A production process of polyalphaolefin

Abstract

The present invention provides a production process of poly alpha-olefin, comprising the following steps: S1. a first raw material system comprising a first alpha-olefin and a first solvent is contacted with a metallocene catalyst, so that the first alpha-olefin undergoes a first polymerization reaction to obtain a first polymerization product; S2. the first polymerization product is contacted with a second raw material system comprising a second solvent and optionally a second alpha-olefin, so that a second polymerization reaction occurs to obtain a second polymerization product comprising the poly alpha-olefin, wherein the second raw material system does not contain a catalyst for catalyzing olefin polymerization. The production process can effectively adjust the viscosity of the poly alpha-olefin to meet the needs of different products.

Description

Technical Field

[0001] The present invention relates to the technical field of poly-alpha-olefin production, and in particular to a poly-alpha-olefin production process. Background Art

[0002] Catalytic oligomerization of olefins is a known technique for preparing hydrocarbon base stocks for use as lubricants. Improving the performance of natural mineral oil-based lubricants by synthesizing oligomeric hydrocarbon fluids has been an important research and development topic in the oil industry for decades, leading to the recent large-scale production of many advanced polyalphaolefin synthetic lubricants (hereinafter referred to as "PAO"). These materials are mainly based on C6-C 12 Oligomerization of olefins such as alpha olefins. Industrial research devoted to synthetic lubricants has generally been focused on fluids that exhibit useful viscosity, i.e., improved viscosity index (VI), over a wide temperature range while also exhibiting better or comparable lubricity, thermal and oxidative stability, and pour point than mineral oils. These newer synthetic lubricants provide lower friction and thus improved mechanical efficiency throughout the entire range of mechanical loads and do so over a wider range of operating conditions than mineral oil lubricants.

[0003] Metallocene polyalphaolefin (mPAO) is a product with a comb-like structure and no upright side chains obtained by polymerizing alpha-olefins catalyzed by metallocene catalysts. This structure affects the performance of PAO products. Compared with traditional PAO, mPAO usually has improved rheological properties and flow characteristics, and can provide better shear stability, lower pour point and higher viscosity index, and has good viscosity-temperature characteristics. These characteristics determine that mPAO can be used in highly harsh environments, including powertrain and gear oils, compressor lubricants, transmission fluids and industrial lubricants. As society's requirements for energy utilization and ecological protection become increasingly higher, people's demand for high-performance mPAO lubricant base oils is increasing.

[0004] Metallocene compounds generally refer to a class of organic metal complexes composed of transition metal elements (such as Group IV B elements titanium, zirconium, hafnium) or rare earth metal elements and at least one cyclopentadiene or cyclopentadiene derivative as a ligand. Metallocene catalysts are generally considered to be third-generation PAO catalysts. Generally, metallocene catalysts catalyze the polymerization of α-olefins to easily obtain high-viscosity PAOs (kinematic viscosity at 100°C is above 40 cSt), while the preparation of low-viscosity (kinematic viscosity at 100°C is below 20 cSt) metallocene PAOs requires the additional addition of molecular weight regulators, such as hydrogen, organic metal compounds, etc. The addition of hydrogen can easily cause the raw materials to be saturated, and the regulation of organic metal compounds can easily increase the cost and complexity of the process. For this reason, it is necessary to find an economical method for regulating the viscosity of metallocene PAOs. Summary of the invention

[0005] In view of the above problems existing in the prior art, one of the objectives of the present invention is to provide a production process of poly-α-olefins. The production process provided by the present invention can effectively adjust the viscosity of metallocene poly-α-olefins.

[0006] A second object of the present invention is to provide a poly-α-olefin corresponding to the first object.

[0007] To achieve one of the above purposes, the technical solution adopted by the present invention is as follows:

[0008] A production process for poly-alpha-olefins comprises the following steps:

[0009] S1. contacting a first raw material system comprising a first α-olefin and a first solvent with a metallocene catalyst, thereby causing a first polymerization reaction of the first α-olefin to obtain a first polymerization product;

[0010] S2. contacting the first polymerization product with a second raw material system comprising a second solvent and optionally a second α-olefin, thereby causing a second polymerization reaction to obtain a second polymerization product comprising the poly-α-olefin,

[0011] Wherein, the second raw material system does not contain a catalyst for catalyzing olefin polymerization.

[0012] According to the present invention, no fresh catalyst for catalyzing olefin polymerization, such as a metallocene catalyst, is introduced in step S2.

[0013] According to the present invention, the first polymerization product includes a polymerization product of a first α-olefin, a first solvent and a metallocene catalyst.

[0014] The inventors of the present application have found through research that by introducing the first polymerization product into a system without a catalyst to continue the polymerization reaction, the viscosity of the obtained poly-α-olefin can be adjusted by utilizing the change in the concentration and existence state of the active center of the catalyst.

[0015] According to some embodiments of the present invention, poly-α-olefins with different viscosities are obtained by controlling the reaction time and / or the reaction temperature of the first polymerization reaction and / or the concentration of the second α-olefin in the second raw material system.

[0016] By adjusting the process conditions (such as reaction time, reaction temperature and monomer dosage) of the first polymerization reaction and the second polymerization reaction, the polymerization degree of the obtained poly-α-olefin can be effectively adjusted. For example, the poly-α-olefin with a desired viscosity can be obtained by adjusting the reaction time of the first polymerization reaction and the dosage of the α-olefin in the second polymerization reaction. In this case, the different reaction times in the first polymerization reaction cause different concentrations and existence states of the active centers of the catalyst, and the different concentrations of the α-olefin in the second polymerization reaction, which ultimately have a comprehensive impact on the viscosity of the product poly-α-olefin.

[0017] According to some embodiments of the present invention, in step S2, isopropanol may be used as a terminator to terminate the second polymerization reaction.

[0018] According to some embodiments of the present invention, after the second polymerization reaction is completed, unreacted monomers and oligomerization products can be removed by filtering and distilling under reduced pressure to obtain the final product poly-α-olefin.

[0019] According to some embodiments of the present invention, the filtration and reduced pressure distillation are conventional operations in the art, and the specific operation methods are not repeated here.

[0020] According to some embodiments of the present invention, the above preparation method can be carried out under an inert atmosphere, for example, under a nitrogen atmosphere.

[0021] In some preferred embodiments of the present invention, the temperature of the first raw material system and the second raw material system is the same, which is 30°C to 190°C, preferably 80°C to 170°C.

[0022] In some preferred embodiments of the present invention, the temperature of the first polymerization reaction is the same as the temperature of the second polymerization reaction, which is 30°C to 190°C, preferably 80°C to 170°C.

[0023] In some preferred embodiments of the present invention, the temperature of the first raw material system is the same as the temperature of the first polymerization reaction.

[0024] In some preferred embodiments of the present invention, the time of the first polymerization reaction is 1 min to 120 min, preferably 1 min to 60 min.

[0025] According to the present invention, the time of the first polymerization reaction can be listed as 1 min, 5 min, 10 min, 15 min, 20 min, 25 min, 30 min, 35 min, 40 min, 45 min, 50 min, 55 min, 60 min, 65 min, 70 min, 75 min, 80 min, 85 min, 90 min, 100 min, 110 min, 120 min and any value therebetween.

[0026] According to the present invention, the properties of the polymerized product, such as viscosity, can be adjusted by adjusting the time of the first polymerization reaction.

[0027] In some preferred embodiments of the present invention, the second polymerization reaction time is 0.1 h to 10 h, preferably 0.5 h to 5 h.

[0028] In some preferred embodiments of the present invention, the amount of the first solvent used is 1 mL to 1000 mL, preferably 1 mL to 100 mL, per gram of the first α-olefin.

[0029] In some preferred embodiments of the present invention, the amount of the second α-olefin used is 0 g to 10 g, preferably 0 g to 5 g, per gram of the first α-olefin.

[0030] According to the present invention, the second raw material system may contain only solvent but no α-olefin.

[0031] According to the present invention, the properties of the polymer product, such as viscosity, can be adjusted by adjusting the amount of the second α-olefin.

[0032] In some preferred embodiments of the present invention, the amount of the second solvent used is 1 mL to 1000 mL, preferably 1 mL to 100 mL, per gram of the first α-olefin.

[0033] In some preferred embodiments of the present invention, the metallocene catalyst comprises a metallocene compound and an activator.

[0034] Wherein, the metallocene compound is selected from dimethylsilylbis-n-propylcyclopentadienyl zirconium dichloride, dimethylsilylbis-indenyl zirconium dichloride, diethylsilylbis-indenyl zirconium dichloride, diphenylsilylbis(4,7-dimethylindenyl) zirconium dichloride, dimethylsilylbis(4,7-dimethylindenyl) zirconium dichloride, dimethylsilylbis-indenyl zirconium dichloride, diphenylsilylbis(2-methylcyclopentadienyl) zirconium dichloride, ethylenebis-indenyl zirconium dichloride, ethylenebis-(2-methylindenyl) zirconium dichloride, dimethylsilylbis-(2-methyl-3-butylcyclopentadienyl) zirconium dichloride, dimethylsilylbis-cyclopentadienyl Zirconium dichloride, diethylmethylenecyclopentadienyl (3,5-dimethylphenylindenyl) zirconium dichloride, diethylmethylenecyclopentadienyl (4,7-dimethylindenyl) zirconium dichloride, dimethylmethylenecyclopentadienyl (4,7-dimethylindenyl) zirconium dichloride, dimethylsilylcyclopentadienyl (4,7-dimethylindenyl) zirconium dichloride, dimethylsilylcyclopentadienyl (3,5-dimethylphenylindenyl) zirconium dichloride, dimethylsilylbis (2-methylcyclopentadienyl) zirconium dichloride, dimethylsilylbis (2-methylindenyl) zirconium dichloride Zirconium, dimethylsilylbis-n-propylcyclopentadienyl hafnium dichloride, dimethylsilylbis-indenyl hafnium dichloride, diethylsilylbis-indenyl hafnium dichloride, diphenylsilylbis(4,7-dimethylindenyl) hafnium dichloride, dimethylsilylbis(4,7-dimethylindenyl) hafnium dichloride, dimethylsilylbis-indenyl hafnium dichloride, diphenylsilylbis(2-methylcyclopentadienyl) hafnium dichloride, ethylenebis-indenyl hafnium dichloride, ethylenebis(2-methylindenyl) hafnium dichloride, dimethylsilylbis(2-methyl-3-butylcyclopentadienyl) hafnium dichloride, dimethylsilylbis-cyclopentadienyl hafnium dichloride, diethylmethylene one or more of dimethylsilylcyclopentadienyl (3,5-dimethylphenylindenyl) hafnium dichloride, diethylmethylenecyclopentadienyl (4,7-dimethylindenyl) hafnium dichloride, dimethylmethylenecyclopentadienyl (4,7-dimethylindenyl) hafnium dichloride, dimethylsilylcyclopentadienyl (4,7-dimethylindenyl) hafnium dichloride, dimethylsilylcyclopentadienyl (3,5-dimethylphenylindenyl) hafnium dichloride, dimethylsilylbis (2-methylcyclopentadienyl) hafnium dichloride, dimethylsilylbis (2-methylindenyl) hafnium dichloride and dimethylsilylcyclopentadienyl (2-methylindenyl) hafnium dichloride;

[0035] The activator is selected from one or more of alkyl aluminum and borate.

[0036] In some preferred embodiments of the present invention, the general formula of the alkyl aluminum is AlR3, wherein R is C1-C 10Alkyl, more preferably, the alkylaluminum is selected from one or more of trimethylaluminum, triethylaluminum, triisopropylaluminum, tri-n-propylaluminum, triisobutylaluminum, tri-n-butylaluminum, triisopentylaluminum, tri-n-pentylaluminum, triisohexylaluminum, tri-n-hexylaluminum, triisoheptylaluminum, tri-n-heptylaluminum, triisooctylaluminum, tri-n-octylaluminum, triisononylaluminum, tri-n-nonylaluminum, triisodecylaluminum and tri-n-decylaluminum.

[0037] In some preferred embodiments of the present invention, the borate is selected from one or more of tetrakis(pentafluorophenyl)borate dimethylanilinium salt, tetrakis(pentafluorophenyl)borate diethylanilinium salt, tetrakis(pentafluorophenyl)borate dibutylanilinium salt, tetrakis(pentafluorophenyl)borate trimethylammonium salt, tetrakis(pentafluorophenyl)borate diethylammonium salt and tetrakis(pentafluorophenyl)borate tributylammonium salt.

[0038] According to some embodiments of the present invention, in the metallocene catalyst, the amounts of the metallocene compound and the activator are conventional amounts. For example, per 100 mL of the metallocene catalyst, the content of the metallocene compound may be 1 μmol to 20 μmol, the content of the alkyl aluminum may be 10 mg to 1000 mg, and the content of the borate may be 5 mg to 500 mg.

[0039] According to some embodiments of the present invention, a weight ratio of the metallocene compound, the activator and the first α-olefin is 1:(10-1000):(100-100000).

[0040] In some preferred embodiments of the present invention, the first α-olefin and the second α-olefin are the same or different, and are independently selected from one or more of 1-hexene, 1-heptene, 1-octene, 1-nonene, 1-decene, 1-undecene, 1-dodecene, 1-tridecene, 1-tetradecene, 1-pentadecene, 1-hexadecene, 1-heptadecene, 1-octadecene, 1-nonadecene and 1-eicosene.

[0041] In some preferred embodiments of the present invention, the first α-olefin and the second α-olefin are the same or different, and are independently selected from one or more of 1-butene, 1-pentene, 1-hexene, 1-heptene, 1-octene, 1-nonene, 1-decene, 1-undecene, 1-dodecene, 1-tridecene and 1-tetradecene.

[0042] In some preferred embodiments of the present invention, the first α-olefin and the second α-olefin are the same.

[0043] In some preferred embodiments of the present invention, the first solvent and the second solvent are the same or different, and are independently selected from one or more of alkanes and aromatic hydrocarbons.

[0044] In some preferred embodiments of the present invention, the first solvent and the second solvent are the same or different, and are independently selected from one or more of hexane, heptane, octane, nonane, decane, cyclohexane, benzene, toluene and xylene.

[0045] In some preferred embodiments of the present invention, the first solvent and the second solvent are the same.

[0046] In some preferred embodiments of the present invention, the preparation method is carried out in two reaction devices connected in series.

[0047] In the present invention, the term "same" may also be understood as substantially the same, for example, the difference is within 1% or even 5%. This is because the difference within 5% or even 1% has little effect on the result and can be ignored and regarded as the same.

[0048] To achieve the second purpose above, the technical solution adopted by the present invention is as follows:

[0049] A poly-α-olefin prepared according to the above preparation method, wherein the viscosity index of the poly-α-olefin is above 140; and / or the weight average molecular weight of the poly-α-olefin is 200-200000; and / or the kinematic viscosity of the poly-α-olefin at 100°C is above 3 cSt.

[0050] According to some preferred embodiments of the present invention, the kinematic viscosity of the poly-α-olefin at 100° C. is between 3 cSt and 5000 cSt.

[0051] The beneficial effects of the present invention are at least in the following aspects:

[0052] Firstly, the production process provided by the present invention is simple and easy to operate, and the viscosity of the poly-α-olefin can be effectively adjusted only by changing the process conditions.

[0053] Secondly, the preparation method provided by the present invention can prepare poly-α-olefin products with different viscosity levels to meet the needs of different occasions or products. BRIEF DESCRIPTION OF THE DRAWINGS

[0054] Figure 1 It is a process flow chart of Example 1 of the present invention. DETAILED DESCRIPTION

[0055] The present invention is described in detail below by way of examples, but the protection scope of the present invention is not limited to the following description.

[0056] If the specific conditions are not specified in the examples, the experiments were carried out under conventional conditions or the conditions recommended by the manufacturer. If the manufacturers of the reagents or instruments are not specified, they are all conventional products that can be obtained through commercial channels.

[0057] In the following embodiments, the yield of poly-alpha-olefin is calculated as follows:

[0058] Yield = m1 / m2×100%, where m1 is the mass of the polymerized product and m2 is the total mass of the polymerized monomers.

[0059] Example 1

[0060] Reaction I: 100 g of 1-octene and 200 mL of toluene were added to a 500 mL flask filled with nitrogen, heated at 100° C. for 30 minutes, and 50 mL of a metallocene catalyst solution (3 μmol of dimethylsilylbisindenylzirconium dichloride, 50 mg of dimethylanilinium tetrakis(pentafluorophenyl)borate, and 35 mg of triethylaluminum) was added.

[0061] Reaction II: 100 g of 1-octene and 200 mL of toluene were added to a 1000 mL flask filled with nitrogen and heated at a constant temperature of 100°C.

[0062] Tandem reaction: After reaction I reacted for 3 minutes, it was immediately transferred to reaction II. After reacting for 1 hour, a small amount of isopropanol was added to terminate the reaction. After the temperature was cooled to room temperature, it was filtered and distilled under reduced pressure to obtain 184.2g of product with a yield of 92%. The kinematic viscosity at 100℃ was 20cSt, the viscosity index was 171, and the weight average molecular weight was 2843.

[0063] Example 2

[0064] Reaction I: 100 g of 1-octene and 200 mL of toluene were added to a 500 mL flask filled with nitrogen, heated at 100° C. for 30 minutes, and 50 mL of a metallocene catalyst solution (3 μmol of dimethylsilylbisindenylzirconium dichloride, 50 mg of dimethylanilinium tetrakis(pentafluorophenyl)borate, and 35 mg of triethylaluminum) was added.

[0065] Reaction II: 100 g of 1-octene and 200 mL of toluene were added to a 1000 mL flask filled with nitrogen and heated at a constant temperature of 100°C.

[0066] Tandem reaction: After reaction I reacted for 5 minutes, it was immediately transferred to reaction II. After reacting for 1 hour, a small amount of isopropanol was added to terminate the reaction. After the temperature was cooled to room temperature, it was filtered and distilled under reduced pressure to obtain 175.6g of product with a yield of 87.8%. The kinematic viscosity at 100℃ was 35cSt, the viscosity index was 180, and the weight average molecular weight was 3370.

[0067] Example 3

[0068] Reaction I: 100 g of 1-octene and 200 mL of toluene were added to a 500 mL flask filled with nitrogen, heated at 100° C. for 30 minutes, and 50 mL of a metallocene catalyst solution (3 μmol of dimethylsilylbisindenylzirconium dichloride, 50 mg of dimethylanilinium tetrakis(pentafluorophenyl)borate, and 35 mg of triethylaluminum) was added.

[0069] Reaction II: 100 g of 1-octene and 200 mL of toluene were added to a 1000 mL flask filled with nitrogen and heated at a constant temperature of 100°C.

[0070] Tandem reaction: After reaction I reacted for 10 minutes, it was immediately transferred to reaction II. After reacting for 1 hour, a small amount of isopropanol was added to terminate the reaction. After the temperature was cooled to room temperature, it was filtered and distilled under reduced pressure to obtain 170.6g of product with a yield of 85.3%. The kinematic viscosity at 100℃ was 85cSt, the viscosity index was 190, and the weight average molecular weight was 5438.

[0071] Example 4

[0072] Reaction I: 100 g of 1-octene and 200 mL of toluene were added to a 500 mL flask filled with nitrogen, heated at 100° C. for 30 minutes, and 50 mL of a metallocene catalyst solution (3 μmol of dimethylsilylbisindenylzirconium dichloride, 50 mg of dimethylanilinium tetrakis(pentafluorophenyl)borate, and 35 mg of triethylaluminum) was added.

[0073] Reaction II: Add 200 mL of toluene into a 1000 mL flask filled with nitrogen and heat at a constant temperature of 100°C.

[0074] Tandem reaction: After reaction I reacted for 3 minutes, it was immediately transferred to reaction II. After reacting for 1 hour, a small amount of isopropanol was added to terminate the reaction. After the temperature was cooled to room temperature, it was filtered and distilled under reduced pressure to obtain 90.3g of product with a yield of 90.3%. The kinematic viscosity at 100℃ was 8cSt, the viscosity index was 160, and the weight average molecular weight was 1472.

[0075] Example 5

[0076] Reaction I: 100 g of 1-octene and 200 mL of toluene were added to a 500 mL flask filled with nitrogen, heated at 100° C. for 30 minutes, and 50 mL of a metallocene catalyst solution (3 μmol of dimethylsilylbisindenylzirconium dichloride, 50 mg of dimethylanilinium tetrakis(pentafluorophenyl)borate, and 35 mg of triethylaluminum) was added.

[0077] Reaction II: 50 g of 1-octene and 200 mL of toluene were added to a 1000 mL flask filled with nitrogen and heated at a constant temperature of 100°C.

[0078] Tandem reaction: After reaction I reacted for 3 minutes, it was immediately transferred to reaction II. After reacting for 1 hour, a small amount of isopropanol was added to terminate the reaction. After the temperature was cooled to room temperature, it was filtered and distilled under reduced pressure to obtain 129.5g of product with a yield of 86.3%. The kinematic viscosity at 100℃ was 15cSt, the viscosity index was 165, and the weight average molecular weight was 2467.

[0079] Example 6

[0080] Reaction I: 100 g of 1-octene and 200 mL of toluene were added to a 500 mL flask filled with nitrogen, heated at 100° C. for 30 minutes, and 50 mL of a metallocene catalyst solution (3 μmol of dimethylsilylbisindenylzirconium dichloride, 50 mg of dimethylanilinium tetrakis(pentafluorophenyl)borate, and 35 mg of triethylaluminum) was added.

[0081] Reaction II: 150 g of 1-octene and 200 mL of toluene were added to a 1000 mL flask filled with nitrogen and heated at a constant temperature of 100°C.

[0082] Tandem reaction: After reaction I reacted for 3 minutes, it was immediately transferred to reaction II. After reacting for 1 hour, a small amount of isopropanol was added to terminate the reaction. After the temperature was cooled to room temperature, it was filtered and distilled under reduced pressure to obtain 225.0g of product with a yield of 90%. The kinematic viscosity at 100℃ was 37cSt, the viscosity index was 180, and the weight average molecular weight was 3597.

[0083] Example 7

[0084] Reaction I: 100 g of 1-octene and 200 mL of toluene were added to a 500 mL flask filled with nitrogen, heated at 80° C. for 30 minutes, and 50 mL of a metallocene catalyst solution (3 μmol of dimethylsilylbisindenylzirconium dichloride, 50 mg of dimethylanilinium tetrakis(pentafluorophenyl)borate, and 35 mg of triethylaluminum) was added.

[0085] Reaction II: 100 g of 1-octene and 200 mL of toluene were added to a 1000 mL flask filled with nitrogen and heated at a constant temperature of 80°C.

[0086] Tandem reaction: After reaction I reacted for 3 minutes, it was immediately transferred to reaction II. After reacting for 1 hour, a small amount of isopropanol was added to terminate the reaction. After the temperature was cooled to room temperature, it was filtered and distilled under reduced pressure to obtain 188.0g of product with a yield of 94%. The kinematic viscosity at 100℃ was 40cSt, the viscosity index was 180, and the weight average molecular weight was 3757.

[0087] Example 8

[0088] Reaction I: 100 g of 1-octene and 200 mL of toluene were added to a 500 mL flask filled with nitrogen, heated at 120° C. for 30 minutes, and 50 mL of a metallocene catalyst solution (3 μmol of dimethylsilylbisindenylzirconium dichloride, 50 mg of dimethylanilinium tetrakis(pentafluorophenyl)borate, and 35 mg of triethylaluminum) was added.

[0089] Reaction II: 100 g of 1-octene and 200 mL of toluene were added to a 1000 mL flask filled with nitrogen and heated at a constant temperature of 120°C.

[0090] Tandem reaction: After reaction I reacted for 3 minutes, it was immediately transferred to reaction II. After reacting for 1 hour, a small amount of isopropanol was added to terminate the reaction. After the temperature was cooled to room temperature, it was filtered and distilled under reduced pressure to obtain 178g of product with a yield of 89%. The kinematic viscosity at 100℃ was 10cSt, the viscosity index was 165, and the weight average molecular weight was 1759.

[0091] It should be noted that the embodiments described above are only used to explain the present invention and do not constitute any limitation to the present invention. The present invention has been described with reference to typical embodiments, but it should be understood that the words used therein are descriptive and explanatory words, rather than restrictive words. The present invention may be modified as specified within the scope of the claims of the present invention, and the present invention may be revised without departing from the scope and spirit of the present invention. Although the present invention described therein relates to specific methods, materials and embodiments, it does not mean that the present invention is limited to the specific examples disclosed therein, on the contrary, the present invention can be extended to all other methods and applications with the same functions.

Claims

1. A process for producing poly-alpha-olefins, comprising the following steps: S1. contacting a first raw material system comprising a first α-olefin and a first solvent with a metallocene catalyst, thereby causing a first polymerization reaction of the first α-olefin to obtain a first polymerization product; S2. contacting the first polymerization product with a second raw material system comprising a second solvent and optionally a second α-olefin, thereby causing a second polymerization reaction to obtain a second polymerization product comprising the poly-α-olefin, Wherein, the second raw material system does not contain a catalyst for catalyzing olefin polymerization; To obtain poly-α-olefins with different viscosities by controlling the reaction time of the first polymerization reaction and / or the reaction temperature of the first polymerization reaction and / or the concentration of the second α-olefin in the second raw material system; The first α-olefin and the second α-olefin are the same or different, and are independently selected from one or more of 1-hexene, 1-heptene, 1-octene, 1-nonene, 1-decene, 1-undecene, 1-dodecene, 1-tridecene, 1-tetradecene, 1-pentadecene, 1-hexadecene, 1-heptadecene, 1-octadecene, 1-nonadecene and 1-eicosene; The poly-α-olefin has a kinematic viscosity at 100° C. of 3 cSt to 85 cSt.

2. The production process according to claim 1, characterized in that: The temperature of the first raw material system and the second raw material system is the same, which is 30°C to 190°C; and / or the temperature of the first polymerization reaction is the same as the temperature of the second polymerization reaction, which is 30°C to 190°C; the temperature of the first raw material system is the same as the temperature of the first polymerization reaction.

3. The production process according to claim 2, characterized in that: The temperature of the first raw material system and the second raw material system is the same, 80°C to 170°C; and / or the temperature of the first polymerization reaction and the temperature of the second polymerization reaction is the same, 80°C to 170°C.

4. The production process according to claim 2 or 3, characterized in that: The temperature of the first raw material system is the same as the temperature of the first polymerization reaction.

5. The production process according to claim 1, characterized in that: The time of the first polymerization reaction is 1 min to 120 min; and / or the time of the second polymerization reaction is 0.1 h to 10 h.

6. The production process according to claim 5, characterized in that: The time of the first polymerization reaction is 1 min to 60 min; and / or the time of the second polymerization reaction is 0.5 h to 5 h.

7. The production process according to claim 1, characterized in that: The amount of the first solvent used is 1 mL to 1000 mL per gram of the first α-olefin; and / or the amount of the second α-olefin used is 0 g to 10 g per gram of the first α-olefin; and / or the amount of the second solvent used is 1 mL to 1000 mL per gram of the first α-olefin.

8. The production process according to claim 7, characterized in that: The amount of the first solvent used is 1 mL to 100 mL per gram of the first α-olefin; and / or the amount of the second α-olefin used is 0 g to 5 g per gram of the first α-olefin; and / or the amount of the second solvent used is 1 mL to 100 mL per gram of the first α-olefin.

9. The production process according to claim 1, characterized in that: The metallocene catalyst comprises a metallocene compound and an activator, Wherein, the metallocene compound is selected from dimethylsilylbis-n-propylcyclopentadienyl zirconium dichloride, dimethylsilylbis-indenyl zirconium dichloride, diethylsilylbis-indenyl zirconium dichloride, diphenylsilylbis(4,7-dimethylindenyl) zirconium dichloride, dimethylsilylbis(4,7-dimethylindenyl) zirconium dichloride, dimethylsilylbis-indenyl zirconium dichloride, diphenylsilylbis(2-methylcyclopentadienyl) zirconium dichloride, ethylenebis-indenyl zirconium dichloride, ethylenebis-(2-methylindenyl) zirconium dichloride, dimethylsilylbis-(2-methyl-3-butylcyclopentadienyl) zirconium dichloride, dimethylsilylbis-cyclopentadienyl Zirconium dichloride, diethylmethylenecyclopentadienyl (3,5-dimethylphenylindenyl) zirconium dichloride, diethylmethylenecyclopentadienyl (4,7-dimethylindenyl) zirconium dichloride, dimethylmethylenecyclopentadienyl (4,7-dimethylindenyl) zirconium dichloride, dimethylsilylcyclopentadienyl (4,7-dimethylindenyl) zirconium dichloride, dimethylsilylcyclopentadienyl (3,5-dimethylphenylindenyl) zirconium dichloride, dimethylsilylbis (2-methylcyclopentadienyl) zirconium dichloride, dimethylsilylbis (2-methylindenyl) zirconium dichloride Zirconium, dimethylsilylbis-n-propylcyclopentadienyl hafnium dichloride, dimethylsilylbis-indenyl hafnium dichloride, diethylsilylbis-indenyl hafnium dichloride, diphenylsilylbis(4,7-dimethylindenyl) hafnium dichloride, dimethylsilylbis(4,7-dimethylindenyl) hafnium dichloride, dimethylsilylbis-indenyl hafnium dichloride, diphenylsilylbis(2-methylcyclopentadienyl) hafnium dichloride, ethylenebis-indenyl hafnium dichloride, ethylenebis(2-methylindenyl) hafnium dichloride, dimethylsilylbis(2-methyl-3-butylcyclopentadienyl) hafnium dichloride, dimethylsilylbis-cyclopentadienyl hafnium dichloride, diethylmethylene one or more of dimethylsilylcyclopentadienyl (3,5-dimethylphenylindenyl) hafnium dichloride, diethylmethylenecyclopentadienyl (4,7-dimethylindenyl) hafnium dichloride, dimethylmethylenecyclopentadienyl (4,7-dimethylindenyl) hafnium dichloride, dimethylsilylcyclopentadienyl (4,7-dimethylindenyl) hafnium dichloride, dimethylsilylcyclopentadienyl (3,5-dimethylphenylindenyl) hafnium dichloride, dimethylsilylbis (2-methylcyclopentadienyl) hafnium dichloride, dimethylsilylbis (2-methylindenyl) hafnium dichloride and dimethylsilylcyclopentadienyl (2-methylindenyl) hafnium dichloride; The activator is selected from one or more of alkyl aluminum and borate.

10. The production process according to claim 9, characterized in that: The general formula of the alkyl aluminum is AlR3, wherein R is a C1-C10 alkyl group.

11. The production process according to claim 10, characterized in that: The alkylaluminum is selected from one or more of trimethylaluminum, triethylaluminum, triisopropylaluminum, tri-n-propylaluminum, triisobutylaluminum, tri-n-butylaluminum, triisopentylaluminum, tri-n-pentylaluminum, triisohexylaluminum, tri-n-hexylaluminum, triisoheptylaluminum, tri-n-heptylaluminum, triisooctylaluminum, tri-n-octylaluminum, triisononylaluminum, tri-n-nonylaluminum, triisodecylaluminum and tri-n-decylaluminum; the borate is selected from one or more of dimethylanilinium tetrakis(pentafluorophenyl)borate, diethylanilinium tetrakis(pentafluorophenyl)borate, dibutylanilinium tetrakis(pentafluorophenyl)borate, trimethylammonium tetrakis(pentafluorophenyl)borate, diethylammonium tetrakis(pentafluorophenyl)borate and tributylammonium tetrakis(pentafluorophenyl)borate.

12. The production process according to claim 9, characterized in that: The weight ratio of the metallocene compound, the activator and the first α-olefin is 1:(10-1000):(100-100000).

13. The production process according to claim 1, characterized in that: The first α-olefin and the second α-olefin are each independently selected from one or more of 1-hexene, 1-heptene, 1-octene, 1-nonene, 1-decene, 1-undecene, 1-dodecene, 1-tridecene and 1-tetradecene.

14. The production process according to claim 13, characterized in that: The first α-olefin and the second α-olefin are the same.

15. The production process according to claim 1, characterized in that: The first solvent and the second solvent are the same or different, and are independently selected from one or more of alkanes and aromatic hydrocarbons.

16. The production process according to claim 15, characterized in that: The first solvent and the second solvent are the same or different, and are independently selected from one or more of hexane, heptane, octane, nonane, decane, cyclohexane, benzene, toluene and xylene.

17. The production process according to claim 16, characterized in that: The first solvent and the second solvent are the same.

18. The production process according to claim 1, characterized in that: The production process is carried out in two reaction devices connected in series.

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