CN108559010A - A kind of process units of F- T synthesis olefinic polymerization production polyalphaolefin - Google Patents
A kind of process units of F- T synthesis olefinic polymerization production polyalphaolefin Download PDFInfo
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- CN108559010A CN108559010A CN201810304521.4A CN201810304521A CN108559010A CN 108559010 A CN108559010 A CN 108559010A CN 201810304521 A CN201810304521 A CN 201810304521A CN 108559010 A CN108559010 A CN 108559010A
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- polyalphaolefin
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- rectifying column
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F8/00—Chemical modification by after-treatment
- C08F8/04—Reduction, e.g. hydrogenation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
- C08F110/14—Monomers containing five or more carbon atoms
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Abstract
A kind of process units of F- T synthesis olefinic polymerization production polyalphaolefin, is related to a kind of polyalphaolefin process units, ten Alkyl distillation tower of carbon（4）, ten alkene rectifying column of carbon（5）, polymer reactor（6）, hydrogenation reactor（10）, oligomer rectifying column（12）, molecular sieve treater（15）, catalyst recycling can（17）With polyalphaolefin rectifying column（20）Between by suitably combining connection；The present invention removes water F- T synthesis alkene using molecular sieve treater, ten Alkyl distillation tower of carbon, ten alkene rectifying column of carbon purify F- T synthesis alkene to obtain ten alkene of carbon, catalyst boron trifluoride, which is added, makes ten alkene of carbon be converted into polyalphaolefin, hydrogenation catalyst, which is added, makes hydrogen and polyalphaolefin reaction be converted into saturation polyalphaolefin, oligomer is detached by oligomer rectifying column, three kinds of different polyalphaolefins of viscosity are obtained by polyalphaolefin rectifying column.
Description
【Technical field】
The present invention relates to a kind of polyalphaolefin process units, and polyalphaolefin is produced more particularly, to a kind of F- T synthesis olefinic polymerization
Process units.
【Background technology】
F- T synthesis alkene is that coal is made by indirect liquefaction, is produced with n-alkane, alhpa olefin liquid coal liquifaction as main component
Product.The main component of F- T synthesis alkene be 60% light dydrocarbon to the alhpa olefin of carbon 16,30%-35% light dydrocarbon to 16 positive structure of carbon
Alkane, a small amount of isoparaffin, cycloalkane and isomeric olefine, impurity grade for minor amount of water.With the development of coal liquifaction technology, I
The production capacity of state's F- T synthesis alkene just improves year by year, has preferable warp using the alkene as the raw material for preparing polyalphaolefin
Ji property.
Polyalphaolefin（PAO）It is the base oil of fully synthetic lubricating oil, is widely used in high-end lubricating area, is by carbon ten
Linear alpha olefin（The 1- last of the ten Heavenly stems is dilute）It is prepared by polymerization and hydrogenation technique；General import alhpa olefin is by ethylene oligomerization method in the world
It prepares, higher price.China not yet grasps ethylene oligomerization technology, mainly by wax destructive distillation method produce alhpa olefin, positive structure content compared with
Low, product quality is poor.
【Invention content】
In order to overcome the shortcomings of in background technology, the present invention discloses a kind of production of F- T synthesis olefinic polymerization production polyalphaolefin
Device, the present invention remove water F- T synthesis alkene using molecular sieve treater, ten Alkyl distillation tower of carbon, ten alkene rectifying column pair of carbon
F- T synthesis alkene is purified to obtain ten alkene of carbon, and catalyst boron trifluoride, which is added, makes ten alkene of carbon be converted into polyalphaolefin, adds
Entering hydrogenation catalyst makes hydrogen and polyalphaolefin reaction be converted into saturation polyalphaolefin, is divided oligomer by oligomer rectifying column
From obtaining three kinds of different polyalphaolefins of viscosity by polyalphaolefin rectifying column.
In order to realize that the goal of the invention, the present invention adopt the following technical scheme that：
A kind of process units of F- T synthesis olefinic polymerization production polyalphaolefin, including ten Alkyl distillation tower of carbon, ten alkene rectifying of carbon
Tower, polymer reactor, hydrogenation reactor, oligomer rectifying column, molecular sieve treater, catalyst recycling can and polyalphaolefin rectifying
Tower, F- T synthesis alkene import are located at the top of molecular sieve treater, and the outlet that molecular sieve treater bottom is equipped with passes through pipeline
The entrance being equipped in the middle part of ten Alkyl distillation tower of connection carbon, ten alkane of carbon and more light fraction outlet are located at the top of ten Alkyl distillation tower of carbon
End, the outlet that ten Alkyl distillation tower bottom of carbon is equipped with pass through the entrance being equipped in the middle part of ten alkene rectifying column of piping connection carbon, carbon ten
One alkane and more recombination sub-export are located at the bottom of ten alkene rectifying column of carbon, and the outlet being equipped at the top of ten alkene rectifying column of carbon passes through
The entrance being equipped in the middle part of piping connection polymer reactor, catalyst boron trifluoride entrance are located at the top of polymer reactor, polymerize
The outlet that reactor bottom is equipped with passes through the entrance being equipped in the middle part of piping connection catalyst recycling can, the outlet of catalyst boron trifluoride
Positioned at the top of catalyst recycling can, the outlet that catalyst recycling pot bottom is equipped at the top of piping connection hydrogenation reactor by setting
Some entrances, the outlet that hydrogenation reactor bottom is equipped with pass through the entrance being equipped in the middle part of piping connection oligomer rectifying column, hydrogen
Entrance is located at the bottom of hydrogenation reactor, and positioned at the top of oligomer rectifying column, oligomer rectifier bottoms are set for oligomer outlet
Some exports the entrance being equipped with by piping connection polyalphaolefin rectifying column middle and lower part, and the outlet of polyalphaolefin four is located at polyalphaolefin essence
The top of tower is evaporated, the outlet of polyalphaolefin ten is located at polyalphaolefin essence positioned at the middle part of polyalphaolefin rectifying column, the outlet of polyalphaolefin 20
Evaporate the bottom of tower.
The process units of the F- T synthesis olefinic polymerization production polyalphaolefin, in ten alkane of molecular sieve treater and carbon
The pipeline between ten alkene rectifying column of pipeline, ten Alkyl distillation tower of carbon and carbon, ten alkene rectifying column of carbon between rectifying column and poly-
Close pipeline, catalyst recycling can and the hydrogenation reaction between pipeline, polymer reactor and the catalyst recycling can between reactor
Pipeline, oligomer rectifying column and polyalphaolefin rectifying column between pipeline, hydrogenation reactor between device and oligomer rectifying column it
Between pipeline on be respectively equipped with delivery pump.
The process units of the F- T synthesis olefinic polymerization production polyalphaolefin, in the pipeline of F- T synthesis alkene import
It is equipped with regulating valve, vacuum pump is equipped on the pipeline of catalyst boron trifluoride outlet.
The process units of the F- T synthesis olefinic polymerization production polyalphaolefin, molecular sieve treater is 3A or 4A molecules
Sieve.
The process units of the F- T synthesis olefinic polymerization production polyalphaolefin, ten Alkyl distillation tower of carbon, carbon ten alkene essence
It is respectively regular stainless steel helices tower or ligulate float valve plate column, effective plate number 60-80 to evaporate tower and polyalphaolefin rectifying column.
The process units of the F- T synthesis olefinic polymerization production polyalphaolefin, polymer reactor are that turbine fan leaf type stirs
Mix kettle.
The process units of the F- T synthesis olefinic polymerization production polyalphaolefin, catalyst recycling can is regular stainless steel
Pressurized tank.
The process units of the F- T synthesis olefinic polymerization production polyalphaolefin, hydrogenation reactor are solid for stainless steel autoclave
Hydrogenation catalyst is filled at fixed bed reactor, middle part, and catalyst is platinum base hydrogenation catalyst.
The process units of the F- T synthesis olefinic polymerization production polyalphaolefin, oligomer rectifying column is regular stainless steel
Packed tower or ligulate float valve plate column, effective plate number 45-60.
By adopting the above-described technical solution, the present invention has the advantages that：
The process units of F- T synthesis olefinic polymerization production polyalphaolefin of the present invention, the present invention use molecular sieve treater
F- T synthesis alkene is removed water, ten Alkyl distillation tower of carbon, ten alkene rectifying column of carbon are purified to obtain carbon to F- T synthesis alkene
Ten alkene, catalyst boron trifluoride, which is added, makes ten alkene of carbon be converted into polyalphaolefin, and hydrogenation catalyst, which is added, makes hydrogen and poly- α alkene
Hydrocarbon reaction is converted into saturation polyalphaolefin, detaches oligomer by oligomer rectifying column, three are obtained by polyalphaolefin rectifying column
The different polyalphaolefin of kind viscosity；The advantageous effect that the present invention has reasonable design, technique unique, energy-saving, environmentally protective.
【Description of the drawings】
Fig. 1 is the structural diagram of the present invention.
In figure：1, F- T synthesis alkene import；2, regulating valve；3, ten alkane of carbon and more light fraction outlet；4, ten alkane of carbon
Rectifying column；5, ten alkene rectifying column of carbon；6, polymer reactor；7, catalyst boron trifluoride entrance；8, catalyst boron trifluoride goes out
Mouthful；9, vacuum pump；10, hydrogenation reactor；11, oligomer exports；12, oligomer rectifying column；13, polyalphaolefin four exports；14、
Polyalphaolefin ten exports；15, molecular sieve treater；16, carbon hendecane hydrocarbon and sub-export is more recombinated；17, catalyst recycling can；18、
Hydrogen inlet；19, delivery pump；20, polyalphaolefin rectifying column；21, polyalphaolefin 20 exports.
【Specific implementation mode】
The present invention can be explained in more detail by the following examples, the invention is not limited in the following examples, open
The purpose of the present invention is intended to all changes and improvements in the protection scope of the invention；
The process units of F- T synthesis olefinic polymerization production polyalphaolefin in conjunction with described in attached drawing 1, including ten Alkyl distillation tower 4 of carbon,
Ten alkene rectifying column 5 of carbon, polymer reactor 6, hydrogenation reactor 10, oligomer rectifying column 12, molecular sieve treater 15, catalyst
Recycling can 17 and polyalphaolefin rectifying column 20, F- T synthesis alkene import 1 are located at the top of molecular sieve treater 15, molecular sieve essence
The entrance that the outlet that 15 bottom of device processed is equipped with is equipped with by the middle part of ten Alkyl distillation tower of piping connection carbon 4, ten alkane of carbon and lighter
Group sub-export 3 is located at the top of ten Alkyl distillation tower 4 of carbon, and the outlet that ten Alkyl distillation tower of carbon, 4 bottom is equipped with passes through piping connection
The entrance that ten alkene rectifying column of carbon, 5 middle part is equipped with, carbon hendecane hydrocarbon and more recombination sub-export 16 are located at ten alkene rectifying column 5 of carbon
Bottom, the entrance that the outlet that ten alkene rectifying column of carbon, 5 top is equipped with is equipped with by 6 middle part of piping connection polymer reactor, catalysis
Agent boron trifluoride entrance 7 is located at the top of polymer reactor 6, and the outlet that 6 bottom of polymer reactor is equipped with is urged by piping connection
The entrance that 17 middle part of agent recycling can is equipped with, catalyst boron trifluoride outlet 8 are located at the top of catalyst recycling can 17, catalyst
The entrance that the outlet that 17 bottom of recycling can is equipped with is equipped with by 10 top of piping connection hydrogenation reactor, 10 bottom of hydrogenation reactor
The entrance that the outlet being equipped with is equipped with by 12 middle part of piping connection oligomer rectifying column, hydrogen inlet 18 are located at hydrogenation reactor 10
Bottom, oligomer outlet 11 be located at oligomer rectifying column 12 tops, the outlet that 12 bottom of oligomer rectifying column is equipped with passes through
The entrance that 20 middle and lower part of piping connection polyalphaolefin rectifying column is equipped with, the outlet of polyalphaolefin four 13 are located at polyalphaolefin rectifying column 20
Top, the outlet of polyalphaolefin ten 14 are located at the middle part of polyalphaolefin rectifying column 20, and the outlet of polyalphaolefin 20 21 is located at polyalphaolefin essence
Evaporate the bottom of tower 20, molecular sieve treater 15 is 3A or 4A molecular sieves, ten Alkyl distillation tower 4 of carbon, ten alkene rectifying column 5 of carbon and poly-
Alhpa olefin rectifying column 20 is respectively regular stainless steel helices tower or ligulate float valve plate column, effective plate number 60-80, polymerisation
Device 6 is turbine fan leaf type stirred tank, and catalyst recycling can 17 is regular stainless steel pressure tank, and hydrogenation reactor 10 is stainless steel kettle
Formula fixed bed reactors, middle part fill hydrogenation catalyst, catalyst be platinum base hydrogenation catalyst, oligomer rectifying column 12 be it is regular not
Stainless steel helices tower or ligulate float valve plate column, effective plate number 45-60, in ten Alkyl distillation tower 4 of molecular sieve treater 15 and carbon
Between ten alkene rectifying column 5 of pipeline, ten Alkyl distillation tower 4 of carbon and carbon between pipeline, ten alkene rectifying column 5 of carbon and polymerization it is anti-
It answers the pipeline between pipeline, polymer reactor 6 and the catalyst recycling can 17 between device 6, catalyst recycling can 17 and adds hydrogen anti-
Answer pipeline, oligomer rectifying column 12 and the poly- α alkene between pipeline, hydrogenation reactor 10 and the oligomer rectifying column 12 between device 10
It is respectively equipped with delivery pump 19 on pipeline between hydrocarbon rectifying column 20, regulating valve is equipped on the pipeline of F- T synthesis alkene import 1
2, it is equipped with vacuum pump 9 on the pipeline of catalyst boron trifluoride outlet 8.
The process units for implementing F- T synthesis olefinic polymerization production polyalphaolefin of the present invention, in use, F- T synthesis
Alkene enters molecular sieve treater 15 from F- T synthesis alkene import 1, by the moisture in F- T synthesis alkene under 25 DEG C, normal pressure
Content is down to 10ppm or less；
F- T synthesis alkene comes out from 15 bottom of molecular sieve treater, will be most of after entering from ten Alkyl distillation tower of carbon, 4 middle part
Ten alkane of carbon and more light fraction outlet 3 is separated that ten alkane of carbon and more light component are equipped with from tower top, it is 99.5% to obtain purity
Above ten alkene of carbon and more heavy constituent make ten alkane of carbon and more light component content be less than 0.5%；
Ten alkene of carbon and more heavy constituent that purity is 99.5% or more come out from ten Alkyl distillation tower of carbon, 4 bottom, from carbon ten alkene essence
It evaporates and separates carbon hendecane hydrocarbon that most of carbon hendecane hydrocarbon and more heavy constituent are equipped with from bottom of tower and more recombination after the middle part of tower 5 enters
Mouth 16 is separated, and is obtained ten alkene of carbon that purity is 99% or more, is made ten alkane of carbon and more light component content less than 0.5%, carbon
Hendecane hydrocarbon and more heavy constituent content are less than 0.5%；
Ten alkene of carbon that purity is 99% or more comes out from ten alkene rectifying column of carbon, 5 top, enters from the middle part of polymer reactor 6
Afterwards, boron trifluoride is added in the catalyst boron trifluoride entrance 7 being equipped with from the top of polymer reactor 6,50 DEG C, 0.2Mpa, stirring
Under conditions of 200 revs/min of rotating speed, catalyst boron trifluoride is catalyzed ten alkene of carbon, and ten alkene of carbon is made to react, warp
5 hours are spent, ten olefin conversion of carbon is not less than 98%, and it is low to obtain polyalphaolefin, a small amount of polyalphaolefin that product is 95% or more purity
The mixture of polymers, a small amount of ten alkene of unreacted carbon and the micro boron trifluoride for being dissolved in liquid phase；
The polyalphaolefin of 95% or more purity, a small amount of polyalphaolefin oligomer, a small amount of ten alkene of unreacted carbon and micro it is dissolved in liquid phase
The mixture of boron trifluoride come out from 6 bottom of polymer reactor, after entering from 17 middle part of catalyst recycling can, open setting and exist
The vacuum pump 9 that the catalyst boron trifluoride outlet 8 at 17 top of catalyst recycling can is equipped with, pressure inside the tank are -0.2Mpa, temperature
It 50 DEG C, by the boron triflouride gas being blended on a small quantity in polyalphaolefin by 8 separation and recovery of catalyst boron trifluoride outlet, is produced
Product are the polyalphaolefin, a small amount of polyalphaolefin oligomer, ten alkene mixture of a small amount of unreacted carbon of 95% or more purity, borontrifluoride
Boron content is less than 10ppm；
The polyalphaolefin of 95% or more purity, a small amount of polyalphaolefin oligomer, a small amount of ten alkene mixture of unreacted carbon are from catalyst
17 bottom of recycling can comes out, and after entering from 10 top of hydrogenation reactor, the hydrogen that hydrogen is equipped with from 10 bottom of hydrogenation reactor enters
Mouth 18 enters, and hydrogen and polyalphaolefin, polyalphaolefin oligomer, ten alkene mixture of unreacted carbon are reacted, and reaction stops
Time is 2 hours, is continually fed into hydrogen, keeps pressure 5.0Mpa, and 300 DEG C of temperature, hydrogen is all consumed after reaction, reaction production
Object is saturation polyalphaolefin, a small amount of saturation polyalphaolefin oligomer and ten alkane of a small amount of carbon；
Saturation polyalphaolefin, a small amount of saturation polyalphaolefin oligomer and ten alkane of a small amount of carbon come out from 10 bottom of hydrogenation reactor, from
It after 12 middle part of oligomer rectifying column enters, is detached at 200 DEG C of temperature, normal pressure, by saturation polyalphaolefin oligomer and carbon ten
The oligomer outlet 11 that alkane is equipped with from 12 top of oligomer rectifying column is separated, and it is saturation polyalphaolefin, impurity to obtain product
Content is negligible；
Saturation polyalphaolefin comes out from 12 bottom of oligomer rectifying column, after entering from 20 middle and lower part of polyalphaolefin rectifying column, according to evaporating
The polyalphaolefin that content is 30%-40% is isolated in Cheng Butong, the outlet of polyalphaolefin four 13 being equipped with from 20 top of polyalphaolefin rectifying column
Four, the outlet of polyalphaolefin ten 14 being equipped with from the middle part of polyalphaolefin rectifying column 20 isolate polyalphaolefin ten that content is 45%-55%,
Isolate the polyalphaolefin 20 that content is 10%-20% in the outlet of polyalphaolefin 20 21 being equipped with from 20 bottom of polyalphaolefin rectifying column.
Part not in the detailed description of the invention is the prior art.
Claims (9)
1. a kind of process units of F- T synthesis olefinic polymerization production polyalphaolefin, including ten Alkyl distillation tower of carbon（4）, ten alkene of carbon
Hydrocarbon rectifying column（5）, polymer reactor（6）, hydrogenation reactor（10）, oligomer rectifying column（12）, molecular sieve treater（15）, urge
Agent recycling can（17）With polyalphaolefin rectifying column（20）, it is characterized in that：F- T synthesis alkene import（1）It is refined positioned at molecular sieve
Device（15）Top, molecular sieve treater（15）The outlet that bottom is equipped with passes through ten Alkyl distillation tower of piping connection carbon（4）Middle part
The entrance being equipped with, ten alkane of carbon and more light fraction outlet（3）Positioned at ten Alkyl distillation tower of carbon（4）Top, ten Alkyl distillation of carbon
Tower（4）The outlet that bottom is equipped with passes through ten alkene rectifying column of piping connection carbon（5）The entrance that middle part is equipped with, carbon hendecane hydrocarbon and more
Recombinate sub-export（16）Positioned at ten alkene rectifying column of carbon（5）Bottom, ten alkene rectifying column of carbon（5）The outlet that top is equipped with passes through
Piping connection polymer reactor（6）The entrance that middle part is equipped with, catalyst boron trifluoride entrance（7）Positioned at polymer reactor（6）'s
Top, polymer reactor（6）The outlet that bottom is equipped with passes through piping connection catalyst recycling can（17）The entrance that middle part is equipped with, is urged
Agent boron trifluoride exports（8）Positioned at catalyst recycling can（17）Top, catalyst recycling can（17）The outlet that bottom is equipped with
Pass through piping connection hydrogenation reactor（10）The entrance that top is equipped with, hydrogenation reactor（10）The outlet that bottom is equipped with passes through pipeline
Connect oligomer rectifying column（12）The entrance that middle part is equipped with, hydrogen inlet（18）Positioned at hydrogenation reactor（10）Bottom, it is oligomeric
Object exports（11）Positioned at oligomer rectifying column（12）Top, oligomer rectifying column（12）The outlet that bottom is equipped with is connected by pipeline
Connect polyalphaolefin rectifying column（20）The entrance that middle and lower part is equipped with, polyalphaolefin four export（13）Positioned at polyalphaolefin rectifying column（20）'s
Top, polyalphaolefin ten export（14）Positioned at polyalphaolefin rectifying column（20）Middle part, polyalphaolefin 20 export（21）Positioned at poly- α
Alkene rectifying column（20）Bottom.
2. the process units of F- T synthesis olefinic polymerization production polyalphaolefin according to claim 1, it is characterized in that：Dividing
Son sieve treater（15）With ten Alkyl distillation tower of carbon（4）Between pipeline, ten Alkyl distillation tower of carbon（4）With ten alkene rectifying column of carbon
（5）Between pipeline, ten alkene rectifying column of carbon（5）And polymer reactor（6）Between pipeline, polymer reactor（6）And catalysis
Agent recycling can（17）Between pipeline, catalyst recycling can（17）And hydrogenation reactor（10）Between pipeline, hydrogenation reactor
（10）With oligomer rectifying column（12）Between pipeline, oligomer rectifying column（12）With polyalphaolefin rectifying column（20）Between pipe
Road is respectively equipped with delivery pump（19）.
3. the process units of F- T synthesis olefinic polymerization production polyalphaolefin according to claim 1, it is characterized in that：Taking
Support synthesis alkene import（1）Pipeline be equipped with regulating valve（2）, exported in catalyst boron trifluoride（8）Pipeline be equipped with it is true
Sky pump（9）.
4. the process units of F- T synthesis olefinic polymerization production polyalphaolefin according to claim 1, it is characterized in that：Molecule
Sieve treater（15）For 3A or 4A molecular sieves.
5. the process units of F- T synthesis olefinic polymerization production polyalphaolefin according to claim 1, it is characterized in that：Carbon ten
Alkyl distillation tower（4）, ten alkene rectifying column of carbon（5）With polyalphaolefin rectifying column（20）Respectively regular stainless steel helices tower or tongue
Shape float valve plate column, effective plate number 60-80.
6. the process units of F- T synthesis olefinic polymerization production polyalphaolefin according to claim 1, it is characterized in that：Polymerization
Reactor（6）For turbine fan leaf type stirred tank.
7. the process units of F- T synthesis olefinic polymerization production polyalphaolefin according to claim 1, it is characterized in that：Catalysis
Agent recycling can（17）For regular stainless steel pressure tank.
8. the process units of F- T synthesis olefinic polymerization production polyalphaolefin according to claim 1, it is characterized in that：Add hydrogen
Reactor（10）For stainless steel autoclave fixed bed reactors, hydrogenation catalyst is filled at middle part, and catalyst is platinum base hydrogenation catalyst.
9. the process units of F- T synthesis olefinic polymerization production polyalphaolefin according to claim 1, it is characterized in that：It is oligomeric
Object rectifying column（12）For regular stainless steel helices tower or ligulate float valve plate column, effective plate number 45-60.
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| CN201810304521.4A CN108559010B (en) | 2018-04-08 | 2018-04-08 | Production device for producing poly alpha olefin by Fischer-Tropsch synthesis olefin polymerization |
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| CN201810304521.4A CN108559010B (en) | 2018-04-08 | 2018-04-08 | Production device for producing poly alpha olefin by Fischer-Tropsch synthesis olefin polymerization |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111875725A (en) * | 2020-06-17 | 2020-11-03 | 南京延长反应技术研究院有限公司 | Micro-interface enhanced reaction system and method for preparing polyethylene by slurry method |
| CN111892673A (en) * | 2020-06-17 | 2020-11-06 | 南京延长反应技术研究院有限公司 | Micro-interface enhanced reaction system and method for preparing polypropylene |
| CN111909293A (en) * | 2020-06-17 | 2020-11-10 | 南京延长反应技术研究院有限公司 | Micro-interface enhanced reaction system and method for preparing poly-alpha-olefin |
| RU2815103C1 (en) * | 2020-06-17 | 2024-03-11 | Наньцзин Яньчан Реэкшн Текнолоджи Рисерч Институт Ко. Лтд | SYSTEM FOR CARRYING OUT REACTION OF PRODUCING POLY α-OLEFIN |
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| CN111909293B (en) * | 2020-06-17 | 2023-02-03 | 南京延长反应技术研究院有限公司 | Micro-interface enhanced reaction system and method for preparing poly-alpha-olefin |
| RU2815103C1 (en) * | 2020-06-17 | 2024-03-11 | Наньцзин Яньчан Реэкшн Текнолоджи Рисерч Институт Ко. Лтд | SYSTEM FOR CARRYING OUT REACTION OF PRODUCING POLY α-OLEFIN |
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