CA2185400C

CA2185400C - Production of monoolefin oligomer

Info

Publication number: CA2185400C
Application number: CA002185400A
Authority: CA
Inventors: Michel Clarembeau
Original assignee: Ineos USA LLC
Current assignee: Ineos USA LLC
Priority date: 1995-09-13
Filing date: 1996-09-12
Publication date: 2008-07-15
Anticipated expiration: 2016-09-12
Also published as: EP0763514A1; DE69511548D1; US6002061A; EP0763514B1; CA2185400A1; DE69511548T2

Abstract

A monoolefin oligomerization process which gives high yields of dimer and trimer at high monoolefin conversions in a single stage reaction is described. The process involves contacting a C6-20 oligomerizable olefin with a catalyst comprising boron trifluoride and from 0.05 to 2.5 mol%, based on the total quantity of monoolefin being used, of an alcohol catalyst promoter which is added portionwise during the oligo-merization.
The oligomerization is performed at a temperature of 45-90°C and under a pressurized atmosphere of boron trifluoride until the monoolefin conversion is at least 90% and the combined total of dimer and trimer in the liquid reaction mixture is at least 70% by weight.

Description

PRODUCTION OF MONQ L~ ~E " OLIGOMER
BACKGROUND
It is known to produce monoolefm oligomers by use of boron trifluoride as the catalyst together with a co-catalyst component. A variety of co-catalysts have been proposed for this use including water, alcohols, ethers, esters, aldehydes, ketones, and acid anhydrides. Oligomers produced in this manner are useful in the production of synthetic lubricating oils of' different: viscosities. Typically the production of such products, often referred to as PAOs, involves oligomer fractionation, hydrogenation and back blending to achieve desired properties. Usually the dimers and trimers, especially those of 1-decene, are of greatest utility in the production of low viscosity PAOs for various end use applications.
U.S. Pat. No. 4,045,507 to Cupples, et al. describes a multi-stage process for oligomerizing 1-decene which includes use of a series of two or more tank type reactors.
The patentees found that the trimer to tetramer ratio decreases with increasing 1-decene conversion in both stages of' a two-stage operation, and that this ratio is higher in the second and succeeding reactors. Thus the process described in the patent operates at low conversion in the first stage and at higher conversions in succeeding stages of the process. The patent shows in Examples 5 and 6 of Table I that at 1-decene conversions of 83.4 % and 90. 5%, the amount of dimer in the product was only 5.2 % and 3.8 Ro , re-spectively. In addition, the combined total of dimer and trimer in the products was 47.8% at 83.4% conversion and 38.9% at 90.5% conversion.
To satisfy commercial requirements, it would be highly desirable to provide a single stage process which can be operated at high olefm conversions (e.g., above 90%) and which can produce a reaction mix.ture containing a combined total of dimer and tri-mer above 70%, and in which at least 20% (preferably at least 30% and more preferably at least 40%) of the reaction rraixture is dimer. "1'his invention makes it possible to achieve all of these goals.

THE INVENTION
In accordance with this invention the oligomerization only requires a single stage reaction using one reactor. In addition, although operated at 1-olefin conversions above 90%, the oligomerization process of this invention gives substantially higher total yields of dimer and trimer than the yields achieved in U.S. Pat. No. 4,045,507 at high conver-sions. Moreover, by operating in accordance with preferred embodiments of this inven-tion, the amount of dimer present in the reaction mixture can be above 40%.
And all of these advantages can be accomplished while at the same time conducting the oligo-merization reaction under commercially attractive reaction conditions.
Provided by this invention is a monoolefm oligomerization process which com-prises contacting an oligomerizable tnonoolefan having in the range of 6 to 20 carbon atoms per molecule with a catalyst comprising boron trifluoride and a total in the range of from 0.05 to 2.5 mol%, based on the mols of monoolefm used, of an alcohol catalyst promoter introduced portionwise during the conduct of the oligomerization, at an oligo-merization temperature of 45-90 C, and under a pressurized atmosphere of boron tri-fluoride in the range of 1 to 4 bars gauge until the monoolefm conversion is at least 90 %
and the combined total of dimer and trimer in the liquid reaction mixture is at least 70%.
In this connection, all percentages pertaining to product composition set forth in the specification and claims hereof are in terms of area percentages by gas chromatography conducted using a Hewlett Packard Model HF'5890 BerieII gas chromatograph fitted with a Chrompack 60 cm Dexil 300 GC column operated under the following conditions:
Injector temperature: 350 C
Detector temperature: 350 C
Oven initial t:emperature : 70 C
Oven fina.it temperature: 350 C
Oven temperature gradient: 10 C/min.
In a preferred embodiment this process is conducted with a linear a-monoolefm having in the range of 8 to 12 carbon atoms per molecule. It is also preferred to conduct the process at an oligomerization temperature of 60-80 C until (a) the monoolefm conversion is at least 92%, (b) the combined total of dimer and tritner in the liquid reaction mixture is at least 70%, and (c) the liquid reaction mixture contains at least 40% of dimer.

With suitable agitation of the reaction mixture (e.g., mechanical stirring with an input of from 50 to 500 W/m' and preferably from 75 to 425 W/m'), reaction proceeds at a highly satisfactory rate under the foregoing conditions. Thus reaction periods in the range of two to three hours will often suffice.
Reaction product composition can be monitored by subjecting periodically-taken samples to gas chromatographic analysis. Once the desired product composition has been achieved, the reaction mixture is quenched with water to terminate the oligomerization.
As indicated above, the alcohol catalyst promoter is introduced into the reaction system on a portionwise basis, and at least 20% (preferably at least 40%, more prefer-ably at least 60%, and most preferably at least 80%) of the total amount of the alcohol promoter is introduced into the reactor containing the monoolefm and the pressurized atmosphere of boron trifluoride as the oligomerization reaction proceeds. The balance, if any, of the alcohol promoter is charged to the reactor before commencing the oligo-merization reaction. The portionwise feed can be conducted by feeding portions of the total alcohol charge as a series of individual increments over a period of time. In this case the alcohol is caused to enter the system as a discontinuous series of small additions until the preselected amount to be used pursuant to this invention has been introduced into the oligomerization mixture. Alternatively, and preferably, the feed of the alcohol to the oligomerization mixture is conducted slowly and continuously until the total selected amount of the alcohol has been added. In either case the alcohol feed rates should be from 0. 8 to 4 parts by weight of alcohol per 1000 parts by weight of olefm per hour, preferably from 1 to 3 parts by weight of alcohol per 1000 parts by weight of olefm per hour, and most preferably from 2 to 2.6 parts by weight of alcohol per 1000 parts by weight of olefm per hour.
Preferably, the amount of alcohol catalyst promoter used is in the range of from 0.1 to 1.5 mol%, based on the mols of oligomerizable monoolefm used in the reaction.
A further important advantage of this invention is the fact that after stripping off the unreacted monomer and recovering the dimer and trimer fractions by distillation, the distillation bottoms represent a highly useful co-product. Upon hydrogenation of these bottoms, products having desirable properties for use as lubricant blending stocks can be produced.

The monoolefms used in the process are preferably vinyl olefms ranging from 1-hexene to 1-eicosene. However oligomerizable C6 to C20 internal olefins can also be used in the process. Likewise, mixtures of one or more such internal olefins with one or more vinyl olefins can be used. "T'he vinyl olefin is either a straight chain olefm (no branching) or a remotely-branched olefin such that the terminal double bond is unhin-dered sterically. Mixtures of such monoolefms can also be used. However, preferably such mixtures are substantially devoid of vinylidene olefins. Preferred linear monoole-fms are those having from 8 to 12 carbon atoms. The most preferred monoolefm is 1-decene.
Alcohol promoters that can be 'used include alkanols having up to about 18 carbon atoms, and preferably up to about 12 carbon atoms, such as, for example, ethanol, 2-propanol, n-butanol, 2-methylpropanol, n-hexanol, n-heptanol, n-octanol, 2-ethylhexanol and n-decanol. More preferably, the alcohol used has up to 6 carbon atoms. The most preferred alcohol is n-butanol. Diols and other polyols can be used, but are less preferred.
Temperatures used in the process are normally in the range of from 45 to 90 C, and preferably from 60 to 80 C.
The boron trifluoride atinosphere within the reactor is typically maintained at a gauge pressure within the range of 1 to 4 bazs including 0.05 to 1.5 bars of nitrogen.
A preferred pressure range is from 2.5 to 3.5 bars gauge with 1 bar (gauge) of nitrogen.
To terminate the oligomerization reaction when the preselected olefm conversion has been achieved, the reaction mixture is preferably quenched with water or any suitable aqueous solution. Unreacted olefin can be recovered and recycled to an ensuing reaction.
For most uses, the recovered oligomer fractions are normally subjected to catalytic hydrogenation under reaction conditions well-known to those skilled in the art.
The following non-limiting examples illustrate the practice and advantages of this invention.

Oligomerization of 1-decene is conducted using a 2-liter stainless steel pressure reactor equipped with an external electrical heating mande, a mechanical stirrer, a cooling coil, a thermocouple sensor, a liquid sampling tube, a rupture disk, a nitrogen inlet, a BF3 inlet and a liquid reactant inlet valve. Charged to the reactor are 1200 g of 1-decene and 0.5 g of 1-butanol. T'he system is purged with nitrogen and then put under a nitrogen blanket (0.1 bar gauge). "1 he temperature of this mixture is maintained at 70 C by suitably regulating the electrical in,put. of the heating mantle and the flow of cold water througb the cooling coil. "To this mixture is added 0.05 g of 1-butanol diluted in 1 mL of 1-decene. Then, the system is pressurized at 1.4 bars gauge with boron trifluo-ride. After 30 minutes of stirring at 70 C, 0.4 g of 1-butanol diluted in 1 mL
of 1-decene is added to the reaction mixture. After 60 minutes from the pressurization with boron trifluoride -- during which titne the oligomerization mixture is continuously stirred, and maintained at 70 C under a boron trifluoride pressure of 1.4 bars (gauge) -- the re-action mixture is quenched with 100 mi. of water and the temperature of the system is raised to 80 C and maintained at this temperature for l hour. Then the reactor contents are transferred to a separatory funnel to separate the organic and aqueous phases. The organic product mixture is then repeatedly washed with additional separate quantities of water until the water phase used shows no acidity. An organic reaction product formed in this manner was shown by gas chromatography to contain the product distribution (in area percentages which are approximately equal to weight percentages) given in Table 1:
Table 1 Components Area by Gas Chromatography Unreacted monomer 3 Dimer 49 Trimer 27 Tetramer 19 Pentamer 2 Hexamer 0 Oligomerization of 19600 kg of 1-decene is conduced under 2.7 bars gauge of catalyst and using 1.14 mol % of 1-butanol based on the 1-decene charged. The butanol is added at a continuous rate of 601cg per hour. Reaction temperature is maintained at 70 C. After a total time of 2 hours, the reaction is terminated by quenching the product mixture with water. The typical composition of the reaction mixture formed in this manner is as shown in Table 2.

Table 2 Components Area by Gas Chromatography Unreacted monomer 5 D'uner 42 Trimer 37 Tetramer 12 Pentamer 4 Hexamer 0 The reaction product mixture from Example 2 is distilled in a 6-tray Oldershaw column operated under a vacuum of 3-5 mm Hg. After stripping off the unreacted monomer, a dimer-enriched cut boiling in the range of 130-190 C is collected.
This dimer fraction is then hydrogenated using a nickel ca.talyst supported on alumina.
Typical properties of such hydrogenated dimer fraction are as shown in Table 3.

Table 3 Property Measured Value Kinematic viscosity at 100 C 1.81 cSt (m'/s) Kinematic viscosity at 40 C 5.58 cSt (m2/s) Kinematic viscosity at -40 C 308 cSt ('-/s) Pour point -68 C

Flash point 155 C

The distillation bottoms remaining from the distillation conducted according to Example 3 are subjected to hydrogenation using a nickel catalyst supported on alumina.
Table 4 gives typical properties for the resultant hydrogenated heavy oligomer.

Table 4 Property Measured Value Kinematic viscosity at 100 C 4.46 cSt (mz/s) Kinematic viscosity at 40 C: 21.4 cSt (m2/s) Kinematic viscosity at -40 C 4445 cSt (m2/s) Viscosity index 122 The oligomerization procedure of Example 2 is repeated under the same conditions except that the temperature is maintained at 50 C:. The composition of a typical product mixture formed in this manner is shown in Table 5.

Table 5 Components Area by Gas Chromatography Unreacted monomer 6 Dimer 26 Trimer 50 Tetramer 13 Pentamer 5 Hexamer 0 EX,AbET.E 6 The reaction product mixture from Example 5 is distilled as in Example 3 to yield a dimer fraction having the properties set forth in Table 6.

Table 6 Property Measured Value Kinematic viscosity at 100 C 1.70 cSt (m=/s) Kinematic viscosity at 40 C 5.10 cSt (m2/s) Kinematic viscosity at .-40 C 233 cSt (mz/s) Pour point -75 C

Flash point 158 C

The distillation bottoms remaining from the distillation conducted as in Example 6 are subjected to hydrogenation using a nickel catalyst supported on alumina.
Table 7 gives typical properties of the resultant hydrogenated oligomer.

Table 7 [_Property Measured Value Kinematic viscosity at 100 C 4.50 cSt (m=/s) Kinematic viscosity at 40 C 21.6 cSt (m'-/s) Kinematic viscosity at -40 C 4175 cSt (m2/s) Viscosity index 124 COMPARATn F~7 EXAMrr E A
When an operation is conducted as described in the example of U.S. Pat. No.
4,950,822 wherein, inter alia, the butanol is used at a concentration of 1.14 mol%, the results were as shown in the following table:

Components Wt. %, by Gas Chromatography Unreacted monomer I

Dimer 2 Trimer 45 Tetramer 32 Pentamer 16 Hexamer 4

Claims

1. A one-stage monoolefin oligomerization process which comprises:
a) contacting in a vinyl monoolefin having in the range of 6 to 20 carbon atoms per molecule with a catalyst comprising boron trifluoride and in the range of from 0.05 to 2.5 mol%, based on the total quantity of olefin being used, of an alcohol catalyst promoter introduced portionwise during the conduct of the oligomerization, at an oligomerization temperature of 60-80°C and under a pressurized atmosphere of boron trifluoride in the range of 1 to 4 bars gauge;
b) monitoring the reactor composition as the reaction proceeds; and c) terminating the reaction when the olefin conversion is at least 92% by weight and the combined total of dimer and trimer in the liquid reaction mixture is at least 70% by weight, and the liquid reaction mixture produced contains at least 40%
by weight of dimer.

2. A process according to claim 1 wherein the monoolefin comprises linear .alpha.-monoolefin.

3. A process according to claim 2 wherein the linear .alpha.-monoolefin has in the range of 8 to 12 carbon atoms per molecule.

4. A process according to claim 3 wherein the linear .alpha.-monoolefin is 1-decene.

5. A process according to claim 1 wherein the temperature is maintained at about 70°C throughout substantially the entire oligomerization.

6. A process according to claim 1 wherein alcohol promoter is introduced into the mixture continuously at a rate equivalent to from 0.8 to 4 parts by weight per 1000 parts by weight of olefin per hour commencing at about the start of the reaction.

7. A process according to claim 6 wherein said rate is equivalent to from 1 to parts by weight per 1000 parts of olefin per hour.

8. A process according to claim 6 wherein the alcohol promoter is 1-butanol.

9. A process according to claim 1 wherein the reaction period is in the range of two to three hours.

10. A process according to claim 1 wherein the oligomerization reaction is terminated by quenching the reaction mixture with water or an aqueous solution.

11. A process according to claim 1 wherein the amount of alcohol catalyst promoter used is in the range of from 0.1 to 1.5 mol%, based on the mols of oligomerizable monoolefin used in the reaction.

12. A process according to claim 1 wherein the liquid reaction mixture is distilled at reduced pressure to (i) strip off unreacted monomer; (ii) recover a dimer-enriched distillate fraction, and (iii) provide distillation bottoms; and wherein said distillate fraction and said distillation bottoms are separately hydrogenated.

13. A hydrogenated dimer-enriched distillate fraction produced according to claim 12.

14. Hydrogenated distillate bottoms produced according to claim 12.