CN104560192A - Preparation method of low-viscosity base oil of lubricating oil - Google Patents

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

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CN104560192A
CN104560192A CN201310515584.1A CN201310515584A CN104560192A CN 104560192 A CN104560192 A CN 104560192A CN 201310515584 A CN201310515584 A CN 201310515584A CN 104560192 A CN104560192 A CN 104560192A
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Prior art keywords
alkene
polymer raw
accordance
alcohol
olefin
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CN104560192B (en
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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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    • 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
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1081—Alkanes
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1088—Olefins
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/302—Viscosity
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature

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

Abstract

The invention provides a preparation method of low-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 boron trifluoride, wherein the polymerization raw materials comprise olefins, alcohols and unnecessary alkanes, and the olefins are C6-C14 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 (2) further performing a hydrofining reaction on a polymerization product in the step (1), and collecting a fraction of the base oil of the lubricating oil in a hydrofining reaction product. 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, excellent low-temperature performance, kinematic viscosity (100 DEG C) of 4-8mm<2>/s, viscosity index of more than 120 and pour point of less than -50 DEG C. The method provided by the invention is simple in polymerization process and high in yield.

Description

The preparation method of low-viscosity 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 low-viscosity oil base oil by Fischer-Tropsch synthesis oil.
Background technology
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.
Low-viscosity PAO is applied in field of engine oil, and low-temperature performance is good, can reduce the loss of engine cold torque, can extend the drain period simultaneously, improve fuel economy; In addition, because having good high temperature performance and viscosity index, be the important integral part of aeronautic hydraulic oil.The cold compressor oil that high viscosity PAO uses under heavy loading gear compound, high temperature gear and turning oil, efficient high loading gear oil of worm gear, severe condition, industry, aviation and the wide temperature lubricating grease of automobile, industrial hydraulic oil, long lifetime compressor wet goods field have suitability widely.
CN101,977,944 preparation methods describing a kind of PAO, it is characterized in that, alpha-olefin and single centre 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 continuous mixing still reactor, and the PAO obtained has 11 ~ 300mm 2the kinematic viscosity of/s scope, viscosity index can reach 150 ~ 249, and in addition, described PAO also has high shear stability.
US6,395,948 report the method being prepared poly-alpha olefins base oil by 1-decene polymerization, comprising: with AlCl 3with trimethyl amine hydrochloride/1,3 diethyl chloro imidazolium ionic liquid are catalyzer, and under condition of no solvent, catalysis 1-decene or the polymerization of 1-laurylene, can obtain highest movement viscosity is 31.6mm 2the PAO of/s.
Other patent related comprises US4,642, and 410, US5,196,635, US4,827,064 and US5,270,273.Be not difficult to find out, 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 holding at high price of 1-decene constrains PAO market and popularize.
As everyone knows, under the reaction conditions of 150 ~ 350 DEG C and 2 ~ 15MPa, CO shortening can generate the organic compound such as straight-chain paraffin, alpha-olefin, alcohol mixture of 1 ~ 100 carbonatoms, and this technique is called F-T synthesis.Alpha-olefin is had any different because Fiscber-Tropscb synthesis technique is different with the content of alcohol mixture.In Fischer-Tropsch synthesis oil, alkene can prepare poly-alpha olefins base oil through separation or direct polymerization, as patent US5, and 382, described by 739.
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 1 kinds 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.Different according to boiling point, different viscosity grade lubricants base oil can be prepared.
US2004267071 discloses a kind of processing scheme of Fischer-Tropsch light hydrocarbon, it is characterized in that, Fischer-Tropsch light ends oil (C5 ~ C19), after alcohol to be converted into alkene by dehydroxylation and molecular sieve adsorption deviates from other oxygenatedchemicals, can obtain diesel oil and lubricating oil component through hydrofining again after ionic liquid-catalyzed olefinic polymerization.
Summary of the invention
The invention provides a kind of preparation method of low-viscosity oil base oil, comprising:
(1) polymer raw polymerization reaction take place under boron trifluoride exists;
Described polymer raw comprises alkene, alcohol and non-essential alkane, and described alkene is C 6~ C 14alkene; 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;
(2) there is hydrofining reaction further in the polymerisate of step (1), collects the lubricant base oil fraction in hydrofining reaction product.
In described polymer raw, with described alkene for benchmark by percentage to the quality, content>=85% of alpha-olefin in described alkene, preferably>=95%; Described alkene can select C 6~ C 14single alkene or mixed olefins, by percentage to the quality, in preferred alkenes containing 0.5% ~ 25% C 6~ C 7alkene, 60% ~ 98% C 8~ C 12alkene, 1% ~ 30% C 13~ C 14alkene, most preferably contains the C of 2% ~ 20% 6~ C 7alkene, 70% ~ 90% C 8~ C 12alkene, 2% ~ 25% C 13~ C 14alkene.
In described polymer raw, olefin(e) centent is 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 15alkane, preferred C 5~ C 14alkane, most preferably C 6~ C 14alkane.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 polymer raw preferably meets the Fischer-Tropsch synthesis oil of above-mentioned condition.
The processing condition of described polymer raw polymerization reaction take place under boron trifluoride exists 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.
The pressure of polyreaction is 0.1 ~ 1MPa, preferably 0.12 ~ 0.75MPa, most preferably 0.15 ~ 0.5MPa.
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 boron trifluoride 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.
After the hydrofining reaction described in step (2) completes, collect the lubricant base oil fraction in hydrofining reaction product, preferred employing distillation cutting method collects lubricant base oil fraction, most preferably adopts distillation cutting method to collect the cut of more than 350 DEG C.
By of light color, oxidation stability and the Heat stability is good of the preparation-obtained lubricant base of the inventive method, have higher viscosity index and excellent low-temperature performance, its kinematic viscosity (100 DEG C) is 4 ~ 8mm 2/ s, viscosity index is greater than 120, and pour point is less than-50 DEG C.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 (oxidizing fire and chemoluminescence method);
Oxygen level is measured according to ASTM D5622-95 determination of oxygen content (elemental analyzer method);
Lubricant base kinematic viscosity presses GB265 petroleum products kinematic viscosity assay method and coefficient of dynamic viscosity computing method 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 B F 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.
Table 2 embodiment 1 and comparative example 1 reaction process condition
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, and cutting cut is mixed into 4mm respectively 2/ s, 6mm 2/ s, 8mm 2the lube base oil production of/s, the results are shown in Table 3.
Table 3 embodiment 1 and comparative example 1 test-results
Be not difficult to find out, the inventive method olefin conversion is high, and prepared lubricant base yield is high, and viscosity-temperature characteristics can be good, low temperature performance excellent.
Embodiment 2
The polymer raw that embodiment 2 adopts is 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) 0.729
Oxygen level/% 0.522
Sulphur content (ugg -1) 1
Nitrogen content (ugg -1) 2
Alcohol content/% 3.840
Aromaticity content/% 0
Olefin(e) centent/% 68.037
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, the peak of chemical shift near 4.8 ~ 5.2 is alpha-olefin CH 2the chemical shift of hydrogen atom in=structure, the peak of chemical shift near 5.7 ~ 6.0 is the chemical shift of hydrogen atom in alpha-olefin end position=CH-structure, and the peak of chemical shift near 5.3 ~ 5.5 is the chemical shift of hydrogen atom in internal olefin-CH=CH-structure.The integral area at each peak as calculated, can calculate alpha-olefin in this F-T synthesis distillate and account for 97.1% of total olefin quality, interior alkene accounts for 2.9% of total olefin quality.
Embodiment 2 prepares lubricant base according to the polymeric reaction condition of table 6 and hydrofining reaction condition.
The reaction process condition of table 6 embodiment 2
The 4mm prepared by embodiment 2 2/ s and 6mm 2the physical and chemical index of/s product is in table 7.
Table 7 embodiment 2 test-results
Comparative example 2
The polymer raw that comparative example 2 adopts is F-T synthesis distillate B, and physical and chemical index is in table 8.
The physical and chemical index of table 8 F-T synthesis distillate B
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 B is as shown in table 9.
The carbon number distribution of table 9 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 96.1% of total olefin quality, interior alkene accounts for 3.9% of total olefin quality.
Except polymer raw adopts F-T synthesis distillate B, the reaction process of comparative example 2 and processing condition are all consistent with embodiment 2, and test conditions is in table 6.
The 4mm prepared by comparative example 2 2/ s and 6mm 2the physical and chemical index of the lube base oil production of/s is in table 10.
Table 10 comparative example 2 test-results
Be not difficult to find out, embodiment 2 obtain the lubricant base of equal viscosity low-temperature performance be obviously better than in comparative example 2 lubricant base.

Claims (15)

1. a preparation method for low-viscosity oil base oil, comprising:
(1) polymer raw polymerization reaction take place under boron trifluoride exists;
Described polymer raw comprises alkene, alcohol and non-essential alkane, and described alkene is C 6~ C 14alkene; 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;
(2) there is hydrofining reaction further in the polymerisate of step (1), collects the lubricant base oil fraction in hydrofining reaction product.
2. in accordance with the method for claim 1, it is characterized in that, the alkene in described polymer raw is selected from C 6~ C 14single 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% ~ 25% in the alkene of described polymer raw 6~ C 7alkene, 60% ~ 98% C 8~ C 12alkene, 1% ~ 30% C 13~ C 14alkene, 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, in described polymer raw, olefin(e) centent 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 15alkane, 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 obtain or additional described alkene, alcohol or alkane concoct form.
10. in accordance with the method for claim 1, it is characterized in that, described polymer raw is Fischer-Tropsch synthesis oil.
11. according to the method for claim 1-10 described in one of them, it is characterized in that, the processing condition of described polymer raw polymerization reaction take place under boron trifluoride exists are: the temperature of polyreaction is-10 ~ 120 DEG C, the time of polyreaction is 15 ~ 360min, and the pressure of polyreaction is 0.1 ~ 1MPa.
12. according to the method for claim 1-10 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).
13. in accordance with the method for claim 12, 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.
14., according to the method for claim 1-10 described in one of them, is characterized in that, after the hydrofining reaction described in step (2) completes, adopt distillation cutting method to collect lubricant base oil fraction.
15. in accordance with the method for claim 14, it is characterized in that, after the hydrofining reaction described in step (2) completes, collects the lubricant base oil fraction of more than 350 DEG C by distillation cutting method.
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110721733A (en) * 2019-09-17 2020-01-24 中国科学院青岛生物能源与过程研究所 Catalyst for preparing aviation oil by oligomerization of low-carbon hydrocarbon and preparation method and application thereof
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

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