CN1062538A - Ziegler-natta catalyst - Google Patents
Ziegler-natta catalyst Download PDFInfo
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- CN1062538A CN1062538A CN91111840A CN91111840A CN1062538A CN 1062538 A CN1062538 A CN 1062538A CN 91111840 A CN91111840 A CN 91111840A CN 91111840 A CN91111840 A CN 91111840A CN 1062538 A CN1062538 A CN 1062538A
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Abstract
With contain (A) 80～95 moles of % magnesium chlorides and (B) 5～20 moles of % contain no reactive hydrogen and do not have the functional at least a pre-activated carrier to electron compound of ester (by the equal diameter D of matter
mBe 10～100 microns, size distribution D
m/ D
nBeing lower than 2 spheroidal particle constitutes) prepare the method for Ziegler-natta catalyst.(i) handle pre-activated carrier with containing at least a of reactive hydrogen to electron compound, (ii) selectively handle the active carrier that obtains with at least a aryl esters, (iii), (iv) behind the catalyst detergent of dipping, make it activation with titanium tetrachloride with the treated carrier of titanium tetrachloride dipping.
Description
The present invention relates to be used for the Ziegler-Natta type carried catalyst of polymerization of olefines; The carrier of the magnesium chloride spheroidal particle that this catalyzer is used; And the method for preparing this catalyzer.This catalyzer has high activity when olefinic polymerization, and has very high steroselectivity in the polypropylene process.
As everyone knows, Ziegler-natta catalyst systems is to be made of together the catalyzer that comprises at least a transition metal (as titanium) compound, the promotor that comprises at least a metal (as aluminium) organometallic compound.In addition, well-known, when using transistion metal compound, when adopting the carrier that is made of the solid inorganic compound such as magnesium chloride, the character of these catalyzer is subjected to very big influence.At the technical elements of preparation carried catalyst, the character of carrier is most important for the characteristic of catalyzer with the method for preparing catalyzer, and this method for preparing catalyzer normally is set in transistion metal compound on the described carrier.
European patent application EP-A-0,098,196 discloses that to prepare a kind of be to be basis and the support of the catalyst method that contains the spheroidal particle that a kind of a small amount of electron donor compound constitutes by magnesium chloride basically.By mole, be benchmark with the magnesium chloride, this electron donor compound is usually less than 3%.EP-A-0,099,773 has disclosed by handling this carrier with the fat of aromatic oxide or aromatic acid, prepares catalyzer with the above-mentioned carrier of titanium tetrachloride dipping then, and like this, each magnesium atom of catalyzer contains the titanium atom of 0.5-3%.
Have found that this catalyzer can be produced polyolefine, especially can produce and have remaining titanium content and be not less than 5PPm, make polymerization efficiency be no more than the polypropylene of about every gram catalyzer 2Kg polymkeric substance thus.Find that also the polymkeric substance of producing thus has residual chlorine content, when the catalyzer that uses contained a little amount of titanium, this content was correspondingly higher.In addition, with this Preparation of Catalyst, the polypropylene of melting index in/10 minutes scopes of 2 grams contain the polymkeric substance that is insoluble to the ebullient normal heptane, its content is usually less than 93%(weight).
Therefore, apparent, one of subject matter that solve is to develop a kind of catalyzer that is stated from the magnesium chloride spheroidal particle, suitable high titanium content is arranged.Another problem is that exploitation a kind ofly can contain the very catalyzer of the polymkeric substance of the residual amount of low catalyst thereby can produce with the extreme efficiency olefin polymerization, more than all be with regard to titanium and chlorine.
In addition, when using very highly active catalyzer, can estimate to have new problem and occur.Specifically, one of these problems relate to catalyzer and must have certain ability and bear between polymerization period owing to particulate increases the huge stress that produces.If this growth is extremely rapidly and reach a certain height (this is to cause because of effective catalyst), so, the sphericity that just is difficult to avoid the particle spalling and keeps polymer beads.Another problem relates to when this activity of such catalysts increases, catalyzer Stereoselective characteristic variation often in propylene polymerization processes.
Therefore, need develop a kind of high-crystallinity that can not only produce in a hurry and gather the house thing, and can produce the catalyzer of amorphous polymer or elasticity co-polymer.Therefore this catalyzer must be fit to the needs of various commercial run olefin polymerizations, especially must be adapted at the needs of suspension method and these two kinds of methods of vapor phase process in liquid phase olefin or the hydrocarbon solvent.
Have now found that, can prepare and a kind ofly can avoid or reduce above-mentioned defective, satisfy the effective catalyst of industrialization polymerization process needs.
So, theme of the present invention is a kind of Ziegler-natta catalyst that can be applied to olefinic polymerization, it is characterized in that it comprises a kind of pre-activated carrier, this carrier contains at least a electron donor Compound D that 80-95 mole % magnesium chloride and 5-20 mole % do not have reactive hydrogen and no ester functional group
1, and by the equal diameter of matter be 10-100 micron and size distribution to be the equal diameter Dm of matter be lower than 2 spheroidal particle with the ratio of number average diameter Dn forms, this pre-activated carrier is in advance respectively with at least a electron donor Compound D that contains reactive hydrogen
2Handle, then, selectively handle with the ester of at least a aromatic acid, when flooding with titanium tetrachloride, during then with the liquid hydrocarbon washing and with the titanium tetrachloride activation treatment, this catalyzer contains each magnesium atom 4-12% titanium atom.
According to the present invention, make us finding uncannily, high active carried catalyst when preparation has high titanium content and olefinic polymerization, mainly being to use a kind of is that the basis is also with the preactivated special carrier of electron donor compound with the magnesium chloride.Preactivated carrier is characterised in that this carrier contains quite a large amount of electron donor Compound D that does not contain reactive hydrogen and ester functional group
1Electron donor compound like this or Lewis base is known, and it has lower coordination ability.Compound D
1Preferentially among ethers, sulfone class, sulfoxide class, thioether class, amine, amides and phosphine class, select.Clearly, should get rid of electron donor compound (as water or alcohol) that contains reactive hydrogen and the electron donor compound that contains ester functional group.Particularly should get rid of can with the electron donor compound of alkyl magnesium compound reaction.Compound D
1Preferably should be selected from ether.
Be used to prepare the pre-activated carrier of catalyzer of the present invention, it is characterized in that this carrier contains quite a large amount of electron donor Compound D
1This feature has constituted and has obtained rich titanium and one of primary condition of extremely active carried catalyst when polymerization thus.Pre-activated carrier composition contains the magnesium chloride of 80-95 mole %, 5-20% Compound D
1Said composition preferably contains magnesium 85-90 mole %, contains Compound D
110-15 mole %.
Have found that, when pre-activated carrier is the homogeneous compositions form, can obtain optimum, in other words, whole magnesium chloride granules is from center to face (not only not from the teeth outwards) component uniform distribution.To obtain this pre-activated carrier in addition, recommend to prepare with the precipitator method.
Also find, when pre-activated carrier structure is amorphous basically, in other words in the structure crystallized form disappear substantially and powder in when not having the characteristic X-ray diffracting spectrum, this pre-activated carrier can be produced the high performance catalyst that can bear huge growth stress between polymerization period.Thus,, be preferably under the quite accurate condition, can obtain the pre-activated carrier of this special shape by the precipitator method.
In addition, the feature of pre-activated carrier is that also it is made up of the equal diameter 10-100 of matter micron, the spheroidal particle that is preferably the 20-50 micron.The particle of pre-activated carrier has very narrow size distribution, and the equal diameter Dm of matter and the ratio Dm/Dn of number average diameter Dn are less than 2 like this.More particularly, these particle grain size degree distribute can be extremely narrow, be too narrow to Dm/Dn than being 1.1-1.5, in fact notice does not have particle diameter more than the 1.5Dm or below the 0.6Dm, size distribution also can be assessed in such a way, and promptly same batch particle is included in the weight greater than 90%() in Dm ± 10% zone.
Pre-activated carrier specific grain surface is long-pending can be 20-100m
2/ g(BET), be preferably 30-60m
2/ g(BET), these particulate relative density scopes are between 1.2-2.1.
Being used for pre-activated carrier of the present invention can make the method for dialkyl magnesium compound and the reaction of a kind of organochlorine compound distinguishingly prepare having when existing to electron compound D.R
1MgR
2Compound can select for use and make this dialkyl magnesium compound, R in the formula
1And R
2Can be to contain C
2-C
12Identical or different alkyl.One of key property of this dialkyl group magnesium compound is to dissolve in this hydrocarbon medium that will prepare carrier.Formula R
3The alkyl chloride of Cl is optional as organic chloride, R in the formula
3Be to contain C
3-12Secondary alkyl, tertiary alkyl preferably.Recommend use formula R
4OR
5Ether as the electron donor compound, R in the formula
4And R
5Contain C
1-12Identical or different alkyl.
In addition, the various reactants that are used to prepare pre-activated carrier can be used under the following conditions:
One mol ratio R
3Cl/R
1MgR
2Be 1.5-2.5, be preferably 1.95-2.2, and
One mol ratio D
1/ R
1Mg/R
2Be 0.1-1.2, be preferably 0.3-0.8.
The electron donor Compound D is being arranged
1When existing, R
1MgR
2With R
3Reaction between the Cl is a kind of precipitin reaction of carrying out under the stirring in liquid hydrocarbon.In this case, the expert thinks under all constant situation of other condition, and physical parameter such as dielectric viscosity, the working conditions that stirs type and stir speed (S.S.), reactant can be in form, structure, separate out in particulate granularity and the size distribution and play an important role.Yet, obtain to be used for the present invention and especially with non-crystal structure with contain a large amount of electron donor Compound D
1Be the pre-activated carrier of feature, recommend promptly 10-50 ℃, to be preferably and to carry out precipitin reaction under 15-35 ℃ than under the lower temperature.In addition, also recommend and slowly to carry out precipitin reaction, at least 10 hours, preferably 10-24 hour,, especially in separating out solid, be bumped into a large amount of D so that make the solid product of formation obtain suitable tissue
1Compound and homodisperse.
From the pre-activated carrier that defines thus, in fact Preparation of catalysts comprises following four consecutive steps:
(a) for obtaining the activatory carrier, at least with a kind of reactive hydrogen D that contains
2The pre-activated carrier of electron donor compound treatment,
(b) selectively handle above-mentioned activatory carrier with a kind of aromatic esters at least,
(c) with the carrier of titanium tetrachloride dipping through above processing, then with the carrier of liquid hydrocarbon washing through dipping, and
(d) with the carrier of titanium tetrachloride activation treatment through dipping and washing.
The first step is for obtaining activated carrier, with containing reactive hydrogen D
2The pre-activated carrier of electron donor compound treatment, that is to say a kind of carrier that can be bumped into a large amount of titanium tetrachlorides subsequently.In fact it is very complicated to carry out this processing, because must make the electron donor Compound D in pre-activated carrier
1With the electron donor Compound D that contains reactive hydrogen
2Between permutoid reaction become possibility.Under this condition, permutoid reaction really may be complete, but do not improve the practical structures of carrier.Specifically, Compound D
1The ability that must show the coordination magnesium chloride is than Compound D
1Big.Make personality outer surprised be that this processing can be carried out under the situation that needn't observe carrier degree of crystallinity or particles dispersed degree fully.
Specifically, by making pre-activated carrier and Compound D
2(D
2Consumption is every mole of magnesium chloride 0.2-1.2 mole, is preferably the 0.5-1.0 mole) contact and handle.Therefore, the temperature when special recommendation contacts is preferably 10-35 ℃ at 0-50 ℃, so that realize permutoid reaction under the situation that does not have obviously to change at former pre-activated carrier.Being preferably in liquid hydrocarbon interior (as in hexane) in addition contacts while stirring.In fact, available various possibility modes realize this contact, for example, add Compound D lentamente to pre-activated carrier suspension (this suspension keeps whipped state in liquid hydrocarbon)
2The Compound D of using in the generally observed reason herein
2Can be bumped at an easy rate in the carrier, not demonstrate non-crystal structure and vehicle group are woven with significant variation.Before carrying out next step, use Compound D thus
2The activatory carrier can be used liquid hydrocarbon (as normal hexane) washing one or many.
The electron donor Compound D that contains reactive hydrogen
2Preferentially from water, alcohol, phenol, mercaptan and hydrogen sulfide, select.Preferably select the alcohol that contains 1 to 12 carbon atom for use.Or rather, Compound D
2From ethanol, propyl alcohol, propyl carbinol, Pentyl alcohol and n-hexyl alcohol, select.
Then, in second step, optionally handle with at least a aromatic acid fat with the electron compound activatory carrier of giving that contains reactive hydrogen thus, this ester can be selected from for example ethyl benzoate, methyl p toluate and phenylformic acid dibutylester or phenylformic acid diisobutyl ester.
To being used for that ethylene homo closes or the copolymerization catalyst of the alpha-olefin with 3 or a plurality of carbon atoms of ethene and trace (being less than 20% weight usually), selectively handle with at least a aryl esters.To being used for the catalyzer that equal polymerization or copolymerization have the alpha-olefin of 3 or a plurality of carbon atoms, the most handy at least a aryl esters is handled.When using this treatment process, this processing is carried out under the condition of structure that does not make carrier and tissue generation considerable change.Specifically, with the activatory carrier with contain every mole of magnesium chloride 0.1-1.0 mole, preferably the aryl esters of 0.2-0.8 contacts and handles.In addition, special recommendation contact treatment temp is 0-60 ℃, is preferably 10-50 ℃, so that this processing is carried out under the condition that original vector is had significant change.In addition, can in liquid hydrocarbon (as normal hexane), contact while stirring, in fact, available different methods contact, specifically, can be by in activatory carrier suspension, adding aryl esters lentamente and in liquid hydrocarbon, keeping stirring contacting.Need, before proceeding to next step, the carrier one or many that available liquid hydrocarbon (as normal hexane) washing is treated thus.
In the 3rd step, with the carrier that titanium tetrachloride dipping was selectively handled through aryl esters, used titanium tetrachloride promptly can be pure, can be again the solution of it and liquid hydrocarbon (as normal hexane).The method that 2-20 mole titanium tetrachloride contacts with carrier that is preferably with every mole of magnesium chloride 1-25 mole is flooded.In addition, recommending dipping temperature is 20-130 ℃, is preferably 70-120 ℃, so that make carrier can keep suitable non-crystal structure, and can bear the stress of high-speed rapid growth between polymerization period fully.In addition, be preferably in the liquid state (as normal hexane) and flood while stirring.In fact, available various method dipping specifically, adds titanium tetrachloride in carrier suspension, keep stirring in liquid hydrocarbon, and thus obtained mixture is kept stirring 0.5-10 hour, is preferably 1-4 hour.Before carrying out next step, wash the carrier one or many of dipping thus with liquid hydrocarbon (as normal hexane).During the washing, with other compound (such as the electron donor Compound D
2) the interior untreated titanium tetrachloride of elimination carrier.
Make us finding uncannily that behind the dipping, contain a large amount of titaniums by the solid that is obtained in the impregnation steps certainly, content is the titanium atom of each magnesium atom 4-12%.And, during dipping and washing, contain the electron donor Compound D of reactive hydrogen
2(D
2Be present at first in the activatory carrier) completely dissolve from solid.
Final step is carried out activation treatment with titanium tetrachloride to the carrier through dipping, and according to the present invention, it is very important that this processing has high active catalyzer when the olefinic polymerization for preparation.For the purpose of indicating, estimate that this activation treatment can make catalyst activity increase by two times or three times.Because the tissue of thus obtained catalyzer and particle diameter be identical with the pre-activated carrier of initial use significantly, the effect of therefore last activation step is more amazing.
Activation treatment comprises that the solid that will flood titanium contacts with titanium tetrachloride, and used titanium tetrachloride is pure or liquid hydrocarbon (as normal hexane) solution.The titanium tetrachloride consumption is every mole of magnesium chloride 1-25 mole, is preferably the 2-20 mole.In addition, the temperature of recommending to contact is 20-130 ℃.Be preferably 20～120 ℃ in liquid hydrocarbon (as normal hexane), preferably under agitation carry out activation step.In fact, the contact that can in all sorts of ways, especially by the dipping in liquid hydrocarbon add titanium tetrachloride in the solids suspension of titanium, and stirred mixture 0.5-10 hour that obtains thus, be preferably 1-4 hour.With the treated solid one or many of liquid hydrocarbon (as normal hexane) washing.Activation treatment can comprise this contact of one or many.
Special discovery in surprise, the effect of activation treatment does not increase the titanium content (content is very high) of catalyzer significantly, however its main effect has but increased the activity of catalyzer between polymerization period widely.
The solid catalyst prepared according to the present invention is made of particle, this particulate physical properties, identical as spherical, the equal diameter of matter and size distribution and former pre-activated carrier (obtaining granules of catalyst by this carrier).Catalyzer contains each magnesium atom 4-12%, is preferably 5-10%, and the best is the titanium atom of 6-9%.
Catalyzer that is obtained and promotor one are used from olefinic polymerization, and promotor is selected from organoaluminum, organic-magnesium or organic compound.In general, use one or more to be selected from the organo-aluminium compound of trialkylaluminium or aikyl aluminum halide.In propylene polymerization or copolymerization in particular cases, use organoaluminum, the mixture of trialkylaluminium and aikyl aluminum halide preferably with a kind of electron donor compound that is selected from aryl esters class or silicoorganic compound (as silane derivative).Specifically, after having handled activated carrier with phthalic ester, preferably use one or more organo-aluminium compound promotors with silicoorganic compound.In all cases, when using organo-aluminium compound with the electron donor compound, the mol ratio of electron donor compound and organo-aluminium compound is 0.1-0.5.
Amount with titanium compound in the catalyzer is as the criterion, and the organo-aluminium compound relative molecular weight that is used as promotor can change in very wide scope.For example, atomic ratio AL/Ti changes in 0.5-200.
By means of catalyzer of the present invention, the efficient of olefinic polymerization is very high.Specifically, in the polymerization of propylene liquid, efficient reaches every gram catalyzer 15-20 kg of polymer.Titanium and cl content remaining in this polymkeric substance are lower than 2PPm and 100PPm usually respectively.It is very high that thus obtained crystalling propylene becomes, this is to be respectively 2 because work as polyacrylic melting index (MI5/190), during 6 or 10 grams/10 minutes (under 190 ℃ and 5Kg weight, measuring), the polymer content that is insoluble to the ebullient normal heptane be equal to or higher than 96%, 95% or 94%(weight).
In addition, observe expediently, by catalyzer of the present invention, each particle is grown between polymerization period evenly, and the result obtains the spheroidal particle polymer powder.These particles are handled easily, have very high tap density, and particularly for polyethylene and polypropylene, its tap density is 0.40-0.50g/cm.
This catalyzer is fit to and all polymerization techniques, particularly vapor phase process and the suspension method in liquefied olefines or hydrocarbon solvent.
By means of catalyzer of the present invention, satisfying under the industrial condition, can produce a large amount of alpha-olefinic polymer or contain the multipolymer of a large amount of repeating units, for example, (relative density is more than 0.940 for high density polyethylene(HDPE), in these high density polyethylene(HDPE)s, based on Alathon, ethylene copolymer with contain the alpha-olefin copolymer of 3-8 carbon atom.), (relative density is lower than 0.940 to low density linear polyethylene, is made of ethylene copolymer and one or more alpha-olefins of containing 3-8 carbon atom, and has content greater than 85% ethylene-derived units.), the elasticity trimer of ethene, propylene or diolefine, ethylene-derived units is between the ethene of about 30-70% weight content and the elastocopolymer of propylene, the multipolymer of isotactic polyprophlene and propylene and ethene or other alpha-olefin (weight content is the propylene derived unit more than 90%), the multipolymer of propylene and butene-1 (weight content is the butene-1 derived units of 10-40%).
Measure the method for matter equal (Dm) and number average (Dn) particle diameter:
According to the present invention, the matter of carrier, catalyzer or polymer beads is (Dm) and number average (Dn) diameter microscopic all, by means of Optomax Quantimet (Micro-Measmowents Ltd., Great Britain).Measuring principle comprises by using opticmicroscope, from the experimental study of particle population, obtain a frequency distribution table, this table provides the granule number (ni) that belongs to each diameter grade (i), and each grade (i) characterizes with the mid-diameter (di) that comprises described level boundaries.According to NF NFX11-630(1981 June) Dm and Dn provide by following formula:
The equal diameter of matter: Dm=(Σ ni (di)
3Di)/(Σ ni (di)
3)
Number average diameter: Dn=(Σ nidi)/(Σ ni)
Ratio Dm/Dn is the sign of size distribution; Sometimes this ratio also is known as " particle diameter distribution width ".Use the Optomax image analyzer, utilize the upset microscope to measure.This microscope can be measured the suspension of carrier granule catalyzer, particle or polymer beads under the situation that 16-200 doubly amplifies.Television camera the upset image that provides of microscope is provided and is transported in the computer and analyzes to pointwise line by line, so that the mensuration particle size is a particle diameter, and sorting then.
Following embodiment for example understands the present invention, but and does not mean that restriction the present invention.
The preparation of the pre-activated carrier of embodiment 1-
The first step contains mixture that 10 moles of dibutylmagnesiums constitute, 6.45 liters of normal hexanes and 1 liter of isoamyl ether in by normal hexane with 10.2 liters and is sequentially added into one and is furnished with in 30 liters of stainless steel reactors that rotating speed is 600 rev/mins agitator and overcoat under nitrogen and room temperature.Second step remained on 600 rev/mins with the speed of agitator, and temperature of reaction keeps 25 ℃, and with constant rate of speed 2.4 liters of tertiary butyl chlorides was joined in the mixture that obtains thus, lasted 12 hours.Behind this end of processing, reaction mixture is incubated 3 hours at 25 ℃.The precipitation that obtains is washed with 15 liters of normal hexanes.Repeated washing precipitation 6 times.The solid product that obtains has formed pre-activated carrier (A), and it is based on magnesium chloride, in magnesium chloride, contains the isoamyl ether of 12 moles of %.When microscopically detected, pre-activated carrier (A) was the spherolite shape, has 21 microns equal diameter of matter and extremely narrow size distribution, and like this, the ratio of particulate Dm/Dn equals 1.4.
The specific surface area of pre-activated carrier (A) is about 45m
2/ g(BET).The structure of the magnesium chloride in the pre-activated carrier is amorphous basically, and the X ray diffracting characteristic figure is not provided in the powder.
Embodiment 2 Preparation of catalysts
Under nitrogen atmosphere, the suspension (containing 4 moles magnesium chloride in 6 liters of normal hexanes) of the pre-activated carrier (A) of preparation among the front embodiment 1 is introduced one, and to be furnished with rotating speed be in 30 liters of stainless steel reactors of agitator of 350 rev/mins.18 liters of normal hexanes are joined in this suspension, keep down stirring, in 30 minutes, slowly add 0.365 liter of n-hexyl alcohol then in room temperature (25 ℃).Then, the activated carrier suspension that obtains is thus continued down to stir 1 hour at 25 ℃.Behind this end of processing, stop to stir, make the activated carrier precipitation, remove the supernatant liquid phase and in 6 liters of normal hexanes, pass through to stir the resuspending activated carrier.
In second step, 10 liters of normal hexanes are joined in the activated carrier suspension that obtains at last, keep stirring down, in 30 minutes, slowly add 0.46 liter of ethyl benzoate then at 25 ℃.Under 25 ℃, the carrier suspension that the continuation stirring is handled thus 1 hour.Behind this end of processing, stop to stir, make the carrier precipitation of processing, remove the supernatant liquid phase, and under 5 ℃ of the calamities, at every turn with 20 liters of normal hexanes to the carrier elder generation after scouring handled 3 times, following steps are all adopted in each washing, be stirred suspension 15 minutes, made the carrier precipitation handled then 20 minutes, グ shovel yield close whiz (16) exorcise＜+the swish swish brain dimple river which rises in the northeastern part of Anhui Province " last, the carrier that resuspending was handled in 6 liters of normal hexanes.
The 3rd step joined 6 liters of titanium tetrachlorides in the most reprocessed carrier, kept stirring down at 25 ℃.The suspension that obtains thus is heated to 100 ℃ and continue to stir 2 hours under this temperature.Behind this end of processing, the carrier suspension that under agitation will flood thus is cooled to 50 ℃, stop then stirring, make the carrier precipitation of dipping, remove the supernatant liquid phase, and under 50 ℃, each divide the carrier 3 times that first after scouring floods with 20 liters of normal hexanes, then, under 25 ℃, use 20 liters of normal hexane elder generation after scouring 2 times at every turn.At last, under 25 ℃, the carrier (B) of resuspending dipping in 6 liters of normal hexanes.The latter is made up of the spheroidal particle of the titanium atom that contains each magnesium atom 6%.
In the 4th step, what 9 liters of titanium tetrachlorides are joined the impregnated carrier (B) that obtains at last is in the supernatant liquid, keeps down stirring at 25 ℃.The suspension that obtains thus is heated to 100 ℃ and continue to stir 2 hours under this temperature.Behind this end of processing, the catalyst suspension that will obtain thus is cooled to 50 ℃ while stirring, stops then stirring, and makes catalyst precipitation, remove the supernatant liquid phase, and under 50 ℃, use 20 liters of normal hexanes priority washing catalysts 3 times at every turn, then, under 20 ℃, with 20 liters of normal hexanes elder generation after scouring 4 times.
Isolate catalyzer (C) and place under the nitrogen atmosphere, catalyzer (C) contains the titanium atom of each magnesium atom 6.5%, and is 21 microns, the very narrow spheroidal particle structure poplar of size distribution by the equal diameter of matter, and like this, particulate Dm/Dn ratio is 1.4.
Embodiment 3(is relatively) Preparation of catalysts
Except the impregnated carrier (B) that do not carry out for the 4th step and obtain during the 3rd EOS as the catalyzer, undertaken by the operation of embodiment 2 fully.
Embodiment 4(is relatively) Preparation of catalysts
Except using the magnesium chloride support (D) that only contains 1.5 moles of % isoamyl ethers (in magnesium chloride) to replace being undertaken by two prefaces of embodiment 2 fully the pre-activated carrier (A).Carrier (D) is pressed embodiment 11(EP-A-0,098,196 fully) preparation.When microscopically detects, carrier (D) particulate state spherical in shape, the equal diameter of matter is that 20 microns and size distribution are extremely narrow, like this, particulate Dm/Dn ratio is about 1.3.
The specific surface area of carrier (D) is about 40m
2/ g(BET).
Obtain containing the catalyzer (E) of each magnesium atom 1.4% titanium atom thus.
Embodiment 5 Preparation of catalysts
Except in second step, replacing being undertaken by the operation of embodiment 2 fully 0.46 liter of ethyl benzoate with 0.85 liter of diisobutyl phthalate.
Obtain containing the catalyzer (F) of 6% titanium atom of each magnesium atom thus.This catalyzer is to be made of identical with catalyzer (C) in every respect spheroidal particle.
Embodiment 6 propylene liquid polymerizations
Under 5 ℃ nitrogen, to contain 0.626 mmole triethyl aluminum, 0.313 mmole diethyl aluminum chloride and 0.313 mmole methyl p toluate, the mixture of catalysts that contains 0.01 mmole titanium amount and volume and be equivalent to hydrogen that the hydrogen dividing potential drop is 0.2MPa and 700g propylene liquid and introduce one and be furnished with 2.2 liters of stainless steel reactors that rotating speed is 350 rev/mins of agitators, reactor will be heated to 70 ℃.React after 1.5 hours, collection polypropylene powder, its characteristic are shown in table 1 as the function of catalyst system therefor.
Table 1
The characteristic of resulting polymers
Catalyzer C B E
(comparison) (comparison)
Efficient
(kg polymkeric substance/g catalysis 18 62
Agent)
Residual chlorine content (ppm) 80 280 620
Remaining titanium content (ppm) 1.4 53
Be insoluble to 95.5 95 91 of ebullient normal hexane
Polymer content (weight %)
MI/190(g restrains 655
/ 10 minutes)
Tap density (g gram/0.45 0.45 0.46
cm
3）
The equal diameter pm(of matter micron) 550 250 150
Size distribution Dm/Dn 1.6 1.6 1.7
Embodiment 7
Except replacing catalyzer (C) with catalyzer (F), benzene three oxosilane mixtures with triethyl aluminum that contains 1 mmole and 0.2 mmole replace containing outside the mixture of triethyl aluminum, diethyl aluminum chloride and methyl p toluate, are undertaken by the operation of embodiment 6 fully.In addition, hydrogen partial pressure is fixed on 0.10MPa, rather than 0.2MPa.Under these conditions.Obtain Powdered polypropylene, it has following characteristic:
-efficient: 15.6 kg of polymer/g catalyzer
-residual chlorine content: 40ppm
-remaining titanium content: 1.9ppm
-be insoluble to the polymer content of boiling n-heptane: 94.9%(weight)
-MI
5/ 190:14 gram/10 minutes
-tap density: 0.43 gram Cm
3
-Dm:450 micron
-Dm/Dn：1.6
The vapour phase polymerization of embodiment 8 propylene
Under nitrogen atmosphere.Restrain the polypropylene powder (preferably inertia and anhydrous) that previous reaction obtain with 60 in order respectively, a certain amount of catalyzer (C) of preparing from embodiment 2 (contains 0.2 mmole titanium, 6 mmole triethyl aluminums, 3 mmole diethyl aluminum chlorides, 3 mmole methyl p toluates) and the hydrogen of certain volume (being equivalent to the hydrogen dividing potential drop is 0.02MPa) introduce one and be furnished with 2.6 liters of stainless steel reactors that rotating speed is 250 rev/mins of dry powder agitators, reactor is heated to 50 ℃ and propylene is introduced reactor reach 0.3MPa up to pressure, whole polymerization process pressure perseverance is worth in this by adding propylene.React after 5 hours, obtain the 200g powdered polypropylene, it has following characteristics:
-efficient: 1.0 kg of polymer/mmole titanium
-MI
5/ 190:11 gram/10 minutes
-be insoluble to ebullient normal heptane polymer content: 93%(weight)
-tap density: 0.45g/cm
3
-Dm:150 micron
-Dm/Dn：1.6
The vapour phase polymerization of embodiment 9 ethene
Under nitrogen atmosphere, respectively the catalyzer (C) (containing 0.1 mmole titanium, 2.5 mmole triethyl aluminums) of the polyethylene powders (preferably inertia and anhydrous) that obtains in the 60 gram front reactions, a certain amount of preparation from embodiment 2 and one of hydrogen (being equivalent to the hydrogen dividing potential drop the is 0.25MPa) introducing of certain volume are furnished with 2.6 liters of stainless steel reactors that rotating speed is 250 rev/mins of dry powder agitators.Reactor is heated to 70 ℃ and ethene is introduced reactor is 0.75MPa until total pressure, between whole polymerization period, the pressure perseverance is worth in this by adding ethene.After about 2 hours reaction is finished, prepare 600 gram powdery polyethylenes, it has following characteristic:
-efficient: 6 kg of polymer/mmole titanium
-MI
5/ 190:1 gram/10 minutes
-tap density: 0.45g/cm
3
-Dm:270 micron
-Dm/D soft-shelled turtle: 1.6
The gas phase copolymerization of embodiment 10 propylene and butene-1
Under nitrogen atmosphere, its polymers of powder (preferably inertia and anhydrous) of the 60 gram propylene that obtain of previous reaction and butene-1 is introduced one be furnished with 2.6 liters of stainless steel reactors that rotating speed is 250 rev/mins a dry powder agitator, add a certain amount of catalyzer (C) (containing 0.2 mmole titanium, 5 mmole triethyl aluminums and 0.75 mmole methyl p toluate) of embodiment 2 preparations then.Reactor is heated to 50 ℃, and with the gaseous mixture of propylene and butene-1 respectively with the 70/30(volume) ratio introduce, be 0.15MPa up to pressure, by adding this gaseous mixture the pressure perseverance between whole polymerization period is worth in this.After about 5 hours reaction, prepare 235 gram powdery copolymers, it has following characteristic:
-efficient: 1.2 kg of polymer/mmole titanium
-MI
5/ 190:4.6 gram/10 minutes
The unitary weight content of the butene-1 that obtains in-the multipolymer: 30%
-Dm:170 micron
-Dm/Dn：1.6
The gas phase copolymerization of embodiment 11 ethene and propylene
Under nitrogen atmosphere, 60 gram ethene and one of propylene powder shape multipolymer (preferably inertia and anhydrous) introducing that previous reaction obtains are furnished with 2.6 liters of stainless steel reactors that rotating speed is 250 rev/mins a dry powder agitator, the hydrogen that adds a certain amount of catalyzer of from embodiment 2, preparing (C) (containing 100.05 mmole titaniums, 1.5 mmole triethyl aluminums, 0.33 mmole methyl p toluate) and 50 ml volumes then.Reactor is heated to 30 ℃ and the gaseous mixture of ethene and propylene introduced with 50/50 volume ratio, is 2MPa up to pressure, by adding this gaseous mixture the pressure perseverance between whole polymerization period is worth in this.After 2 hours the reaction, prepare 210 gram powdery copolymers, it has following characteristic:
-efficient: 1.05 kg of polymer/mmole titanium
-MI
5/ 190:0.1 gram/10 minutes
The weight content of the ethylene unit that obtains in-the multipolymer: 49.5%
-Dm:150 micron
-Dm/Dn：1.6
Embodiment 12 ethene and propylene and 2-methyl isophthalic acid, the gas phase copolymerization of 5-hexadiene
Under nitrogen atmosphere, restrain ethene, propylene and the 2-methyl isophthalic acid that previous reaction obtain with 60, the powdery copolymer of 5-hexadiene (preferably inertia and anhydrous) is introduced one and is furnished with 2.6 liters of stainless steel reactors that rotating speed is 250 rev/mins a dry powder agitator, adds a certain amount of catalyzer of preparing from embodiment 2 (C) (containing 0.2 mmole titanium and 5 mmole triethyl aluminums) then.Reactor is heated to 20 ℃, and with ethene and propylene etc. molar mixture introduce with the steady rate of 30 Grams Per Hours, last 6 hours.In the reaction beginning, introduce 3.3 milliliters of 2-methyl isophthalic acids, the 5-hexadiene was reacting 2 hours and was reacting this kind material of introducing same volume in 4 hours respectively then.React after 6 hours, prepare 130 gram powdery copolymers, it has following characteristic:
-efficient: 0.65 kg of polymer/mmole titanium
-MI
5/ 190:4 gram/10 minutes
The ethylene unit molar content that obtains in-the multipolymer: 49.9%
The 2-methyl isophthalic acid that obtains in-the multipolymer, 5-hexadiene unit molar content: 0.8%
-Dm:170 micron
-Dm/Dn：1.7
The suspending copolymerization of ethene and propylene in embodiment 13 propylene liquids
Under nitrogen atmosphere, introduce 2 liters of stainless steel reactors being furnished with 350 rev/mins agitator from the catalyzer of implementing to prepare 2 (C) (containing 0.02 mmole titanium, 1.6 mmole triethyl aluminums and 0.75 mmole methyl p toluate) with a certain amount of.With reactor cooling to 0 ℃, and introduce 500 gram propylene liquid and a certain amount of ethene, like this, the dividing potential drop of ethene is 0.3MPa.In 5 ℃, copolymerization was collected 150 gram copolymer powders after 90 minutes with the homo(io)thermism of reactor, and it has following characteristic:
-efficient: 7.5 kg of polymer/mmole titanium
-viscosity-average mole mass: 1.2 * 10
6
The weight content of the ethylene unit that obtains in-the multipolymer: 42%
-Dm:290 micron
-Dm/Dn：1.6
The suspending copolymerization of ethene and propylene in embodiment 14 normal hexanes
Under nitrogen atmosphere, with 2 liters of normal hexanes, a certain amount of catalyzer of preparing from embodiment 2 (C) (containing 0.1 mmole titanium, 5 mmole triethyl aluminums and 1 milli that methyl p toluate) is introduced one and is furnished with 2 liters of stainless steel reactors that rotating speed is 350 rev/mins a agitator.Reactor is heated to 70 ℃, and,, lasts 1 hour with the steady rate introducing ethene of 130 Grams Per Hours and the gaseous mixture of propylene respectively with 60/40 volume ratio.After the polymerization, collect 120 gram powdery copolymers, it has following feature:
-efficient: 1.2 kg of polymer/mmole titanium
-viscosity-average mole mass: 2 * 10
5
The ethylene unit weight content that obtains in-the multipolymer: 54%
-Dm:160 micron
-Dm/Dn：1.6
The suspension polymerization of ethene and propylene in embodiment 15 normal hexanes
Except with reactor cooling to 3.5 ℃ rather than be heated to 70 ℃, undertaken by the operation of embodiment 14 fully.React after 1 hour, collect 70 gram powdery copolymers, it has following feature:
-efficient: 0.7 kg of polymer/mmole titanium
The ethylene unit weight content that obtains in-the multipolymer: 84%
-Dm:140 micron
-Dm/Dn：1.6
Ethene and propylene and 4-methyl isophthalic acid in embodiment 16 normal hexanes, the suspending copolymerization of 4-hexadiene
Under nitrogen atmosphere, with 1 liter of normal hexane, a certain amount of catalyzer of preparing from embodiment 2 (C) (containing 0.2 mmole and 5 mmole triethyl aluminums) is introduced 3 liters of stainless steel reactors being furnished with 250 rev/mins agitator.Reactor is heated to 70 ℃, introduces equimolar ethene and propylene gaseous mixture with the steady rate of 60 Grams Per Hours then, last 1.5 hours.With 3.3 milliliters of 4-methyl isophthalic acids, the 4-hexadiene is introduced reactor, introduces this kind material of same volume then respectively after 0.5 hour and 1 hour in reaction.React after 1.5 hours, collect 75 gram powdery copolymers, it has following characteristic:
-efficient: 0.375 kg of polymer/mmole titanium
-weight-average molar mass: 9 * 10
4
The ethylene unit molar content that obtains in-the multipolymer: 47.6%
The 4-methyl isophthalic acid that obtains in-the multipolymer, 4-hexadiene unit molar content: 0.7%
-Dm:110 micron
-Dm/Dn：1.6
The gas phase copolymerization of embodiment 17 ethene and butene-1
Under nitrogen atmosphere, the ethene that 60 grams obtain from previous reaction is furnished with 2.6 liters of stainless steel reactors that rotating speed is 250 rev/mins a dry powder agitator with one of powdery copolymer (preferably inertia and the anhydrous) introducing of butene-1, adds a certain amount of catalyzer of from embodiment 2, preparing (C) (containing 0.05 mmole titanium and 3.5 mmole triisobutyl aluminiums) then.Reactor is heated to 70 ℃, will contains the 70%(volume then), the 10%(volume) butene-1 and 20%(volume) gaseous mixture of hydrogen introduces reactor, like this, total pressure is 1.3MPa in the reactor, and is constant at this pressure in whole copolymerization process.Behind the multipolymer 5 hours, prepare 1.05 kg ethylene and butene-1 powdery copolymer, it has following characteristic:
-efficient: 21 kg of polymer/mmole titanium
-density: 0.902
-MI
5/ 190:1 gram/10 minutes
The unitary weight content of the butene-1 that obtains in-the multipolymer: 8.5%
-Dm:500 micron
-tap density: 0.49 gram per centimeter
3
Claims (4)
1, the pre-activated carrier of catalyst for olefines polymerizing, it contain 80～95 mole of magnesium chloride and 5～20 moles of no reactive hydrogens and no ester functional group to electron compound D
1, and be that the spheroidal particle of 10～100 microns and narrow size distribution constitutes by the equal diameter of matter, like this, the equal diameter D of matter
mWith number average diameter D
nRatio be lower than 2.
2, according to the pre-activated carrier of claim 1, the specific surface area that it is characterized in that this carrier is 20～100m
2/ g(BET).
3,, it is characterized in that being selected from ether, alum, inferior alum, thioether, amine, acid amides and phosphine to electron compound according to the pre-activated carrier of claim 1.
4, preparation is according to the method for the pre-activated carrier of claim 1, this method be included in a kind of do not have reactive hydrogen and no ester functional group to electron compound D
1Exist down, in liquid hydrocarbon medium, make (a) can be dissolved in the formula R of liquid hydrocarbon medium
1MgR
2Dialkyl magnesium (R wherein
1And R
2Be identical or different C
2-12Alkyl) with (b) formula R
3The alkyl chloride of Cl (R wherein
3Be C
3-C
12The second month in a season or tertiary alkyl) with R
3Cl/R
1MgR
2Be that 1.5～2.5 mol ratio is reacted, the method is characterized in that mol ratio D
1/ R
1MgR
2Be 0.1～1.2, and at 10～45 ℃ with stir under the situation of liquid hydrocarbon medium, by contact R
1MgR
2, R
3Cl and D
1, reaction was carried out 10 hours at least.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR8802900 | 1988-03-03 | ||
| FR8802900A FR2628110B1 (en) | 1988-03-03 | 1988-03-03 | CATALYST FOR POLYMERIZATION OF ZIEGLER-NATTA-TYPE OLEFINS, SUPPORTED ON SPHERICAL MAGNESIUM CHLORIDE PARTICLES, AND PROCESS FOR PREPARING THE SAME |
| CN89101025A CN1016609B (en) | 1988-03-03 | 1989-03-02 | Ziegler-Natta type catalyst |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN89101025A Division CN1016609B (en) | 1988-03-03 | 1989-03-02 | Ziegler-Natta type catalyst |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1062538A true CN1062538A (en) | 1992-07-08 |
| CN1036852C CN1036852C (en) | 1997-12-31 |
Family
ID=25742549
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN91111840A Expired - Fee Related CN1036852C (en) | 1988-03-03 | 1989-03-02 | Ziegler-Natta Catalyst |
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| Country | Link |
|---|---|
| CN (1) | CN1036852C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103052656A (en) * | 2010-08-24 | 2013-04-17 | 巴塞尔聚烯烃意大利有限责任公司 | Catalyst components for the polymerization of olefins |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3366573D1 (en) * | 1982-06-24 | 1986-11-06 | Bp Chimie Sa | Process for the polymerization and copolymerization of alpha-olefins in a fluidized bed |
| FR2529209A1 (en) * | 1982-06-24 | 1983-12-30 | Bp Chimie Sa | CATALYSTS FOR THE POLYMERIZATION AND COPOLYMERIZATION OF PROPYLENE AND POLYMERIZATION METHODS USING THESE CATALYSTS |
| FR2529206A1 (en) * | 1982-06-24 | 1983-12-30 | Bp Chimie Sa | PROCESS FOR THE PREPARATION OF MAGNESIUM CHLORIDE SUPPORTS FOR THE PREPARATION OF ALPHA-OLEFIN POLYMERIZATION CATALYSTS AND SUPPORTS OBTAINED |
-
1989
- 1989-03-02 CN CN91111840A patent/CN1036852C/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103052656A (en) * | 2010-08-24 | 2013-04-17 | 巴塞尔聚烯烃意大利有限责任公司 | Catalyst components for the polymerization of olefins |
| CN103052656B (en) * | 2010-08-24 | 2016-06-01 | 巴塞尔聚烯烃意大利有限责任公司 | Catalyst Components for Olefin Polymerization |
| US10155825B2 (en) | 2010-08-24 | 2018-12-18 | Basell Poliolefine Italia S.R.L. | Catalyst components for the polymerization of olefins |
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|---|---|
| CN1036852C (en) | 1997-12-31 |
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