CN104560190A - Preparation method of high-viscosity base oil of lubricating oil - Google Patents

Preparation method of high-viscosity base oil of lubricating oil Download PDF

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Publication number
CN104560190A
CN104560190A CN201310514631.0A CN201310514631A CN104560190A CN 104560190 A CN104560190 A CN 104560190A CN 201310514631 A CN201310514631 A CN 201310514631A CN 104560190 A CN104560190 A CN 104560190A
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alkene
polymer raw
lewis acid
acid catalyst
alcohol
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CN201310514631.0A
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Inventor
张耀
段庆华
刘依农
李玲
辛世豪
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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Priority to CN201310514631.0A priority Critical patent/CN104560190A/en
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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
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M109/00—Lubricating compositions characterised by the base-material being a compound of unknown or incompletely defined constitution
    • C10M109/02—Reaction products
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M177/00—Special methods of preparation of lubricating compositions; Chemical modification by after-treatment of components or of the whole of a lubricating composition, not covered by other classes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10N—INDEXING SCHEME ASSOCIATED WITH SUBCLASS C10M RELATING TO LUBRICATING COMPOSITIONS
    • C10N2020/00—Specified physical or chemical properties or characteristics, i.e. function, of component of lubricating compositions
    • C10N2020/01—Physico-chemical properties
    • C10N2020/02—Viscosity; Viscosity index

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Lubricants (AREA)

Abstract

The invention provides a preparation method of high-viscosity base oil of lubricating oil. The preparation method comprises the following steps: (1) performing a polymerization reaction on polymerization raw materials in the presence of an aluminum-containing Lewis acid catalyst, wherein the polymerization raw materials comprise olefins, alcohols and unnecessary alkanes, and the olefins are C5-C17 alkenes; and calculated by mass percentage, the content of the olefins in the polymerization raw materials is above 10%, and the oxygen content provided by the alcohols is 0.2%-2%; and by taking the olefins as the reference and performing calculation by mass percentage, the content of alpha-olefin in the olefins is not less than 85%; and the mass ratio of the aluminum-containing Lewis acid catalyst to the olefins in the polymerization raw materials is (1:200)-(1-5), and the mass ratio of the aluminum-containing Lewis acid catalyst to oxygen element in the polymerization raw materials is (2:1)-(70:1); and (2) further performing a hydrofining reaction on a polymerization product in the step (1), and collecting a fraction with initial boiling point of more than 350 DEG C in a reaction product to obtain the high-viscosity base oil of the lubricating oil. The base oil of the lubricating oil prepared by adopting the method provided by the invention has the advantages of light color, good oxidation stability and thermal stability, relatively high viscosity index and excellent low-temperature performance. The method provided by the invention is simple in polymerization process and high in yield.

Description

The preparation method of high viscosity lubricating oil base oil
Technical field
The present invention relates to a kind of preparation method of lubricant base, particularly a kind of method being prepared high viscosity lubricating oil base oil by Fischer-Tropsch synthesis oil.
Background technology
At present, high viscosity lubricating oil market of base oil is formed primarily of bright stock and high viscosity poly-alpha olefins base oil (being called for short PAO).Sulphur in the bright stock that old three cover techniques obtain, nitrogen, aromaticity content are high, and oxidation stability, low-temperature fluidity are all poor, and after hydrofining, low-temperature performance does not significantly improve, and bright stock is subject to the impact of raw material fluctuation in addition, and market supply is limited; And high viscosity poly-alpha olefins base oil not sulfur-bearing, nitrogen, and viscosity-temperature characteristics energy, low-temperature fluidity and oxidation stability are all abnormal remarkable, are widely used in high-end lubricating grease.
Poly-alpha olefins base oil is by C 6~ C 16alpha-olefin be polymerized under catalyst action, then by the regular long chain alkane that hydrogenation obtains, as patent US4,219,691 and the patent quoted described by.The commercially available poly-alpha olefins base oil criteria for classifying is determined by 100 DEG C of kinematic viscosities, main product by 4,6,10,40,100mm 2the formations such as/s.Wherein, high viscosity PAO(kinematic viscosity >20mm 2/ s) in heavy loading gear compound, high temperature gear and turning oil, efficient high loading gear oil of worm gear, industry, aviation and wide temperature lubricating grease, industrial hydraulic oil, long lifetime compressor wet goods field, there is suitability widely.
The raw material preparing different viscosity rank PAO is substantially identical, and many employing ethylene oligomerization alkene, with 1-C 10alkene is main.As US7,547,811 disclose a kind of method preparing high viscosity PAO, comprising: to be selected from 1-decene or 1-laurylene mixture for polymer raw, at catalyst A lCl 3there is lower polymerization with deionized water, the PAO with high-quality low-temperature performance can be prepared.Wherein said 40mm 2/ s rank PAO synthesizes under condition of no solvent, 100mm 2need the solvent of interpolation 25% ~ 30% olefin(e) centent to improve the heat transfer of polyreaction in/s and above rank PAO building-up process.
CN101,977,944 preparation methods describing high shear stability PAO.It is characterized in that, alpha-olefin and single active center's metallocene catalyst, two (2-tetrahydro indenyl) zirconium dimethyl as silica-based in dimethyl is Primary Catalysts and N, N-dimethyl puratized agricultural spray four (pentafluorophenyl group) borate is that auxiliary agent contacts in mixed-flow or flow reactor, and can obtain kinematic viscosity (100 DEG C) is 11 ~ 300mm 2/ s, viscosity index can reach the PAO of 150 ~ 249.
Other patent related comprises US4,642, and 410, US5,196,635, US4,827,064 and US5,270,273.Alpha-olefin required in above-mentioned report is ethylene oligomer, and based on 1-decene, but under the global 1-decene background that supply falls short of demand, the market constraining PAO that holds at high price of 1-decene is popularized.
As everyone knows, under the reaction conditions of 150 ~ 350 DEG C and 2.0 ~ 15.0MPa, adopt Fischer-tropsch process that CO shortening can be generated C 1~ C 100the gas of scope, liquid, solid carbon hydrogen compound.Difference according to cut is mainly divided into F-T synthesis lightweight oil and Fischer-Tropsch wax.Under the situation that nowadays petroleum resources are in short supply, the processing route adopting F-T synthesis to prepare liquid fuel or Chemicals is supported gradually and is obtained fast development.Because Fischer-Tropsch synthesis oil and natural oil product have larger difference, lower to produce the processing scheme economic benefit that oil fuel takes as the leading factor, how to carry out secondary processing, voluminous high value added product is the problem that Fischer-tropsch process practitioner needs to pay close attention to.
US6,518,473 describe a kind of method being generated lubricant base by olefin oligomerization in Fischer-Tropsch synthesis oil, described olefin oligomerization in two steps dimerization is formed, and catalyzer is that VIII B race element is carried on molecular sieve, preferred Ni/ZSM-5, the method material choice C5 ~ C10 Fischer-Tropsch petroleum naphtha, before polymerization, raw material need through absorption or hydrofining, and to reduce S, N, O impurity to murder by poisoning catalyzer, it is 3 ~ 20mm that the method obtains lubricant base kinematic viscosity 2/ s, viscosity index >80, pour point is not higher than-10 DEG C.
US6,605,206 describe a kind of increase C 10the method of above hydrocarbon products, it comprises: Fischer-Tropsch product is divided into Fischer-Tropsch wax and light liquid hydrocarbons by (1); (2) Fischer-Tropsch wax prepares high boiling point low pour point hydrocarbon component through hydroisomerizing; (3) in Fischer-Tropsch light hydrocarbon, alkene is prepared in alcohol deoxidation; (4) high-molecular-weight hydrocarbons is prepared in olefinic polymerization; (5) cutting and separating diesel oil and base oil component.
Summary of the invention
The invention provides a kind of preparation method of high viscosity lubricating oil base oil, comprising:
(1) polymer raw polymerization reaction take place under existing containing aluminium Lewis acid catalyst;
Described polymer raw comprises alkene, alcohol and non-essential alkane, and described alkene is C 5~ C 17alkene; By percentage to the quality, the oxygen level that in described polymer raw, olefin(e) centent provides more than 10%, by alcohol is 0.2% ~ 2%; With described alkene for benchmark by percentage to the quality, content>=85% of alpha-olefin in described alkene; Described is 1:200 ~ 1:5 containing the mass ratio of alkene in aluminium Lewis acid catalyst and polymer raw, and described is 2:1 ~ 70:1 containing the mass ratio of oxygen element in aluminium Lewis acid catalyst and polymer raw;
(2) there is hydrofining reaction further in the polymerisate of step (1), and the cut that in collecting reaction product, initial boiling point is greater than 350 DEG C obtains high viscosity lubricating oil base oil.
In described polymer raw, described alkene can select C 5~ C 17single alkene or mixed olefins, by percentage to the quality, in preferred alkenes containing 0.5% ~ 40% C 5~ C 7alkene, 40% ~ 98% C 8~ C 12alkene, 1% ~ 30% C 13~ C 17alkene, most preferably contains the C of 2% ~ 35% 5~ C 7alkene, 55% ~ 90% C 8~ C 12alkene, 2% ~ 25% C 13~ C 17alkene.With described alkene for benchmark by percentage to the quality, content >=85% of alpha-olefin in described alkene, preferably >=95%.
Olefin(e) centent in described polymer raw more than 10%, preferably more than 25%, most preferably more than 40%.
Alcohol in described polymer raw is selected from C 1~ C 12single alcohol or alcohol mixture, preferred C 2~ C 10single n-alkanol or mixing n-alkanol, most preferably C 2~ C 10single primary alconol or mixing primary alconol.
The oxygen level provided by alcohol in described polymer raw is 0.2% ~ 2%, preferably 0.25% ~ 1.5%, most preferably 0.3% ~ 1%.
Can not alkane be comprised in polymer raw of the present invention, also can comprise alkane.Described alkane is C 4~ C 20alkane, preferred C 6~ C 20alkane, most preferably C 7~ C 20alkane.When comprising alkane in described polymer raw, the mass ratio of described alkane and described alkene is 10:1 ~ 1:10, preferred 5:1 ~ 1:5, most preferably 3:1 ~ 1:3.
Described polymer raw can be concocted by above-mentioned alkene, alcohol or alkane and form, also can select in some Fischer-Tropsch synthesis oil meeting above-mentioned composition, wax olefin cracking and coking distillates one or more, and for not meeting Fischer-Tropsch synthesis oil, wax olefin cracking, the coking distillate of above-mentioned composition, also can form as polymer raw of the present invention through distillation cutting or the blending of additional above-mentioned alkene, alcohol or alkane, the popularity of raw material sources can be improved like this.For Fischer-Tropsch synthesis oil, for the Fischer-Tropsch synthesis oil not meeting above-mentioned condition, also its composition can be made to meet the requirement of polymer raw of the present invention by the method for distillation cutting, if still do not met the demands after distillation cutting, can additional above-mentioned alkene or alcohol and non-essential alkane meet the demands.
Described is 1:200 ~ 1:5 containing the mass ratio of alkene in aluminium Lewis acid catalyst and polymer raw, preferred 1:100 ~ 1:10, most preferably 1:80 ~ 1:13.
Described is 2:1 ~ 70:1 containing the mass ratio of oxygen element in aluminium Lewis acid catalyst and polymer raw, preferred 4:1 ~ 40:1, most preferably 5:1 ~ 30:1.
The described structure containing aluminium Lewis acid catalyst is R nalX 3-n, the alkyl of wherein n is selected from 0 ~ 3, R to be carbonatoms be 1-6, preferred carbonatoms is the alkyl of 1-4, and X is selected from the one in Cl-, Br-, I-; Described containing one or more in the preferred aluminum chloride of aluminium Lewis acid catalyst, chloro aluminum alkyls, aluminum alkyls, aluminum bromide and bromo aluminum alkyls, such as can select AlCl 3, AlBr 3, (C 2h 5) 2alCl, C 4h 9alCl 2, most preferably AlCl 3.
The processing condition of described polymer raw polymerization reaction take place under existing containing aluminium Lewis acid catalyst are:
The temperature of polyreaction is-10 ~ 120 DEG C, preferably-5 ~ 100 DEG C, most preferably 0 ~ 80 DEG C.
The time of polyreaction is 15 ~ 360min, preferably 30 ~ 300min, most preferably 45 ~ 280min.
In the preparation method of step (1), one or more methods in stratification/filtering separation, washing, absorption and distillation method are preferably adopted to carry out aftertreatment to polymerisate.
In the preparation method of step (1), except above-mentioned containing except aluminium Lewis acid catalyst, without the need to additionally adding other catalyst adjuvant.
In step (2), the method that the polymerisate of step (1) is occurred further to for hydrofining reaction is: contacted with hydrogen under Hydrobon catalyst exists by the polymerisate of step (1).
Described Hydrobon catalyst can select group vib or VIII B race metal, such as can select in molybdenum, nickel, ruthenium, rhodium, cobalt, platinum and palladium one or more, preferred negative is loaded in group vib on carrier or VIII B race metal catalyst, described carrier can select in silicon oxide, aluminum oxide, clay, magnesium oxide, titanium oxide and zirconium white one or more;
Hydrogen dividing potential drop in described hydrofining reaction is 1 ~ 25MPa, preferably 2 ~ 20MPa, most preferably 3 ~ 15MPa;
The temperature of described hydrofining reaction is 150 ~ 350 DEG C, preferably 160 ~ 300 DEG C, most preferably 180 ~ 260 DEG C;
In generation hydrofining reaction process, volume ratio (hydrogen-oil ratio) between the polymerisate of described hydrogen and step (1) is 100 ~ 2000 (v/v), preferably 200 ~ 1500 (v/v), most preferably 250 ~ 1000 (v/v); During the liquid of described hydrogen, volume space velocity is 0.2 ~ 5h -1, preferably 0.5 ~ 3h -1, most preferably 0.6 ~ 2.5h -1.
Adopt of light color, oxidation stability and the Heat stability is good of lubricant base prepared by the inventive method, have higher viscosity index and excellent low-temperature performance, its kinematic viscosity (100 DEG C) is not less than 20mm 2/ s, viscosity index is greater than 130, and pour point is less than-20 DEG C, and over-all properties is significantly better than bright stock.The polymerization technique of the inventive method is simple, yield is high.
Embodiment
Unless stated otherwise, the per-cent below mentioned is mass percent.
The analytical procedure that present embodiment is applied is as follows:
Carbon number distribution measures according to RIPP-GC47 Fischer-Tropsch oil phase n-alkanol and carbon number distribution;
Sulphur content records according to ASTM D7039 light oil sulfur content method;
Nitrogen content is measured according to trace N2 method in SH/T0657 Naphtha solvent;
Oxygen level is measured according to ASTM D5622-95 determination of oxygen content (elemental analyzer method);
Lubricant base kinematic viscosity is pressed GB265 petroleum products viscosimetry and is measured;
Viscosity index calculates according to GB2541 petroleum products viscosity index calculation table;
Pour point is measured according to GB3535 petroleum products pour point assay method.
Catalyst A lCl 3, NaOH is commercially available prod.
Embodiment 1 and comparative example 1
The polymer raw that embodiment 1 and comparative example 1 adopt is the mixed olefins of allotment, and its composition is in table 1.
The composition of polymer raw in table 1 embodiment 1 and comparative example 1
Embodiment 1 and comparative example 1 prepare lubricant base according to the polymeric reaction condition of table 2 and hydrofining reaction condition respectively.
The reaction conditions of table 2 embodiment 1 and comparative example 1
The product obtained after carrying out polyreaction, hydrofining reaction to the polymer raw of embodiment 1 and comparative example 1 respectively carries out distillation cutting, excision is less than 350 DEG C of cuts, more than 350 DEG C remaining cuts are high viscosity lubricating oil base oil of the present invention, the results are shown in Table 3.
Table 3 embodiment 1 and comparative example 1 test-results
Be not difficult to find out, under alkene compositing range of the presently claimed invention and oxygen level, good, the low temperature performance excellent of viscosity-temperature characteristics energy of prepared lubricant base, olefin conversion is high.
Embodiment 2 ~ 5
The polymer raw that embodiment 2 adopts is certain F-T synthesis distillate A, and its physical and chemical index is in table 4.
The physical and chemical index of table 4 F-T synthesis distillate A
Project Respective value
20 DEG C of density/(Kgm -3) 0.730
Oxygen level/% 0.500
Sulphur content/(ugg -1) 2
Alcohol content/% 3.061
Nitrogen content/(ugg -1) 3
Aromaticity content/% 0
Olefin(e) centent/% 66.743
The carbon number distribution of this F-T synthesis distillate A is as shown in table 5.
The carbon number distribution of table 5 F-T synthesis distillate A
Carried out H-NMR sign to this F-T synthesis distillate feedstock, the peak near chemical shift 4.8 ~ 5.2 is alpha-olefin CH 2the chemical shift of the hydrogen atom in=structure, the peak near chemical shift 5.7 ~ 6.0 is the chemical shift of the hydrogen atom in alpha-olefin end position=CH-structure, and the peak near chemical shift 5.3 ~ 5.5 is the chemical shift of the hydrogen atom in internal olefin-CH=CH-structure.The integral area at each peak as calculated, can calculate alpha-olefin in adopted F-T synthesis distillate and account for 96.1% of total olefin quality, interior alkene accounts for 3.9% of total olefin quality.
Embodiment 2 ~ 5 adopts above-mentioned Fischer-Tropsch synthesis oil to be raw material, and except catalyst levels is different with polymeric reaction temperature, other reaction process is all consistent with embodiment 1, and its partial reaction condition and test-results are in table 6.
The partial reaction condition of table 6 embodiment 2 ~ 5 and test-results
Comparative example 2 ~ 3
The polymer raw that comparative example 2 ~ 3 adopts is certain F-T synthesis distillate B, and its physical and chemical index is in table 7.
The physical and chemical index of table 7 F-T synthesis distillate B
Project Respective value
20 DEG C of density/(Kgm -3) 0.751
Oxygen level/% 0.32
Sulphur content/(ugg -1) 2
Alcohol content/% 3.077
Nitrogen content/(ugg -1) 5
Aromaticity content/% 0
Olefin(e) centent/% 64.732
The carbon number distribution of this F-T synthesis distillate B is as shown in table 8.
The carbon number distribution of table 8 F-T synthesis distillate B
H-NMR sign has been carried out to this F-T synthesis distillate feedstock.The integral area at each peak as calculated, can calculate alpha-olefin in this F-T synthesis distillate and account for 76.3% of total olefin quality, interior alkene accounts for 23.7% of total olefin quality.
Comparative example 2 ~ 3 adopts F-T synthesis distillate B to be raw material, and except catalyst levels changes, other reaction process is respectively with embodiment 2,4 consistent.The physical properties of the lubricant base that comparative example 2 ~ 3 prepares is in table 9.
Table 9 comparative example 2 ~ 3 partial reaction condition and test-results
Be not difficult to find out, the low-temperature performance of the lubricant base adopting F-T synthesis distillate B raw material to prepare in comparative example 2 ~ 3 is poor, olefin conversion is low, and in embodiment 2 ~ 5, olefin conversion is high, and prepared lubricant base has good low-temperature performance.

Claims (16)

1. a preparation method for high viscosity lubricating oil base oil, comprising:
(1) polymer raw polymerization reaction take place under existing containing aluminium Lewis acid catalyst;
Described polymer raw comprises alkene, alcohol and non-essential alkane, and described alkene is C 5~ C 17alkene; By percentage to the quality, the oxygen level that in described polymer raw, olefin(e) centent provides more than 10%, by alcohol is 0.2% ~ 2%; With described alkene for benchmark by percentage to the quality, content>=85% of alpha-olefin in described alkene; Described is 1:200 ~ 1:5 containing the mass ratio of alkene in aluminium Lewis acid catalyst and polymer raw, and described is 2:1 ~ 70:1 containing the mass ratio of oxygen element in aluminium Lewis acid catalyst and polymer raw;
(2) there is hydrofining reaction further in the polymerisate of step (1), and the cut that in collecting reaction product, initial boiling point is greater than 350 DEG C obtains high viscosity lubricating oil base oil.
2. in accordance with the method for claim 1, it is characterized in that, the alkene in described polymer raw is selected from C 5~ C 17single alkene or mixed olefins.
3. in accordance with the method for claim 1, it is characterized in that, by percentage to the quality, containing the C of 0.5% ~ 40% in the alkene of described polymer raw 5~ C 7alkene, 40% ~ 98% C 8~ C 12alkene, 1% ~ 30% C 13~ C 17alkene; With described alkene for benchmark, content>=95% of alpha-olefin in described alkene.
4. in accordance with the method for claim 3, it is characterized in that, by percentage to the quality, the olefin(e) centent in described polymer raw is more than 25%.
5. in accordance with the method for claim 1, it is characterized in that, the alcohol in described polymer raw is selected from C 1~ C 12single alcohol or alcohol mixture.
6. in accordance with the method for claim 5, it is characterized in that, the alcohol in described polymer raw is selected from C 2~ C 10single n-alkanol or mixing n-alkanol.
7. in accordance with the method for claim 1, it is characterized in that, the alcohol in described polymer raw is selected from C 2~ C 10single primary alconol or mixing primary alconol, the oxygen level provided by alcohol in described polymer raw is 0.25% ~ 1.5%.
8. in accordance with the method for claim 1, it is characterized in that, comprise alkane in described polymer raw, described alkane is C 4~ C 20alkane, the mass ratio of described alkane and described alkene is 10:1 ~ 1:10.
9. in accordance with the method for claim 1, it is characterized in that, described polymer raw be by one or more in Fischer-Tropsch synthesis oil, wax olefin cracking and coking distillate through distillation cutting form or additional described alkene, alcohol or alkane concoct form.
10. according to the method for claim 1-9 described in one of them, it is characterized in that, described is 1:100 ~ 1:10 containing the mass ratio of alkene in aluminium Lewis acid catalyst and polymer raw.
11., according to the method for claim 1-9 described in one of them, is characterized in that, described is 4:1 ~ 40:1 containing the mass ratio of oxygen element in aluminium Lewis acid catalyst and polymer raw.
12., according to the method for claim 1-9 described in one of them, is characterized in that, described is R containing aluminium Lewis acid catalyst nalX 3-n, wherein n is selected from the integer of 0 ~ 3, and the alkyl of R to be carbonatoms be 1-6, X is selected from Cl -, Br -, I -in one.
13., according to the method for claim 1-9 described in one of them, is characterized in that, described is one or more in aluminum chloride, chloro aluminum alkyls, aluminum alkyls, aluminum bromide and bromo aluminum alkyls containing aluminium Lewis acid catalyst.
14. according to the method for claim 1-9 described in one of them, it is characterized in that, the processing condition of described polymer raw polymerization reaction take place under existing containing aluminium Lewis acid catalyst are: the temperature of polyreaction is-10 ~ 120 DEG C, and the time of polyreaction is 15 ~ 360min.
15. according to the method for claim 1-9 described in one of them, it is characterized in that, in step (2), the method that the polymerisate of step (1) is occurred further to for hydrofining reaction is: contacted with hydrogen under Hydrobon catalyst exists by the polymerisate of step (1).
16. in accordance with the method for claim 15, it is characterized in that, described Hydrobon catalyst is selected from group vib or VIII B race metal, hydrogen dividing potential drop in described hydrofining reaction is 1 ~ 25MPa, the temperature of described hydrofining reaction is 150 ~ 350 DEG C, volume ratio (hydrogen-oil ratio) between the polymerisate of described hydrogen and step (1) is 100 ~ 2000 (v/v), and during the liquid of described hydrogen, volume space velocity is 0.2 ~ 5h -1.
CN201310514631.0A 2013-10-28 2013-10-28 Preparation method of high-viscosity base oil of lubricating oil Pending CN104560190A (en)

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CN108473897A (en) * 2015-11-13 2018-08-31 埃克森美孚研究工程公司 High viscosity oil base stock composition
CN112725029A (en) * 2019-10-28 2021-04-30 南京中科康润新材料科技有限公司 Process method for directly synthesizing high-performance low-viscosity base oil by polymerizing low-carbon olefins
CN113684079A (en) * 2020-05-19 2021-11-23 山西中能奥博节能科技有限公司 Liquid lubricant taking Fischer-Tropsch synthesis base oil as raw material and preparation method thereof

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CN101565651A (en) * 2009-03-06 2009-10-28 大连海事大学 Method for preparing high viscosity lubricating oil
CN102776022A (en) * 2011-05-11 2012-11-14 中国石油化工股份有限公司 High-viscosity poly alpha-olefin synthetic oil and preparation method thereof

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US4219691A (en) * 1977-08-31 1980-08-26 The Lion Fat And Oil Co., Ltd. Process for producing olefin oligomer
CN101565651A (en) * 2009-03-06 2009-10-28 大连海事大学 Method for preparing high viscosity lubricating oil
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Publication number Priority date Publication date Assignee Title
CN108473897A (en) * 2015-11-13 2018-08-31 埃克森美孚研究工程公司 High viscosity oil base stock composition
CN108473897B (en) * 2015-11-13 2022-01-04 埃克森美孚研究工程公司 High viscosity base stock composition
CN112725029A (en) * 2019-10-28 2021-04-30 南京中科康润新材料科技有限公司 Process method for directly synthesizing high-performance low-viscosity base oil by polymerizing low-carbon olefins
CN113684079A (en) * 2020-05-19 2021-11-23 山西中能奥博节能科技有限公司 Liquid lubricant taking Fischer-Tropsch synthesis base oil as raw material and preparation method thereof

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Application publication date: 20150429