WO2022217985A1 - 一种α-烯烃聚合的催化剂组合物及其制备与应用 - Google Patents

一种α-烯烃聚合的催化剂组合物及其制备与应用 Download PDF

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WO2022217985A1
WO2022217985A1 PCT/CN2022/070680 CN2022070680W WO2022217985A1 WO 2022217985 A1 WO2022217985 A1 WO 2022217985A1 CN 2022070680 W CN2022070680 W CN 2022070680W WO 2022217985 A1 WO2022217985 A1 WO 2022217985A1
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catalyst
catalyst composition
acid
butanol
proton
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French (fr)
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曹媛媛
刘通
褚洪岭
王力搏
王玉龙
徐显明
王秀绘
高晗
孙维
李洪鹏
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Petrochina Co Ltd
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    • C08F4/00—Polymerisation catalysts
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/12—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/12—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
    • C10G69/126—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step polymerisation, e.g. oligomerisation
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
    • B01J2231/20—Olefin oligomerisation or telomerisation
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F2410/00—Features related to the catalyst preparation, the catalyst use or to the deactivation of the catalyst
    • C08F2410/04—Dual catalyst, i.e. use of two different catalysts, where none of the catalysts is a metallocene
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/10—Lubricating oil

Definitions

  • the invention relates to the technical field of poly-alpha-olefin synthetic oil base oil, in particular to a catalyst composition for alpha-olefin polymerization and its preparation and application.
  • Poly ⁇ -olefin (PAO) synthetic oil is the best synthetic lubricating oil base oil at present, with high viscosity index, low volatility, low fluidity, good shear performance and excellent high temperature oxidation resistance; Compared with other mineral lubricating base oils (I, II, III base oils), PAO has the characteristics of small evaporation loss, good stability, wide operating temperature range, good compatibility with common materials and non-toxicity. , industry and other civil industries are widely used, and it is the main source of high-grade lubricating base oils used in aviation, aerospace, military and other industries.
  • PAO is generally a class of branched saturated oligomers catalyzed by C 6 -C 20 ⁇ -olefins.
  • Catalytic polymerization of alpha-olefins is a known technique for the preparation of PAO synthetic lubricating oils.
  • catalyst systems for the preparation of PAO are commonly used BF 3 system, Cr system, Al compound system, Ziegler-Natta, metallocene, and ionic liquid.
  • the selection of different types of catalysts has a significant impact on the yield of the polymer, the control of the degree of polymerization and the performance of the product.
  • the PAO synthetic oil prepared by Lewis acid catalyst has high yield and narrow molecular weight distribution. Therefore, BF 3 and initiator are selected as the catalytic system for preparing low-viscosity poly ⁇ -olefin synthetic oil base oil.
  • PAO low-viscosity PAO
  • the products are mainly trimers, tetramers, and pentamers, and the product distribution is narrow. It is an ideal component with a viscosity range of 4-6cSt.
  • straight-chain alkanes have high viscosity index, but poor low temperature performance, and only have a certain degree of isomerization, that is, reasonable isomerized alkanes are ideal components of lubricating oil. Therefore, by selecting a suitable cationic catalytic system, in the presence of catalytic active centers, a certain degree of isomerization occurs, and PAO base oils with excellent comprehensive properties can be obtained.
  • US3763244 discloses a method for preparing lubricating oil base oil by using BF 3 /water system to catalyze C 6 -C 16 ⁇ -olefins. Under the condition of reaction temperature of 10-60 ° C, water is used as an initiator, wherein water and trifluoroboron are used. The molar ratio of the catalyst system is excessive, and the product under the action of the catalyst system has a low pour point and a high viscosity index.
  • US5191140A uses boron trifluoride as the main catalyst, water or alcohols and acetic anhydride as cocatalysts, and through the polymerization of olefins, a product with a kinematic viscosity of 3.58 cSt at 100°C and a viscosity index of 125 is obtained, and the olefin conversion rate is 76.8%.
  • the method can improve the yield of low-viscosity olefin oligomer, and improve the production efficiency by shortening the reaction time.
  • US3742082A discloses a method for catalyzing ⁇ -olefin with BF3 as the main catalyst and phosphoric acid or water as the co-catalyst.
  • Base oil products have lower pour points.
  • the above patent uses water as a co-catalyst, which has good product performance and catalytic efficiency, and reduces production costs, but is particularly prone to corrosion problems, so it is necessary to improve the corrosion resistance grade of materials, which will greatly increase the investment cost of the device. Therefore, this type of method Not suitable for mass production.
  • CN1274725C provides that in the presence of BF catalyst and alcohol cocatalyst, oligomerization occurs at a temperature of 20°C to 60°C to obtain a kinematic viscosity of 4 to 6 cSt at 100°C, a Noack weight loss of 4 to 9%, and a viscosity index of 4 to 9%.
  • CN101883838A uses C8- C12 ⁇ -olefin as raw material, carries out polymerization with boron trifluoride-butanol catalyst, then separates unreacted raw material and dimer, and the vacuum fraction is used as base oil after hydrorefining, and the product
  • the 100°C kinematic viscosity is 5 mm 2 /s
  • the pour point is below -50°C
  • the viscosity at -40°C is below 3000 cSt.
  • CN105925340A uses BF 3 as catalyst alcohols or alkyl esters as cocatalysts, uses decene-1 and dodecene-1 as raw materials, the ratio of decene-1 and dodecene-1 is 7:3, the reaction is in Under the conditions of 18°C and 0.2MPa, the co-initiator is ethanol: ethyl acetate ratio is 12:1, the 100°C kinematic viscosity of the oligomerization product is 4mm 2 /s, the pour point is less than -60°C, but the product yield is insufficient 80%.
  • CN101054332A adopts boron trifluoride as catalyst and alcohol as initiator, and the alcohol is methanol, ethanol, propanol, butanol or amyl alcohol, wherein the weight ratio of initiator dosage and raw material olefin is 0.01-1.0%, BF 3 The weight ratio of the amount to the raw material olefin is 1-5%.
  • the invention proposes a novel proton-type co-catalyst for the boron trifluoride catalytic system, develops a catalyst composition for ⁇ -olefin polymerization, and realizes the directional polymerization of ⁇ -olefin. , the target product selectivity is high.
  • the first object of the present invention is to provide a catalyst composition for ⁇ -olefin polymerization.
  • the second object of the present invention is to provide a preparation method of the catalyst composition for the polymerization of ⁇ -olefin.
  • the third object of the present invention is to provide an application of the catalyst composition for the polymerization of ⁇ -olefin.
  • a first aspect of the present invention provides a catalyst composition for ⁇ -olefin polymerization, the catalyst composition comprising boron trifluoride and at least one proton-type cocatalyst;
  • n is selected from the integer of 1-10;
  • X is selected from nitro (-NO 2 ), halogen, cyano (-CN), sulfonic acid (-SO 3 H), aldehyde (-CHO), acyl (-COR, R is an alkyl group), carboxyl (- -COOH) and amino ( -NH2 ).
  • the cationic polymerization of long-chain ⁇ -olefins goes through five steps: catalyst complexation, initiation, chain extension, chain transfer and chain termination.
  • the carbocation desorption ability affects the acidity of the active center and the yield of the reaction product; the stability of the carbocation intermediate affects the polymerization regularity.
  • the catalyst composition provided by the invention is used to prepare low-viscosity PAO synthetic oil base oil.
  • a proton-type co-catalyst is introduced to form a composite catalytic system with the main catalyst.
  • the effect affects the dissociation ability of carbocations (that is, the ability to release H + ), thereby adjusting the acidity of the catalytic system, improving the stability of the active center, controlling the degree of product isomerism, and solving the problem of regular polymerization of long-chain ⁇ -olefin molecules in the active site.
  • to achieve narrow molecular weight oligomerization of ⁇ -olefins improve the selectivity of target products, and prepare low-viscosity PAO products with excellent viscosity-temperature properties and low-temperature properties.
  • the structure of the proton-type cocatalyst finally selected in the present invention includes both a hydroxyl group and another functional group X, and the X group can specifically be a nitro group, a halogen group, a cyano group, a sulfonic acid group, an aldehyde group, an acyl group, a carboxyl group and Amino groups can adjust the acidity of the catalytic system through the heteroatom-induced effect, thereby affecting the dissociation ability of carbocations and H + .
  • the acyl group is -COR, wherein R is an alkyl group, preferably a methyl group.
  • the halogen includes fluorine (-F), chlorine (-Cl), bromine (-Br) and iodine (-I).
  • the molar ratio of the boron trifluoride to the proton-type cocatalyst is 0.1-3.0, preferably 0.5-2.0, more preferably 0.8-1.5.
  • the protic co-catalyst is selected from 2-nitroethanol, 3-nitropropanol, 2-chloroethanol, 3-chloro-1-propanol, 4-chloro- 1-butanol, 5-chloro-1-pentanol, 6-chloro-1-hexanol, 7-chloro-1-heptanol, 8-chloro-1-octanol, 9-chloro-1-nonanol, 10-Chloro-1-decanol, 2-fluoroethanol, 3-fluoro-1-propanol, 4-fluoro-1-butanol, 5-fluoro-1-pentanol, 6-fluoro-1-hexanol, 7-Fluoro-1-heptanol, 8-fluoro-1-octanol, 9-fluoro-1-nonanol, 10-fluoro-1-decanol, 2-bromoethanol, 3-bromo
  • the protic co-catalyst is selected from 4-fluoro-1-butanol, 3-chloro-1-propanol, 3-iodo-1-propanol, 4-bromo- 1-Butanol, 6-hydroxyhexanoic acid, 3-nitropropanol, 2-hydroxyethanesulfonic acid, 4-hydroxybutanesulfonic acid, 6-hydroxy-2-hexanone, 5-hydroxyvaleraldehyde, 8-hydroxy One or a combination of two or more of caprylic acid and 10-hydroxydecanoic acid.
  • X in the protic co-catalyst is selected from halogen and carboxyl group.
  • the protic co-catalyst is selected from one or a combination of two or more selected from 4-fluoro-1-butanol, 4-bromo-1-butanol and 8-hydroxyoctanoic acid , the molar ratio of the boron trifluoride to the proton-type co-catalyst is 1-1.2.
  • a second aspect of the present invention provides a preparation method of the above catalyst composition, the preparation method comprising: mixing the proton-type co-catalyst and the main catalyst boron trifluoride, and reacting at a predetermined temperature for a predetermined time to obtain the catalyst combination thing.
  • the process of mixing the proton-type co-catalyst and boron trifluoride includes: firstly using nitrogen to thermally purge the catalyst to prepare a reactor, and after nitrogen purging, adding the proton type co-catalyst, start stirring at the same time, raise the temperature to a predetermined temperature, and add boron trifluoride in proportion.
  • the catalyst preparation reactor is a closed container, which is thermally purged with nitrogen to remove water and oxygen.
  • the predetermined temperature is -30°C to 50°C, preferably -10°C to 30°C.
  • the predetermined time is 0.5h-4.0h, preferably 0.5h-3.0h.
  • the proton-type cocatalyst is purified.
  • the refining treatment includes but is not limited to distillation, adsorbent removal methods, etc., and the water content of the proton-type cocatalyst after the refining treatment is less than 100 ppm.
  • the preparation method comprises: firstly using nitrogen to thermally purge the catalyst to prepare a reaction kettle for 5 min to 10 min, after nitrogen purging, adding the refined proton-type cocatalyst, simultaneously starting stirring, and controlling the temperature to be -30°C to 50°C; After adding boron trifluoride and reacting for 0.5h-4.0h, the catalyst composition is obtained.
  • the third aspect of the present invention provides an application of the above-mentioned catalyst composition in synthesizing a poly-alpha-olefin synthetic oil base oil, that is, a preparation method of a poly-alpha-olefin synthetic oil base oil by using the above-mentioned catalyst composition.
  • the application comprises the following steps:
  • the raw material ⁇ -olefin is added to the kettle type polymerization reactor, the catalyst composition is continuously added to the kettle type polymerization reactor, the reaction temperature is controlled to be 20°C to 50°C (preferably 25°C), and the residence time is 20min to 100min. (preferably 60 min); after the reaction is completed, the catalyst is separated, and the poly- ⁇ -olefin synthetic oil base oil is obtained after hydrogenation.
  • the added amount of the catalyst composition is 0.1%-2.0% of the mass of the raw material ⁇ -olefin.
  • the catalyst composition of the present invention can be used for producing poly-alpha-olefin synthetic oil base oil, especially suitable for preparing low-viscosity poly-alpha-olefin synthetic oil base oil, and the obtained polymerization products mainly include dimer, trimer, tetramer Among them, by adjusting the ratio of Lewis acid and proton-type cocatalyst, unexpected test results were obtained, and the chromatographic analysis of trimers and tetramers can reach more than 90%.
  • poly ⁇ -olefin synthetic oil The base oil had a viscosity of 4.02 mm 2 /s, a viscosity index of 132, and a pour point ⁇ -60°C.
  • the present invention provides a catalyst composition that can be used to prepare a low-viscosity poly-alpha-olefin synthetic oil base oil for the deficiencies in the existing catalytic system, and its advantages are mainly reflected in:
  • the catalyst composition of the present invention introduces a proton-type co-catalyst, which forms a composite catalytic system with the main catalyst, and affects the carbocation and H + dissociation ability through the heteroatom-induced effect in the proton-type co-catalyst, and then adjusts the
  • the catalytic system is acidic, improves the stability of the active center, controls the degree of product isomerization, solves the problem of difficult regular polymerization of long-chain ⁇ -olefin molecules at the active site, realizes narrow molecular weight oligomerization of ⁇ -olefin, and improves the selectivity of target products.
  • the poly ⁇ -olefin synthetic oil base oil obtained by using the catalyst composition of the present invention has a relatively high viscosity index, good quality and relatively high yield of the target product.
  • Fig. 1 is the carbon nuclear magnetic spectrum of the boron trifluoride-4-fluoro-1-butanol complex prepared in Example 1.
  • Fig. 2 is the carbon nuclear magnetic spectrum of the boron trifluoride-3-chloro-1-propanol complex prepared in Example 2.
  • Fig. 3 is the hydrogen nuclear magnetic spectrum of the boron trifluoride-3-chloro-1-propanol complex prepared in Example 2.
  • Fig. 4 is the carbon nuclear magnetic spectrum of the boron trifluoride-hydroxyacetic acid complex prepared in Example 6.
  • Figure 5 is a gas chromatogram of the product obtained from the catalyst composition of Example 1.
  • Figure 6 is a gas chromatogram of the product obtained from the catalyst composition of Comparative Example 3.
  • the cocatalysts in the following examples are all obtained through commercial purchase, and have been refined to remove impurities and moisture therein as much as possible.
  • the specific refining treatment includes, but is not limited to, conventional techniques such as rectification or physical adsorption, and the water content of the proton-type cocatalyst after the refining treatment is less than 100 ppm.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst 4-fluoro-1-butanol (1 mol) was added. At the same time, the stirring was started, the temperature was raised to 50 °C, and the main catalyst was added in proportion.
  • Catalyst boron trifluoride the molar ratio of main catalyst and co-catalyst is 0.1:1, after 0.5h of reaction, the prepared polymerization catalyst (boron trifluoride-4-fluoro-1-butanol complex) is obtained and stored stand-by.
  • TMS tetramethylsilane
  • D 2 O D 2 O
  • NOVA 400MHz nuclear magnetic resonance instrument was set to adjust the relevant parameters of the instrument, and the obtained boron trifluoride-4-fluoro-1-butanol was analyzed.
  • the complex was characterized by 13 C NMR, and the carbon nuclear magnetic spectrum was obtained as shown in Figure 1.
  • the ⁇ -C atoms move towards the lower field and the higher ⁇ value, while the change trend of the ⁇ -C atoms is the opposite.
  • the main catalyst BF 3 molecule itself has a strong electron-withdrawing induction effect.
  • BF 3 also attracts electrons as much as possible to adjacent atoms (C atom and H atom on ⁇ -C).
  • the electron-withdrawing induction effect is produced, resulting in the enhancement of the deshielding effect of the corresponding atoms, the decrease of the electron cloud density, and the ⁇ value shows a shift to the low-field and high-displacement direction.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst 3-chloro-1-propanol (1 mol) was added. At the same time, stirring was started, the temperature was raised to 40 °C, and Lewis was added in proportion. Acid main catalyst boron trifluoride, the molar ratio of main catalyst and co-catalyst is 0.5, after 0.8h of reaction, the prepared polymerization catalyst (boron trifluoride-3-chloro-1-propanol complex) is obtained and stored stand-by.
  • TMS tetramethylsilane
  • D 2 O D 2 O
  • NOVA 400MHz nuclear magnetic resonance instrument was set to adjust the relevant parameters of the instrument.
  • the compound was characterized by 1 H NMR and 13 C NMR, as shown in Figure 2 and Figure 3 .
  • the ⁇ values of the ⁇ -C, ⁇ -C, and ⁇ -C atoms of the boron trifluoride-3-chloro-1-propanol complex are located at 59.1 ppm, 41.3 ppm, and 35.4 ppm, respectively.
  • the carbon nuclear magnetic spectra of the catalyst compositions in Example 4 and Example 8 are similar to this spectrum, except that ⁇ -C and ⁇ -C have certain shifts.
  • the electron-withdrawing ability of the terminal group is enhanced, and the ⁇ -C atoms move to the direction of low field and high ⁇ value, while the change trend of ⁇ -C atoms is the opposite.
  • the ⁇ of the hydrogen protons in the ⁇ -CH 2 -, ⁇ -CH 2 - and ⁇ -CH 2 - groups of the boron trifluoride-3-chloro-1-propanol complexes are respectively in the range of 3.83ppm ⁇ 3.85ppm, 2.05ppm ⁇ 2.08ppm and 3.62ppm ⁇ 3.66ppm.
  • Boron trifluoride has an electron-withdrawing induction effect on the hydrogen protons (2.19 ppm, alcoholic hydroxyl hydrogen proton peak) on the 3-chloro-1-propanol ligand, which enhances the deshielding effect of the respective hydrogen atoms and reduces the electron cloud density. , the corresponding hydrogen atoms move to the direction of low field and high ⁇ value.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 minutes. After purging with nitrogen, the refined cocatalyst 4-chloro-1-butanol (1 mol) was added.
  • the catalyst is boron trifluoride, the molar ratio of the main catalyst and the co-catalyst is 0.8, and after the reaction for 1.0 h, the prepared polymerization catalyst is obtained, which is stored for later use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst 3-iodo-1-propanol (1 mol) was added.
  • the catalyst aluminum trichloride the molar ratio of the main catalyst to the co-catalyst is 1.0, and after the reaction for 1.5 hours, the prepared polymerization catalyst is obtained, which is stored for later use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst 4-bromo-1-butanol (1 mol) was added. At the same time, the stirring was started, the temperature was raised to 10 °C, and the main catalyst was added in proportion.
  • the catalyst is boron trifluoride, the molar ratio of the main catalyst to the co-catalyst is 1.5, and after 2.0 hours of reaction, the prepared polymerization catalyst is obtained, which is stored for later use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst glycolic acid (1 mol) was added. At the same time, the stirring was turned on, the circulating cooler was turned on, the temperature was controlled to 0 °C, and the main catalyst was added in proportion. Sulfur trioxide, the molar ratio of the main catalyst to the co-catalyst is 2.0, and after 2.5 hours of reaction, the prepared polymerization catalyst (boron trifluoride-glycolic acid complex) is obtained, which is stored for later use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by gas-heat purging catalyst for 10 min. After purging with nitrogen, the refined cocatalyst 6-hydroxyhexanoic acid (1 mol) was added. At the same time, the stirring was turned on, the circulating cooler was turned on, and the temperature was controlled to -10 °C in proportion to Ferric bromide, a main catalyst, was added, and the molar ratio of the main catalyst to the co-catalyst was 2.5. After 3.0 hours of reaction, the prepared polymerization catalyst was obtained, which was stored for later use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst 3-nitropropanol (1 mol) was added. At the same time, the stirring was turned on, the circulating cooler was turned on, and the temperature was controlled to -10°C. The main catalyst boron trifluoride is added in proportion, and the molar ratio of the main catalyst to the co-catalyst is 3.0. After 4.0 hours of reaction, the prepared polymerization catalyst is obtained, which is stored for later use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst 2-hydroxyethanesulfonic acid (1 mol) was added. At the same time, the stirring was turned on, the circulating cooler was turned on, and the temperature was controlled to -20°C, The main catalyst boron trifluoride is added in proportion, and the molar ratio of the main catalyst to the co-catalyst is 2.0. After 1.0 h of reaction, the prepared polymerization catalyst is obtained, which is stored for later use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 minutes. After purging with nitrogen, the refined cocatalyst 4-hydroxybutanesulfonic acid (1 mol) was added. At the same time, the stirring was turned on, the circulating cooler was turned on, and the temperature was controlled to -30°C, The main catalyst boron trifluoride is added in proportion, and the molar ratio of the main catalyst to the co-catalyst is 0.5. After 2.0 hours of reaction, the prepared polymerization catalyst is obtained, which is stored for later use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst 6-hydroxy-2-hexanone (1 mol) was added. At the same time, the stirring was turned on, the circulating cooler was turned on, and the temperature was controlled to -10 °C, the main catalyst boron trifluoride is added in proportion, and the molar ratio of the main catalyst to the co-catalyst is 1.5. After 0.7 hours of reaction, the prepared polymerization catalyst is obtained and stored for use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst 5-hydroxyvaleraldehyde (1 mol) was added, stirring was started, the circulating cooler was turned on, and the temperature was controlled to -30°C, and the The main catalyst boron trifluoride is added in a proportion, and the molar ratio of the main catalyst to the co-catalyst is 0.6. After 1.0 h of reaction, the prepared polymerization catalyst is obtained, which is stored for later use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst 8-hydroxyoctanoic acid (1 mol) was added. At the same time, the stirring was turned on, the circulating cooler was turned on, and the temperature was controlled to -20°C in proportion to The main catalyst boron trifluoride is added, and the molar ratio of the main catalyst to the co-catalyst is 1.2. After 2.0 hours of reaction, the prepared polymerization catalyst is obtained, which is stored for later use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst 10-hydroxydecanoic acid (1 mol) was added, stirring was started at the same time, the temperature was controlled to 10 °C, and the main catalyst trifluorocarbon was added in proportion. Boronide, the molar ratio of the main catalyst to the co-catalyst is 0.5, and after 4.0 hours of reaction, the prepared polymerization catalyst is obtained, which is stored for later use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 minutes. After purging with nitrogen, the purified cocatalysts 4-fluoro-1-butanol (0.5mol) and 6-hydroxy-hexanoic acid (0.5mol) (4-fluoro-1-butanol) were added. -1-butanol and 6-hydroxy-hexanoic acid in a molar ratio of 1:1), start stirring at the same time, control the temperature to 10 ° C, add the main catalyst boron trifluoride in proportion, and the molar ratio of the main catalyst to the co-catalyst is 0.6, After the reaction for 3.0 hours, the prepared polymerization catalyst was obtained and stored for later use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalysts 3-nitropropanol (1 mol) and 4-hydroxybutanesulfonic acid (0.5 mol) (3-nitropropanol and 4-Hydroxybutanesulfonic acid molar ratio 2:1), at the same time start stirring, control the temperature to 10 ° C, add the main catalyst boron trifluoride in proportion, the molar ratio of the main catalyst to the co-catalyst is 1.0, after the reaction for 2.0h, The prepared polymerization catalyst is obtained and stored for use.
  • the present embodiment prepares a catalyst composition, which specifically includes the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the purified cocatalysts 5-hydroxyvaleraldehyde (1mol), 10-hydroxydecanoic acid (1mol) and 4-chloro-1-butanol ( 1mol) (5-hydroxyvaleraldehyde, 10-hydroxydecanoic acid and 4-chloro-1-butanol molar ratio 1:1:1), open stirring simultaneously, control the temperature to 20 ° C, add the main catalyst trifluorocarbon in proportion Boronide, the molar ratio of the main catalyst to the co-catalyst is 0.8, and after the reaction for 4.0 hours, the prepared polymerization catalyst is obtained, which is stored for later use.
  • This comparative example prepares a kind of catalyst composition, specifically comprises the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst 4-fluoro-1-butanol (1 mol) was added, stirring was started at the same time, the temperature was controlled at 50 °C, and the main catalyst was added in proportion With boron trifluoride, the molar ratio of the main catalyst to the co-catalyst is 4.0, and after the reaction for 0.5 h, the prepared polymerization catalyst is obtained, which is stored for later use.
  • This comparative example prepares a kind of catalyst composition, specifically comprises the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst 4-fluoro-1-butanol (1 mol) was added, stirring was started at the same time, the temperature was controlled at 50 °C, and the main catalyst was added in proportion Boron trifluoride, the molar ratio of the main catalyst to the co-catalyst is 0.05, and after the reaction for 0.5 h, the prepared polymerization catalyst is obtained, which is stored for later use.
  • This comparative example prepares a kind of catalyst composition, specifically comprises the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst butanol (1 mol) was added, stirring was started at the same time, the temperature was controlled to 50 °C, the main catalyst boron trifluoride was added in proportion, The molar ratio of the catalyst to the co-catalyst was 0.1, and after the reaction for 0.5 h, the prepared polymerization catalyst was obtained, which was stored for later use.
  • This comparative example prepares a kind of catalyst composition, specifically comprises the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst isopropanol (1 mol) was added, and stirring was started at the same time.
  • the molar ratio of the main catalyst to the co-catalyst was 0.1, and after the reaction for 0.5 h, the prepared polymerization catalyst was obtained, which was stored for later use.
  • This comparative example prepares a kind of catalyst composition, specifically comprises the following steps:
  • the reactor was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined co-catalyst acetic acid (1 mol) was added, and stirring was started at the same time.
  • the molar ratio to the co-catalyst is 0.1, and after the reaction for 0.5 h, the prepared polymerization catalyst is obtained, which is stored for later use.
  • This comparative example prepares a kind of catalyst composition, specifically comprises the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the purified cocatalyst deionized water (1 mol) was added, and stirring was started at the same time. The molar ratio of the main catalyst to the co-catalyst was 0.1, and after the reaction for 0.5 h, the prepared polymerization catalyst was obtained, which was stored for later use.
  • This comparative example prepares a kind of catalyst composition, specifically comprises the following steps:
  • the reactor was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst ethyl acetate (1 mol) was added, and stirring was started at the same time. The molar ratio of the main catalyst to the co-catalyst was 0.1, and after the reaction for 0.5 h, the prepared polymerization catalyst was obtained, which was stored for later use.
  • This comparative example prepares a kind of catalyst composition, specifically comprises the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 minutes. After purging with nitrogen, the refined cocatalyst phosphoric acid (1 mol) was added, and stirring was started at the same time. The molar ratio to the co-catalyst is 0.1, and after the reaction for 0.5 h, the prepared polymerization catalyst is obtained, which is stored for later use.
  • This comparative example prepares a kind of catalyst composition, specifically comprises the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined cocatalyst dimethyl ether (1 mol) was added, and stirring was started at the same time. The temperature was controlled to 50 °C, and the main catalyst boron trifluoride was added in proportion. , the molar ratio of the main catalyst to the co-catalyst is 0.1, and the prepared polymerization catalyst is obtained after the reaction for 0.5 h, which is stored for later use.
  • This comparative example prepares a kind of catalyst composition, specifically comprises the following steps:
  • the reaction kettle was prepared by thermally purging the catalyst with nitrogen for 10 min. After purging with nitrogen, the refined co-catalyst acetone (1 mol) was added, and stirring was started at the same time.
  • the molar ratio to the co-catalyst is 0.1, and after the reaction for 0.5 h, the prepared polymerization catalyst is obtained, which is stored for later use.
  • Example 10 0.5 2.3 52.2 39.6 1.6 3.8 91.8
  • Example 11 0.2 1.2 56.5 36.3 4.8 1.0 92.8
  • Example 12 0.1 5.5 50.2 40.0 1.0 3.2 90.2
  • Example 13 0.4 2.2 52.3 39.0 2.7 3.4 91.3
  • Example 14 0.6 2.3 52.6 38.2 1.3 0.2 90.8
  • Example 15 0.9 0.8
  • Lewis acid is used as the main catalyst, 4-fluoro-1-butanol, 3-chloro-1-propanol, 4-chloro-1-butanol, 3- Iodo-1-propanol, 4-bromo-1-butanol, glycolic acid, 6-hydroxy-hexanoic acid, 3-nitropropanol, 4-amino-1-butanol, 4-hydroxybutanesulfonic acid, 6 -Hydroxy-2-hexanone, 5-hydroxyvaleraldehyde, 8-hydroxyoctanoic acid and 10-hydroxydecanoic acid were used as cocatalysts respectively.
  • the kinematic viscosity of the obtained base oil at 100°C was 4-10mm 2 /s, and the viscosity index was greater than 130 , the target product (C 30 +C 40 ) is much higher than the comparative examples 3-10 (using conventional butanol, isopropanol, acetic acid, deionized water, ethyl acetate, phosphoric acid or dimethyl ether acetone as cocatalysts).
  • the inlet temperature is 250 °C
  • the detector temperature is 400 °C
  • the vaporization chamber temperature is 450 °C
  • the split ratio is 100:1
  • the temperature program is adopted: the initial temperature is 50 °C, and the temperature is maintained for 10 min; then the temperature is increased at a heating rate of 9 °C/min to the end temperature. 380°C for 10min.
  • Example 1 By comparing Example 1 and Comparative Examples 1 and 2, it can be known that within the molar ratio range of the main catalyst and the co-catalyst provided by the present invention, a target product with good product performance and high selectivity can be obtained.
  • the catalyst composition prepared in Example 1 was used to test the performance of other ⁇ -olefins as raw materials.
  • the specific process was as follows: using 1-octene, 1-dodecene, and coal-to- ⁇ -olefins as raw materials, firstly The raw materials are injected into the kettle-type polymerization reactor, and the catalyst composition prepared in Example 1 is continuously added to the polymerization reactor, wherein the amount of the catalyst composition is 1.0wt. ⁇ (accounting for the mass fraction of the ⁇ -olefin raw material), The reaction temperature was controlled at 25 °C, and the residence time was 60 min. After the reaction, the catalyst was separated, and the product was obtained after hydrogenation, and the product was collected for chromatographic analysis and performance test. The results are shown in Table 3.
  • the catalyst composition of the present invention is suitable for the polymerization of various ⁇ -olefins (1-octene, 1-dodecene, coal-made ⁇ -olefin), and the viscosity-temperature properties of the obtained polymerization products are similar to Low temperature performance is better.

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Abstract

本发明公开了一种α-烯烃聚合的催化剂组合物及其制备与应用。该催化剂组合物包括三氟化硼和至少一种质子型助催化剂；所述质子型助催化剂的结构通式为：X-(CH 2) n-OH，式中，n选自1-10的整数；X选自硝基、卤素、氰基、磺酸基、醛基、酰基、羧基和氨基。该催化剂可用于生产聚α-烯烃合成油基础油，特别适合用于低黏度聚α-烯烃合成油基础油，目标产品选择性高。

Description

一种α-烯烃聚合的催化剂组合物及其制备与应用 技术领域
本发明涉及聚α-烯烃合成油基础油技术领域，具体涉及一种α-烯烃聚合的催化剂组合物及其制备与应用。
背景技术
聚α-烯烃(PAO)合成油是目前性能最佳的合成润滑油基础油，具有高黏度指数、低挥发性、低流动性、较好的剪切性能及优良的抗高温氧化性；与传统的矿物润滑油基础油(Ⅰ、Ⅱ、Ⅲ类基础油)相比，PAO具有蒸发损失小、稳定性好，使用温度范围宽、与普通材料相容性好及无毒等特点，不仅在汽车、工业等民用行业应用广泛，更是航空、航天、军工等行业所用高档润滑油基础油的主要来源。
PAO一般是由C 6-C 20的α-烯烃催化低聚合成的一类带有支链饱和的低聚物。α-烯烃的催化聚合是制备PAO合成润滑油的已知技术。一般来说，制备PAO的催化剂体系常用的有BF 3体系、Cr体系、Al化合物体系、Ziegler-Natta、茂金属以及离子液体等。选用不同类型的催化剂，对聚合物的收率、聚合度控制以及产品的性能有明显的影响。路易斯酸型催化剂制备的PAO合成油收率高、分子量分布窄，因此，选用BF 3和引发剂作为制备低黏度聚α-烯烃合成油基础油的催化体系效果较好。
低黏度PAO采用BF 3催化体系生产时，产物中主要以三聚体、四聚体、五聚体为主，产物分布窄，是黏度范围4～6cSt的理想组分。同时，根据PAO结构与性能研究结果，直链烷烃的黏度指数高，但是低温性能差，只有具有一定异构化程度，即合理异构的烷烃是润滑油理想组分。因此，选用合适的阳离子催化体系，在催化活性中心的存在下，发生一定程度的异构，能够获取综合性能优异的PAO基础油。
US3763244公开了采用BF 3/水体系催化C 6～C 16的α-烯烃制备润滑油基础油的方法，在反应温度10-60℃的条件下，使用水作为引发剂，其中水与三氟硼化的摩尔比要过量，该催化剂体系作用下的产品具有低倾点和高黏度指数。US5191140A以三氟化硼作为主催化剂，水或醇类和乙酸酐为助催化剂，通过烯烃的聚合反应，得到100℃运动黏度为3.58cSt和黏度指数为125的产品，烯烃转化率为76.8％，该方法可以提高低黏度烯烃低聚物的产率，并且通过缩短反应时间来提高生产效率。US3742082A公开了一种以BF 3为主催化剂，磷酸或水为助催化剂催化α-烯烃的方法，催化剂与烯烃的摩尔比为0.005:1～0.1:1，反应温度为100～150℃，获得的基础油产品具有较低的倾点。上述 专利采用水为助催化剂，产品性能和催化效率均较好，并且降低了生产成本，但是特别容易带来腐蚀问题，从而需要提高材质耐腐蚀等级，会大幅增加装置投资成本，因此该类方法不适用于大规模生产。
在后续的催化剂技术开发中，也有一些基于BF 3为主催化剂，以醇类、醚类、酯类和酮类为助催化剂的相关报道，但醇类为助催化剂的文献居多。CN1274725C中提供了在BF 3催化剂及醇类助催化剂存在时，在温度20℃～60℃下发生低聚反应，得到100℃时运动黏度为4～6cSt，Noack失重为4～9％，黏度指数为130～145，倾点为-60℃～-50℃的聚α-烯烃基础油，经组成分析目标产品组分收率仅为70％。CN101883838A采用C 8～C 12的α-烯烃为原料，以三氟化硼-丁醇催化剂进行聚合，然后分离出未反应原料和二聚体，减压馏分经加氢精制后作为基础油，产品的100℃运动黏度为5mm 2/s，倾点低于-50℃，并且在-40℃的黏度低于3000cSt。CN105925340A以BF 3为催化剂醇类或烷基酯类为助催化剂，以癸烯-1和十二烯-1为原料，癸烯-1和十二烯-1的比例为7:3，反应在18℃、0.2MPa条件下，共引发剂为乙醇：乙酸乙酯的比例为12:1，齐聚产物的100℃运动黏度为4mm 2/s，倾点小于-60℃，但产品收率不足80％。CN101054332A采用三氟化硼为催化剂，醇为引发剂，所述的醇为甲醇、乙醇、丙醇、丁醇或戊醇，其中引发剂用量与原料烯烃的重量比为0.01～1.0％，BF 3用量与原料烯烃的重量比为1-5％。
传统用于生产低黏度PAO的催化体系，虽然产品的黏温性能和低温性能相对较好，但在聚合反应中路易斯酸催化剂和醇、酯、醚等助催化剂作用后，形成的低聚物产品异构程度不可控，产品的性能受工艺条件影响较大，产品稳定性差，另外黏度范围4～6cSt的理想组分选择性低。因此，为了解决上述问题，需要开发新型助催化剂，以期待提高目标产品(三聚体和四聚体)的选择性。
发明内容
本发明针对现有催化体系中存在的不足，针对三氟化硼催化体系提出了一种新型质子型助催化剂，开发了一种α-烯烃聚合的催化剂组合物，实现了α-烯烃的定向聚合，目标产品选择性高。
本发明的第一个目的在于提供一种α-烯烃聚合的催化剂组合物。
本发明的第二个目的在于提供一种所述α-烯烃聚合的催化剂组合物的制备方法。
本发明的第三个目的在于提供一种所述α-烯烃聚合的催化剂组合物的应用。
为了实现以上目的，本发明采用以下技术方案：
本发明第一方面提供一种α-烯烃聚合的催化剂组合物，该催化剂组合物包括三氟化 硼和至少一种质子型助催化剂；
所述质子型助催化剂的结构通式为：
X-(CH 2) n-OH
其中，n选自1-10的整数；
X选自硝基(-NO 2)、卤素、氰基(-CN)、磺酸基(-SO 3H)、醛基(-CHO)、酰基(-COR，R为烷基)、羧基(-COOH)和氨基(-NH 2)。
本发明在研发过程中设计选用了多种不同助催化剂，在试验过程中惊奇的发现，在同一分子中引入多种不同官能团，能够控制基础油的异构程度，提高目标产品(三聚体和四聚体)的选择性。
长链α-烯烃阳离子聚合反应经过催化剂络合、引发、链增长、链转移和链终止五个步骤。其中，碳正离子解析能力影响活性中心的酸性，影响反应产物收率；碳正离子中间体的稳定性影响聚合规整度。
采用本发明提供的催化剂组合物制备低黏度PAO合成油基础油，相比于传统催化体系，引入一种质子型助催化剂，与主催化剂构成复合催化体系，通过质子型助催化剂中的杂原子诱导效应影响碳正离子解离能力(即释放H +的能力)，进而调节催化体系酸性，改善活性中心稳定性，控制产品异构程度，解决了长链α-烯烃分子在活性位的规整聚合难题，实现α-烯烃窄分子量低聚，提高目标产物的选择性，制备出黏温性能和低温性能优异的低黏度PAO产品。
具体的，本发明最终选定的质子型助催化剂的结构中同时包括羟基和另一官能团X，X基团具体可以为硝基、卤素、氰基、磺酸基、醛基、酰基、羧基和氨基，通过杂原子诱导效应调节催化体系酸性，进而影响碳正离子、H +解离能力。
根据本发明的催化剂组合物，优选地，所述酰基为-COR，其中R为烷基，优选为甲基。
根据本发明的催化剂组合物，优选地，所述卤素包括氟(-F)、氯(-Cl)、溴(-Br)和碘(-I)。
根据本发明的催化剂组合物，优选地，所述三氟化硼与质子型助催化剂的摩尔比为0.1～3.0，优选为0.5～2.0，更优选0.8～1.5。
根据本发明的催化剂组合物，优选地，所述质子型助催化剂选自2-硝基乙醇、3-硝基丙醇、2-氯乙醇、3-氯-1-丙醇、4-氯-1-丁醇、5-氯-1-戊醇、6-氯-1-己醇、7-氯-1-庚醇、8-氯-1-辛醇、9-氯-1-壬醇、10-氯-1-癸醇、2-氟乙醇、3-氟-1-丙醇、4-氟-1-丁醇、5-氟-1-戊醇、6-氟-1-己醇、7-氟-1-庚醇、8-氟-1-辛醇、9-氟-1-壬醇、10-氟-1-癸醇、2-溴乙醇、 3-溴-1-丙醇、4-溴-1-丁醇、5-溴-1-戊醇、6-溴-1-己醇、7-溴-1-庚醇、8-溴-1-辛醇、9-溴-1-壬醇、10-溴-1-癸醇、2-碘乙醇、3-碘-1-丙醇、4-碘-1-丁醇、5-碘-1-戊醇、6-碘-1-己醇、7-碘-1-庚醇、8-碘-1-辛醇、9-碘-1-壬醇、10-碘-1-癸醇、3-羟基丙腈、4-羟基丁腈、2-羟乙基磺酸、3-羟基丙磺酸、4-羟基丁磺酸、羟乙醛、3-羟基丙醛、4-羟基丁醛、5-羟基戊醛、6-羟基己醛、8-羟基辛醛、6-羟基-2-己酮、5-羟基-2-己酮、羟基乙酸、3-羟基丙酸、4-羟基丁酸、6-羟基己酸、7-羟基庚酸、8-羟基辛酸、9-羟基壬酸、10-羟基癸酸、3-氨基-1-丙醇、4-氨基-1-丁醇、5-氨基-1-戊醇、6-氨基-1-己醇、7-氨基-1-庚醇、8-氨基-1-辛醇和10-氨基-1-癸醇中的一种或两种以上的组合。
根据本发明的催化剂组合物，优选地，所述质子型助催化剂选自4-氟-1-丁醇、3-氯-1-丙醇、3-碘-1-丙醇、4-溴-1-丁醇、6-羟基己酸、3-硝基丙醇、2-羟基乙磺酸、4-羟基丁磺酸、6-羟基-2-己酮、5-羟基戊醛、8-羟基辛酸和10-羟基癸酸中的一种或两种以上的组合。
根据本发明的催化剂组合物，优选地，所述质子型助催化剂中的X选自卤素和羧基。
根据本发明的催化剂组合物，优选地，所述质子型助催化剂选自4-氟-1-丁醇、4-溴-1-丁醇和8-羟基辛酸中的一种或两种以上的组合，所述三氟化硼与质子型助催化剂的摩尔比为1～1.2。
本发明第二方面提供一种上述催化剂组合物的制备方法，该制备方法包括：将所述质子型助催化剂和主催化剂三氟化硼混合，在预定温度进行反应预定时间，得到所述催化剂组合物。
根据本发明的制备方法，优选地，所述将所述质子型助催化剂和三氟化硼混合的过程包括：首先利用氮气热吹扫催化剂制备反应釜，经氮气吹扫后，加入所述质子型助催化剂，同时开启搅拌，将温度升至预定温度，按比例加入三氟化硼。所述催化剂制备反应釜为密闭容器，经氮气热吹扫以除水除氧。
根据本发明的制备方法，优选地，所述预定温度为-30℃至50℃，优选-10℃至30℃。
根据本发明的制备方法，优选地，所述预定时间为0.5h～4.0h，优选0.5h～3.0h。
根据本发明的制备方法，优选地，所述质子型助催化剂经过精制处理。
根据本发明的制备方法，优选地，所述精制处理包括但不限于蒸馏、吸附剂脱除方法等，精制处理后的质子型助催化剂的水含量小于100ppm。
该制备方法包括：首先利用氮气热吹扫催化剂制备反应釜5min～10min，经氮气吹扫后，加入精制好的质子型助催化剂，同时开启搅拌，控制温度为-30℃至50℃；按比例加入三氟化硼，反应0.5h～4.0h后，得到所述催化剂组合物。
本发明第三方面提供一种上述催化剂组合物在合成聚α-烯烃合成油基础油中的应用，即利用上述催化剂组合物进行的聚α-烯烃合成油基础油的制备方法。
根据本发明的应用，优选地，该应用包括以下步骤：
将原料α-烯烃加入釜式聚合反应器中，将所述催化剂组合物连续加入到所述釜式聚合反应器中，控制反应温度20℃～50℃(优选25℃)，停留时间20min～100min(优选60min)；反应结束后，分离出催化剂，加氢后得到所述聚α-烯烃合成油基础油。
根据本发明的应用，优选地，所述催化剂组合物的加入量为原料α-烯烃质量的0.1％-2.0％。
本发明的催化剂组合物可用于生产聚α-烯烃合成油基础油，特别适合用于制备低黏度聚α-烯烃合成油基础油，得到的聚合产物主要包括二聚体、三聚体、四聚体和五聚体，其中，通过调整路易斯酸和质子型助催化剂的比例，得到了意想不到的试验结果，色谱分析三聚体和四聚体可达到90％以上，另外聚α-烯烃合成油基础油的黏度为4.02mm 2/s，黏度指数为132，倾点＜-60℃。
与现有技术相比，本发明针对现有催化体系中存在的不足，提供可用于制备低黏度聚α-烯烃合成油基础油的催化剂组合物，其优势主要体现在：
(1)本发明的催化剂组合物引入了一种质子型助催化剂，与主催化剂构成复合催化体系，通过质子型助催化剂中的杂原子诱导效应影响碳正离子、H +解离能力，进而调节催化体系酸性，改善活性中心稳定性，控制产品异构程度，解决了长链α-烯烃分子在活性位的规整聚合难的问题，实现α-烯烃窄分子量低聚，提高目标产物的选择性。
(2)使用本发明催化剂组合物所得的聚α-烯烃合成油基础油，具有较高的黏度指数，品质好，目标产物收率较高。
附图说明
图1为实施例1制备得到的三氟化硼-4-氟-1-丁醇络合物的核磁碳谱图。
图2为实施例2制备得到的三氟化硼-3-氯-1-丙醇络合物的核磁碳谱图。
图3为实施例2制备得到的三氟化硼-3-氯-1-丙醇络合物的核磁氢谱图。
图4为实施例6制备得到的三氟化硼-羟基乙酸络合物的核磁碳谱图。
图5为实施例1催化剂组合物获得的产品气相色谱图。
图6为对比例3催化剂组合物获得的产品气相色谱图。
具体实施方式
为了更清楚地说明本发明，下面结合优选实施例对本发明做进一步的说明。本领域技术人员应当理解，下面所具体描述的内容是说明性的而非限制性的，不应以此限制本发明的保护范围。
本发明所有数值指定(例如温度、时间、浓度及重量等，包括其中每一者的范围)通常可是适当以0.1或1.0的增量改变(+)或(-)的近似值。所有数值指定均可理解为前面有术语“约”。
以下实施例中助催化剂均通过商业购买获得，并经过精制处理，以尽可能的去除其中的杂质和水分。具体的精制处理包括但不限于精馏或者物理吸附等常规工艺方法，精制处理后的质子型助催化剂的水含量小于100ppm。
实施例1
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂4-氟-1-丁醇(1mol)，同时开启搅拌，将温度升至50℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.1:1，反应0.5h后，得到制备好的聚合催化剂(三氟化硼-4-氟-1-丁醇络合物)，保存待用。
以四甲基硅烷(TMS)为内标物，D 2O为外标锁场溶剂，设置NOVA 400MHz型核磁共振仪调节仪器相关参数，对所得三氟化硼-4-氟-1-丁醇络合物进行 13C NMR表征，得到核磁碳谱如图1所示。
由图1可知，三氟化硼-4-氟-1-丁醇络合物的α-C、β-C、ω-C、γ-C原子的δ值分别位于61.6ppm、44.3ppm、28.4ppm、26.6ppm处。另外，实施例3、实施例5、实施例10中的催化剂组合物核磁碳谱与该谱图类似，不同之处在于α-C、β-C有一定位移。随着引入基团的吸电子能力增强，α-C原子向低场高δ值方向移动，而β-C原子的变化趋势与之相反。另外，主催化剂BF 3分子自身具有强烈的吸电子诱导效应，在形成B-O配位键时，BF 3为了尽可能地吸引电子，对临近的原子(α-C上的C原子与H原子)也产生了吸电子诱导效应，造成相应原子去屏蔽效应增强，电子云密度下降，其δ值表现为向低场高位移方向移动。
实施例2
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂 3-氯-1-丙醇(1mol)，同时开启搅拌，将温度升至40℃，按比例加入路易斯酸主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.5，反应0.8h后，得到制备好的聚合催化剂(三氟化硼-3-氯-1-丙醇络合物)，保存待用。
以四甲基硅烷(TMS)为内标物，D 2O为外标锁场溶剂，设置NOVA 400MHz型核磁共振仪调节仪器相关参数，对三氟化硼-3-氯-1-丙醇络合物进行 1H NMR与 13C NMR表征，如图2和图3所示。
由图2可知，三氟化硼-3-氯-1-丙醇络合物的α-C、β-C、ω-C原子的δ值分别位于59.1ppm、41.3ppm、35.4ppm处。另外，实施例4、实施例8中的催化剂组合物核磁碳谱与该谱图类似，不同之处在于α-C、β-C有一定位移。端位基团的吸电子能力增强，α-C原子向低场高δ值方向移动，而β-C原子的变化趋势与之相反。
由图3可知，三氟化硼-3-氯-1-丙醇络合物α-CH 2-、β-CH 2-、ω-CH 2-基团中氢质子的δ分别在3.83ppm～3.85ppm、2.05ppm～2.08ppm与3.62ppm～3.66ppm处。三氟化硼对3-氯-1-丙醇配体上的氢质子(2.19ppm，醇羟基氢质子峰)产生了吸电子诱导效应，使各自氢原子的去屏蔽效应增强，电子云密度降低，相应氢原子向低场高δ值方向移动。
实施例3
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂4-氯-1-丁醇(1mol)，同时开启搅拌，将温度升至30℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.8，反应1.0h后，得到制备好的聚合催化剂，保存待用。
实施例4
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂3-碘-1-丙醇(1mol)，同时开启搅拌，将温度升至20℃，按比例加入主催化剂三氯化铝，主催化剂与助催化剂的摩尔比为1.0，反应1.5h后，得到制备好的聚合催化剂，保存待用。
实施例5
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂4-溴-1-丁醇(1mol)，同时开启搅拌，将温度升至10℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为1.5，反应2.0h后，得到制备好的聚合催化剂，保存待用。
实施例6
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂羟基乙酸(1mol)，同时开启搅拌，打开循环冷却机，将温度控制为0℃，按比例加入主催化剂三氧化硫，主催化剂与助催化剂的摩尔比为2.0，反应2.5h后，得到制备好的聚合催化剂(三氟化硼-羟基乙酸络合物)，保存待用。
以四甲基硅烷(TMS)为内标物，D 2O为外标锁场溶剂，设置NOVA 400MHz型核磁共振仪调节仪器相关参数，对三氟化硼-羟基乙酸络合物进行 13C NMR表征，得到谱图如图4所示。
由图4可知，三氟化硼-羟基乙酸络合物的羧基位的碳原子和α-C的δ值分别位于177.1ppm和60.5ppm处。另外，实施例7、实施例9、实施例10、实施例13、实施例14中的催化剂组合物核磁碳谱与该谱图类似，均具有明显的羧基上的碳产生的谱峰，不同之处在于碳数不同，有多个仲碳产生的谱峰。
实施例7
本实施例制备一种催化剂组合物，具体包括以下步骤：
气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂6-羟基己酸(1mol)，同时开启搅拌，打开循环冷却机，将温度控制为-10℃，按比例加入主催化剂溴化铁，主催化剂与助催化剂的摩尔比为2.5，反应3.0h后，得到制备好的聚合催化剂，保存待用。
实施例8
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂3-硝基丙醇(1mol)，同时开启搅拌，打开循环冷却机，将温度控制为-10℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为3.0，反应4.0h后，得到制备好的聚合催化剂，保存待用。
实施例9
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂2-羟基乙磺酸(1mol)，同时开启搅拌，打开循环冷却机，将温度控制为-20℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为2.0，反应1.0h后，得到制备好的聚合催化剂，保存待用。
实施例10
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂4-羟基丁磺酸(1mol)，同时开启搅拌，打开循环冷却机，将温度控制为-30℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.5，反应2.0h后，得到制备好的聚合催化剂，保存待用。
实施例11
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂6-羟基-2-己酮(1mol)，同时开启搅拌，打开循环冷却机，将温度控制为-10℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为1.5，反应0.7h后，得到制备好的聚合催化剂，保存待用。
实施例12
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂5-羟基戊醛(1mol)，同时开启搅拌，打开循环冷却机，将温度控制为-30℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.6，反应1.0h后，得到制备好的聚合催化剂，保存待用。
实施例13
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂8-羟基辛酸(1mol)，同时开启搅拌，打开循环冷却机，将温度控制为-20℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为1.2，反应2.0h后，得到制备好的聚合催化剂，保存待用。
实施例14
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂10-羟基癸酸(1mol)，同时开启搅拌，将温度控制为10℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.5，反应4.0h后，得到制备好的聚合催化剂，保存待用。
实施例15
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂4-氟-1-丁醇(0.5mol)和6-羟基-己酸(0.5mol)(4-氟-1-丁醇和6-羟基-己酸摩尔比1:1)，同时开启搅拌，将温度控制为10℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.6，反应3.0h后，得到制备好的聚合催化剂，保存待用。
实施例16
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂3-硝基丙醇(1mol)和4-羟基丁磺酸(0.5mol)(3-硝基丙醇和4-羟基丁磺酸摩尔比比2:1)，同时开启搅拌，将温度控制为10℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为1.0，反应2.0h后，得到制备好的聚合催化剂，保存待用。
实施例17
本实施例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂5-羟基戊醛(1mol)、10-羟基癸酸(1mol)和4-氯-1-丁醇(1mol)(5-羟基戊醛、10-羟基癸酸和4-氯-1-丁醇摩尔比比1:1:1)，同时开启搅拌，将温度控制为20℃，按比例 加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.8，反应4.0h后，得到制备好的聚合催化剂，保存待用。
对比例1
本对比例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂4-氟-1-丁醇(1mol)，同时开启搅拌，温度控制为50℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为4.0，反应0.5h后，得到制备好的聚合催化剂，保存待用。
对比例2
本对比例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂4-氟-1-丁醇(1mol)，同时开启搅拌，温度控制为50℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.05，反应0.5h后，得到制备好的聚合催化剂，保存待用。
对比例3
本对比例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂丁醇(1mol)，同时开启搅拌，温度控制为50℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.1，反应0.5h后，得到制备好的聚合催化剂，保存待用。
对比例4
本对比例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂异丙醇(1mol)，同时开启搅拌，温度控制为50℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.1，反应0.5h后，得到制备好的聚合催化剂，保存待用。
对比例5
本对比例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂乙酸(1mol)，同时开启搅拌，温度控制为50℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.1，反应0.5h后，得到制备好的聚合催化剂，保存待用。
对比例6
本对比例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂去离子水(1mol)，同时开启搅拌，温度控制为50℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.1，反应0.5h后，得到制备好的聚合催化剂，保存待用。
对比例7
本对比例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂乙酸乙酯(1mol)，同时开启搅拌，温度控制为50℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.1，反应0.5h后，得到制备好的聚合催化剂，保存待用。
对比例8
本对比例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂磷酸(1mol)，同时开启搅拌，温度控制为50℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.1，反应0.5h后，得到制备好的聚合催化剂，保存待用。
对比例9
本对比例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂二甲基醚(1mol)，同时开启搅拌，温度控制为50℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.1，反应0.5h后，得到制备好的聚合催化剂，保存待用。
对比例10
本对比例制备一种催化剂组合物，具体包括以下步骤：
利用氮气热吹扫催化剂制备反应釜10min，经氮气吹扫后，加入精制好的助催化剂丙酮(1mol)，同时开启搅拌，温度控制为50℃，按比例加入主催化剂三氟化硼，主催化剂与助催化剂的摩尔比为0.1，反应0.5h后，得到制备好的聚合催化剂，保存待用。
催化剂性能评价试验：
以1-癸烯为原料，首先将原料打入到釜式聚合反应器中，分别将实施例1-17和对比例1-4中制备的催化剂组合物连续加入到聚合反应器中，其中催化剂组合物用量为1.0wt.‰(占1-癸烯原料的质量分数)，控制反应温度25℃，停留时间均为60min。反应结束后，分离出催化剂，加氢后得到产品，收集产品进行色谱分析和性能测试，结果如表1和表2所示。
表1各实施例和对比例中催化剂组合物的制备条件和对应获得的产品性能参数
Figure PCTCN2022070680-appb-000001
Figure PCTCN2022070680-appb-000002
表2各实施例和对比例的催化剂组合物制备获得的产品组成分布
编号 C 10 C 20 C 30 C 40 C 50 C 60以上 C 30+C 40
实施例1 1.5 4.4 57.3 33.5 1.4 1.9 90.8
实施例2 0.7 2.1 56.2 35.6 1.5 3.9 91.8
实施例3 2.2 1.7 54.3 36.3 4.3 1.2 90.6
实施例4 2.1 3.5 53.2 37.0 1.6 2.6 90.2
实施例5 1.0 2.2 58.8 31.9 2.7 3.4 90.7
实施例6 1.2 5.8 56.3 35.2 1.3 0.2 91.5
实施例7 0.9 5.2 55.9 34.3 0.9 2.8 90.2
实施例8 1.6 4.3 55.3 35.3 2.8 0.7 90.6
实施例9 0.1 4.4 57.3 34.9 1.4 1.9 92.2
实施例10 0.5 2.3 52.2 39.6 1.6 3.8 91.8
实施例11 0.2 1.2 56.5 36.3 4.8 1.0 92.8
实施例12 0.1 5.5 50.2 40.0 1.0 3.2 90.2
实施例13 0.4 2.2 52.3 39.0 2.7 3.4 91.3
实施例14 0.6 2.3 52.6 38.2 1.3 0.2 90.8
实施例15 0.9 0.8 51.6 38.4 0.9 0.7 90.0
实施例16 0.2 4.2 60.1 32.0 2.8 0.7 92.1
实施例17 0.3 2.1 50.6 39.4 1.6 6.0 90.0
对比例1 10.7 9.1 46.2 24.6 7.5 1.9 70.8
对比例2 8.6 8.3 44.5 24.3 6.5 7.8 68.8
对比例3 5.9 10.3 35.6 26.3 9.6 12.3 61.9
对比例4 6.2 14.3 39.2 24.3 5.9 10.1 63.5
对比例5 0.7 9.1 56.2 24.6 7.5 1.9 80.8
对比例6 3.8 10.8 34.8 32.9 6.9 10.8 67.7
对比例7 4.3 7.8 29.9 34.8 9.7 13.5 64.7
对比例8 2.5 8.5 40.1 29.9 10.7 8.3 70.0
对比例9 2.9 11.5 37.8 34.7 6.9 6.2 72.5
对比例10 3.5 9.9 40.8 33.2 8.9 3.7 74.0
由上述各实施例的产品性能参数和组成分布可知，以路易斯酸为主催化剂，4-氟-1-丁醇、3-氯-1-丙醇、4-氯-1-丁醇、3-碘-1-丙醇、4-溴-1-丁醇、羟基乙酸、6-羟基-己酸、3-硝基丙醇、4-氨基-1-丁醇、4-羟基丁磺酸、6-羟基-2-己酮、5-羟基戊醛、8-羟基辛酸和10-羟基癸酸分别作为助催化剂，所获得的基础油100℃运动黏度为4-10mm 2/s，黏度指数大于130，目标产品(C 30+C 40)远高于对比例3-10(采用常规丁醇、异丙醇、乙酸、去离子水、乙酸乙酯、磷酸或二甲基醚丙酮为助催化剂)。
对实施例1和对比例3中催化剂组合物下获得的产品进行气相色谱分析，结果如图5和图6所示，采用本发明的引发剂获得产物组成主要为C 30和C 40(图5中保留时间分别为15-17min，20-23min)，而丁醇为引发剂获得的产物组成分布较宽，如图6所示。色谱分析采用氢火焰离子化检测器，载气为氮气，柱前压为0.07MPa，氢气流速30mL/min，空气的流速250mL/min。进样口温度250℃，检测器温度400℃，汽化室温度450℃，分流比100:1，采用程序升温：初始温度50℃，保持10min；之后以9℃/min的升温速率升温至终止温度380℃，保持10min。
通过对比实施例1和对比例1和2可知，在本发明提供的主催化剂和助催化剂摩尔比范围内，能够获得良好的产品性能和高选择性的目标产品。
另外，采用实施例1制备的催化剂组合物进行了其他α-烯烃为原料的性能测试，具体过程如下：分别以1-辛烯、1-十二烯、煤制α-烯烃为原料，首先将原料打入到釜式聚合反应器中，将实施例1中制备的催化剂组合物连续加入到聚合反应器中，其中催化剂组合物用量为1.0wt.‰(占α-烯烃原料的质量分数)，控制反应温度25℃，停留时间均为60min。反应结束后，分离出催化剂，加氢后得到产品，收集产品进行色谱分析和性能测试，结果如表3所示。
由表3可知，本发明的催化剂组合物对于多种α-烯烃(1-辛烯、1-十二烯、煤制α-烯烃)的聚合反应均适用，且所得聚合产品的黏温性能和低温性能比较好。
表3不同α-烯烃原料对应获得的产品性能参数
Figure PCTCN2022070680-appb-000003
显然，本发明的上述实施例仅仅是为清楚地说明本发明所作的举例，而并非是对本 发明的实施方式的限定，对于所属领域的普通技术人员来说，在上述说明的基础上还可以做出其它不同形式的变化或变动，这里无法对所有的实施方式予以穷举，凡是属于本发明的技术方案所引伸出的显而易见的变化或变动仍处于本发明的保护范围之列。

Claims (20)

  1. 一种α-烯烃聚合的催化剂组合物，其中，该催化剂组合物包括三氟化硼和至少一种质子型助催化剂；
    所述质子型助催化剂的结构通式为：
    X-(CH 2) n-OH
    式中，n选自1-10的整数；
    X选自硝基、卤素、氰基、磺酸基、醛基、酰基、羧基和氨基。
  2. 根据权利要求1所述的催化剂组合物，其中，所述三氟化硼与质子型助催化剂的摩尔比为0.1～3.0。
  3. 根据权利要求1所述的催化剂组合物，其中，所述酰基的结构为-COR，R为烷基；优选地，R为甲基。
  4. 根据权利要求1所述的催化剂组合物，其中，所述质子型助催化剂选自2-硝基乙醇、3-硝基丙醇、2-氯乙醇、3-氯-1-丙醇、4-氯-1-丁醇、5-氯-1-戊醇、6-氯-1-己醇、7-氯-1-庚醇、8-氯-1-辛醇、9-氯-1-壬醇、10-氯-1-癸醇、2-氟乙醇、3-氟-1-丙醇、4-氟-1-丁醇、5-氟-1-戊醇、6-氟-1-己醇、7-氟-1-庚醇、8-氟-1-辛醇、9-氟-1-壬醇、10-氟-1-癸醇、2-溴乙醇、3-溴-1-丙醇、4-溴-1-丁醇、5-溴-1-戊醇、6-溴-1-己醇、7-溴-1-庚醇、8-溴-1-辛醇、9-溴-1-壬醇、10-溴-1-癸醇、2-碘乙醇、3-碘-1-丙醇、4-碘-1-丁醇、5-碘-1-戊醇、6-碘-1-己醇、7-碘-1-庚醇、8-碘-1-辛醇、9-碘-1-壬醇、10-碘-1-癸醇、3-羟基丙腈、4-羟基丁腈、2-羟乙基磺酸、3-羟基丙磺酸、4-羟基丁磺酸、羟乙醛、3-羟基丙醛、4-羟基丁醛、5-羟基戊醛、6-羟基己醛、8-羟基辛醛、6-羟基-2-己酮、5-羟基-2-己酮、羟基乙酸、3-羟基丙酸、4-羟基丁酸、6-羟基己酸、7-羟基庚酸、8-羟基辛酸、9-羟基壬酸、10-羟基癸酸、3-氨基-1-丙醇、4-氨基-1-丁醇、5-氨基-1-戊醇、6-氨基-1-己醇、7-氨基-1-庚醇、8-氨基-1-辛醇和10-氨基-1-癸醇中的一种或两种以上的组合。
  5. 根据权利要求1所述的催化剂组合物，其中，所述质子型助催化剂选自4-氟-1-丁醇、3-氯-1-丙醇、3-碘-1-丙醇、4-溴-1-丁醇、6-羟基己酸、3-硝基丙醇、2-羟基乙磺酸、4-羟基丁磺酸、6-羟基-2-己酮、5-羟基戊醛、8-羟基辛酸和10-羟基癸酸中的一种或两种以上的组合。
  6. 根据权利要求1所述的催化剂组合物，其中，X选自卤素和羧基。
  7. 根据权利要求6所述的催化剂组合物，其中，所述质子型助催化剂选自4-氟-1-丁醇、4-溴-1-丁醇和8-羟基辛酸中的一种或两种以上的组合。
  8. 根据权利要求1所述的催化剂组合物，其中，所述三氟化硼与质子型助催化剂的 摩尔比为0.5～2.0。
  9. 根据权利要求1所述的催化剂组合物，其中，所述三氟化硼与质子型助催化剂的摩尔比为0.8～1.5。
  10. 根据权利要求1所述的催化剂组合物，其中，所述质子型助催化剂选自4-氟-1-丁醇、4-溴-1-丁醇和8-羟基辛酸中的一种或两种以上的组合，所述三氟化硼与质子型助催化剂的摩尔比为1～1.2。
  11. 一种权利要求1-10任一项所述催化剂组合物的制备方法，其中，该制备方法包括：将所述质子型助催化剂和三氟化硼混合，在预定温度进行反应预定时间，得到所述催化剂组合物。
  12. 根据权利要求11所述的制备方法，其中，所述将所述质子型助催化剂和三氟化硼混合的过程包括：首先利用氮气热吹扫催化剂制备反应釜，经氮气吹扫后，加入所述质子型助催化剂，同时开启搅拌，将温度升至预定温度，按比例加入三氟化硼。
  13. 根据权利要求11所述的制备方法，其中，所述预定温度为-30℃至50℃，优选-10℃至30℃。
  14. 根据权利要求11所述的制备方法，其中，所述预定时间为0.5h～4.0h，优选0.5h～3.0h。
  15. 根据权利要求11所述的制备方法，其中，所述质子型助催化剂经过精制处理。
  16. 根据权利要求15所述的制备方法，其中，所述精制处理包括蒸馏和/或吸附剂脱除方法，精制处理后的质子型助催化剂的水含量小于100ppm。
  17. 根据权利要求11所述的制备方法，其中，该制备方法包括：首先利用氮气热吹扫催化剂制备反应釜5min～10min，经氮气吹扫后，加入精制好的质子型助催化剂，同时开启搅拌，控制温度为-30℃至50℃；按比例加入三氟化硼，反应0.5h～4.0h后，得到所述催化剂组合物。
  18. 权利要求1-9任一项所述催化剂组合物在合成聚α-烯烃合成油基础油中的应用。
  19. 根据权利要求18所述的应用，其中，该应用包括以下步骤：
    将原料α-烯烃加入釜式聚合反应器中，将所述催化剂组合物连续加入到所述釜式聚合反应器中，控制反应温度20℃～50℃，停留时间20min～100min；反应结束后，分离出催化剂，加氢后得到所述聚α-烯烃合成油基础油。
  20. 根据权利要求19所述的应用，其中，所述催化剂组合物的加入量为原料α-烯烃质量的0.1％-2.0％。
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Families Citing this family (1)

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Publication number Priority date Publication date Assignee Title
CN116920888B (zh) * 2023-07-20 2024-09-24 上海多纶化工有限公司 用于脂肪醇乙氧基化的酸性催化剂及其应用

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5068487A (en) * 1990-07-19 1991-11-26 Ethyl Corporation Olefin oligomerization with BF3 alcohol alkoxylate co-catalysts
EP0477673A1 (en) * 1990-09-20 1992-04-01 Idemitsu Petrochemical Co., Ltd. Process for producing olefin oligomer
CN108251155A (zh) * 2016-12-28 2018-07-06 中国石油天然气股份有限公司 一种低粘度聚α-烯烃合成油的制备方法
CN111450778A (zh) * 2019-01-22 2020-07-28 中国石化工程建设有限公司 一种用于制备聚α-烯烃的聚合反应系统和方法

Family Cites Families (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL280822A (zh) 1961-07-11
US3382291A (en) 1965-04-23 1968-05-07 Mobil Oil Corp Polymerization of olefins with bf3
US3780128A (en) 1971-11-03 1973-12-18 Ethyl Corp Synthetic lubricants by oligomerization and hydrogenation
US3763244A (en) 1971-11-03 1973-10-02 Ethyl Corp Process for producing a c6-c16 normal alpha-olefin oligomer having a pour point below about- f.
US3742082A (en) 1971-11-18 1973-06-26 Mobil Oil Corp Dimerization of olefins with boron trifluoride
US4172855A (en) 1978-04-10 1979-10-30 Ethyl Corporation Lubricant
US4956122A (en) 1982-03-10 1990-09-11 Uniroyal Chemical Company, Inc. Lubricating composition
US5420373A (en) * 1994-03-24 1995-05-30 Chevron Chemical Company Controlled formation of olefin oligomers
BR0013176A (pt) * 1999-07-20 2002-04-02 Exxon Chemical Patents Inc Resinas de petróleo e sua produção com catalisador de bf3
RU2212936C2 (ru) 2001-07-12 2003-09-27 Институт проблем химической физики РАН Каталитическая система для олигомеризации олефинов, способ её приготовления и способ олигомеризации
US6646174B2 (en) 2002-03-04 2003-11-11 Bp Corporation North America Inc. Co-oligomerization of 1-dodecene and 1-decene
CN100455554C (zh) 2005-10-14 2009-01-28 中国人民解放军空军油料研究所 高粘度指数聚α-烯烃合成油的制备方法
CN101054332B (zh) 2006-04-14 2011-05-25 中国石油抚顺石油化工公司 一种合成聚α-烯烃油的方法
US7820580B2 (en) * 2007-11-15 2010-10-26 Bridgestone Corporation Nickel-based catalysts for preparing high cis 1,4-polydienes
ES2444921T3 (es) 2007-11-29 2014-02-27 Ineos Usa, Llc Proceso para fabricar productos oleosos oligoméricos de baja viscosidad
US8865959B2 (en) 2008-03-18 2014-10-21 Exxonmobil Chemical Patents Inc. Process for synthetic lubricant production
US7880047B2 (en) 2008-05-06 2011-02-01 Chemtura Corporation Polyalphaolefins and processes for forming polyalphaolefins
CN101877879A (zh) 2009-04-30 2010-11-03 宏达国际电子股份有限公司 具有蓝牙模块与无线网络模块的电子装置与其控制方法
US9234151B2 (en) 2011-10-10 2016-01-12 Exxonmobil Research And Engineering Company Lubricating compositions
CN102924208A (zh) 2012-10-30 2013-02-13 陕西高新能源发展有限公司 聚α-烯烃合成润滑油的制备方法
EP3585822B1 (en) * 2017-02-21 2025-05-07 NTP Tec, LLC Processes for making polyisobutylene compositions
CN111689995B (zh) 2020-06-15 2023-09-19 万华化学集团股份有限公司 一种高溶解度的三芳基碳硼酸盐及其制备方法和应用

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5068487A (en) * 1990-07-19 1991-11-26 Ethyl Corporation Olefin oligomerization with BF3 alcohol alkoxylate co-catalysts
EP0477673A1 (en) * 1990-09-20 1992-04-01 Idemitsu Petrochemical Co., Ltd. Process for producing olefin oligomer
CN108251155A (zh) * 2016-12-28 2018-07-06 中国石油天然气股份有限公司 一种低粘度聚α-烯烃合成油的制备方法
CN111450778A (zh) * 2019-01-22 2020-07-28 中国石化工程建设有限公司 一种用于制备聚α-烯烃的聚合反应系统和方法

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