CN116023562A - Production process of poly alpha-olefin - Google Patents

Production process of poly alpha-olefin Download PDF

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Publication number
CN116023562A
CN116023562A CN202111243183.6A CN202111243183A CN116023562A CN 116023562 A CN116023562 A CN 116023562A CN 202111243183 A CN202111243183 A CN 202111243183A CN 116023562 A CN116023562 A CN 116023562A
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olefin
dimethylindenyl
alpha
zirconium dichloride
reaction
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毛远洪
梁胜彪
曹育才
杨庆伟
李禄建
李永清
刘国禹
李叶思
卢瑞真
孙望平
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China Petroleum and Chemical Corp
Shanghai Research Institute of Chemical Industry SRICI
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China Petroleum and Chemical Corp
Shanghai Research Institute of Chemical Industry SRICI
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    • Y02P20/00—Technologies relating to chemical industry
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Abstract

The invention provides a process for producing poly alpha-olefin, which comprises the following steps: s1, a first raw material system containing first alpha-olefin and a first solvent is contacted with a metallocene catalyst, so that the first alpha-olefin is subjected to a first polymerization reaction to obtain a first polymerization product; s2, contacting the first polymerization product with a second raw material system containing a second solvent and optionally a second alpha-olefin, so as to carry out a second polymerization reaction, and obtaining a second polymerization product containing the poly alpha-olefin, wherein the second raw material system does not contain a catalyst for catalyzing olefin polymerization. The viscosity of the poly alpha-olefin can be effectively regulated by using the production process, and the requirements of different products are met.

Description

Production process of poly alpha-olefin
Technical Field
The invention relates to the technical field of production of poly-alpha-olefin, in particular to a production process of poly-alpha-olefin.
Background
Catalytic oligomerization of olefins is a known technique for preparing hydrocarbon base stocks for use as lubricants. The improvement of the performance of natural mineral oil-based lubricants by synthetic oligomeric hydrocarbon fluids has been an important research and development topic in the petroleum industry for decades, resulting in the recent mass production of many higher polyalphaolefin synthetic lubricants (hereinafter "PAOs"). These materials are based mainly on materials such as C 6 -C 12 Oligomerization of alpha olefins such as olefins. Industrial research directed to synthetic lubricants has generally focused on fluids that exhibit useful viscosities, 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 increase mechanical efficiency throughout the entire mechanical load range and over a wider range of operating conditions than mineral oil lubricantsThis is shown in the surrounding.
Metallocene poly alpha-olefins (mPAO) are catalyzed by metallocene catalysts to polymerize alpha-olefins to obtain products with comb structures and no upright side chains. Such structures affect PAO product performance and mPAO typically possesses improved rheological and flow characteristics compared to conventional PAOs, providing better shear stability, lower pour point and higher viscosity index, and good visco-thermal properties. These characteristics determine that the mPAO can be used in high severity environments, including power transmission and gear oils, compressor lubricating oils, transmission fluids, and industrial lubricating oils. Along with the increasing requirements of society on energy utilization rate and ecological environment protection, the demand of people on high-performance mPAO lubricating oil base oil is increased.
Metallocene compounds generally refer to a class of organometallic complexes consisting of transition metal elements (e.g., group IV B elements titanium, zirconium, hafnium) or rare earth metal elements and at least one cyclopentadiene or cyclopentadiene derivative as ligands. Metallocene catalysts are generally considered to be third generation PAO catalysts. In general, metallocene catalysts catalyze the polymerization of alpha-olefins to readily produce PAOs of high viscosity (kinematic viscosity at 100 ℃ above 40 cSt), while the preparation of metallocene PAOs of low viscosity (kinematic viscosity at 100 ℃ below 20 cSt) requires the addition of molecular weight regulators such as hydrogen, organometallic compounds, and the like. The addition of hydrogen tends to saturate the feedstock and the conditioning of the organometallic compounds tends to increase cost and complexity of the process. For this reason, it is necessary to find an economical way to adjust the viscosity of metallocene PAOs.
Disclosure of Invention
In view of the above problems in the prior art, it is an object of the present invention to provide a process for producing a polyalphaolefin, by which the viscosity of the metallocene polyalphaolefin can be effectively adjusted.
It is a second object of the present invention to provide a polyalphaolefin corresponding to one of the objects.
In order to achieve one of the above purposes, the technical scheme adopted by the invention is as follows:
a process for producing a polyalphaolefin comprising the steps of:
s1, contacting a first raw material system containing first alpha-olefin and a first solvent with a metallocene catalyst, so that the first alpha-olefin is subjected to first polymerization reaction to obtain a first polymerization product;
s2, contacting the first polymerization product with a second feed system comprising a second solvent and optionally a second alpha-olefin, whereby a second polymerization reaction occurs, yielding a second polymerization product comprising the polyalphaolefin,
wherein the second feedstock system is free of a catalyst for catalyzing the polymerization of olefins.
According to the invention, no fresh catalyst, for example a metallocene catalyst, for catalyzing the polymerization of olefins is introduced in step S2.
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.
The inventors of the present application have found that by introducing the first polymerization product into a system containing no catalyst to continue the polymerization reaction, the viscosity of the produced polyalphaolefin can be adjusted by using the change in the active center concentration and the presence state of the catalyst.
According to some embodiments of the invention, polyalphaolefins having different viscosities are obtained 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 alpha-olefin in the second feed system.
By adjusting the process conditions (e.g., reaction time, reaction temperature, and monomer amount, etc.) of the first polymerization reaction and the second polymerization reaction, the polymerization degree of the produced polyalphaolefin can be effectively adjusted. For example, a polyalphaolefin of a desired viscosity can be obtained by adjusting the reaction time of the first polymerization reaction and the amount of the alpha-olefin used in the second polymerization reaction, in which case the concentration of active sites and the presence of the catalyst are different due to the different reaction times in the first polymerization reaction, and the concentration of the alpha-olefin in the second polymerization reaction are different, ultimately comprehensively affecting the viscosity of the product polyalphaolefin.
According to some embodiments of the invention, in step S2, isopropanol may be used as a terminator to terminate the second polymerization reaction.
According to some embodiments of the present invention, after the completion of the second polymerization reaction, unreacted monomers as well as the oligomerization product may be removed by filtration, distillation under reduced pressure to obtain the final product polyalphaolefin.
According to some embodiments of the present invention, the filtration and reduced pressure distillation are all conventional operations in the art, and specific operation modes are not described herein.
According to some embodiments of the invention, the above preparation process may be carried out under an inert atmosphere, for example under a nitrogen atmosphere.
In some preferred embodiments of the present invention, the first feedstock system and the second feedstock system are at the same temperature, ranging from 30 ℃ to 190 ℃, preferably from 80 ℃ to 170 ℃.
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, and is 30 to 190 ℃, preferably 80 to 170 ℃.
In some preferred embodiments of the invention, the temperature of the first feed system and the temperature of the first polymerization reaction are the same.
In some preferred embodiments of the invention, the time of the first polymerization reaction is from 1min to 120min, preferably from 1min to 60min.
According to the present invention, the time of the first polymerization reaction may be exemplified by 1min, 5min, 10min, 15min, 20min, 25min, 30min, 35min, 40min, 45min, 50min, 55min, 60min, 65min, 70min, 75min, 80min, 85min, 90min, 100min, 110min, 120min and any value therebetween.
According to the present invention, the properties of the polymerization product, such as viscosity, can be adjusted by adjusting the time of the first polymerization reaction.
In some preferred embodiments of the invention, the second polymerization reaction is carried out for a period of time ranging from 0.1h to 10h, preferably from 0.5h to 5h.
In some preferred embodiments of the present invention, the first solvent is used in an amount of 1 mL-1000 mL, preferably 1 mL-100 mL, per gram of the first alpha-olefin.
In some preferred embodiments of the invention, the second alpha-olefin is used in an amount of 0g to 10g, preferably 0g to 5g, per gram of the first alpha-olefin.
According to the invention, the second feed system may have only solvent and no alpha-olefin.
According to the present invention, properties of the polymerization product, such as viscosity, can be adjusted by adjusting the amount of the second alpha-olefin.
In some preferred embodiments of the present invention, the second solvent is used in an amount of 1 mL-1000 mL, preferably 1 mL-100 mL, per gram of the first alpha-olefin.
In some preferred embodiments of the present invention, the metallocene catalyst comprises a metallocene compound and an activator,
wherein the metallocene compound is selected from the group consisting of dimethylsilylbis-n-propylcyclopentadienyl zirconium dichloride, dimethylsilylbis-indenyl zirconium dichloride, diphenylsilylbis (4, 7-dimethylindenyl) zirconium dichloride, dimethylsilylbis-indenyl zirconium dichloride, diphenylsilylbis (2-methylcyclopentadienyl) zirconium dichloride, ethylenebisindenyl zirconium dichloride, ethylenebis (2-methylindenyl) zirconium dichloride, dimethylsilylbis (2-methyl-3-butylcyclopentadienyl) zirconium dichloride, dimethylsilylbiscyclopentadienyl zirconium dichloride, diethylcyclopentadienyl (3, 5-dimethylindenyl) zirconium dichloride, diethylcyclopentadienyl (4, 7-dimethylindenyl) zirconium dichloride, dimethylcyclopentadienyl (4, 7-dimethylindenyl) zirconium dichloride, dimethylsilylbis (4, 7-dimethylindenyl) hafnium dichloride, ethylenebis (2-methylindenyl) zirconium dichloride, n-dimethylindenyl) dimethylsilndenyl zirconium dichloride, dimethylsilindindenyl (2-dimethylindenyl) zirconium dichloride, dimethylsilindindenyl (2, 5-dimethylindenyl) zirconium dichloride, dimethylsilindindenyl (2-dimethylindenyl) zirconium dichloride, one or more of diphenylsilylbis (4, 7-dimethylindenyl) hafnium dichloride, dimethylsilylbis (4, 7-dimethylindenyl) hafnium dichloride, dimethylsilylbisindenyl hafnium dichloride, diphenylsilylbis (2-methylcyclopentadienyl) hafnium dichloride, ethylenebisindenyl hafnium dichloride, ethylenebis (2-methylindenyl) hafnium dichloride, dimethylsilylbis (2-methyl-3-butylcyclopentadienyl) hafnium dichloride, dimethylsilylbiscyclopentadienyl hafnium dichloride, diethylmethylenecyclopentadienyl (3, 5-dimethylphenylindenyl) hafnium dichloride, diethylmethylenecyclopentadienyl (4, 7-dimethylindenyl) hafnium dichloride, dimethylcyclopentadienyl (4, 7-dimethylindenyl) hafnium dichloride, dimethylsilylcyclopentadienyl (3, 5-dimethylindenyl) hafnium dichloride, dimethylsilylbis (2-methylcyclopentadienyl) hafnium dichloride, dimethylsilylbis (2-dimethylindenyl) hafnium dichloride and dimethylindenyl) dimethylsilyl (2-dimethylindenyl) hafnium dichloride;
the activator is selected from one or more of aluminum alkyls and borates.
In some preferred embodiments of the invention, the aluminum alkyls have the formula AlR 3 Wherein R is C 1 -C 10 Alkyl, more preferably, the alkyl aluminum 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.
In some preferred embodiments of the present invention, 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.
According to some embodiments of the invention, the metallocene compound and the activator are used in conventional amounts, for example, the metallocene compound may be contained in an amount of 1. Mu. Mol to 20. Mu. Mol, the aluminum alkyl may be contained in an amount of 10mg to 1000mg, and the borate may be contained in an amount of 5mg to 500mg per 100mL of the metallocene catalyst.
According to some embodiments of the invention, the weight ratio of the metallocene compound, the activator, and the first alpha-olefin is 1 (10-1000): (100-100000).
In some preferred embodiments of the present invention, the first α -olefin and the second α -olefin are the same or different and 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, 1-tetradecene, 1-pentadecene, 1-hexadecene, 1-heptadecene, 1-octadecene, 1-nonadecene, and 1-eicosene.
In some preferred embodiments of the present invention, the first α -olefin and the second α -olefin are the same or different and are each 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.
In some preferred embodiments of the invention, the first alpha-olefin and the second alpha-olefin are the same.
In some preferred embodiments of the present invention, the first solvent and the second solvent are the same or different and are each independently selected from one or more of alkanes and aromatics.
In some preferred embodiments of the present invention, the first solvent and the second solvent are the same or different and are each independently selected from one or more of hexane, heptane, octane, nonane, decane, cyclohexane, benzene, toluene and xylene.
In some preferred embodiments of the invention, the first solvent and the second solvent are the same.
In some preferred embodiments of the invention, the preparation process is carried out in two reaction units connected in series.
In the present invention, the term "identical" is also understood to be substantially identical, for example within 1%, even 5%. This is because differences within 5% or even within 1% have a small effect on the results and are therefore negligible and considered the same.
In order to achieve the second purpose, the technical scheme adopted by the invention is as follows:
a polyalphaolefin produced according to the above-described production process, the polyalphaolefin having a viscosity index of 140 or greater; and/or the weight average molecular weight of the poly alpha-olefin is 200 to 200000; and/or the polyalphaolefin has a kinematic viscosity at 100 ℃ of 3cSt or greater.
According to some preferred embodiments of the invention, the polyalphaolefin has a kinematic viscosity at 100 ℃ of from 3cSt to 5000cSt.
The beneficial effects of the invention are at least the following aspects:
firstly, the production process provided by the invention is simple and easy to operate, and the viscosity of the poly-alpha-olefin can be effectively regulated only by changing the process conditions.
Secondly, the preparation method provided by the invention can prepare the poly alpha-olefin products with different grades of viscosity, thereby meeting the requirements of different occasions or products.
Drawings
Fig. 1 is a process flow diagram of example 1 of the present invention.
Detailed Description
The present invention will be described in detail with reference to examples, but the scope of the present invention is not limited to the following description.
The specific conditions are not noted in the examples and are carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or apparatus used were conventional products available commercially without the manufacturer's knowledge.
In the following embodiments, the yield of polyalphaolefins is calculated as:
yield = m 1 /m 2 X 100%, where m 1 For the mass of the polymeric product, m 2 Is the total mass of the polymerized monomers.
Example 1
Reaction I: into a 500mL flask filled with nitrogen gas were charged 100g of 1-octene and 200mL of toluene, and the mixture was heated at a constant temperature of 100℃for 30 minutes, and 50mL of a metallocene catalyst solution (dimethylsilyl bis-indenyl zirconium dichloride 3. Mu. Mol, dimethylanilinium tetrakis (pentafluorophenyl) borate 50mg, triethylaluminum 35 mg) was added.
Reaction II: a1000 mL flask filled with nitrogen was charged with 100g of 1-octene and 200mL of toluene, and heated at a constant temperature of 100 ℃.
Serial reaction: after 3min of reaction I, the reaction was immediately transferred to reaction II, and after 1 hour of reaction, the reaction was terminated by adding a small amount of isopropanol. After cooling to room temperature, filtration and distillation under reduced pressure gave 184.2g of product in 92% yield. The kinematic viscosity at 100℃was 20cSt, the viscosity index was 171 and the weight-average molecular weight was 2843.
Example 2
Reaction I: into a 500mL flask filled with nitrogen gas were charged 100g of 1-octene and 200mL of toluene, and the mixture was heated at a constant temperature of 100℃for 30 minutes, and 50mL of a metallocene catalyst solution (dimethylsilyl bis-indenyl zirconium dichloride 3. Mu. Mol, dimethylanilinium tetrakis (pentafluorophenyl) borate 50mg, triethylaluminum 35 mg) was added.
Reaction II: a1000 mL flask filled with nitrogen was charged with 100g of 1-octene and 200mL of toluene, and heated at a constant temperature of 100 ℃.
Serial reaction: after 5min of reaction I, the reaction was immediately transferred to reaction II, and after 1 hour of reaction, the reaction was terminated by adding a small amount of isopropanol. After cooling to room temperature, filtration and distillation under reduced pressure gave 175.6g of the product in 87.8% yield. The kinematic viscosity at 100℃was 35cSt, the viscosity index was 180 and the weight average molecular weight was 3370.
Example 3
Reaction I: into a 500mL flask filled with nitrogen gas were charged 100g of 1-octene and 200mL of toluene, and the mixture was heated at a constant temperature of 100℃for 30 minutes, and 50mL of a metallocene catalyst solution (dimethylsilyl bis-indenyl zirconium dichloride 3. Mu. Mol, dimethylanilinium tetrakis (pentafluorophenyl) borate 50mg, triethylaluminum 35 mg) was added.
Reaction II: a1000 mL flask filled with nitrogen was charged with 100g of 1-octene and 200mL of toluene, and heated at a constant temperature of 100 ℃.
Serial reaction: after 10min of reaction I, the reaction was immediately transferred to reaction II, and after 1 hour of reaction, the reaction was terminated by adding a small amount of isopropanol. After cooling to room temperature, filtration and distillation under reduced pressure gave 170.6g of the product in 85.3% yield. The kinematic viscosity at 100℃was 85cSt, the viscosity index was 190 and the weight average molecular weight was 5438.
Example 4
Reaction I: into a 500mL flask filled with nitrogen gas were charged 100g of 1-octene and 200mL of toluene, and the mixture was heated at a constant temperature of 100℃for 30 minutes, and 50mL of a metallocene catalyst solution (dimethylsilyl bis-indenyl zirconium dichloride 3. Mu. Mol, dimethylanilinium tetrakis (pentafluorophenyl) borate 50mg, triethylaluminum 35 mg) was added.
Reaction II: 200mL of toluene was added to a 1000mL flask filled with nitrogen, and the flask was heated at a constant temperature of 100 ℃.
Serial reaction: after 3min of reaction I, the reaction was immediately transferred to reaction II, and after 1 hour of reaction, the reaction was terminated by adding a small amount of isopropanol. After cooling to room temperature, filtration and distillation under reduced pressure gave 90.3g of the product in 90.3% yield. The kinematic viscosity at 100℃was 8cSt, the viscosity index was 160 and the weight average molecular weight 1472.
Example 5
Reaction I: into a 500mL flask filled with nitrogen gas were charged 100g of 1-octene and 200mL of toluene, and the mixture was heated at a constant temperature of 100℃for 30 minutes, and 50mL of a metallocene catalyst solution (dimethylsilyl bis-indenyl zirconium dichloride 3. Mu. Mol, dimethylanilinium tetrakis (pentafluorophenyl) borate 50mg, triethylaluminum 35 mg) was added.
Reaction II: a1000 mL flask filled with nitrogen was charged with 50g of 1-octene and 200mL of toluene, and heated at a constant temperature of 100 ℃.
Serial reaction: after 3min of reaction I, the reaction was immediately transferred to reaction II, and after 1 hour of reaction, the reaction was terminated by adding a small amount of isopropanol. After cooling to room temperature, filtration and distillation under reduced pressure gave 129.5g of the product in 86.3% yield. The kinematic viscosity at 100℃was 15cSt, the viscosity index was 165 and the weight average molecular weight was 2467.
Example 6
Reaction I: into a 500mL flask filled with nitrogen gas were charged 100g of 1-octene and 200mL of toluene, and the mixture was heated at a constant temperature of 100℃for 30 minutes, and 50mL of a metallocene catalyst solution (dimethylsilyl bis-indenyl zirconium dichloride 3. Mu. Mol, dimethylanilinium tetrakis (pentafluorophenyl) borate 50mg, triethylaluminum 35 mg) was added.
Reaction II: 150g of 1-octene and 200mL of toluene were charged into a 1000mL flask charged with nitrogen and heated at a constant temperature of 100 ℃.
Serial reaction: after 3min of reaction I, the reaction was immediately transferred to reaction II, and after 1 hour of reaction, the reaction was terminated by adding a small amount of isopropanol. After cooling to room temperature, filtration and distillation under reduced pressure gave 225.0g of the product in 90% yield. The kinematic viscosity at 100℃was 37cSt, the viscosity index was 180 and the weight average molecular weight 3597.
Example 7
Reaction I: into a 500mL flask filled with nitrogen gas, 100g of 1-octene and 200mL of toluene were charged, and the mixture was heated at a constant temperature of 80℃for 30 minutes, and 50mL of a metallocene catalyst solution (dimethylsilyl bis-indenyl zirconium dichloride 3. Mu. Mol, dimethylanilinium tetrakis (pentafluorophenyl) borate, 50mg, triethylaluminum, 35 mg) was added.
Reaction II: a1000 mL flask filled with nitrogen was charged with 100g of 1-octene and 200mL of toluene, and heated at 80 ℃.
Serial reaction: after 3min of reaction I, the reaction was immediately transferred to reaction II, and after 1 hour of reaction, the reaction was terminated by adding a small amount of isopropanol. After cooling to room temperature, filtration and distillation under reduced pressure gave 188.0g of the product in 94% yield. The kinematic viscosity at 100℃was 40cSt, the viscosity index was 180 and the weight average molecular weight was 3757.
Example 8
Reaction I: into a 500mL flask filled with nitrogen gas, 100g of 1-octene and 200mL of toluene were charged, and the mixture was heated at a constant temperature of 120℃for 30 minutes, and 50mL of a metallocene catalyst solution (dimethylsilyl bis-indenyl zirconium dichloride 3. Mu. Mol, dimethylanilinium tetrakis (pentafluorophenyl) borate, 50mg, triethylaluminum, 35 mg) was added.
Reaction II: a1000 mL flask filled with nitrogen was charged with 100g of 1-octene and 200mL of toluene, and heated at 120℃under constant temperature.
Serial reaction: after 3min of reaction I, the reaction was immediately transferred to reaction II, and after 1 hour of reaction, the reaction was terminated by adding a small amount of isopropanol. After cooling to room temperature, filtration and distillation under reduced pressure gave 178g of the product in 89% yield. The kinematic viscosity at 100℃was 10cSt, the viscosity index was 165 and the weight average molecular weight was 1759.
It should be noted that the above-described embodiments are only for explaining the present invention and do not constitute any limitation of the present invention. The invention has been described with reference to exemplary embodiments, but it is understood that the words which have been used are words of description and illustration, rather than words of limitation. Modifications may be made to the invention as defined in the appended claims, and the invention may be modified without departing from the scope and spirit of the invention. Although the invention is described herein with reference to particular means, materials and embodiments, the invention is not intended to be limited to the particulars disclosed herein, as the invention extends to all other means and applications which perform the same function.

Claims (10)

1. A process for producing a polyalphaolefin comprising the steps of:
s1, contacting a first raw material system containing first alpha-olefin and a first solvent with a metallocene catalyst, so that the first alpha-olefin is subjected to first polymerization reaction to obtain a first polymerization product;
s2, contacting the first polymerization product with a second feed system comprising a second solvent and optionally a second alpha-olefin, whereby a second polymerization reaction occurs, yielding a second polymerization product comprising the polyalphaolefin,
wherein the second feedstock system is free of a catalyst for catalyzing the polymerization of olefins;
preferably, polyalphaolefins having different viscosities are obtained 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 alpha-olefin in the second feed system.
2. The production process according to claim 1, characterized in that the temperature of the first and the second raw material system is the same, ranging from 30 ℃ to 190 ℃, preferably from 80 ℃ to 170 ℃; and/or the temperature of the first polymerization reaction is the same as the temperature of the second polymerization reaction, and is 30-190 ℃, preferably 80-170 ℃; more preferably, the temperature of the first feed system is the same as the temperature of the first polymerization reaction.
3. The production process according to claim 1 or 2, characterized in that the time of the first polymerization reaction is 1min to 120min, preferably 1min to 60min; and/or the second polymerization reaction is carried out for a period of 0.1 to 10 hours, preferably 0.5 to 5 hours.
4. A production process according to any one of claims 1-3, wherein the first solvent is used in an amount of 1mL to 1000mL, preferably 1mL to 100mL, per gram of the first α -olefin; and/or the second alpha-olefin is used in an amount of 0g to 10g, preferably 0g to 5g, per gram of the first alpha-olefin; and/or the second solvent is used in an amount of 1mL to 1000mL, preferably 1mL to 100mL, per gram of the first alpha-olefin.
5. The production process according to any one of claims 1 to 4, wherein the metallocene catalyst comprises a metallocene compound and an activator,
wherein the metallocene compound is selected from the group consisting of dimethylsilylbis-n-propylcyclopentadienyl zirconium dichloride, dimethylsilylbis-indenyl zirconium dichloride, diphenylsilylbis (4, 7-dimethylindenyl) zirconium dichloride, dimethylsilylbis-indenyl zirconium dichloride, diphenylsilylbis (2-methylcyclopentadienyl) zirconium dichloride, ethylenebisindenyl zirconium dichloride, ethylenebis (2-methylindenyl) zirconium dichloride, dimethylsilylbis (2-methyl-3-butylcyclopentadienyl) zirconium dichloride, dimethylsilylbiscyclopentadienyl zirconium dichloride, diethylcyclopentadienyl (3, 5-dimethylindenyl) zirconium dichloride, diethylcyclopentadienyl (4, 7-dimethylindenyl) zirconium dichloride, dimethylcyclopentadienyl (4, 7-dimethylindenyl) zirconium dichloride, dimethylsilylbis (4, 7-dimethylindenyl) hafnium dichloride, ethylenebis (2-methylindenyl) zirconium dichloride, n-dimethylindenyl) dimethylsilndenyl zirconium dichloride, dimethylsilindindenyl (2-dimethylindenyl) zirconium dichloride, dimethylsilindindenyl (2, 5-dimethylindenyl) zirconium dichloride, dimethylsilindindenyl (2-dimethylindenyl) zirconium dichloride, one or more of diphenylsilylbis (4, 7-dimethylindenyl) hafnium dichloride, dimethylsilylbis (4, 7-dimethylindenyl) hafnium dichloride, dimethylsilylbisindenyl hafnium dichloride, diphenylsilylbis (2-methylcyclopentadienyl) hafnium dichloride, ethylenebisindenyl hafnium dichloride, ethylenebis (2-methylindenyl) hafnium dichloride, dimethylsilylbis (2-methyl-3-butylcyclopentadienyl) hafnium dichloride, dimethylsilylbiscyclopentadienyl hafnium dichloride, diethylmethylenecyclopentadienyl (3, 5-dimethylphenylindenyl) hafnium dichloride, diethylmethylenecyclopentadienyl (4, 7-dimethylindenyl) hafnium dichloride, dimethylcyclopentadienyl (4, 7-dimethylindenyl) hafnium dichloride, dimethylsilylcyclopentadienyl (3, 5-dimethylindenyl) hafnium dichloride, dimethylsilylbis (2-methylcyclopentadienyl) hafnium dichloride, dimethylsilylbis (2-dimethylindenyl) hafnium dichloride and dimethylindenyl) dimethylsilyl (2-dimethylindenyl) hafnium dichloride;
the activator is selected from one or more of aluminum alkyl and borate; preferably, the aluminum alkyl has the formula AlR 3 Wherein R is C 1 -C 10 Alkyl, more preferably, the alkyl aluminum is selected from one 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-decylaluminumOne or more species; the borate is selected from one or more of dimethyl phenyl ammonium tetra (pentafluorophenyl) borate, diethyl phenyl ammonium tetra (pentafluorophenyl) borate, dibutyl phenyl ammonium tetra (pentafluorophenyl) borate, trimethyl ammonium tetra (pentafluorophenyl) borate, diethyl ammonium tetra (pentafluorophenyl) borate and tributyl ammonium tetra (pentafluorophenyl) borate.
6. The process according to any one of claims 1 to 5, wherein the weight ratio of the metallocene compound, the activator and the first α -olefin is 1 (10 to 1000): 100 to 100000.
7. The production process according to any one of claims 1 to 6, wherein the first alpha-olefin and the second alpha-olefin are the same or different and 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, 1-tetradecene, 1-pentadecene, 1-hexadecene, 1-heptadecene, 1-octadecene, 1-nonadecene and 1-eicosene, preferably 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; more preferably, the first alpha-olefin and the second alpha-olefin are the same.
8. The production process according to any one of claims 1 to 7, wherein the first solvent and the second solvent are the same or different, each being independently selected from one or more of alkanes and aromatics, preferably one or more of hexane, heptane, octane, nonane, decane, cyclohexane, benzene, toluene and xylene, more preferably the first solvent and the second solvent are the same.
9. The production process according to any one of claims 1 to 8, wherein the production process is carried out in two reaction units connected in series.
10. A polyalphaolefin produced by the production process of any one of claims 1-9, wherein the polyalphaolefin has a viscosity index of 140 or greater; and/or the weight average molecular weight of the poly alpha-olefin is 200 to 200000; and/or the polyalphaolefin has a kinematic viscosity at 100 ℃ of 3cSt or more, preferably 3cSt to 5000cSt.
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