively, it may be desirable to obtain a mixture of alkylated biphenyl and alkylated dicyclohexyl ether and / or alkylated bicyclohexyl. Compounds having one aromatic ring and one cyclohexyl (reduced) ring may be prepared and included.

According to another embodiment, the starting material is a mixture of long-chain linear olefins and preferably 1 to 40% by weight of anisole (ie anisole: linear olefins weight ratio of 1:99 to 2: 3). If it consists of, the viscosity of these feedstocks is improved. It is even more preferred that the mixture of long chain linear olefin and anisole comprises 5 to 25% by weight of anisole (ie a weight ratio of anisole: linear olefin of 1:20 to 1: 4). The mixture of long-chain linear olefin and anisole is about 20 anisole.
It is especially preferred to include wt% (ie, the anisole: linear olefin weight ratio is about 1: 5). Co-reacting the anisole with the linear olefin feedstock yields a mixture of olefin oligomer and alkylated anisole. Then, optionally, the double bond existing in the oligomer and the alkylated anisole contained in the mixture may be hydrogenated to obtain a mixture of the reduced oligomer and the alkylated methoxycyclohexane. Preferably, the resulting feedstock contains 1-80% by weight of alkylated methoxycyclohexane. More preferably, the resulting feedstock contains 5-40% by weight of alkylated methoxycyclohexane. One skilled in the art may also find it desirable to obtain a mixture of reduced oligomer and alkylated anisole using hydrogenation conditions that reduce only the oligomer. One of ordinary skill in the art may also find it desirable to obtain a mixture of reduced oligomer, alkylated anisole and alkylated methoxycyclohexane using hydrogenation conditions that reduce a portion of the oligomer and alkylated anisole.

Olefin monomer feedstocks useful in the present invention include α represented by formula (1) R ″ CH═CH _{2 where} R ″ is an alkyl group having 8 to 22 carbon atoms. -Olefin, and (2) Formula RCH = CHR '(wherein R
And R'is an identical or different alkyl group having 1 to 20 carbon atoms), wherein the total number of carbon atoms in any one olefin is 10 to 24. Individual). The preferred range of the total number of carbon atoms in any one olefin molecule is 12 to 18, and the particularly preferred range is 13 to
It is 16 pieces. Mixtures of internal olefins and α-olefins may be used, and if the total number of carbon atoms in any one olefin is 10 to 24, use a mixture of olefins having different numbers of carbon atoms. Good.
The α-olefins and internal olefins useful in the present invention can be obtained by methods well known to those skilled in the art,
It is commercially available. It is also possible to co-oligomerize further unsaturated hydrocarbons with linear olefins. Examples of further unsaturated hydrocarbons are propylene, diisopropenylbenzene, α-methylstyrene and vinylidene olefins. For more details, please refer to our previous application (Japanese Patent Application No. 3-85952).
See.

Anisole, also known as methyldiphenyl ether, can be obtained by methods well known to those skilled in the art and is commercially available. Although anisole is preferred for this embodiment of the invention, alternatives to anisole include the formula:

[Chemical 19] (In the formula, R ¹¹ is an alkyl group having 1 to 10 carbon atoms, R ¹² is hydrogen, and R ¹³ and R ¹⁴ are each hydrogen or an alkyl group having 1 to 10 carbon atoms. A group).

Diphenyl ether and biphenyl can be obtained by methods well known to those skilled in the art and are commercially available. In this embodiment of the invention diphenyl ether (C ₆ H ₅ OC ₆ H ₅ ) and biphenyl (C ₆ H ₅ C
₆ H ₅ ) is preferred, but those that can substitute for diphenyl ether and biphenyl include those of the formula

[Chemical 20] (In the formula, R ¹ is

[Chemical 21] And R ² , R ³ , R ⁴ , R ⁵ , R ⁶ and R ⁷ are each hydrogen or an alkyl group having 1 to 24 carbon atoms). R
² , R ³ , R ⁴ , R ⁵ , R ⁶ and R ⁷ preferably contain not more than 10 carbon atoms. R ² , R ³ , R
^At least one of ⁴ , R ⁵ , R ⁶ or R ⁷ is H.

The oligomerization of linear olefins can be carried out according to the general formula

[Chemical formula 22] (In the formula, n represents the number of moles of the monomer, and m represents the number of carbon atoms in the monomer). For example, the oligomerization of 1-decene has the formula

[Chemical formula 23] Can be shown as.

The reactions occur sequentially. First, olefin monomers react with each other to form a dimer. next,
The dimer formed reacts with additional olefin monomer to form a trimer and the reaction proceeds in the same manner. This results in a distribution of oligomer products that changes with reaction time. As the reaction time increases, the conversion of olefin monomer increases and the selectivity to heavier oligomers increases. Generally, the resulting oligomers each have one double bond.

Monoalkylation of diphenyl ether, anisole and biphenyl with linear olefins is carried out according to the formulas

[Chemical formula 24] (Where m is the number of carbon atoms in the olefin monomer). Depending on the molar ratio of linear olefin: diphenyl ether, anisole and / or biphenyl and the reaction conditions, polyalkylation of diphenyl ether, anisole and / or biphenyl will occur as well. Alkylation of diphenyl ether, anisole and / or biphenyl with a linear olefin feed occurs simultaneously with the oligomerization of the olefin feed. Thus, this co-reaction results in oligomers (dimers, trimers, tetramers, etc.) with alkylated diphenyl ethers, alkylated anisole and / or alkylated biphenyls such as mono-, di- and tri-alkylated diphenyl ethers, anisole and / or A mixture with biphenyl is obtained. The number of carbon atoms in the alkyl group of the alkylated diphenyl ether, anisole and / or biphenyl should match the number of carbon atoms in the linear olefin feed. Therefore,
The alkyl group of the alkylated diphenyl ether, anisole and / or biphenyl will have 10 to 24 carbon atoms.

A catalyst useful in carrying out these reactions is silica-alumina clay, also called aluminosilicate. Silica-alumina clays consist primarily of silicon, aluminum and oxygen, with occasional minor amounts of magnesium and iron. Differences in the proportions of these components and differences in their crystal lattice shapes have produced as many as 50 different clays, each with its own properties.

One class of silica-alumina clays is the smectite clays, which have small particle size and unique intercalation properties, resulting in large surface areas. The smectites are composed of laminar planes in which octahedral sites are coordinated between the faces of tetrahedral sites, and the interlayer distance can be adjusted by expanding with an appropriate solvent. Three
Layered smectites include montmorillonite.
The structure of montmorillonite has the formula

[Chemical 25] Where M is an interlamellar balanced cation, usually sodium or lithium; x, y and n are numbers.
Can be shown by

Montmorillonite clay can be acid activated with mineral acids such as sulfuric acid and hydrochloric acid. Mineral acid
It activates montmorillonite by attacking and solubilizing structural cations in the octahedral layer. This opens up the clay structure and increases the surface area. These acid-treated clays act as strong Bronsted acids. It has been found that certain acid-treated montmorillonite clay catalysts are particularly effective in producing synthetic lube feedstocks in good yield by oligomerizing long chain olefins. These clays are acidic calcium-montmorillonite clays with a water content of up to 20% by weight, a residual acidity of 3 to 30 mg KOH / g (by titration up to the end of phenolphthalein) and a surface area of 30 m ² / g or more.
A typical example contains 8.5% KOH containing 12% by weight of water.
exhibits a residual acidity of / g and has a surface area of 425 m ² / g,
Filtrol grade 24; containing 2% by weight water;
Filtrol grade 124, showing a residual acidity of 0 mg KOH / g, having a surface area of 400 m ² / g; containing 16% by weight of water, showing a residual acidity of 15 mg KOH / g, 300 m ² / g
Filtrol grade 13 with a surface area of 4; containing 4% by weight of water, showing a residual acidity of 10 mg KOH / g, 30
There is Filtrol grade 113, which has a surface area of 0 m ² / g; and Filtrol grade 224, which is virtually free of water, shows a residual acidity of 3.0 mg KOH / g and has a surface area of 350 m ² / g.

The clay catalyst is preferably activated by heat treatment before carrying out the co-reaction. It has been found that heat treating the catalyst prior to carrying out the oligomerization reaction makes the catalyst more active, resulting in higher olefin conversion. Furthermore, the clay thus heat treated is more stable and remains active during the reaction for a longer period of time. The clay can be heat treated at 50-400 ° C, whether or not vacuum is used. A more preferable temperature range is 50 to 300 ° C. Optionally, an inert gas may be used during the heat treatment. Preferably, the clay should be heat treated under conditions and for a time period that reduces the water content of the clay to less than about 1% by weight. Alternatively, the clay may be activated with a Lewis acid.
See our earlier application (Japanese Patent Application No. 3-85952).

The oligomerization / alkylation co-reaction can be carried out in either a stirred slurry reactor or a fixed bed continuous flow reactor. The catalyst should be in a concentration sufficient to produce the desired catalytic effect. The temperature for carrying out the oligomerization and the alkylation is generally 50 to 300 ° C, preferably 150 to 180 ° C. The reaction is 0.1 to 7 MPa (0 to 1,000 psig)
Can be implemented in.

Following the oligomerization / alkylation co-reaction, the partially unsaturated oligomer is completely reduced by catalytic hydrogenation. Depending on the hydrogenation conditions used, alkylated diphenyl ether, alkylated anisole and / or
Alternatively, the alkylated biphenyl may be wholly or partially reduced and, if desired, may remain in aromatic form. It is preferable to reduce completely. Hydrogenation of oligomers and alkylated anisole, alkylated diphenyl ethers and / or alkylated biphenyls improves their thermal stability and has the effect of preventing oxidative degradation during the use of the mixture as a lubricating oil. The hydrogenation reaction for the 1-decene oligomer is
formula

[Chemical formula 26] Where n is the number of moles of monomer used to form the oligomer.
Complete hydrogenation of mono-alkylated diphenyl ether, mono-alkylated anisole or mono-alkylated biphenyl is described by the formula

[Chemical 27] Can be shown by

Hydrogenation methods known to those skilled in the art can be used. Many metal catalysts are suitable for promoting the hydrogenation reaction, including nickel, platinum, palladium, copper and Raney nickel. These metals may be supported on a wide variety of porous materials such as diatomaceous earth, alumina or charcoal. A particularly preferred catalyst for this hydrogenation is
The nickel / copper / chromium oxide catalyst described in US Pat. No. 3,152,998. Other known hydrogenation processes are described in US Pat. Nos. 4,045,508, 4,01
No. 3,736, No. 3,997,621 and No. 3,99
No. 7,622. The hydrogenation conditions described in the examples below can be used to reduce the double bonds of both the oligomer and the alkylated anisole, alkylated diphenyl ether and / or alkylated biphenyl. To reduce only the oligomer,
For example, while using 0.5% palladium on alumina catalyst (10% by weight based on the charged raw material), pressurize to 3.5 MPa (500 psig) with hydrogen, and
Heat to ℃, 4MPa for 7 hours with hydrogen if necessary
Less vigorous conditions should be used, such as repressurization to (1,000 psig).

Unreacted monomer and anisole, diphenyl ether and / or biphenyl should be removed before or after hydrogenation. Optionally, unreacted monomer and anisole, diphenyl ether and / or biphenyl are stripped from the oligomer / alkylated diphenyl ether, alkylated anisole and / or alkylated biphenyl prior to hydrogenation and recycled to the co-reacted catalyst bed. May be. Unreacted alkanes and unalkylated dicyclohexyl ethers and / or unalkylated vinyls, if after removal or recycling of unreacted monomers and anisole, diphenyl ethers and / or biphenyls, or hydrogenation. Removal of cyclohexyl should be carried out under mild conditions using vacuum distillation methods known to those skilled in the art. Distillation at temperatures above 250 ° C may decompose the oligomer in some way and separate it as volatiles. Therefore, the temperature of the reboiler or kettle is preferably 255 ° C or lower, most preferably 18 ° C.
It should be kept below 0 ° C. Alternatives to vacuum distillation, techniques known to those skilled in the art may be used to separate unreacted components from the mixture.

After the hydrogenation procedure, including the distillation step, 100
Although it is known to obtain products with different viscosities at 0 ° C., in the process of the invention further distillation (removal of unreacted monomers / linear alkanes and diphenyl ether / dicyclohexyl ether and / or biphenyl / alkylated bicyclohexyl (Other than what you do)
Is not preferred. Thus, the process of the present invention does not require expensive and customary distillation steps, yet surprisingly yields a synthetic lubricating oil component having excellent properties and acting in a great way. However, in some cases, one skilled in the art may find that subsequent distillation is useful in the practice of the present invention.

[0036]

The present invention will be further described by the following examples.

Procedure The reactants and clay catalyst were charged to a three neck flask equipped with an overhead stirrer, heating mantle and nitrogen purge. The mixture was vigorously stirred and heated at the desired temperature for the desired time. At the end of the reaction, the mixture was cooled to ambient temperature and filtered by suction. Olefin conversion and dimer / trimer ratios were determined by liquid chromatography and recorded in the table below.

An autoclave was charged with nickel catalyst (5% by weight) and the mixture prepared as described above. The autoclave was then sealed and flushed with hydrogen three or four times. Next, the autoclave was hydrogenated to 7MP.
Pressurized to a (1,000 psig) and heated to 200 ° C. The mixture was stirred at this temperature for 4.0 hours. If necessary, re-autoclave again 13.7MPa (2,000ps
ig). The mixture was then cooled to ambient temperature and filtered. And about 133Pa (1mmHg)
The unreacted monomer was removed from the filtrate under reduced pressure. The properties shown in the table are measured on "striped" bottom product.

[0039]

[Table 1]

[0040]

[Table 2]

─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. ⁶ Identification code Internal reference number FI Technical indication C10M 129: 16) (C10M 109/02 105: 04 105: 16 105: 18) C10N 30:02 40 : 04 40:25 60:02 70:00 (72) Inventor Edward Thomas Marquis Texas 78758, Austin, Colinfield Drive 9004

Claims (10)

[Claims] 1. A synthetic lubricating oil feedstock comprising an oligomer produced from an olefin composition comprising a linear olefin having 10 to 24 carbon atoms, having the formula: (In the formula, R ¹ is represented by the formula: A group represented by; R ² , R ³ , R ⁴ , R ⁵ ,
At least one of R ⁶ and R ⁷ is 10 to 24.
R is an alkyl group having 1 to 10 carbon atoms; R is H or an alkyl group having 1 to 24 carbon atoms; R ¹¹ is an alkyl group having 1 to 10 carbon atoms; ¹² is an alkyl group having 10 to 24 carbon atoms; R ¹³ and R ¹⁴ are each H or 1
A synthetic lubricating oil feedstock further comprising an alkyl-substituted biphenyl, diphenyl ether or anisole, represented by an alkyl group having up to 0 carbon atoms. 2. A synthetic lubricating oil feedstock comprising a reduced oligomer prepared from an olefin composition comprising a linear olefin having 10 to 24 carbon atoms, the formula (A): (In the formula, R ¹ is represented by the formula: And the formula (B) (In the formula, R ¹ is represented by the formula: Or formula (C) Wherein R ^{2 to} R ⁷ and R ^{11 to} R ¹⁴ have the same meanings as defined in claim 1 and further comprise an alkyl-substituted aromatic or cycloaliphatic compound. Lubricating oil raw material. 3. The linear olefin comprises an α-olefin, an internal olefin or a mixture thereof.
The described synthetic lubricating oil raw material. 4. The synthetic lubricating oil feedstock according to claim 1, wherein the olefin composition comprises the linear olefin and up to 20% by weight of propylene. 5. Synthetic lubrication according to claim 1, wherein the olefin composition comprises the linear olefin and up to 20% by weight of 1,3-diisopropenylbenzene or α-methylstyrene. Oil raw material. 6. The synthetic lubricating oil feedstock according to claim 1, wherein the olefin composition comprises the linear olefin and a vinylidene olefin having 10 to 24 carbon atoms. 7. The synthetic lubricating oil feedstock according to claim 6, wherein the olefin composition comprises 5 to 40% by weight of vinylidene olefin. 8. A method for producing a synthetic lubricating oil feedstock according to any one of claims 1 and 3 to 7 by contacting the olefin composition with an acidic montmorillonite clay, the method comprising: [Chemical 8] (In the formula, R ¹ is represented by the formula: R ^{2 to} R ⁷ have the same meaning as defined in claim 1 if at least one of them is hydrogen; R ¹¹ is 1 to 10 carbon atoms. R ¹² is hydrogen; R ¹³ and R ¹⁴ are each hydrogen or an alkyl group having 1 to 10 carbon atoms), alkyl-substituted biphenyl, diphenyl ether or A manufacturing method characterized by reacting with anisole. 9. The method according to claim 8, wherein the clay is activated by a Lewis acid. 10. A method for producing the synthetic lubricating oil feedstock according to claim 2, wherein the synthetic lubricating oil feedstock according to claim 1 is wholly or partially hydrogenated.