CN106957666A - The preparation method of biological poly alhpa olefin artificial oil - Google Patents
The preparation method of biological poly alhpa olefin artificial oil Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
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- 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
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used
- C10G2/331—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals
- C10G2/332—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals of the iron-group
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- 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
- C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
- C10G57/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process with polymerisation
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/34—Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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Abstract
The invention discloses a kind of preparation method of biological poly alhpa olefin artificial oil, including：Lignocellulose raw material is obtained after hydrolysis in lignin semicoke, lignin semicoke, and the weight percentage of semicoke is 88 92%, and the weight percentage of ash content is 8 12%；Lignin char Gasification obtains crude synthesis gas；Crude synthesis gas is varied, elution processes production synthesis gas；Synthesis gas Fischer-Tropsch synthesis or F-T produces head fraction；The two sections of polymerizations of fore-running lease making, alkylation process production biological poly alhpa olefin artificial oil.The present invention has raw material cheap and easy to get, and process green, the features such as properties of product are reliable is adapted to industrialized production.
Description
Technical field
The present invention relates to a kind of biochemical technology, specifically, it is related to a kind of preparation of biological poly alpha olefine synthetic oil
Method
Background technology
The mankind use inherently one history of social development of history of lubricant, and from early stage, simply use environment is harmless
Animal and plant fat lubricant, develop into largely use it is various high performance but environmentally harmful by representative of petroleum based oil
Lubricant, and then seek new concept-" lubrication+environmental protection+energy-conservation " of modern lubrication.
Modern industry proposes that wide temperature range, low frictional resistance, high abrasion, long-life, environment-friendly etc. are required to lubricant.Make at present
Mineral based lubricants have a common feature, i.e., because demand is improved constantly, be reached their performance pole
Limit, often occurs that premature abrasion destruction, short life, energy resource consumption be more, liquid waste processing is difficult.
Syntholube is by the lubricant of the compound chemical synthesis of diverse separation.Meeting strict specification
It is required that and keep to the use of syntholube being the best way in equipment protection, environmental protection, healthy and safe challenge, can
To reach the purpose of " lubrication+environmental protection+energy-conservation ".
Lube base oil is classified by API (American Petroleum Institute (API)), is divided into five major classes (I, II, III, IV, V class), its
In, I, II, Group III are mineral oil, and IV is poly alpha olefine synthetic oil, and V classes are other synthetic lubricant fluids.
Poly alpha olefine synthetic oil uses ethylene oligomerization and wax destructive distillation synthetic method in advance, and the performance of product is not so good, viscosity
Index reaches more than 100；Later using the higher olefin polymer of F- T synthesis, such as 1- decene, carbon laurylene, carbon tetradecene etc.
Thermal polymerization is carried out, the Performance comparision of product is preferable, and viscosity index (VI) reaches more than 150.Manufacturer is concentrated mainly on U.S., Europe, South Africa
With Japan and other countries and area.
The raw material of synthetic gas of F- T synthesis is typically from coal, natural gas and oil.Directly produced with lignocellulose raw material
Biosynthesis gas, because material calorific value is low, causes gasification temperature low, produces tar in gasification, blocks pipeline, thus so far without
Ripe Large Scale and Continuous equipment for gasification.And it is defocused that wood fiber biomass is transformed into lignin half, its calorific value is close to mark
Coal, carbon content can be gasified using large-scale coal gasification apparatus more than 90%, the road of gasification of biomass got through indirectly
Footpath, with cost of material it is low, without pretreatment, gasification process it is ripe the features such as, the commercial operation of biosynthesis gas can be achieved.
Lignin base synthesis gas is adopted through the technique productions poly alpha olefin such as F- T synthesis, polymerization, alkylation, raw material without sulphur environmental protection,
Technical maturity, the features such as equipment investment is few, conversion process is simple, comprehensive cost effectiveness is better than fossil based raw material gas.
Catalyst used by polymerization technique includes Ziegler catalyst, three-way catalyst (by the hydride of alkali metal, with aluminium
And the halide composition of titanium) or Fred-Kerafyrm hereby catalyst (BF3, AlCl3, SnCl4, SnF4) etc., mostly there is process
Contamination phenomenon.
The content of the invention
Technical problem solved by the invention is to provide a kind of preparation method of biological poly alpha olefine synthetic oil, with original
Material is cheap and easy to get, and process green, the features such as properties of product are reliable is adapted to industrialized production.
Technical scheme is as follows：
A kind of preparation method of biological poly alpha olefine synthetic oil, including：
Lignocellulose raw material is obtained after hydrolysis in lignin semicoke, lignin semicoke, and the weight percentage of semicoke is
88-92%, the weight percentage of ash content is 8-12%；
Lignin char Gasification obtains crude synthesis gas；
Crude synthesis gas is varied, elution processes production synthesis gas；
Synthesis gas Fischer-Tropsch synthesis or F-T produces head fraction；
The two sections of polymerizations of fore-running lease making, alkylation process production biological poly alpha olefine synthetic oil.
Further, the production process of lignin semicoke includes：
The first stage hydrolysis of lignocellulose raw material, xylo-oligosaccharide is converted into by the hemicellulose in lignocellulose raw material；
First stage hydrolyzes：Temperature is 200-240 DEG C, pressure is 2.2-2.4MPa, and time 0.5-5 minute, reaction is former by wood fibre
Hemicellulose in material is converted into xylo-oligosaccharide；
The second segment hydrolysis of lignocellulose raw material, cellooligosaccharide is converted into by the cellulose in lignocellulose raw material；The
Two-stage hydrolyzes：Temperature is 180-200 DEG C, pressure is 1.4-1.6MPa, time 10-30 minute, and reaction is by lignocellulose raw material
In cellulose be converted into cellooligosaccharide.
The phase III hydrolysis of lignocellulose raw material, acetic acid is catalyst, and temperature is 180-200 DEG C, and pressure is 1.4-
1.6MPa, time 5-20 minute, lignin conversion is lignin semicoke.
Further, lignin char Gasification, which obtains the production process of crude synthesis gas, includes：
Using lignin semicoke as raw material, using space flight stove gasification installation, air separation unit yield is 52000Nm3/ h, oxygen is extracted
Rate is more than 90%, and gasifying agent is 99.6% pure oxygen；
Feeding manner is semicoke dry-coal feeding, and conveying gas is CO2, single injector spurts into gasification to feeding burner from top to bottom
Stove, gasification temperature is 1250-1450 DEG C, and pressure is 3-3.5MPa, the crude synthesis gas and slag of the generation deslagging after water Quench, slightly
Synthesis gas is discharged on shock chamber top, enters subsequent handling after further cooling, dedusting.
Further, the production process that crude synthesis gas is varied, elution processes produce synthesis gas includes：
Crude synthesis gas adjusts H through vapor transformationreation device2Ratio with CO is 1.3-1.5, uses iron for catalyst,
Pressure 0.8-1MPa, reaction temperature is 220-280 DEG C, and the conversion gas of generation turns into：33-39%H2, 26-28%CO, 33-35%
CO2；
Conversion gas removes CO through low-temp methanol washing process again2Gas, gas cooling is washed tower to reduce to 10 DEG C into ammonia
NH3With HCN contents, then in -21 DEG C of temperature, CO is sprayed under pressure 3.43MPa2Absorption tower, with -53 DEG C of methanol absorption CO2,
Obtain synthesis gas.
Further, synthesis gas Fischer-Tropsch synthesis or F-T production head fraction uses slurry bed system F-T reactors, and raw material is synthesis gas, catalysis
Agent is Fe-series catalyst, 230-250 DEG C of reaction temperature, pressure 2.5-3.5Mpa；Reaction generation head fraction.
Further, the step of two sections of polymerizations of fore-running lease making, alkylation process production biological poly alpha olefine synthetic oil includes：
One-step polymerization produces oligomer；Raw material is head fraction, using polymerization reaction kettle, including first paragraph polymerisation, is urged
Agent is trifluoromethanesulfonic acid based composite catalyst, and consumption 1-2wt%, reaction temperature is 50-80 DEG C, and pressure is 0.1-0.3MPa；
Reaction time 1-2h, one-step polymerization reaction terminates rear oil product and separated into separator；
Separating technology is divided into two sections, and first section is low temperature crystallization, and temperature is -30 DEG C, solid precipitate (C11Above alkane group
Point) removed through filtering technique；Secondary segment is separated into distilation, and temperature is 180 DEG C, steams cut for C10Following alkane；Through two sections
Oligomer is obtained after separating technology purification；
Two sections of polymerization high polymers；Second segment polymerisation is carried out by raw material of oligomer, n-butanol is initiator, nitrogen
Start reaction after gas displacement, reaction temperature is 150-200 DEG C, and pressure is 0.3-0.5MPa；Time 4-6h, catalyst is urged for ternary
Agent, consumption 1-2wt%, obtains high polymer；
High polymer contains double bond, is subject to saturation by isoparaffin alkylation reaction；Isoparaffin is isopentane, in autoclave
Is reacted with high polymer in reactor, reaction temperature is 100-200 DEG C, pressure is 1-3MPa, catalyst amount 1-2wt%,
Hydrocarbon mixture and poly alpha olefin mol ratio 8-15:1, reaction time 1-2h；Alkylated reaction removes not anti-through vacuum distillation after terminating
Thing is answered, biological poly alpha olefine synthetic oil finished product is obtained.
Further：Three-way catalyst selects lanthanum hydroxide, cerium mixture/chromium-silicon composite catalyst, isoparaffin alkylation
The catalyst of reaction is trifluoromethanesulfonic acid based composite catalyst.
Further：Acetic acid concentration is 95%wt, and acetic acid consumption is the 0.5-0.8% of raw material gross weight.
Compared with prior art, the technology of the present invention effect includes：
The lignin semicoke that the present invention is produced using lignocellulose raw material through pipe race step decompressing and continuous hydrolysis process is original
Material, biological poly alpha olefine synthetic oil is produced through char Gasification, F- T synthesis, two sections of polymerizations, alkylated reactions, honest and clean with raw material
Valency is easy to get, and process green, the features such as properties of product are reliable is adapted to industrialized production.
(1) wood fibre (urban garden and green space system residue, agriculture and forestry organic waste material, resource crop etc.) raw material is utilized, it is cheap easy
Obtain, mostly waste resource, belong to twice laid.
(2) hemicellulose, cellulose and lignin are separately converted to using pipe race's step decompressing and continuous hydrolysis process low
Xylan, cellooligosaccharide and lignin semicoke, realize that wooden resource full constituent is utilized.
(3) lignin semicoke calorific value is 5500-6500 kilocalories, close to mark coal, and without sulphur, contributes to present coal gas in fact
Disguise the direct utilization put, greatly reduce equipment investment.
(4) using lignin semicoke production biological poly alpha olefine synthetic oil, raw material is without sulphur, technical maturity, equipment investment
Few, the features such as conversion process is simple, comprehensive cost effectiveness is better than fossil based raw material gas.
(5) lignin semicoke production biosynthesis air to close key technology.
Using space flight stove gasification installation, semicoke sized particles are 40-90 μm, can directly use dry-coal feeding, gasification temperature
1350-1500 DEG C, while the thermal efficiency 95% and efficiency of carbon con version 99% are realized, the synthesis gas CO+H of production2>=93%, technology into
Ripe, product is stable.
(6) head fraction alkylation key technology.
Reaction is alkylated using isopentane and iso-butane hydrocarbon mixture, it is compound using new catalyst trifluoromethanesulfonic acid base
Catalyst, can be achieved the features such as alkylation process green, product separating-purifying are simple, reaction transformation efficiency is high.
(7) alpha-olefin synthesizing poly alpha-olefin key technology
Using two sections of polymerisations, new catalyst trifluoromethanesulfonic acid base complex is respectively adopted and lanthanum hydroxide, cerium are mixed
Compound/chromium-silicon compound, consumption 1-2wt%.Alpha-olefin conversion ratio is up to 99%.
Double bond removes change conventional selective and is hydrogenated with this high-risk, high energy consumption and inefficient processing mode, selects same on the contrary
Isopentane and iso-butane hydrocarbon mixture are alkylated reaction, substantially reduce energy consumption, improve safety coefficient and efficiency, product is stable.
Brief description of the drawings
Fig. 1 is the technique that lignocellulose raw material obtains lignin semicoke after the step decompressing and continuous hydrolysis of pipe race in the present invention
Route map；
Fig. 2 is the process route chart that lignin char Gasification obtains crude synthesis gas in the present invention；
Fig. 3 is the process route chart that crude synthesis gas is varied in the present invention, elution processes produce synthesis gas；
Fig. 4 is the process route chart of synthesis gas Fischer-Tropsch synthesis or F-T production head fraction in the present invention；
Fig. 5 is the two sections of polymerizations of fore-running lease making, the work of alkylation process production biological poly alpha olefine synthetic oil in the present invention
Skill route map.
Embodiment
Technical solution of the present invention is elaborated below with reference to example embodiment.However, example embodiment can
Implement in a variety of forms, and be not understood as limited to embodiment set forth herein；On the contrary, thesing embodiments are provided so that
The design of example embodiment more comprehensively and completely, and is comprehensively conveyed to those skilled in the art by the present invention.
As shown in figure 1, being that lignocellulose raw material obtains lignin half after the step decompressing and continuous hydrolysis of pipe race in the present invention
Burnt process route chart.
The preparation method of biological poly alpha olefine synthetic oil, specifically includes following steps：
Step 1：Lignocellulose raw material obtains lignin semicoke (hundred containing composition after the step decompressing and continuous hydrolysis of pipe race
Divide ratio：Semicoke content 88-92%, content of ashes 8-12%, calorific value 5500-6500 kilocalorie)；
Step 11：The first stage hydrolysis of lignocellulose raw material, the hemicellulose in lignocellulose raw material is converted into low
Xylan；
First stage hydrolyzes：Temperature is 200-240 DEG C, pressure is 2.2-2.4MPa, time 0.5-5 minute, and reaction is by wood
Hemicellulose in matter fibrous raw material is converted into xylo-oligosaccharide.
Step 12：The second segment hydrolysis of lignocellulose raw material, is converted into fiber low by the cellulose in lignocellulose raw material
Glycan；
Second stage is hydrolyzed：Temperature is 180-200 DEG C, pressure is 1.4-1.6MPa, time 10-30 minute, and reaction is by wood
Cellulose in matter fibrous raw material is converted into cellooligosaccharide.
Step 13：The phase III hydrolysis of lignocellulose raw material, by the lignin in lignocellulose raw material, (fiber is oligomeric
Sugar, xylo-oligosaccharide) it is converted into lignin semicoke.
Concentration 95%wt acetic acid catalysts (acetic acid consumption is the 0.5-0.8% of raw material total amount), temperature is 180-200 DEG C,
Pressure is 1.4-1.6MPa, and time 5-20 minute, lignin conversion is lignin semicoke.
Semicoke lignin
| Particle size (μm) | Water content (wt%) | Phosphorus content (%) |
| 40-90 | 2-5 | 90-95 |
As shown in Fig. 2 being the process route chart that lignin char Gasification obtains crude synthesis gas in the present invention.
Step 2：Lignin char Gasification obtains crude synthesis gas；
Using lignin semicoke as raw material, using space flight stove gasification installation, air separation unit yield is 52000Nm3/ h, oxygen is extracted
Rate is more than 90%, and gasifying agent is 99.6% pure oxygen.
Feeding manner is semicoke dry-coal feeding (40-90 μm of particle), and conveying gas is CO2, discharge pressure is 4.0MPa, is sent
Entering burner, single injector spurts into gasification furnace from top to bottom, and gasification temperature is 1250-1450 DEG C, and pressure is 3-3.5MPa, generation
Crude synthesis gas and the slag deslagging after water Quench, crude synthesis gas are discharged on shock chamber top, are entered after further cooling, dedusting
Subsequent handling.
Crude synthesis gas key component is：
| CO | H2 | CO2 | CH4 | Sulfide |
| 59-61% | 31-33% | 4-8% | 0.1%-0.5% | Less than 0.05ppm |
As shown in figure 3, being the process route chart that crude synthesis gas is varied in the present invention, elution processes produce synthesis gas.
Step 3：Crude synthesis gas is varied, elution processes production synthesis gas；
Crude synthesis gas adjusts H through vapor transformationreation device2Ratio with CO is 1.3-1.5, uses iron for catalyst,
Pressure 0.8-1MPa, reaction temperature is 220-280 DEG C；The conversion gas basic parameter of generation is as follows：Flow 178000m3/ h, temperature
40 DEG C, pressure 3.5MPa, gas, which is constituted, is：33-39%H2, 26-28%CO, 33-35%CO2。
Conversion gas removes CO through low-temp methanol washing process again2Gas, gas cooling is washed tower to reduce to 10 DEG C into ammonia
NH3With HCN contents, CO is then sprayed into2Absorption tower (- 21 DEG C of temperature, pressure 3.43MPa) (- 53 DEG C) absorption CO of methanol2, obtain
Synthesis gas.
Reaction equation is as follows：
CH4+H2O→CO+H2
CO+H2O→CO2+H2
Synthesis gas gas componant is as follows：
| CO | H2 | CO2 | Sulfide |
| 40-41.4% | 58-59% | Less than 0.064 | Less than 0.05ppm |
As shown in figure 4, being the process route chart of synthesis gas Fischer-Tropsch synthesis or F-T production head fraction in the present invention.
Step 4：Synthesis gas Fischer-Tropsch synthesis or F-T produces head fraction；
Using slurry bed system F-T reactors, raw material is synthesis gas, and catalyst is middle section ICC-II sections series catalysts, reaction
230-250 DEG C of temperature, pressure 2.5-3.5Mpa；Reaction generation head fraction.
Reaction equation is as follows：
nCO+2nH2→CnH2n+nH2O
2nCO+nH2→CnH2n+nCO2
3nCO+nH2O→CnH2n+2nCO2
nCO2+3nH2→CnH2n+2nH2O
Head fraction (C5-C16Based on) constitute as follows：
| Total olefin | Total alkane | Oxygenatedchemicals |
| 56-62% | 35-38% | 2-4% |
As shown in figure 5, being the two sections of polymerizations of fore-running lease making, alkylation process production biological poly alpha-olefin synthesis in the present invention
The process route chart of oil.
Step 5：The two sections of polymerizations of fore-running lease making, alkylation process production biological poly alpha olefine synthetic oil.
Reactant is head fraction, including：
Step 51：One-step polymerization produces oligomer：Raw material is head fraction, is polymerize using polymerization reaction kettle, including first paragraph
Reaction, catalyst is trifluoromethanesulfonic acid based composite catalyst, and consumption 1-2wt%, reaction temperature is 50-80 DEG C, and pressure is 0.1-
0.3MPa；Reaction time 1-2h, one-step polymerization reaction terminates rear oil product and separated into separator；
Step 52：Separating technology is divided into two sections, and first section is low temperature crystallization, and temperature is -30 DEG C, solid precipitate (C11More than
Alkane component) removed through filtering technique；Secondary segment is separated into distilation, and temperature is 180 DEG C, steams cut for C10Following alkane；
Oligomer is obtained after being purified through two-phase seperation technique；
Step 53：Two sections of polymerization high polymers：Second segment polymerisation is carried out by raw material of oligomer, n-butanol is to draw
Send out and start reaction after agent, nitrogen displacement, reaction temperature is 150-200 DEG C, and pressure is 0.3-0.5MPa；Time 4-6h, catalyst
For three-way catalyst (lanthanum hydroxide, cerium mixture/chromium-silicon composite catalyst), consumption 1-2wt%.Alpha-olefin conversion ratio is
99%, obtain high polymer；
Step 54：Above-mentioned high polymer contains double bond, is subject to saturation by isoparaffin alkylation reaction.Isoparaffin is different
Pentane, is reacted in tank reactor with high polymer, and reaction temperature is 100-200 DEG C, and pressure is 1-3MPa, and catalyst is
Trifluoromethanesulfonic acid based composite catalyst, consumption 1-2wt%, hydrocarbon mixture and poly alpha olefin mol ratio 8-15:1, reaction time 1-2h.
Alkylated reaction removes unreacted reactant after terminating through vacuum distillation, obtains biological poly alpha olefine synthetic oil finished product.
Reaction equation is as follows：
Polymerisation
Alkylated reaction
Biological poly alpha-olefin performance indications such as following table：
Poly ＆ Alpha ,-olefin oil technical conditions and test method
Embodiment 1：
(1) 200kg maize straws (moisture content 25%) are crushed to below 1cm, anti-into the step decompressing and continuous hydrolysis of pipe race
Answer device, including first stage hydrolysis：Temperature is 205-210 DEG C, pressure is 2.2-2.3MPa, and 3 minutes time, half in stalk is fine
Dimension element is converted into xylo-oligosaccharide and is percolated out；Cellulose and lignin are hydrolyzed into second stage：Temperature is 180-185 DEG C, pressure
Power is 1.4-1.5MPa, 20 minutes time, the cellulose in stalk is converted into cellooligosaccharide and is percolated out；Lignin enters
Phase III hydrolyzes：95%wt acetic acid catalysts, temperature is 180-185 DEG C, pressure is 1.4-1.5MPa, 10 minutes time, wood
Mediated conversion is lignin semicoke 114.2kg (aqueous 37-40%).
(2) using the dry lignin semicokes of 72kg as raw material (aqueous 2-5%), using space flight stove gasification installation, air separation unit production
Measure as 52000Nm3/ h, oxygen extraction ratio is more than 90%, and gasifying agent is 99.6% pure oxygen.
Feeding manner is semicoke dry-coal feeding (40-90 μm of particle), and conveying gas is CO2, discharge pressure 4.0MPa, feeding
Single injector spurts into gasification furnace, 1250-1450 DEG C of gasification temperature to burner from top to bottom, and pressure is 3-3.5MPa, the thick conjunction of generation
Into gas and slag after water Quench deslagging, crude synthesis gas discharges on shock chamber top, enters follow-up through further cooling, after dedusting
Process.Crude synthesis gas key component is：35%H2, 39%CO, 11%CO2, 14%H2O and micro H2S、N2、CH4Deng gas.
(3) crude synthesis gas adjusts H through vapor transformationreation device2Ratio with CO is 1.38, uses iron for catalyst,
Pressure 0.8-1MPa, reaction temperature is 220-280 DEG C；The conversion gas basic parameter of generation is as follows：Flow 178000m3/ h, temperature
40 DEG C, pressure 3.5MPa, gas, which is constituted, is：36%H2, 26%CO, 38%CO2。
Conversion gas removes CO through low-temp methanol washing process again2Gas, gas cooling is washed tower to reduce to 10 DEG C into ammonia
NH3With HCN contents, CO is then sprayed into2Absorption tower (- 21 DEG C of temperature, pressure 3.43MPa) (- 53 DEG C) absorption CO of methanol2, obtain
Synthesis gas.
(4) slurry bed system F-T reactors are used, raw material is synthesis gas, and catalyst is middle section ICC-II sections series catalysts, instead
Answer 230-250 DEG C of temperature, pressure 2.5-3.5Mpa；Reaction generation head fraction 18kg.
(5) one-step polymerization production oligomer：Raw material is 18kg head fractions, is polymerize using polymerization reaction kettle, including first paragraph
Reaction, catalyst is trifluoromethanesulfonic acid based composite catalyst, and consumption 1-2wt%, reaction temperature is 50-80 DEG C, and pressure is 0.1-
0.3MPa；Reaction time 1.5h, one-step polymerization reaction terminates rear oil product and separated into separator.
Separating technology is divided into two sections, and first section is low temperature crystallization, and temperature is -30 DEG C, solid precipitate (C11Above alkane group
Point) removed through filtering technique；Secondary segment is separated into distilation, and temperature is 180 DEG C, steams cut for C10Following alkane；Through two sections
Oligomer 9.5kg is obtained after separating technology purification.
Two sections of polymerization high polymers：Second segment polymerisation is carried out by raw material of oligomer, n-butanol is initiator, nitrogen
Start reaction after gas displacement, reaction temperature is 150-200 DEG C, and pressure is 0.3-0.5MPa；Time 5h, catalyst is three-element catalytic
Agent (lanthanum hydroxide, cerium mixture/chromium-silicon composite catalyst), consumption 1.2wt%.Alpha-olefin conversion ratio is 99%, is obtained
9.2kg high polymers.
Above-mentioned high polymer contains double bond, is subject to saturation by isoparaffin alkylation reaction.Isoparaffin is isopentane,
Reacted in tank reactor with high polymer, reaction temperature is 100-200 DEG C, and pressure is 1-3MPa, and catalyst is fluoroform
Sulfonic acid based composite catalyst, consumption 1.5wt%, hydrocarbon mixture and poly alpha olefin mol ratio 9:1, reaction time 1.5h.Alkylation is anti-
Unreacted reactant is removed through vacuum distillation after should terminating, 10kg biological poly alpha olefine synthetic oils are obtained.
Biological poly alhpa olefin artificial oil characteristic index：
Embodiment 2：
(1) 200kg maize straws (moisture content 25%) are crushed to below 1cm, anti-into the step decompressing and continuous hydrolysis of pipe race
Answer device, including first stage hydrolysis：Temperature is 205-210 DEG C, pressure is 2.2-2.3MPa, and 3 minutes time, half in stalk is fine
Dimension element is converted into xylo-oligosaccharide and is percolated out；Cellulose and lignin are hydrolyzed into second stage：Temperature is 180-185 DEG C, pressure
Power is 1.4-1.5MPa, 20 minutes time, the cellulose in stalk is converted into cellooligosaccharide and is percolated out；Lignin enters
Phase III hydrolyzes：95%wt acetic acid catalysts, temperature is 180-185 DEG C, pressure is 1.4-1.5MPa, 10 minutes time, wood
Mediated conversion is lignin semicoke 118.2kg (aqueous 37-40%).
(2) using the dry lignin semicokes of 74kg as raw material (aqueous 2-5%), using space flight stove gasification installation, air separation unit production
Measure as 52000Nm3/ h, oxygen extraction ratio is more than 90%, and gasifying agent is 99.6% pure oxygen.
Feeding manner is semicoke dry-coal feeding (40-90 μm of particle), and conveying gas is CO2, discharge pressure 4.0MPa, feeding
Single injector spurts into gasification furnace, 1250-1450 DEG C of gasification temperature to burner from top to bottom, and pressure is 3-3.5MPa, the thick conjunction of generation
Into gas and slag after water Quench deslagging, crude synthesis gas discharges on shock chamber top, enters follow-up through further cooling, after dedusting
Process.Crude synthesis gas key component is：35%H2, 38%CO, 10%CO2, 16%H2O and micro H2S、N2、CH4Deng gas.
(3) crude synthesis gas adjusts H through vapor transformationreation device2Ratio with CO is 1.39, uses iron for catalyst,
Pressure 0.8-1MPa, reaction temperature is 220-280 DEG C；The conversion gas basic parameter of generation is as follows：Flow 178000m3/ h, temperature
40 DEG C, pressure 3.5MPa, gas, which is constituted, is：39%H2, 28%CO, 33%CO2。
Conversion gas removes CO through low-temp methanol washing process again2Gas, gas cooling is washed tower to reduce to 10 DEG C into ammonia
NH3With HCN contents, CO is then sprayed into2Absorption tower (- 21 DEG C of temperature, pressure 3.43MPa) (- 53 DEG C) absorption CO of methanol2, obtain
Synthesis gas.
(4) slurry bed system F-T reactors are used, raw material is synthesis gas, and catalyst is middle section ICC-II sections series catalysts, instead
Answer 230-250 DEG C of temperature, pressure 2.5-3.5Mpa；Reaction generation head fraction 18.5kg.
(5) one-step polymerization production oligomer：Raw material is 18.5kg head fractions, poly- using polymerization reaction kettle, including first paragraph
Reaction is closed, catalyst is trifluoromethanesulfonic acid based composite catalyst, and consumption 1.2wt%, reaction temperature is 50-80 DEG C, and pressure is
0.1-0.3MPa；Reaction time 1.2h, one-step polymerization reaction terminates rear oil product and separated into separator.
Separating technology is divided into two sections, and first section is low temperature crystallization, and temperature is -30 DEG C, solid precipitate (C11Above alkane group
Point) removed through filtering technique；Secondary segment is separated into distilation, and temperature is 180 DEG C, steams cut for C10Following alkane；Through two sections
Oligomer 9.8kg is obtained after separating technology purification.
Two sections of polymerization high polymers：Second segment polymerisation is carried out by raw material of oligomer, n-butanol is initiator, nitrogen
Start reaction after gas displacement, reaction temperature is 150-200 DEG C, and pressure is 0.3-0.5MPa；Time 4-6h, catalyst is urged for ternary
Agent (lanthanum hydroxide, cerium mixture/chromium-silicon composite catalyst), consumption 1.2wt%.Alpha-olefin conversion ratio is 99%, is obtained
9.5kg high polymers.
Above-mentioned high polymer contains double bond, is subject to saturation by isoparaffin alkylation reaction.Isoparaffin is isopentane,
Reacted in tank reactor with high polymer, reaction temperature is 100-200 DEG C, and pressure is 1-3MPa, and catalyst is fluoroform
Sulfonic acid based composite catalyst, consumption 1.4wt%, hydrocarbon mixture and poly alpha olefin mol ratio 10:1, reaction time 1.2h.Alkylation is anti-
Unreacted reactant is removed through vacuum distillation after should terminating, 10.2kg poly alpha olefine synthetic oils are obtained.
Poly-a-olefin oil characteristic index is as follows：
Embodiment 3：
(1) 200kg maize straws (moisture content 25%) are crushed to below 1cm, anti-into the step decompressing and continuous hydrolysis of pipe race
Answer device, including first stage hydrolysis：Temperature is 205-210 DEG C, pressure is 2.2-2.3MPa, and 3 minutes time, half in stalk is fine
Dimension element is converted into xylo-oligosaccharide and is percolated out；Cellulose and lignin are hydrolyzed into second stage：Temperature is 180-185 DEG C, pressure
Power is 1.4-1.5MPa, 20 minutes time, the cellulose in stalk is converted into cellooligosaccharide and is percolated out；Lignin enters
Phase III hydrolyzes：95%wt acetic acid catalysts, temperature is 180-185 DEG C, pressure is 1.4-1.5MPa, 10 minutes time, wood
Mediated conversion is lignin semicoke 115.2kg (aqueous 37-40%).
(2) using the dry lignin semicokes of 73kg as raw material (aqueous 2-5%), using space flight stove gasification installation, air separation unit production
Measure as 52000Nm3/ h, oxygen extraction ratio is more than 90%, and gasifying agent is 99.6% pure oxygen.
Feeding manner is semicoke dry-coal feeding (40-90 μm of particle), and conveying gas is CO2, discharge pressure 4.0MPa, feeding
Single injector spurts into gasification furnace, 1250-1450 DEG C of gasification temperature to burner from top to bottom, and pressure is 3-3.5MPa, the thick conjunction of generation
Into gas and slag after water Quench deslagging, crude synthesis gas discharges on shock chamber top, enters follow-up through further cooling, after dedusting
Process.Crude synthesis gas key component is：36%H2, 37%CO, 10%CO2, 16%H2O and micro H2S、N2、CH4Deng gas.
(3) crude synthesis gas adjusts H through vapor transformationreation device2Ratio with CO is 1.39, uses iron for catalyst,
Pressure 0.8-1MPa, reaction temperature is 220-280 DEG C；The conversion gas basic parameter of generation is as follows：Flow 178000m3/ h, temperature
40 DEG C, pressure 3.5MPa, gas, which is constituted, is：39%H2, 28%CO, 33%CO2。
Conversion gas removes CO through low-temp methanol washing process again2Gas, gas cooling is washed tower to reduce to 10 DEG C into ammonia
NH3With HCN contents, CO is then sprayed into2Absorption tower (- 21 DEG C of temperature, pressure 3.43MPa) (- 53 DEG C) absorption CO of methanol2, obtain
Synthesis gas.
(4) slurry bed system F-T reactors are used, raw material is synthesis gas, and catalyst is middle section ICC-II sections series catalysts, instead
Answer 230-250 DEG C of temperature, pressure 2.5-3.5Mpa；Reaction generation head fraction 18.2kg.
(5) one-step polymerization production oligomer：Raw material is 18.2kg head fractions, poly- using polymerization reaction kettle, including first paragraph
Reaction is closed, catalyst is trifluoromethanesulfonic acid based composite catalyst, and consumption 1.2wt%, reaction temperature is 50-80 DEG C, and pressure is
0.1-0.3MPa；Reaction time 1.2h, one-step polymerization reaction terminates rear oil product and separated into separator.
Separating technology is divided into two sections, and first section is low temperature crystallization, and temperature is -30 DEG C, solid precipitate (C11Above alkane group
Point) removed through filtering technique；Secondary segment is separated into distilation, and temperature is 180 DEG C, steams cut for C10Following alkane；Through two sections
Oligomer 9.6kg is obtained after separating technology purification.
Two sections of polymerization high polymers：Second segment polymerisation is carried out by raw material of oligomer, n-butanol is initiator, nitrogen
Start reaction after gas displacement, reaction temperature is 150-200 DEG C, and pressure is 0.3-0.5MPa；Time 4-6h, catalyst is urged for ternary
Agent (lanthanum hydroxide, cerium mixture/chromium-silicon composite catalyst), consumption 1.2wt%.Alpha-olefin conversion ratio is 99%, is obtained
9.4kg high polymers.
Above-mentioned high polymer contains double bond, is subject to saturation by isoparaffin alkylation reaction.Isoparaffin is isopentane,
Reacted in tank reactor with high polymer, reaction temperature is 100-200 DEG C, and pressure is 1-3MPa, and catalyst is fluoroform
Sulfonic acid based composite catalyst, consumption 1.4wt%, hydrocarbon mixture and poly alpha olefin mol ratio 10:1, reaction time 1.2h.Alkylation is anti-
Unreacted reactant is removed through vacuum distillation after should terminating, 10.1kg poly alpha olefine synthetic oils are obtained.
Poly-a-olefin oil characteristic index is as follows：
Embodiment 4：
(1) 200kg maize straws (moisture content 25%) are crushed to below 1cm, anti-into the step decompressing and continuous hydrolysis of pipe race
Answer device, including first stage hydrolysis：Temperature is 205-210 DEG C, pressure is 2.2-2.3MPa, and 3 minutes time, half in stalk is fine
Dimension element is converted into xylo-oligosaccharide and is percolated out；Cellulose and lignin are hydrolyzed into second stage：Temperature is 180-185 DEG C, pressure
Power is 1.4-1.5MPa, 20 minutes time, the cellulose in stalk is converted into cellooligosaccharide and is percolated out；Lignin enters
Phase III hydrolyzes：95%wt acetic acid catalysts, temperature is 180-185 DEG C, pressure is 1.4-1.5MPa, 10 minutes time, wood
Mediated conversion is lignin semicoke 119.2kg (aqueous 37-40%).
(2) using the dry lignin semicokes of 74.5kg as raw material (aqueous 2-5%), using space flight stove gasification installation, air separation unit
Yield is 52000Nm3/ h, oxygen extraction ratio is more than 90%, and gasifying agent is 99.6% pure oxygen.
Feeding manner is semicoke dry-coal feeding (40-90 μm of particle), and conveying gas is CO2, discharge pressure 4.0MPa, feeding
Single injector spurts into gasification furnace, 1250-1450 DEG C of gasification temperature to burner from top to bottom, and pressure is 3-3.5MPa, the thick conjunction of generation
Into gas and slag after water Quench deslagging, crude synthesis gas discharges on shock chamber top, enters follow-up through further cooling, after dedusting
Process.Crude synthesis gas key component is：36%H2, 37%CO, 10%CO2, 16%H2O and micro H2S、N2、CH4Deng gas.
(3) crude synthesis gas adjusts H through vapor transformationreation device2Ratio with CO is 1.36, uses iron for catalyst,
Pressure 0.8-1MPa, reaction temperature is 220-280 DEG C；The conversion gas basic parameter of generation is as follows：Flow 178000m3/ h, temperature
40 DEG C, pressure 3.5MPa, gas, which is constituted, is：38%H2, 28%CO, 34%CO2。
Conversion gas removes CO through low-temp methanol washing process again2Gas, gas cooling is washed tower to reduce to 10 DEG C into ammonia
NH3With HCN contents, CO is then sprayed into2Absorption tower (- 21 DEG C of temperature, pressure 3.43MPa) (- 53 DEG C) absorption CO of methanol2, obtain
Synthesis gas.
(4) slurry bed system F-T reactors are used, raw material is synthesis gas, and catalyst is middle section ICC-II sections series catalysts, instead
Answer 230-250 DEG C of temperature, pressure 2.5-3.5Mpa；Reaction generation head fraction 18.7kg.
(5) one-step polymerization production oligomer：Raw material is 18.7kg head fractions, poly- using polymerization reaction kettle, including first paragraph
Reaction is closed, catalyst is trifluoromethanesulfonic acid based composite catalyst, and consumption 1.2wt%, reaction temperature is 50-80 DEG C, and pressure is
0.1-0.3MPa；Reaction time 1.5h, one-step polymerization reaction terminates rear oil product and separated into separator.
Separating technology is divided into two sections, and first section is low temperature crystallization, and temperature is -30 DEG C, solid precipitate (C11Above alkane group
Point) removed through filtering technique；Secondary segment is separated into distilation, and temperature is 180 DEG C, steams cut for C10Following alkane；Through two sections
Oligomer 9.9kg is obtained after separating technology purification.
Two sections of polymerization high polymers：Second segment polymerisation is carried out by raw material of oligomer, n-butanol is initiator, nitrogen
Start reaction after gas displacement, reaction temperature is 150-200 DEG C, and pressure is 0.3-0.5MPa；Time 4-6h, catalyst is urged for ternary
Agent (lanthanum hydroxide, cerium mixture/chromium-silicon composite catalyst), consumption 1.3wt%.Alpha-olefin conversion ratio is 99%, is obtained
9.6kg high polymers.
Above-mentioned high polymer contains double bond, is subject to saturation by isoparaffin alkylation reaction.Isoparaffin is isopentane,
Reacted in tank reactor with high polymer, reaction temperature is 100-200 DEG C, and pressure is 1-3MPa, and catalyst is fluoroform
Sulfonic acid based composite catalyst, consumption 1.4wt%, hydrocarbon mixture and poly alpha olefin mol ratio 10:1, reaction time 1.5h.Alkylation is anti-
Unreacted reactant is removed through vacuum distillation after should terminating, 10.5kg poly alpha olefine synthetic oils are obtained.
Poly-a-olefin oil characteristic index is as follows：
Term used herein is explanation and exemplary and nonrestrictive term.Because the present invention can be with a variety of
Form specific implementation without departing from the spiritual or substantive of invention, it should therefore be appreciated that above-described embodiment be not limited to it is any foregoing
Details, and should widely being explained in the spirit and scope that appended claims are limited, thus fall into claim or its etc.
Whole changes and remodeling in the range of effect all should be appended claims and covered.
Claims (8)
1. a kind of preparation method of biological poly alpha olefine synthetic oil, including：
Lignocellulose raw material is obtained after hydrolysis in lignin semicoke, lignin semicoke, and the weight percentage of semicoke is 88-
92%, the weight percentage of ash content is 8-12%；
Lignin char Gasification obtains crude synthesis gas；
Crude synthesis gas is varied, elution processes production synthesis gas；
Synthesis gas Fischer-Tropsch synthesis or F-T produces head fraction；
The two sections of polymerizations of fore-running lease making, alkylation process production biological poly alpha olefine synthetic oil.
2. the preparation method of biological poly alpha olefine synthetic oil as claimed in claim 1, it is characterised in that the life of lignin semicoke
Production process includes：
The first stage hydrolysis of lignocellulose raw material, xylo-oligosaccharide is converted into by the hemicellulose in lignocellulose raw material；First
Stage hydrolysis：Temperature is 200-240 DEG C, pressure is 2.2-2.4MPa, time 0.5-5 minute, is reacted in lignocellulose raw material
Hemicellulose be converted into xylo-oligosaccharide；
The second segment hydrolysis of lignocellulose raw material, cellooligosaccharide is converted into by the cellulose in lignocellulose raw material；Second-order
Section hydrolysis：Temperature is 180-200 DEG C, pressure is 1.4-1.6MPa, time 10-30 minute, is reacted in lignocellulose raw material
Cellulose is converted into cellooligosaccharide.
The phase III hydrolysis of lignocellulose raw material, acetic acid is catalyst, and temperature is 180-200 DEG C, and pressure is 1.4-1.6MPa,
Time 5-20 minute, lignin conversion is lignin semicoke.
3. the preparation method of biological poly alpha olefine synthetic oil as claimed in claim 1, it is characterised in that lignin char Gasification
Obtaining the production process of crude synthesis gas includes：
Using lignin semicoke as raw material, using space flight stove gasification installation, air separation unit yield is 52000Nm3/ h, oxygen extraction ratio surpasses
90% is crossed, gasifying agent is 99.6% pure oxygen；
Feeding manner is semicoke dry-coal feeding, and conveying gas is CO2, single injector spurts into gasification furnace, gas to feeding burner from top to bottom
It is 1250-1450 DEG C to change temperature, and pressure is 3-3.5MPa, the crude synthesis gas and slag of generation deslagging, thick synthesis after water Quench
Gas is discharged on shock chamber top, enters subsequent handling after further cooling, dedusting.
4. the preparation method of biological poly alpha olefine synthetic oil as claimed in claim 1, it is characterised in that crude synthesis gas is through becoming
Change, the production process of elution processes production synthesis gas includes：
Crude synthesis gas adjusts H through vapor transformationreation device2Ratio with CO is 1.3-1.5, uses iron for catalyst, pressure
0.8-1MPa, reaction temperature is 220-280 DEG C, and the conversion gas of generation turns into：33-39%H2, 26-28%CO, 33-35%CO2；
Conversion gas removes CO through low-temp methanol washing process again2Gas, gas cooling is washed tower to reduce NH to 10 DEG C into ammonia3With
HCN contents, then in -21 DEG C of temperature, CO is sprayed under pressure 3.43MPa2Absorption tower, with -53 DEG C of methanol absorption CO2, closed
Into gas.
5. the preparation method of biological poly alpha olefine synthetic oil as claimed in claim 1, it is characterised in that synthesis gas Fischer-Tropsch synthesis or F-T
Produce head fraction and use slurry bed system F-T reactors, raw material is synthesis gas, and catalyst is Fe-series catalyst, reaction temperature 230-250
DEG C, pressure 2.5-3.5Mpa；Reaction generation head fraction.
6. the preparation method of biological poly alpha olefine synthetic oil described in claim 1, it is characterised in that two sections of fore-running lease making gathers
The step of conjunction, alkylation process production biological poly alpha olefine synthetic oil, includes：
One-step polymerization produces oligomer；Raw material is head fraction, using polymerization reaction kettle, including first paragraph polymerisation, catalyst
For trifluoromethanesulfonic acid based composite catalyst, consumption 1-2wt%, reaction temperature is 50-80 DEG C, and pressure is 0.1-0.3MPa；Reaction
Time 1-2h, one-step polymerization reaction terminates rear oil product and separated into separator；
Separating technology is divided into two sections, and first section is low temperature crystallization, and temperature is -30 DEG C, solid precipitate (C11Above alkane component) warp
Filtering technique is removed；Secondary segment is separated into distilation, and temperature is 180 DEG C, steams cut for C10Following alkane；Through two-phase seperation work
Oligomer is obtained after skill purification；
Two sections of polymerization high polymers；Second segment polymerisation is carried out by raw material of oligomer, n-butanol is initiator, and nitrogen is put
Start reaction after changing, reaction temperature is 150-200 DEG C, and pressure is 0.3-0.5MPa；Time 4-6h, catalyst is three-element catalytic
Agent, consumption 1-2wt%, obtains high polymer；
High polymer contains double bond, is subject to saturation by isoparaffin alkylation reaction；Isoparaffin is isopentane, in still reaction
Reacted in device with high polymer, reaction temperature is 100-200 DEG C, pressure is 1-3MPa, catalyst amount 1-2wt%, mixing
Hydrocarbon and poly alpha olefin mol ratio 8-15:1, reaction time 1-2h；Alkylated reaction removes unreacted reactant after terminating through vacuum distillation,
Obtain biological poly alpha olefine synthetic oil finished product.
7. the preparation method of biological poly alpha olefine synthetic oil described in claim 6, it is characterised in that：Three-way catalyst selects hydrogen
Lanthana, cerium mixture/chromium-silicon composite catalyst, the catalyst of isoparaffin alkylation reaction are compound for trifluoromethanesulfonic acid base
Catalyst.
8. the preparation method of biological poly alpha olefine synthetic oil described in claim 2, it is characterised in that：Acetic acid concentration is 95%
Wt, acetic acid consumption is the 0.5-0.8% of raw material gross weight.
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