CN104560192B - 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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CN104560192B
CN104560192B CN201310515584.1A CN201310515584A CN104560192B CN 104560192 B CN104560192 B CN 104560192B CN 201310515584 A CN201310515584 A CN 201310515584A CN 104560192 B CN104560192 B CN 104560192B
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alkene
polymer raw
alcohol
accordance
oil
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CN104560192A (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 lube base oil, more particularly to a kind of to prepare low sticking by Fischer-Tropsch synthesis oil The method of degree lube base oil.
Background technology
Poly alpha olefin base oil is by C6～C16Alpha-olefin be polymerized under catalyst action, then by be hydrogenated with obtain rule Then long chain alkane, such as patent US4,219,691 and its patent quoted described by.The commercially available poly alpha olefin base oil criteria for classifying is Determined by 100 DEG C of dynamic viscosities, main product is by 4,6,10,40,100mm2/ s etc. is constituted.
Low-viscosity PAO is applied in field of engine oil, low temperature performance well, can reduce the cold torque loss of electromotor, while The drain period can be extended, fuel economy is improved；Additionally, because with good high temperature performance and Viscosity Index, being aviation liquid The important ingredient of force feed.High viscosity PAO is in heavy load transmission oil, high temperature gear and recycle oil, efficient high load capacity worm gear snail Cold compressor oil, industry, aviation and automobile width temperature lubricating grease, industrial hydraulic oil, the length used under bar gear oil, harsh conditions The fields such as life-span compressor oil have wide applicability.
CN101,977,944 describe a kind of preparation method of PAO, it is characterised in that alpha-olefin and single centre metallocene Double (2- tetrahydro indenyls) zirconium dimethyls of catalyst, such as dimethyl silicon substrate are four (phenyl-pentafluoride of major catalyst and N, N- dimethyl puratized agricultural spray Base) borate contacted in mixed-flow or continuous mixing kettle reactor for auxiliary agent, and the PAO for being obtained has 11～300mm2/s The dynamic viscosity of scope, Viscosity Index is up to 150～249, additionally, the PAO also has high shear stability.
US6,395,948 report the method for preparing poly alpha olefin base oil by 1-decene polymerization, including：With AlCl3With Trimethyl amine hydrochloride/1,3 diethyl chloro imidazolium ionic liquids be catalyst, under condition of no solvent, catalysis 1-decene or 1- laurylenes are polymerized, and highest movement viscosity is obtained for 31.6mm2The PAO of/s.
Related other patents include US4,642,410, US5,196,635, US4,827,064 and US5,270,273. It is not difficult to find out, the alpha-olefin needed for above-mentioned report is ethylene oligomer, and based on 1-decene, but in the global 1- last of the ten Heavenly stems Under the alkene background that supply falls short of demand, holding at high price for 1-decene constrains the popularization of PAO markets.
It is well known that under 150～350 DEG C and 2～15MPa of reaction condition, CO catalytic hydrogenations can generate 1～100 The organic compound such as the linear paraffin of carbon number, alpha-olefin, mixed alcohol, the technique are referred to as F- T synthesis.Alpha-olefin and mixing The content of alcohol is had any different because Fiscber-Tropscb synthesis technique is different.In Fischer-Tropsch synthesis oil, alkene is separated or direct polymerization can prepare it is poly- Alpha-olefin base oil, such as patent US5, described by 382,739.
US6,518,473 describe a kind of method for generating lube base oil by olefin oligomerization in Fischer-Tropsch synthesis oil, institute Dimerization is constituted in two steps to state olefin oligomerization, and catalyst is carried on molecular sieve, preferably Ni/ZSM-5 for VIII B races element, and the method is former Material selects C5～C10 Fischer-Tropsch Petroleums, and before polymerization, raw material needs Jing absorption or hydrofinishing, murder by poisoning is urged with reducing S, N, O impurity Agent, obtained by the method, lube base oil dynamic viscosity is 3～20mm2/ s, Viscosity Index>80, pour point not higher than -10 ℃。
US6,605,206 is a kind of to increase C10The method of above hydrocarbon productss, which includes：（1）Fischer-Tropsch product is divided into into Fischer-Tropsch Wax and light liquid hydrocarbons；（2）The hydrogenated isomery of Fischer-Tropsch wax prepares high boiling point low pour point hydrocarbon component；（3）In Fischer-Tropsch light hydrocarbon, alcohol takes off Oxygen prepares alkene；（4）Olefinic polymerization prepares high-molecular-weight hydrocarbons；（5）Cutting separates diesel oil and base oil component.According to boiling point not Together, different viscosity grade lubricants base oils can be prepared.
US2004267071 discloses a kind of processing scheme of Fischer-Tropsch light hydrocarbon, it is characterised in that Fischer-Tropsch light ends oil （C5～C19）Jing after alcohol to be converted into dehydroxylation alkene and molecular sieve adsorption deviates from other oxygenatedchemicalss, Jing ionic liquids Diesel oil and lubricating oil component is obtained through hydrofinishing again after catalysis in olefine polymerization.
The content of the invention
The invention provides a kind of preparation method of low-viscosity oil base oil, including：
（1）There is polyreaction in the presence of boron trifluoride in polymer raw；
The polymer raw includes alkene, alcohol and non-essential alkane, and the alkene is C6～C14Alkene；With mass percent Meter, in the polymer raw, olefin(e) centent is 0.2%～2% more than 10%, by the oxygen content that alcohol is provided；With the alkene as base It is accurate and by percentage to the quality, content >=85% of alpha-olefin in the alkene；
（2）Step（1）Polymerizate further there is hydrofining reaction, collect the profit in hydrofining reaction product Lubricant base oil distillate.
In the polymer raw, on the basis of the alkene and by percentage to the quality, alpha-olefin in the alkene Content >=85%, preferably >=95%；The alkene can select C6～C14Single alkene or mixed olefins, with mass percent Meter, containing 0.5%～25% C in preferred alkenes6～C7Alkene, 60%～98% C8～C12Alkene, 1%～30% C13～C14Alkene Hydrocarbon, most preferably 2%～20% C6～C7Alkene, 70%～90% C8～C12Alkene, 2%～25% C13～C14Alkene.
In the polymer raw, olefin(e) centent is more than 10%, preferably more than 25%, most preferably more than 40%.
Alcohol in the polymer raw is selected from C1～C12Single alcohol or mixed alcohol, preferably C2～C10Single n-alkanol or Mixing n-alkanol, most preferably C2～C10Single primary alconol or mixing primary alconol.
In the polymer raw by alcohol provide oxygen content be 0.2%～2%, preferably 0.25%～1.5%, most preferably 0.3%～ 1%。
Alkane can not included in polymer raw of the present invention, it is also possible to comprising alkane.The alkane is C4～C15 Alkane, preferably C5～C14Alkane, most preferably C6～C14Alkane.When alkane is included in the polymer raw, the alkane Hydrocarbon is 10 with the mass ratio of the alkene:1～1:10, preferably 5:1～1:5, most preferably 3:1～1:3.
The polymer raw can be formed by the blending of above-mentioned alkene, alcohol or alkane, also be can select some and met above-mentioned composition Fischer-Tropsch synthesis oil, one or more in wax olefin cracking and coking distillate, and for not meeting the Fischer-Tropsch of above-mentioned composition Artificial oil, wax olefin cracking, coking distillate, can also Jing distillation cutting or additional above-mentioned alkene, alcohol or alkane blending form work For the polymer raw of the present invention, the popularity of raw material sources can be so improved.By taking Fischer-Tropsch synthesis oil as an example, on not meeting State the Fischer-Tropsch synthesis oil of condition, it is also possible to cause its composition to meet polymer raw of the present invention by the method for distilling cutting Require, if Jing after distillation cutting being still unsatisfactory for requiring, can be wanted to meet with additional above-mentioned alkene or alcohol and non-essential alkane Ask.
The polymer raw preferably conforms to the Fischer-Tropsch synthesis oil of above-mentioned condition.
There are the process conditions of polyreaction in the presence of boron trifluoride in the polymer raw：
The temperature of polyreaction is -10～120 DEG C, preferably -5～100 DEG C, most preferably 0～80 DEG C.
The time of polyreaction be 15～360min, preferably 30～300min, most preferably 45～280min.
The pressure of polyreaction be 0.1～1MPa, preferably 0.12～0.75MPa, most preferably 0.15～0.5MPa.
In step（1）Preparation method in, it is preferred to use stratification/be separated by filtration, wash, adsorb and the way of distillation in One or more method carries out post processing to polymerizate.
In step（1）Preparation method in, in addition to above-mentioned boron trifluoride catalyst, without the need for additionally add other catalysis Agent aid.
In step（2）In, to step（1）Polymerizate further there is the method for hydrofining reaction and be：By step （1）Polymerizate contact with hydrogen in the presence of Hydrobon catalyst.
The Hydrobon catalyst can select group vib or VIII B races metal, for example can from molybdenum, nickel, ruthenium, One or more in rhodium, cobalt, platinum and palladium, the group vib being preferably supported on carrier or VIII B races metallic catalyst, the load Body can be from one or more in silicon oxide, aluminium oxide, clay, magnesium oxide, titanium oxide and zirconium oxide；
Hydrogen dividing potential drop in the hydrofining reaction be 1～25MPa, preferably 2～20MPa, most preferably 3～15MPa；
The temperature of the hydrofining reaction is 150～350 DEG C, preferably 160～300 DEG C, most preferably 180～260 DEG C；
During it there is hydrofining reaction, the hydrogen and step（1）Polymerizate between volume ratio（Hydrogen oil Than）For 100～2000 (v/v), preferably 200～1500 (v/v), most preferably 250～1000 (v/v)；The body during liquid of the hydrogen Product air speed is 0.2～5h-1, preferably 0.5～3h-1, most preferably 0.6～2.5h-1。
In step（2）Described in hydrofining reaction complete after, collect hydrofining reaction product in lubricating oil Base oil fractions, it is preferred to use distillation cutting method collects lubricant base oil fraction, are most preferably received using distillation cutting method The fraction that more than 350 DEG C of collection.
It is good by the of light color of the preparation-obtained lube base oil of the inventive method, oxidation stability and heat stability, With higher Viscosity Index and excellent cryogenic property, its dynamic viscosity（100℃）For 4～8mm2/ s, Viscosity Index are more than 120, pour point is less than -50 DEG C.The polymerization technique of the inventive method is simple, high income.
Specific embodiment
Unless stated otherwise, percentage ratio mentioned below is mass percent.
The analysis method applied by present embodiment is as follows：
Carbon number distribution is determined according to RIPP-GC47 Fischer-Tropsch oil phase n-alkanols and carbon number distribution；
Sulfur content is measured according to ASTM D7039 light oil sulfur content methods；
Nitrogen content is according to trace N2 method in SH/T0657 Naphtha solvents（Oxidizing fire and chemoluminescence method）Measurement；
Oxygen content is according to ASTM D5622-95 determination of oxygen content（Elemental analyzer method）Measurement；
Lube base oil dynamic viscosity presses GB265 oil product dynamic viscosity algoscopys and dynamic viscosity calculating method is surveyed Amount；
Viscosity Index is calculated according to GB2541 oil product Viscosity Index calculation tables；
Pour point is measured according to GB3535 petroleum products pour points algoscopy；
Catalyst BF3, NaOH is commercially available prod.
Embodiment 1 and comparative example 1
Mixed olefins of the polymer raw adopted by embodiment 1 and comparative example 1 for allotment, its composition are shown in Table 1.
The composition of polymer raw in 1 embodiment 1 of table and comparative example 1
Embodiment 1 and comparative example 1 prepare lubricating oil according to the polymeric reaction condition and hydrofining reaction condition of table 2 respectively Base oil.
2 embodiment 1 of table and 1 reaction process condition of comparative example
The product obtained after polyreaction, hydrofining reaction are carried out to the polymer raw of embodiment 1 and comparative example 1 respectively Distillation cutting is carried out, cutting fraction is mixed into into 4mm respectively2/s、6mm2/s、8mm2The lube base oil product of/s, is as a result shown in Table 3.
3 embodiment 1 of table and 1 result of the test of comparative example
It is not difficult to find out, the inventive method olefin conversion is high, prepared lube base oil high income, viscosity-temperature characteristics energy It is good, low temperature performance excellent.
Embodiment 2
The polymer raw adopted by embodiment 2 is F- T synthesis distillate A, and its physical and chemical index is shown in Table 4.
The physical and chemical index of 4 F- T synthesis distillate A of table
Project Respective value
20 DEG C of density/(Kg m-3) 0.729
Oxygen content/% 0.522
Sulfur content (ug g-1) 1
Nitrogen content (ug g-1) 2
Alcohol content/% 3.840
Arene 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 5 F- T synthesis distillate A of table
H-NMR signs have been carried out to this F- T synthesis distillate, and peak of the chemical shift near 4.8～5.2 is alpha-olefin CH2The chemical shift of hydrogen atom in=structure, chemical shift hydrogen in the peak near 5.7～6.0 is alpha-olefin end position=CH- structures The chemical shift of atom, the chemical potential of chemical shift hydrogen atom in the peak near 5.3～5.5 is internal olefin-CH=CH- structures Move.The integral area at each peak is computed, alpha-olefin accounts for total olefin quality in can calculating this F- T synthesis distillate 97.1%, interior alkene accounts for the 2.9% of total olefin quality.
Embodiment 2 according to table 6 polymeric reaction condition and hydrofining reaction condition prepare lube base oil.
The reaction process condition of 6 embodiment 2 of table
The 4mm prepared by embodiment 22/ s and 6mm2The physical and chemical index of/s products is shown in Table 7.
7 embodiment of table, 2 result of the test
Comparative example 2
The polymer raw adopted by comparative example 2 is F- T synthesis distillate B, and physical and chemical index is shown in Table 8.
The physical and chemical index of 8 F- T synthesis distillate B of table
Project Respective value
20 DEG C of density/(Kg m-3) 0.730
Oxygen content/% 0.500
Sulfur content/(ug g-1) 2
Alcohol content/% 3.061
Nitrogen content/(ug g-1) 3
Arene 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 9 F- T synthesis distillate B of table
H-NMR signs have been carried out to this F- T synthesis distillate feedstock.The integral area at each peak is computed, can be calculated In this F- T synthesis distillate, alpha-olefin accounts for the 96.1% of total olefin quality, and interior alkene accounts for the 3.9% of total olefin quality.
In addition to polymer raw is using F- T synthesis distillate B, the same embodiment of course of reaction and process conditions of comparative example 2 2 is consistent, and experimental condition is shown in Table 6.
The 4mm prepared by comparative example 22/ s and 6mm2The physical and chemical index of the lube base oil product of/s is shown in Table 10.
10 comparative example of table, 2 result of the test
It is not difficult to find out, obtained by embodiment 2, the cryogenic property of the lube base oil of equal viscosity is clearly superior to comparative example 2 In lube base oil.

Claims (15)

1. a kind of preparation method of low-viscosity oil base oil, including：
(1) there is polyreaction in polymer raw in the presence of boron trifluoride；
The polymer raw includes alkene, alcohol and non-essential alkane, and the alkene is C6～C14Alkene；By percentage to the quality, In the polymer raw, olefin(e) centent is 0.2%～2% more than 10%, by the oxygen content that alcohol is provided；With the alkene as base It is accurate and by percentage to the quality, content >=85% of alpha-olefin in the alkene；
(2) further there is hydrofining reaction in the polymerizate of step (1), collect the lubricating oil in hydrofining reaction product Base oil fractions.
2. in accordance with the method for claim 1, it is characterised in that the alkene in the polymer raw is selected from C6～C14It is single Alkene or mixed olefins.
3. in accordance with the method for claim 1, it is characterised in that by percentage to the quality, in the alkene of the polymer raw Containing 0.5%～25% C6～C7Alkene, 60%～98% C8～C12Alkene, 1%～30% C13～C14Alkene, with institute On the basis of stating alkene, content >=95% of alpha-olefin in the alkene.
4. in accordance with the method for claim 3, it is characterised in that by percentage to the quality, in the polymer raw, alkene contains Amount is more than 25%.
5. in accordance with the method for claim 1, it is characterised in that the alcohol in the polymer raw is selected from C1～C12Single alcohol Or mixed alcohol.
6. in accordance with the method for claim 5, it is characterised in that the alcohol in the polymer raw is selected from C2～C10It is single just Structure alcohol or mixing n-alkanol.
7. in accordance with the method for claim 1, it is characterised in that the alcohol in the polymer raw is selected from C2～C10Single primary Alcohol or mixing primary alconol, in the polymer raw by alcohol provide oxygen content be 0.25%～1.5%.
8. in accordance with the method for claim 1, it is characterised in that include alkane in described polymer raw, the alkane is C4 ～C15Alkane, the mass ratio of the alkane and the alkene is 5:1～1:5.
9. in accordance with the method for claim 1, it is characterised in that the polymer raw is by Fischer-Tropsch synthesis oil, wax destructive distillation alkene One or more Jing distillation cutting in hydrocarbon and coking distillate is obtained or the blending of the additional alkene, alcohol or alkane is formed.
10. in accordance with the method for claim 1, it is characterised in that the polymer raw is Fischer-Tropsch synthesis oil.
11. according to the method described in one of claim 1-10, it is characterised in that the polymer raw is deposited in boron trifluoride In the lower process conditions that polyreaction occurs it is：The temperature of polyreaction is -10～120 DEG C, time of polyreaction is 15～ 360min, the pressure of polyreaction is 0.1～1MPa.
12. according to the method described in one of claim 1-10, it is characterised in that in step (2), to step (1) Further there is the method for hydrofining reaction in polymerizate：The polymerizate of step (1) is deposited in Hydrobon catalyst Contact with hydrogen lower.
13. in accordance with the method for claim 12, it is characterised in that the Hydrobon catalyst is selected from group vib or VIII Race's metal, the hydrogen dividing potential drop in the hydrofining reaction are 1～25MPa, and the temperature of the hydrofining reaction is 150～350 DEG C, the volume ratio between the polymerizate of the hydrogen and step (1) be 100～2000 (v/v), the volume during liquid of the hydrogen Air speed is 0.2～5h-1。
14. according to the method described in one of claim 1-10, it is characterised in that the hydrogenation essence described in step (2) After reaction processed is completed, lubricant base oil fraction is collected using distillation cutting method.
15. in accordance with the method for claim 14, it is characterised in that the hydrofining reaction described in step (2) is completed Afterwards, more than 350 DEG C of lubricant base oil fraction is collected with distillation cutting method.
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