CN103193902A - Method for preparing ethylene oligomer - Google Patents
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- CN103193902A CN103193902A CN201210005406XA CN201210005406A CN103193902A CN 103193902 A CN103193902 A CN 103193902A CN 201210005406X A CN201210005406X A CN 201210005406XA CN 201210005406 A CN201210005406 A CN 201210005406A CN 103193902 A CN103193902 A CN 103193902A
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Abstract
The invention relates to a method for preparing ethylene oligomer. The method is characterized by employing a rotating disk reactor for preparation, and employing a late transition metal catalyst system. The method is as below: sending a mixed liquid containing a catalyst, a diluent, a cocatalyst and a comonomer into a rotating disk reactor by a metering pump with a feed rate of 0.1ml / s-1L / s; heating the reactor to a desired temperature, introducing ethylene, starting the rotating disk, and controlling the reaction temperature at 70-200 DEG C, pressure at 1bar -60bar, and reaction time at 3-6000 s; controlling rotating speed of the reactor at 3000-5000rpm in the reaction process and residence time of materials on the rotating disk for 0.1-5 s; and after the reaction, separating to obtain the ethylene oligomer. Compared with a traditional mixing polymerization, average residence time of material in the rotating disk reactor is shortened by at least 30 times, so as to realize low energy consumption and high production efficiency. In particular, polymerization temperature of each stage in the polymerization process of an initial polymerization strong exothermic reaction involved in the invention is precisely controlled, and catalyst activity, C8-C24 alpha-olefin selectivity and yield are greatly increased.
Description
Technical field
The present invention relates to a kind of preparation method of ethylene oligomer, specifically is a kind of the rotating disk reactor to be used for field of olefin polymerisation, prepares the method for ethylene oligomer.
Background technology
Ethylene oligomer be molecular weight less than the ethene polymers of 1000g/mol, wherein the alhpa olefin of C8-C24 is important high-end lube product additive.The pyridine diimine title complex that Gibson etc. and Brookhart etc. find Fe (II) and Co (II) simultaneously is catalyzed ethylene polymerization (J.Chem.Commun.1998 such as Gibson V C, 849 efficiently; WO99/12981,1999; J.Am.Chem Soc.1998 such as Brookhart M, 120,4049; Bennett AM AWO98/27124,1998).Patent ZL 200910101039.1 has announced a kind of for the ethylene polymerization catalysts system, can make a series of products from the ethylene oligomer to the ultrahigh molecular weight polyethylene(UHMWPE) by changing the pyridine diimine ligand structure.Wherein, the molar percentage of C8-C24 alhpa olefin is 50-70% in the ethylene oligomerization product.Patent CN1142142C and patent CN1179982 have announced the late transition metal catalyst based on the pyridine diimine ligand structure, polymerisate is mainly ethylene oligomer, product is dissolved in the thinner toluene in the polymerization process, system becomes the feature of polymerization in homogeneous phase, and the molar percentage of C8-C20 alhpa olefin is 55-75%.Ubiquitous phenomenon is the catalyst activity height in the late transition metal catalyst of producing ethylene oligomer at present, especially in the polyreaction starting stage, active abrupt release, produce a large amount of heat of polymerization 5-10 of Ziegler-Natta, the heat release of metallocene catalyst polymerisation starting stage (be doubly), traditional balance of moving hot mode (as water of condensation, cool brine etc.) can not the maintenance system temperature is brought the unmanageable problem of initial polymerization stage polymerization temperature.And concerning this type of catalyzer, polymerization temperature more oligomerization activity is more high, and the alhpa olefin selectivity of C8-C20 is more high.If inaccurate to the control of polymerization initial temperature, will bring negative impact to the distribution of polymerisate, this has higher requirement to the mass transfer in the polymerization process, heat-transfer effect.
The rotating disk reactor is a kind of reactor technology of process intensification.This technology makes fluid prolong axial distribution at rotating disk by atwirl rotating disk, forms thickness liquid film as thin as a wafer, and this thin liquid film mass transfer, heat-transfer effect are splendid.Patent CN101081878B adopts rotating disk reactor made hydrogenated nitrile-butadiene rubber.This method is compared with the method for preparing hydrogenated nitrile-butadiene rubber of routine, and reaction conditions requires low, has strengthened the heat-transfer effect of process, has significantly lowered the cost of hydrogenation process.Patent US7683142 has announced and has utilized the rotating disk reactor to carry out method of emulsion polymerization, can carry out homogeneous phase and heterogeneous emulsion polymerization by rotating disk reactor technology single or combination, prepares evengranular polymer beads.Alavi SM etc. (Journal of Applied Polymer Science, 2009,113,709-715) in the rotating disk reactor, carry out cinnamic bulk polymerization.The rotating disk reactor significantly improves speed of reaction, transformation efficiency.Yet, do not find the rotating disk reactor technology for the preparation of ethylene oligomer at present in the disclosed document as yet.
Summary of the invention
Technical problem to be solved by this invention provides a kind of preparation method of ethylene oligomer, adopt the rotating disk reactor to be prepared, greatly having strengthened the mass transfer in the polymerization process, heat transfer and microcosmic mixes, improve the heat energy power of moving at polymerization initial stage, thereby proposed the preparation method of a kind of efficient height, energy consumption is low and olefin conversion is higher ethylene oligomer.
The present invention solves the problems of the technologies described above the technical scheme that adopts: a kind of preparation method of ethylene oligomer, it is characterized in that adopting the rotating disk reactor to be prepared, catalyzer adopts post-transition metal catalyst system, with catalyzer, thinner, the mixed solution of promotor and comonomer is pumped in the rotating disk reactor with metering, feeding rate 0.1ml/s-1L/s, with reactor be heated to temperature required after, feed ethene, start rotating disk, polymeric reaction temperature control is between-70-200 ℃, pressure 1bar-60bar, polymerization reaction time is 3s-6000s, the rotary speed 3000-5000rpm of control reactor in the reaction process, the residence time of material on rotating disk is 0.1-5s, reaction separates after finishing, and obtains ethylene oligomer.
As preferably, described rotating disk reactor is 1 or 2-10 reactors in series, the disk diameter 8-50cm of rotating disk reactor, preferred 15-30cm; Rotating speed is 10,000rpm to the maximum, preferred 800-10,000rpm; Shearing force is 1kwm
2/ K-30kwm
2/ K, preferred 10-15kwm
2/ K.
As preferably, described post-transition metal catalyst system comprises: a) pyridine diimine part; B) methyl ethyl diketone salt compound or halide salt compound; The ratio of both amount of substances is 100～0.01, and described promotor is the product of the partial hydrolysis of alkylaluminium cpd or alkylaluminium cpd, and the ratio of the amount of substance of described promotor and methyl ethyl diketone salt compound is 100～10000.
Described methyl ethyl diketone salt compound is ferric acetyl acetonade (Fe (acac)
n) or acetylacetone cobalt (Co (acac)
n), n=2,3, the halide salt compound is FeX
nOr CoX
n, n=2 wherein, 3, X is F, Cl, Br or I.
Preferred again, described catalyzer is homogeneous catalyst or heterogeneous catalyst, and wherein the diameter of heterogeneous catalyst is between 100nm-50um, and that the carrier that is suitable for comprises is solid, particle, have greater than 50m
2G
-1The metal oxide with high-specific surface area, nonmetal oxide, organism or its mixture, when using heterogeneous catalyst, before the polyreaction, earlier heterogeneous catalyst is evenly spread upon on the rotating disk.
Described comonomer is C
1-C
20Alpha-olefin, can add or not add during polymerization, preferably do not add.
Preferably, described thinner is the inertia alkane diluent, comprises one or both and the above mixture of forming in the alkane of benzene,toluene,xylene, perhydronaphthalene or C6-C12.Preferably to the good thinner of ethylene oligomer dissolving power such as toluene, dimethylbenzene, perhydronaphthalene, normal heptane, octane etc.
Improve, described feeding rate is preferably 0.1ml/s-100ml/s again, and polymerization temperature is preferably-40-100 ℃, polymerization pressure is preferably 1bar-21bar, and polymerization reaction time is preferably 10s-3000s, and the residence time of material on rotating disk is preferably 1s-3s.
At last, the carrier of described heterogeneous catalyst is preferably the inorganic carrier of silicon-dioxide, aluminum oxide, Thorotrast, titanium dioxide, silica-alumina, silicon carbide, illiteracy holder soil and their compositions.
Compared with prior art, the invention has the advantages that: adopted the rotating disk reactor, because the high speed rotating of reactor inner rotary table, make reaction mass form one deck reactive film as thin as a wafer at rotating disk, can produce great shear forces, show and move thermal effect excellently, and reach microcosmic admixture completely fast.Compare with traditional stirring polymerization, the mean residence time of material in the rotating disk reactor shortens more than 30 times at least, and energy consumption is low, production efficiency is high.Especially be fit to accurately control in the initial polymerization strong exothermal reaction involved in the present invention the polymerization temperature in each stage of polymerization process, significantly improve selectivity and the yield of catalyst activity and C8-C24 alpha-olefin.
Figure of description
Fig. 1 is the structural representation of rotating disk reactor of the present invention;
1. temperature control tank, 2. reactor, 3. rotating disk, 4. rotation axis, 5. gas feed pipe, 6. liquid feeding pipeline, 7. drainage conduit;
Fig. 2 is typical ethylene oligomerization products distribution figure.
Embodiment
Describe in further detail below in conjunction with the present invention of embodiment.
The double line anhydrous and oxygen-free of standard vacuum working method is all adopted in the operation of all air-sensitive materials.Agents useful for same all needs to use after the refinement treatment.
Product liquid portion qualitative test on gas chromatography instrument Nicolet HPGC6890/MS5973 earlier in the oligomerisation experiment.
The content of each component of product liquid portion (sample should not have suspended solid) is measured at gas chromatograph Agilent 68090N in the oligomerisation experiment.The correction factor that each components contents is got the alkene homologue is 1, adopts the calibration curve of 1-hexene and normal heptane to calculate.Pillar flow rate of carrier gas 3.0mlmin during measurement
-1, 50 ℃ of starting temperatures, constant temperature 5min, 20 ℃/min is raised to 270 ℃ then.
Above-mentioned implementation process can adopt the mode of continuous feeding or the mode of employing batch feed according to the known measure of professional.
Vinyl polymerization is in the 250ml glass reactor, adds 100ml toluene, constant temperature to 30 ℃.Add 2umol2 again, 6-two (1-(2-aminotoluene base ethyl)) pyridine (L), 2umol ferric acetyl acetonade and 3000umol MAO.Under agitation feed ethylene gas, ethylene pressure is normal pressure, reacts 30 minutes.And add the interior mark of 1ml normal heptane when measuring as GC (gas-chromatography).Sample centrifugation behind-18 ℃ of cold 4h, the product liquid portion is preserved in refrigerator, solid part adds 10% ethanol solution hydrochloride, and with after the washing with alcohol in vacuum drying oven 50 ℃ of dry 12h down.Among the initial 5min of polymerization, temperature rises to 65 ℃ from 30 ℃.This reactive behavior is 3.967 * 10
6G polyethylene/(mol Feh atm).Typical oligomerization product distribution plan as shown in Figure 2.The molar percentage of C8-C24 alhpa olefin is 70% in the ethylene oligomerization product.
Vinyl polymerization is in the 250ml glass reactor, adds 100ml toluene, constant temperature to 0 ℃.Add 2umol2 again, 6-two (1-(2-aminotoluene base ethyl)) pyridine, 2umol ferric acetyl acetonade and 3000umol MAO.Under agitation feed ethylene gas, ethylene pressure is normal pressure, reacts 30 minutes.And add the interior mark of 1ml normal heptane when measuring as GC (gas-chromatography).Sample centrifugation behind-18 ℃ of cold 4h, the product liquid portion is preserved in refrigerator, solid part adds 10% ethanol solution hydrochloride, and with after the washing with alcohol in vacuum drying oven 50 ℃ of dry 12h down.Among the initial 5min of polymerization, temperature rises to 65 ℃ from 0 ℃.This reactive behavior is 5.967 * 10
6G polyethylene/(mol Feh atm).Typical oligomerization product distribution plan as shown in Figure 2.The molar percentage of C8-C24 alhpa olefin is 80% in the ethylene oligomerization product.
Vinyl polymerization is in the 250ml glass reactor, adds 100ml toluene, constant temperature to 50 ℃.Add 2umol2 again, 6-two (1-(2-aminotoluene base ethyl)) pyridine, 2umol ferric acetyl acetonade and 3000umol MAO.Under agitation feed ethylene gas, ethylene pressure is normal pressure, reacts 30 minutes.And add the interior mark of 1ml normal heptane when measuring as GC (gas-chromatography).Sample centrifugation behind-18 ℃ of cold 4h, the product liquid portion is preserved in refrigerator, solid part adds 10% ethanol solution hydrochloride, and with after the washing with alcohol in vacuum drying oven 50 ℃ of dry 12h down.Among the initial 5min of polymerization, temperature rises to 80 ℃ from 50 ℃.This reactive behavior is 1.324 * 10
6G polyethylene/(mol Feh atm).Typical oligomerization product distribution plan as shown in Figure 2.The molar percentage of C8-C24 alhpa olefin is 65% in the ethylene oligomerization product.
The rotating disk reactor synoptic diagram that present embodiment adopts as shown in Figure 1.Disk diameter is 20cm
Purge reaction unit with high pure nitrogen down at 100 ℃, except being cooled to 30 ℃ behind the empty G﹠W in the dereaction dress.With 100ml toluene, 2umol2,6-two (1-(2-aminotoluene base ethyl)) pyridine, 2umol ferric acetyl acetonade and 3000umolMAO fully mix, and constant temperature to 30 ℃ is sent into the rotating disk reactor.Regulating the rotating disk rotating speed is 4000rpm, incision ethene, and reaction pressure is normal pressure, the beginning polyreaction.The material mean residence time is sent into the product jar with material with the speed of 10ml/min and is added terminator less than 3s.Subsequently, sample centrifugation behind-18 ℃ of cooling 4h, the product liquid portion is preserved in refrigerator, solid part adds 10% ethanol solution hydrochloride, and with after the washing with alcohol in vacuum drying oven 50 ℃ of dry 12h down.Temperature fluctuation is in ± 0.5 ℃ in the polymerization process.This reactive behavior is 2.427 * 10
7G oligomer/ (molFeh atm).The molar percentage of C8-C24 alhpa olefin is 90% in the ethylene oligomerization product.
The rotating disk reactor synoptic diagram that present embodiment adopts as shown in Figure 1.Disk diameter is 20cm
Purge reaction unit with high pure nitrogen down at 100 ℃, except being cooled to 0 ℃ behind the empty G﹠W in the dereaction dress.With 100ml toluene, 2umol2,6-two (1-(2-aminotoluene base ethyl)) pyridine, 2umol ferric acetyl acetonade and 3000umolMAO fully mix, and constant temperature to 0 ℃ is sent into the rotating disk reactor.Regulating the rotating disk rotating speed is 4000rpm, incision ethene, and reaction pressure is normal pressure, the beginning polyreaction.The material mean residence time is sent into the product jar with material with the speed of 10ml/min and is added terminator less than 3s.Subsequently, sample centrifugation behind-18 ℃ of cold 4h, the product liquid portion is preserved in refrigerator, solid part adds 10% ethanol solution hydrochloride, and with after the washing with alcohol in vacuum drying oven 50 ℃ of dry 12h down.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.This reactive behavior is 6.317 * 10
7G oligomer/ (molFeh atm).The molar percentage of C8-C24 alhpa olefin is 96% in the ethylene oligomerization product.
The rotating disk reactor synoptic diagram that present embodiment adopts as shown in Figure 1.Disk diameter is 20cm
Purge reaction unit with high pure nitrogen down at 100 ℃, except being cooled to 50 ℃ behind the empty G﹠W in the dereaction dress.With 100ml toluene, 2umol2,6-two (1-(2-aminotoluene base ethyl)) pyridine, 2umol ferric acetyl acetonade and 3000umolMAO fully mix, and constant temperature to 50 ℃ is sent into the rotating disk reactor.Regulating the rotating disk rotating speed is 4000rpm, incision ethene, and reaction pressure is normal pressure, the beginning polyreaction.The material mean residence time is sent into the product jar with material with the speed of 10ml/min and is added terminator less than 3s.Subsequently, sample centrifugation behind-18 ℃ of cold 4h, the product liquid portion is preserved in refrigerator, solid part adds 10% ethanol solution hydrochloride, and with after the washing with alcohol in vacuum drying oven 50 ℃ of dry 12h down.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.This reactive behavior is 2.939 * 10
7G oligomer/ (molFeh atm).The molar percentage of C8-C24 alhpa olefin is 87% in the ethylene oligomerization product.
The rotating disk reactor synoptic diagram that present embodiment adopts as shown in Figure 1.Disk diameter is 20cm
Purge reaction unit with high pure nitrogen down at 100 ℃, except being cooled to-30 ℃ behind the empty G﹠W in the dereaction dress.With 100ml toluene, 2umol2,6-two (1-(2-aminotoluene base ethyl)) pyridine, 2umol ferric acetyl acetonade and 3000umolMAO fully mix, and constant temperature is sent into the rotating disk reactor to-30 ℃.Regulating the rotating disk rotating speed is 4000rpm, incision ethene, and reaction pressure is normal pressure, the beginning polyreaction.The material mean residence time is sent into the product jar with material with the speed of 10ml/min and is added terminator less than 3s.Subsequently, sample centrifugation behind-18 ℃ of cold 4h, the product liquid portion is preserved in refrigerator, solid part adds 10% ethanol solution hydrochloride, and with after the washing with alcohol in vacuum drying oven 50 ℃ of dry 12h down.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.This reactive behavior is 8.459 * 10
7G oligomer/ (mol Feh atm).The molar percentage of C8-C24 alhpa olefin is 98.57% in the ethylene oligomerization product.
The rotating disk reactor synoptic diagram that present embodiment adopts as shown in Figure 1.Disk diameter is 30cm
Purge reaction unit with high pure nitrogen down at 100 ℃, except being cooled to-30 ℃ behind the empty G﹠W in the dereaction dress.With 100ml toluene, 2umol2,6-two (1-(2-aminotoluene base ethyl)) pyridine, 2umol ferric acetyl acetonade and 3000umolMAO fully mix, and constant temperature is sent into the rotating disk reactor to-30 ℃.Regulating the rotating disk rotating speed is 4000rpm, incision ethene, and reaction pressure is normal pressure, the beginning polyreaction.The material mean residence time is sent into the product jar with material with the speed of 10ml/min and is added terminator less than 5s.Subsequently, sample centrifugation behind-18 ℃ of cold 4h, the product liquid portion is preserved in refrigerator, solid part adds 10% ethanol solution hydrochloride, and with after the washing with alcohol in vacuum drying oven 50 ℃ of dry 12h down.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.This reactive behavior is 7.459 * 10
7G oligomer/ (mol Feh atm).The molar percentage of C8-C24 alhpa olefin is 97.57% in the ethylene oligomerization product.
Embodiment 9
Except rotary speed was 800rpm, all the other experiment conditions were identical with embodiment 5.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.This reactive behavior is 4.317 * 10
7G oligomer/ (mol Feh atm).The molar percentage of C8-C24 alhpa olefin is 93.5% in the ethylene oligomerization product.
Except rotary speed is outside 10, the 000rpm, all the other experiment conditions are identical with embodiment 5.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.This reactive behavior is 4.317 * 10
7G oligomer/ (mol Feh atm).The molar percentage of C8-C24 alhpa olefin is 96.5% in the ethylene oligomerization product.
Embodiment 11
Adopt 2 rotating disk reactors in series, enter after reactor 1 discharging and continue reaction in the reactor 2.Every group reaction device operation is regulated identical with embodiment 5, and material residence time in each reactor is 3s.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.Calculate as can be known with product in second reactor, this reactive behavior is 3.517 * 10
7G oligomer/ (mol Feh atm).The molar percentage of C8-C24 alhpa olefin is 96.9% in the ethylene oligomerization product.
Adopt 10 rotating disk reactors in series, enter after reactor 1 discharging and continue reaction in the reactor 2, enter the next stage reactor successively.Every group reaction device operation is regulated identical with embodiment 5, and material residence time in each reactor is 3s.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.Calculate as can be known with product in the 10th reactor, this reactive behavior is 3.817 * 10
7G oligomer/ (mol Feh atm).The molar percentage of C8-C24 alhpa olefin is 98.9% in the ethylene oligomerization product.
Embodiment 13
Adopt 1 rotating disk reactor that has circulation device, send into the liquid material import of reactor 1 after reactor 1 discharging by recycle pump again, all the other operations are regulated identical with embodiment 5.Material at every turn in reactor the residence time be 3s.10min is carried out in polymerization altogether.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.This reactive behavior is 4.817 * 10
7Goligomer/ (mol Feh atm).The molar percentage of C8-C24 alhpa olefin is 98.4% in the ethylene oligomerization product.
Adopt 1 rotating disk reactor that has circulation device, send into the liquid material import of reactor 1 after reactor 1 discharging by recycle pump again, all the other operations are regulated identical with embodiment 5.Material at every turn in reactor the residence time be 3s.30min is carried out in polymerization altogether.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.This reactive behavior is 4.317 * 10
7Goligomer/ (mol Feh atm).The molar percentage of C8-C24 alhpa olefin is 98.9% in the ethylene oligomerization product.
Embodiment 15
Preparation contains part 2, the loaded catalyst of 6-two (1-(2-aminotoluene base ethyl)) pyridine.Use following silica-gel carrier in the present embodiment:
955 of Grace company production, median size is 40 microns, following activation before using:
150Kg silica gel 955 (Grace company) is added in the activation furnace, is under the nitrogen gas stream of 0.24m/s in gas speed, and the activation furnace temperature is risen to 120 ℃, behind the constant temperature 2 hours, be warming up to 600 ℃ by 50 ℃/hour speed, constant temperature is 4 hours under this temperature, is cooled to envrionment temperature then.The silica gel The adsorbed hydroxyl content of handling is between 0.5-0.7mmol/g.Under nitrogen protection, be stored in the dry bottle stand-by.
The clean Schlenk catalyzer bottle processed that magnetic stir bar is housed of oven dry is vacuumized, took out roasting 20 minutes with alcohol blast burner, and charge into high pure nitrogen and repeatedly take a breath, the 1g that packs into then is through Davison 955 silica gel of thermal activation, adding 50ml is dissolved with the toluene solution of a certain amount of catalyzer (Fe (acac) 3/L), at room temperature stirs 12.React the final vacuum that finishes and take toluene solvant away.Add a certain amount of MAO (concentration is the MAO toluene solution of 1.5mol/L) then, stir 2h under the room temperature, vacuum-drying obtains loaded catalyst CatA to the pressed powder of good fluidity.Keep standby under the nitrogen atmosphere.
Be aggregated in the rotating disk reactor among the embodiment 5 and carry out, earlier catalyzer is evenly spread upon on the rotating disk before the polymerization, all the other experiment conditions are identical with embodiment 5.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.This reactive behavior is 3.817 * 10
6G oligomer/ (mol Feh atm).The molar percentage of C8-C24 alhpa olefin is 96.4% in the ethylene oligomerization product.
The catalyzer of preparation among the selected embodiment 15, other conditions are identical with embodiment 1.Temperature is elevated in 55 ℃ from 30 ℃ in the polymerization process.This reactive behavior is 5.817 * 10
5G oligomer/ (mol Feh atm).The molar percentage of C8-C24 alhpa olefin is 66.4% in the ethylene oligomerization product.
Embodiment 17
Used catalyzer is acetylacetone cobalt among the embodiment 17, and is identical among all the other experiment conditions and the embodiment 5.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.This reactive behavior is 2.817 * 10
6G oligomer/ (mol Coh atm).The molar percentage of C8-C24 alhpa olefin is 93.4% in the ethylene oligomerization product.
Used catalyzer is iron protochloride among the embodiment 18, and is identical among all the other experiment conditions and the embodiment 5.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.This reactive behavior is 4.817 * 10
6G oligomer/ (mol Feh atm).The molar percentage of C8-C24 alhpa olefin is 95.4% in the ethylene oligomerization product.
Embodiment 19
Add the 5ml1-hexene among the embodiment 19 during polymerization, all the other polymerization adjustings are identical with embodiment 5.Temperature fluctuation is in ± 0.1 ℃ in the polymerization process.This reactive behavior is 5.817 * 10
6G oligomer/ (mol Feh atm).The molar percentage of C8-C24 alhpa olefin is 96.4% in the ethylene oligomerization product.
Claims (10)
1. the preparation method of an ethylene oligomer, it is characterized in that adopting the rotating disk reactor to be prepared, catalyzer adopts post-transition metal catalyst system, with catalyzer, thinner, the mixed solution of promotor and comonomer is pumped in the rotating disk reactor with metering, feeding rate 0.1ml/s-1L/s, with reactor be heated to temperature required after, feed ethene, start rotating disk, polymeric reaction temperature control is between-70-200 ℃, pressure 1bar-60bar, polymerization reaction time is 3s-6000s, the rotary speed 3000-5000rpm of control reactor in the reaction process, the residence time of material on rotating disk is 0.1-5s, reaction separates after finishing, and obtains ethylene oligomer.
2. preparation method according to claim 1 is characterized in that described rotating disk reactor is 1 or 2-10 reactors in series, the disk diameter 8-50cm of rotating disk reactor, and rotating speed is 10,000rpm to the maximum, and shearing force is 1kwm
2/ K-30kwm
2/ K.
3. preparation method according to claim 1 is characterized in that described post-transition metal catalyst system comprises: a) pyridine diimine part; B) methyl ethyl diketone salt compound or halide salt compound; The ratio of both amount of substances is 100～0.01, and described promotor is the product of the partial hydrolysis of alkylaluminium cpd or alkylaluminium cpd, and the ratio of the amount of substance of described promotor and methyl ethyl diketone salt compound is 100～10000.
4. preparation method according to claim 1 is characterized in that described catalyzer is homogeneous catalyst or heterogeneous catalyst, and wherein the diameter of heterogeneous catalyst is between 100nm-50um, and that the carrier that is suitable for comprises is solid, particle, have greater than 50m
2G
-1Metal oxide, nonmetal oxide, organism or its mixture of high-specific surface area, when using heterogeneous catalyst, before the polyreaction, earlier heterogeneous catalyst is evenly spread upon on the rotating disk.
5. preparation method according to claim 1 is characterized in that described comonomer is C
1-C
20Alpha-olefin, can add or not add during polymerization.
6. preparation method according to claim 1 is characterized in that described thinner is the inertia alkane diluent, comprises one or both and the above mixture of forming in the alkane of benzene,toluene,xylene, perhydronaphthalene or C6-C12.
7. preparation method according to claim 1, it is characterized in that described feeding rate 0.1ml/s-100ml/s, polymerization temperature is-40-100 ℃, polymerization pressure 1bar-21bar, polymerization reaction time is 10s-3000s, and the residence time of material on rotating disk is 1s-3s.
8. preparation method according to claim 2, the shearing force that it is characterized in that described rotating disk reactor is 10-15kwm
2/ K, disk diameter 15-30cm.
9. preparation method according to claim 3 is characterized in that described methyl ethyl diketone salt compound is ferric acetyl acetonade (Fe (acac)
n) or acetylacetone cobalt (Co (acac)
n), n=2,3, the halide salt compound is FeX
nOr CoX
n, n=2 wherein, 3, X is F, Cl, Br, I.
10. preparation method according to claim 4 is characterized in that the carrier of described heterogeneous catalyst is selected from the inorganic carrier of silicon-dioxide, aluminum oxide, Thorotrast, titanium dioxide, silica-alumina, silicon carbide, illiteracy holder soil and their compositions.
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| CN104844741A (en) * | 2015-05-13 | 2015-08-19 | 宁波大学 | Preparation method for mixture of ethylene-undecylenyl alcohol copolymer and ultrahigh molecular weight polyethylene |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7247202B1 (en) * | 1999-02-17 | 2007-07-24 | Protensive Limited | Process for the conversion of a fluid phase substrate by dynamic heterogeneous contact with a solid agent |
| CN101649012B (en) * | 2009-07-30 | 2011-06-29 | 浙江大学 | Catalyst system for ethylene polymerization |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7247202B1 (en) * | 1999-02-17 | 2007-07-24 | Protensive Limited | Process for the conversion of a fluid phase substrate by dynamic heterogeneous contact with a solid agent |
| CN101649012B (en) * | 2009-07-30 | 2011-06-29 | 浙江大学 | Catalyst system for ethylene polymerization |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104844741A (en) * | 2015-05-13 | 2015-08-19 | 宁波大学 | Preparation method for mixture of ethylene-undecylenyl alcohol copolymer and ultrahigh molecular weight polyethylene |
| CN104844741B (en) * | 2015-05-13 | 2016-11-23 | 宁波大学 | A kind of ethylene-undecylenic alcohol copolymer and the preparation method of ultra-high molecular weight polyethylene mixture |
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