CN106622039B - The integrated reaction and separation technique and device of synthesizing poly alpha-olefin (PAO) - Google Patents
The integrated reaction and separation technique and device of synthesizing poly alpha-olefin (PAO) Download PDFInfo
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- CN106622039B CN106622039B CN201611139564.9A CN201611139564A CN106622039B CN 106622039 B CN106622039 B CN 106622039B CN 201611139564 A CN201611139564 A CN 201611139564A CN 106622039 B CN106622039 B CN 106622039B
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
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Abstract
The invention discloses a kind of integrated reaction and separation technique of synthesizing poly alpha-olefin (PAO) and devices, alpha-olefin raw material and magnetic lewis acid catalyst by proportion are launched to integrated reaction and separation device, after reaction, open the magnechuck inside reaction kettle, magnetic lewis acid catalyst is magnetized and is adsorbed in magnechuck surface, the reaction clear liquid of discharge enters next process, and integrated reaction and separation device solves the problems, such as that lewis acid catalyst is difficult to separate in PAO synthesis.The present invention highly shortened PAO process flow, reduce process units quantity, saves catalyst separating energy consumption, reduces the production cost of PAO, realize the green of PAO, environmental protection, efficiently produce.
Description
Technical field
The present invention relates to coal chemical industry and petrochemical industry, specially a kind of lube base oil poly alpha olefin (PAO)
Integrated reaction and separation technique and device.
Background technique
Poly alpha olefin (PAO) has as high-grade lubricating base oil applied to fields such as machinery, aviation, military project and automobiles
Viscosity index (VI) is high, operating temperature range is wide, low temperature fluidity is good, oxidation resistance is strong, evaporation loss is small, flash-point is high and inclines
The low advantage of point.
PAO production process includes the works such as long-chain alpha-olefin catalytic polymerization, catalyst removal, distillation desolventizing plus hydrogen saturation
Sequence obtains the lubricating base oil of high saturation, and the performance of base oil is mainly determined by raw material type and catalyst property.Wherein,
The alpha-olefin that 90% or more raw material is synthesized from ethylene oligomerization method, remaining is for the alpha-olefin of wax cracking method preparation or from taking
The C that support (F-T) synthetic oil is cut through rectifying8~C12Mixed olefins.In addition, different System Catalysts also will affect the polymerization of PAO
Degree, molecular structure and molecular weight distribution, currently, the catalyst of synthesis PAO is mainly homogeneous catalyst, representative catalyst has
Aluminum chloride-catalyzed system, boron trifluoride catalyst system, ziegler-natta catalyzed system, metallocene catalysis system and ionic liquid
Catalyst system etc..
US4218330 is disclosed using BF3Catalytic polymerization C12~C18PAO is prepared, PAO pour point is -29 DEG C, viscosity index (VI)
130,100 DEG C of kinematic viscosity 3.37mm2/s.US5191140 is disclosed with BF3Decanol is catalyzed C6、C8、C10And C12Mixture system
Standby PAO, PAO pour point are lower than -60 DEG C, 126,100 DEG C of kinematic viscosity 6.69mm of viscosity index (VI)2/s。
CA104152176 discloses the method for preparing poly alpha olefine synthetic oil using coal base, by indirect coal liquefaction process
The isolated boiling range range of the alpha-olefin crude product of output is 40 DEG C ~ 275 DEG C, carbon number C5~C12Alpha-olefin component, catalyst
For AlCl3Or AlCl3With the complex compound of alcohols.The PAO viscosity index (VI) of preparation is greater than 145.CN104250564 is disclosed using halogen
Change aluminium and halogenation titanium catalyst, using the alpha-olefin of coal wax destructive distillation as raw material, PAO viscosity index (VI) is greater than 135,100 DEG C of kinematic viscosity 6
~13mm2/ s, condensation point are not higher than -45 DEG C.CN105368489 discloses the light oil for using ICL for Indirect Coal Liquefaction to generate as raw material, passes through
It crosses polymerization intermittent reaction, then by tap water and alkali liquid washing, is refining to obtain PAO product using filter and fixed bed hydrogenation.
Currently, homogeneous catalyst has widely been applied in PAO industrialization.But it is homogeneously urged in actual production process
There are still more disadvantages for agent system: (1) homogeneous catalyst and reaction solution separation are extremely difficult；(2) homogeneous catalyst cannot follow
Loopback, which is received, to be used；(3) homogeneous catalyst easily sandwiches in PAO oil phase, and a large amount of waste liquid is generated in product washing process；
(4) homogeneous catalyst uses alkali neutralization, the contaminated wastewater environment generated after water-oil separating.
With the strategy implementation of coal chemical industry green production, PAO produce the separation of catalyst present in homogeneous catalyst system,
The problems such as alkaline waste water and its generation emulsion, is badly in need of solving.Researchers at home and abroad are also attempted to prepare using loaded catalyst
The research of PAO, this kind of loaded catalyst are by AlCl3Etc. catalytic active components be carried on the inorganic carrier of bulky grain, nothing
The oxygen that airborne body is formed-metallic bond links so that AlCl3It is firmly adhered to inorganic basic surface.
CN103305263 is disclosed with alkali modification AlCl3/Al2O3Supported catalyst is catalyzed 1- decene or C8~C12α-alkene
Hydrocarbon oligomerisation reaction is made PAO yield by catalyst, washing, distillation and is greater than 60%, 100 DEG C of 10 ~ 25mm of kinematic viscosity2/ s, chlorine
Content is less than 2%.CN103657710 is disclosed active component A lCl3It is immobilized in molecular sieve MCM-22, AlCl3Account for catalyst weight
The 2 ~ 30% of amount composition, with fixed bed synthesizing poly alpha-olefin, be made PAO yield be greater than 45 ~ 80%, 20 DEG C of kinematic viscosity 23 ~
40mm2/s。
Support type lewis acid catalyst preparation PAO can solve mutually catalyst and be difficult to the problem of separating, but load
The catalytic efficiency of type catalyst cannot reach far below the conversion ratio of homogeneous catalyst, especially alpha-olefin and the yield of PAO
Requirement on industrial application, main cause are that carrier granular is larger, and active component is carried in carrier hole, relative to homogeneous catalysis
Agent, alpha-olefin reactant are more difficult to reach the active sites of loaded catalyst, this be also current loaded catalyst catalytic efficiency compared with
The main reason for low.The size for reducing carrier can reduce reactant in duct inside diffusional resistance, but carrier be narrowed down to micro-
Metrical scale is hereinafter, the separation of solid and liquid of catalyst just becomes main problem again.
Summary of the invention
The object of the present invention is to provide a kind of PAO catalytic polymerizations and catalyst magnetic for integrating polymerization reaction and Magneto separate
Isolated technique and device, solves that the separation of catalyst existing for traditional handicraft is difficult, filtering rate is slow, production efficiency is low asks
Topic.
The present invention is achieved by the following technical scheme:
A kind of integrated reaction and separation device of synthesizing poly alpha-olefin (PAO), including reactor body, the reactor master
External face is equipped with collet, and the collet upper end setting heating/cooling medium outlet, heating/cooling medium entrance is arranged in lower end；Institute
It states center in reactor body and blender motor-driven is housed, the reactor body inner wall is fixed with magnechuck, institute
It states equipped with electromagnetic chuck controller outside reactor body, the electromagnetic chuck controller controls the unlatching of magnechuck and closes
It closes；The top of the reactor body is equipped with feed opening and temperature-measuring port, and bottom is equipped with discharge gate.
The integrated reaction and separation technique of synthesizing poly alpha-olefin (PAO) applied to above-mentioned apparatus is as follows: by raw material α-alkene
Hydrocarbon and magnetic lewis acid catalyst are added to inside the reactor body of separation integrated apparatus, control reaction temperature and reaction
Pressure carries out polymerization reaction；Reaction terminates, and opens electromagnetic chuck controller power supply, the magnechuck inside reactor body
Magnetic field is generated, magnetic lewis acid catalyst assembles absorption on magnechuck, isolates the anti-of magnetic lewis acid catalyst
Liquid discharge reaction kettle is answered to enter a procedure；Raw material alpha-olefin is added, magnechuck power supply is closed, opens stirring, magnetic road
Lewis acid catalyst is scattered in liquid phase again, after reaction, then carries out Magneto separate, is recycled.
Magnetic lewis acid catalyst category existing product, uses super-paramagnetism nano magnetic-particle for carrier in the present invention,
Catalytic active component (lewis acid catalyst) is carried on magnetic-particle surface by chemical control method, being formed has shell core
The magnetic lewis acid catalyst of structure or hybrid architecture.Raw material alpha-olefin and magnetic lewis acid catalyst by proportion are added
Enter polymer reactor, after the completion of polymerization reaction, the reaction solution containing magnetic lewis acid catalyst is divided by Magneto separate unit
From, under the action of external magnetic field, make magnetic lewis acid catalyst rapid aggregation and the deposition in reaction solution, realize catalyst with
React the rapidly and efficiently separation of clear liquid.Since the overall dimension of magnetic lewis acid catalyst is still controlled in nanometer scope, not
With having good dispersibility in solvent so that the active group on reactant and magnetic lewis acid catalyst have it is more tight
Close contact, conversion ratio and selectivity etc. are superior to blocky or bulky grain supported catalyst.When needing to be separated by solid-liquid separation, adding outside
Under the action of magnetic field, magnetic lewis acid catalyst is assembled under magnetic field environment, is isolated from reaction system by fast-magnetic
Come；When cancelling external magnetic field, the magnetic of magnetic lewis acid catalyst disappears, and can disperse in the liquid phase, to reach again
The function that catalyst is reused.Magnetic lewis acid catalyst makes heterogeneous catalyst " homogeneousization ", and makes homogeneous catalyst
" heterogeneouss " are provided simultaneously with the feature of suspended state and loaded catalyst.Magnetic Louis acid catalysis is used in PAO synthesis process
PAO yield not only can be improved in agent, also can be convenient the catalyst in quick separating reaction solution.
The magnetic lewis acid catalyst can choose AlCl3/SiO2/Fe2O4, AlCl3/SiO2/NiFe2O4,
AlCl3/SiO2/CoFe2O4, AlCl3/SiO2/BaFe2O4, AlCl3+TiCl4/SiO2/Fe2O4, AlCl3+TiCl4/SiO2/
NiFe2O4, AlCl3+TiCl4/SiO2/CoFe2O4, AlCl3+TiCl4/SiO2/BaFe2O4In any one or a few mixing
Object.The kernel of magnetic lewis acid catalyst has superparamagnetism, and outer layer is catalytic active component, and middle layer is to shield
Inert layer, there is magnetism, after removing external magnetic field, remanent magnetism disappears quickly when magnetic lewis acid catalyst is in external magnetic field.
The raw material is 1- octene, 1- nonene, 1- decene, 1-11 alkene, any one or a few mixture of 1-12 alkene.
It is also possible to the C from olefins from paraffin cracking8~C12Alkene mixture or coal oil separate C8~C12Alkene mixture.Alpha-olefin and
Magnetic lewis acid catalyst by proportion control is in 1 ~ 5%(mass percent).Reaction temperature is 40 DEG C ~ 120 DEG C, reaction pressure
For 0.1 ~ 5MPa, the reaction time is 2 ~ 10 hours.
Since the partial size of magnetic lewis acid catalyst is tiny, existing magnetic separator is for magnetic lewis acid catalyst
When being separated by solid-liquid separation, existing magnetism lewis acid catalyst by macroscopical flow effect have little time to magnetize and the shortcomings that be lost.
Meanwhile magnetic lewis acid catalyst is lost by pumping conveying and also easily wearing in the duct.
Magnechuck is set to the inside of reactor by integrated reaction and separation technique and device in the present invention, is not required to be pump
It is transported in reactor, also can solve magnetic lewis acid catalyst the problem of transmission process and pipe friction are worn.Instead
It answers isolation integral technique and device during the reaction, is not turned on magnechuck power supply, do not generate magnetic field, it is anti-not influence polymerization
Answer effect.When after reaction, opening magnechuck power supply, magnechuck generates magnetic field, the magnetic field of reaction solution and magnechuck
From the farther away liquid in magnetic field under stirring, magnetic Louis has been significantly greatly increased in liquid in face contact, easily magnetization aggregation
The magnetization probability of acid catalyst, admirably realizes the separation of magnetic lewis acid catalyst and PAO reaction solution.
Integrated reaction and separation technique and device can greatly shorten PAO production technology in the present invention, reduce production dress
Quantity is set, catalyst separating energy consumption is saved, reduces the production cost of PAO, realizes that PAO is environmentally protective and efficiently produces.
Detailed description of the invention
Fig. 1 shows the integrated reaction and separation technique of synthesizing poly alpha-olefin (PAO) and the structural schematic diagrams of device.
In figure, 1- reactor body, 2- reactor jacket, 3- motor, 4- blender, 5- feed opening, 6- temperature-measuring port, 7- row
Material mouth, 8- heating/cooling medium outlet, 9- heating/cooling medium entrance, 10- magnechuck, 11- electromagnetic chuck controller,
12- reactor support.
Specific embodiment
Specific embodiments of the present invention are described in detail below.
Embodiment 1
A kind of integrated reaction and separation device of synthesizing poly alpha-olefin (PAO), as shown in Figure 1, include reactor body 1,
Collet 2,2 upper end of the collet setting heating/cooling medium outlet 8 are equipped with outside the reactor body 1, lower end setting adds
Hot/cold but medium inlet 9；Center is equipped with the blender 4 driven by motor 3, the reactor body in the reactor body 1
1 inner wall is fixed with magnechuck 10, and electromagnetic chuck controller 11, the magnechuck control are housed outside the reactor body 1
Device 11 processed controls the unlatching and closure of magnechuck 10；The top of the reactor body 1 is equipped with feed opening 5 and temperature-measuring port 6, bottom
Portion is equipped with discharge gate 7；The reactor body 1 is located on reactor support 12.
Embodiment 2
Take 1m31- decene solution be added jacketed stirred autoclave, be added 5%(mass fraction) AlCl3+TiCl4/
SiO2/NiFe2O4, stirring is opened, adjusting temperature is 80 DEG C, and reaction pressure control after the reaction time is 3h, opens electricity in 0.1MPa
Magnetic disk controller, Magneto separate go out AlCl3+TiCl4/SiO2/NiFe2O4Catalyst obtains after adding hydrogen using light point of distillation removing
To PAO product.PAO product is detected, 130,100 DEG C of kinematic viscosity of viscosity index (VI) are 12mm2/ s, condensation point are 50 DEG C.
Embodiment 3
Take 1m31- nonene solution be added jacketed stirred autoclave, be added 4%(mass fraction) AlCl3+TiCl4/
SiO2/Fe2O4, stirring is opened, adjusting temperature is 75 DEG C, and reaction pressure control after the reaction time is 5h, opens electromagnetism in 0.5MPa
Sucker controller, Magneto separate go out AlCl3+TiCl4/SiO2/Fe2O4Catalyst obtains after adding hydrogen using light point of distillation removing
PAO product.PAO product is detected, 125,100 DEG C of kinematic viscosity of viscosity index (VI) are 10mm2/ s, condensation point are 45 DEG C.
Embodiment 4
Take 1m31- octene solution be added jacketed stirred autoclave, be added 4%(mass fraction) AlCl3+TiCl4/
SiO2/CoFe2O4, stirring is opened, adjusting temperature is 40 DEG C, and reaction pressure control after the reaction time is 10h, opens electricity in 0.1MPa
Magnetic disk controller, Magneto separate go out AlCl3+TiCl4/SiO2/CoFe2O4Catalyst obtains after adding hydrogen using light point of distillation removing
To PAO product.PAO product is detected, 115,100 DEG C of kinematic viscosity of viscosity index (VI) are 8mm2/ s, condensation point are 20 DEG C.
Embodiment 5
Take 1m3Coal oil Fischer-Tropsch synthesis oil separate C through rectifying8~C12The jacketed that alkene mixture is added is stirred to react
Kettle, be added 3%(mass fraction) AlCl3/SiO2/CoFe2O4, stirring is opened, adjusting temperature is 120 DEG C, and reaction pressure control exists
0.2MPa opens electromagnetic chuck controller after the reaction time is 5h, and Magneto separate goes out AlCl3/SiO2/CoFe2O4Catalyst, then pass through
Light point of distillation removing is crossed, obtains PAO product after adding hydrogen.PAO product is detected, 150,100 DEG C of kinematic viscosity of viscosity index (VI) are
11mm2/ s, condensation point are 53 DEG C.
Embodiment 6
Take 1m3Olefins from paraffin cracking C8~C121%(matter is added in the jacketed stirred autoclave that alkene mixture is added
Amount divide rate) AlCl3/SiO2/CoFe2O4, stirring is opened, adjusting temperature is 90 DEG C, and reaction pressure control is in 0.3MPa, reaction
Between to open electromagnetic chuck controller after 4h, Magneto separate goes out AlCl3/SiO2/CoFe2O4Catalyst is light using distillation removing
Point, PAO product is obtained after adding hydrogen.PAO product is detected, 130,100 DEG C of kinematic viscosity of viscosity index (VI) are 9mm2/ s, condensation point 40
℃。
The present embodiment highly shortened PAO process flow, reduce process units quantity, saves catalyst and separates energy
Consumption, reduces the production cost of PAO, realizes the green of PAO, environmental protection, efficiently produces.
It should be noted last that the above examples are only used to illustrate the technical scheme of the present invention and are not limiting, although ginseng
It is described in detail according to the embodiment of the present invention, those skilled in the art should understand that, to technical solution of the present invention
It is modified or replaced equivalently, without departure from the spirit and scope of technical solution of the present invention, claim should all be covered
In protection scope.
Claims (1)
1. a kind of integrated reaction and separation technique of synthesizing poly alpha-olefin (PAO), it is characterised in that: as follows:
The reactor body (1) that raw material alpha-olefin and magnetic lewis acid catalyst are added to separation integrated apparatus is internal,
It controls reaction temperature and reaction pressure carries out polymerization reaction；Reaction terminates, and opens electromagnetic chuck controller (11) power supply, is located at anti-
The magnechuck (10) for answering device main body (1) internal generates magnetic field, and magnetic lewis acid catalyst assembles absorption on magnechuck,
The reaction solution discharge reaction kettle for isolating magnetic lewis acid catalyst enters next process；Raw material alpha-olefin is added, is closed
Magnechuck power supply is closed, stirring is opened, magnetic lewis acid catalyst is scattered in liquid phase again, after reaction, then Magneto separate is carried out,
It is recycled；
The magnetism lewis acid catalyst is AlCl3/SiO2/CoFe2O4；
The raw material alpha-olefin is that coal oil separates C8~C12Alkene mixture；
Reaction temperature is 120 DEG C, reaction pressure 0.2MPa, and the reaction time is 5 hours；
The magnetism lewis acid catalyst loading is the 3% of raw material alpha-olefin；
The separation integrated apparatus includes reactor body (1), is equipped with collet (2) outside the reactor body (1), described
Heating/cooling medium outlet (8) is arranged in collet (2) upper end, and heating/cooling medium entrance (9) is arranged in lower end；The reactor master
Body (1) interior center is equipped with the blender (4) driven by motor (3), and reactor body (1) inner wall is fixed with magnechuck
(10), electromagnetic chuck controller (11) are housed outside the reactor body (1), electromagnetic chuck controller (11) the control electricity
The unlatching and closure of magnetic-disc (10)；The top of the reactor body (1) is equipped with feed opening (5) and temperature-measuring port (6), and bottom is set
There are discharge gate (7).
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| CN107051553B (en) * | 2017-05-18 | 2019-11-05 | 华东理工大学 | Novel immobilized alpha-olefin polymerization catalyst of one kind and its preparation method and application |
| CN110624487A (en) * | 2018-06-21 | 2019-12-31 | 中国石化工程建设有限公司 | Poly alpha-olefin reaction equipment and method |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1187497A (en) * | 1997-01-10 | 1998-07-15 | 中国石油化工总公司 | Catalyst for preparing magnetic alpha-olefin polymer |
| CN1194988A (en) * | 1997-04-03 | 1998-10-07 | 中国石油化工总公司 | Magnetic alpha-olefine polymer and preparing process thereof |
| CN201098614Y (en) * | 2007-07-31 | 2008-08-13 | 北京理工大学 | Magnetic control still type reactor |
| CN101654655A (en) * | 2009-09-03 | 2010-02-24 | 华中科技大学 | Bioreactor applied to magnetic nano-catalyst |
| CN201942646U (en) * | 2011-01-30 | 2011-08-24 | 山东大学 | Fuel oil desulfurization reaction device with effect of magnetically separating and recovering magnetically-supported catalyst |
| CN102786177A (en) * | 2012-07-19 | 2012-11-21 | 湖南先科环保有限公司 | Magnetic nanometer titanium dioxide wastewater treatment and recovery device |
| CN103769245A (en) * | 2012-10-23 | 2014-05-07 | 中国石油化工股份有限公司 | Magnetically-stabilized separation sleeving use method of catalyst |
| CN104370675A (en) * | 2014-08-05 | 2015-02-25 | 上海纳克润滑技术有限公司 | Method for preparing poly-alpha-olefin in continuous manner |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU2003214956A1 (en) * | 2002-02-01 | 2003-09-09 | Exportech Company, Inc. | Process and apparatus for recovery of magnetic particles in a slurry phase reactor |
-
2016
- 2016-12-12 CN CN201611139564.9A patent/CN106622039B/en not_active Expired - Fee Related
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1187497A (en) * | 1997-01-10 | 1998-07-15 | 中国石油化工总公司 | Catalyst for preparing magnetic alpha-olefin polymer |
| CN1194988A (en) * | 1997-04-03 | 1998-10-07 | 中国石油化工总公司 | Magnetic alpha-olefine polymer and preparing process thereof |
| CN201098614Y (en) * | 2007-07-31 | 2008-08-13 | 北京理工大学 | Magnetic control still type reactor |
| CN101654655A (en) * | 2009-09-03 | 2010-02-24 | 华中科技大学 | Bioreactor applied to magnetic nano-catalyst |
| CN201942646U (en) * | 2011-01-30 | 2011-08-24 | 山东大学 | Fuel oil desulfurization reaction device with effect of magnetically separating and recovering magnetically-supported catalyst |
| CN102786177A (en) * | 2012-07-19 | 2012-11-21 | 湖南先科环保有限公司 | Magnetic nanometer titanium dioxide wastewater treatment and recovery device |
| CN103769245A (en) * | 2012-10-23 | 2014-05-07 | 中国石油化工股份有限公司 | Magnetically-stabilized separation sleeving use method of catalyst |
| CN104370675A (en) * | 2014-08-05 | 2015-02-25 | 上海纳克润滑技术有限公司 | Method for preparing poly-alpha-olefin in continuous manner |
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