CN102816270B - High-melt-strength propylene/butene copolymer and preparation method thereof - Google Patents
High-melt-strength propylene/butene copolymer and preparation method thereof Download PDFInfo
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Abstract
The invention provides a method for preparing random high-melt-strength propylene/butene copolymer by direct polymerization. The method includes that during different serially operated polymerization reaction steps, according to requirements of different molecular grades, the propylene/butene copolymer with wide molecule distribution and 'overhigh molecular weight grade' propylene/butane copolymer can be prepared by controlling types and proportions of electron donor component in a Ziegler-Natta catalyst system in different reaction steps. Compared with homopolymer polypropylene, the prepared polymer is provided with better optical property and toughness and lower melting point, and compared with corresponding propylene/butene copolymer, extractable hexane content is reduced while the optical property of products is improved. The invention correspondingly provides random high-melt-strength propylene/butene copolymer. The propylene/butene copolymer is mainly utilized for producing forming products, bidirectionally oriented film, heat molding products and blow molding products in medical and sanitary fields.
Description
Technical field
The present invention relates to and a kind ofly prepare the method with high melt strength, propylene, be specifically related to a kind of preparation method of propylene/butene random copolymer.The invention still further relates to a kind of propylene/butene random copolymer with high fondant-strength.
Technical background
Obtain a wide range of applications in the manufacture fields such as the cutting out property of propylene polymer structures makes it in injection moulding, extrudes, curtain coating, two-way stretch, but common polypropylene molecule limits its application in fields such as thermoforming, foaming and blowings because melt strength is not high.Therefore, development has the polypropylene of high fondant-strength and good ductility, is the interested problems of people always.So-called high melt strength, propylene (HMSPP) just refers to melt under tension, can bear higher power during fracture.In the prior art, melt flow rate (MFR) MFR is the propene polymer of about 2g/10min, and its higher melt strength can reach 0.8-1N (newton).
The principal element affecting melt strength of polypropylene is the structure of polymer molecule, comprises the size of molecular weight, and whether molecular weight distribution and molecular chain contain the length of long-chain branch and long-chain branch and distribution etc.Usually, the molecular weight of propene polymer is larger, and its melt strength is larger; But molecular weight is larger, more unfavorable for polyacrylic post-treatment processability.Therefore, consider the practical application of material, making polypropylene have wider molecular weight distribution is needs; In addition, make to produce long branched chain structure in polypropylene molecular chain, also can improve polyacrylic melt strength.
In prior art, the method for conventional raising melt strength of polypropylene mainly contains: the methods such as reactive extrursion method, radiation modification method and modulation polymerization technique technology.Reactive extrursion method is by adding superoxide and other polyfunctional reactant monomers in polypropylene powder, forms polyacrylic crosslinked or long chain branching, thus improve polyacrylic melt strength by the technique of reactive extrursion.The principle of radiation modification selects suitable source of radiation and dose delivery polypropylene, caused, reach the object of grafting by irradiation, can directly linear chain be ruptured, shift and reconfigure, formation branching by irradiated polypropylene during irradiation; Also irradiation is carried out again after can adding polyfunctional monomer in polypropylene, between macromole, ligation is played after polyfunctional monomer is excited, thus formation branched structure, make to produce long branched chain structure in polypropylene molecular chain, thus improve polyacrylic melt strength.
And modulation polymerization technique technology is the method more commonly used, it is normally prepared broad molecular weight distribution polypropylene by multiple reactor or obtains long chain branched polypropylene with metallocene catalyst in-situ polymerization, thus improves the melt strength of final polymkeric substance.Wherein, adopt the reactor of multiple series connection to prepare broad molecular weight distribution polypropylene to commonly use the most, it is normally selecting different amounts of hydrogen, different comonomers, namely the polypropylene being obtained wide molecular weight distribution (MWD) in the different reactor of production differing molecular weight polymers by series polymerizations is conducive to, such as: wherein a kind of reactor is conducive to the polymkeric substance producing higher molecular weight, another kind of reactor is then conducive to the polymkeric substance producing lower molecular weight.
Such as, disclose a kind of method preparing the propene polymer with high fondant-strength and wide molecular weight distribution in US Patent No. 6875826 and US7365136, it is in the endless tube-gas-phase polymerization reactor of series connection, select a kind of Ziegler-Natta catalyst with lower hydrogen response, the maximum feature of this Ziegler-Natta catalyst is exactly need to adopt a kind of siloxanes containing cycloalkyl such as dicyclopentyl dimethoxyl silane as external electron donor, to carry out multistage (two reactors) propylene homo and close or copolymerization.By controlling the density of hydrogen of each reactor, the polypropylene (MFR < 0.1g/10min) of first stage production " high molecular weight block ", its weight content is 10-35%, subordinate phase produces the polypropylene (MFR > 0.5g/10min) of " low molecular weight fraction ", its weight content is the MFR=0.1-20g/10min of 65-90%, final polymkeric substance.Reaction finally obtains having wide molecular weight distribution (M
w/ M
n> 6), linear high fondant-strength alfon.
When adopt above-mentioned prepare the method for broad molecular weight distribution polypropylene by multiple reactor time, perfect condition makes the molecular weight of the high molecular weight block of decision mechanical properties of polymer and degree of isotacticity more high better, especially possesses a certain amount of " very high molecular weight block "; And determine that the molecular weight of " low molecular weight fraction " of polymer-extruded performance (processing characteristics) is more low better, and need to possess more content.For propylene polymerization, the kind of external electron donor can produce significantly impact to the taxis of polymkeric substance and molecular weight distribution usually; But the component of catalyzer and characteristic not change in two reactors in above-mentioned patent, therefore in the polyreaction in two stages, catalyzer is consistent for the reaction sensibility of molecular weight regulator (hydrogen), has certain limitation like this for the control of polymer chain characteristic or adjustment.
Specifically, when in catalyst system, use has the external electron donor of lower hydrogen response, as used dicyclopentyl dimethoxyl silane in patent US6875826, although the molecular weight of polymkeric substance can be made higher in the first stage of producing higher molecular weight fraction, but it is when producing the subordinate phase of lower molecular weight fraction, due to the insensitivity that external electron donor is adjusted hydrogen, then need high hydrogen content, just likely reach actual requirement.And if in catalyst system use have higher hydrogen adjust susceptibility external electron donor time, although hydrogen usage is less when producing the subordinate phase of lower molecular weight fraction, the polyacrylic extrusion performance of product is also easy to be met, but it is when producing the first stage of higher molecular weight fraction, it is enough large that molecular weight can not do, thus affect the mechanical property of the finished product.
Polypropylene resin composite described in patent CN1241196A and uses thereof, also uses two-stage method to obtain the polypropylene resin composite of high melting tension force; Wherein the first stage prepares the polypropylene of high molecular under no hydrogen condition, and second segment prepares low-molecular-weight polypropylene under hydrogen existence condition, uses identical external electron donor, as dicyclopentyl dimethoxyl silane in whole process; Preparation-obtained polypropylene can be greater than 1.5 × 10 containing molecular weight
6high molecular weight components.But it can not solve the adjoint problem of aforementioned patent US6875826 equally.
Although disclosed the method using the catalyzer of two kinds of different external electron donors in different steps in prior art, such as in patent CN1156999A " dual donor catalyst system for olefinic polymerization ", its first stage uses tetraethoxysilane to make external electron donor, and subordinate phase uses dicyclopentyl dimethoxyl silane to make external electron donor; Patent CN1612901A and US6686433B1 in addition similarly.Its processing step is all first prepare small molecules polypropylene, then at the more macromolecular polypropylene of subordinate phase preparation, thus obtain the polyolefine of high-crystallinity.If use method described in these patents to produce polypropylene, when the first stage prepares small molecules, this adjusts responsive higher external electron donor also will work in subordinate phase to hydrogen, thus cannot prepare supramolecular in subordinate phase.Equally, the propene polymer of the high fondant-strength with superior mechanical property and processing characteristics cannot also be obtained in these patents.
Summary of the invention
In order to solve prior art Problems existing, the invention provides a kind of direct polymerization legal system that adopts for the method for the propene/but-1-ene copolymer of high fondant-strength.
In the present invention, described " high fondant-strength " refers to that the melt strength of propene polymer is at more than 0.8N.
The present inventor is found by repetition test, in the different propylene polymerization stages of serial operation, according to the requirement of different molecular weight fraction, by controlling external electron donor component in Ziegler-Natta catalyst system in the kind in differential responses stage and ratio, the preferably control of binding molecule amount conditioning agent consumption, again in conjunction with the adjustment of comonomer butene add-on, can prepare and there is wide molecular weight distribution, and the propene/but-1-ene copolymer containing " very high molecular weight block " and a certain amount of " low molecular weight fraction ", this polymkeric substance has lower fusing point, good mechanical property and optical property, particularly there is lower hexane extractable and very high melt strength.
Propene/but-1-ene process for copolymerization of the present invention, is included in the reactor of plural serial operation, carries out the above propene/but-1-ene copolymerization of two benches, wherein:
First stage: under Ziegler-Natta catalyst exists, under the polymerization temperature of 50 ~ 100 DEG C, carry out the copolymerization of propene/but-1-ene, the MFR of resulting polymers controls as 0.01-0.3g/10min, and described Ziegler-Natta catalyst comprises the first external electron donor component; Subordinate phase: on the basis of first stage resultant of reaction, hydrogen adds the copolymerization that the second external electron donor component proceeds propene/but-1-ene under existing; The MFR of final polymkeric substance controls as 0.2-10g/10min; Wherein, described first external electron donor adjusts susceptibility low than the hydrogen of the second external electron donor; All add butylene in described each stage, the ratio of each stage butylene add-on is determined according to the duty ratio in each stage.
Preferably, in the first stage, Ziegler-Natta catalyst is composed of the following components: a kind of be main ingredient with magnesium, titanium, halogen and internal electron donor ingredient of solid catalyst A, a kind of organoaluminum B component, the first external electron donor component C; Ratio wherein between component A and B component counts 1: 10 ~ 500 (weight ratios) with titanium aluminum ratio; Ratio between B component and component C is 10 ~ 150: 1 (weight ratio); In subordinate phase, the ratio between organoaluminum component and the second external electron donor component of filling into is 1 ~ 50: 1 (weight ratio).
Preferably, for realizing the requirement to different molecular weight fraction, in first stage reaction, adjusting the consumption of the first external electron donor component, making itself and organoaluminum ratio be 1: 15 ~ 100 (weight ratios); In subordinate phase reaction, the amount of the organoaluminum component added by the first stage is determined, fills into the second external electron donor component, makes itself and organoaluminum ratio be 1: 2 ~ 20 (weight ratios).
The added hydrogen of first stage and subordinate phase controls with the requirement of final MFR.Preferably, in the first phase, hydrogen content is less than or equal to 300ppmV.
Wherein the first external electron donor component is as general formula R
1 nsi (OR
2)
4-nshown in, R in formula
1identical or different, be C
3-C
6branching or the aliphatic group of ring-type; R
2for C
1-C
3straight chain aliphatic, such as methyl, ethyl or propyl group; N is 1 or 2.Wherein the second external electron donor component is as general formula R
3 nsi (OR
4)
4-nshown in, in formula, n is 0 or 1 or 2, R
3and R
4for identical or different C
1-C
3straight chain aliphatic; Or as general formula be R
5r
6si (OR
7)
2shown in, R in general formula
7for C
1-C
3straight chain aliphatic, R
5for C
1-C
3straight chain aliphatic, R
6for C
3-C
6branching or the aliphatic group of ring-type.
Preferably wherein the first external electron donor is dicyclopentyl dimethoxyl silane and/or diisopropyl dimethoxy silane.Second external electron donor is tetraethoxysilane and/or Cyclohexylmethyldimethoxysilane.
In polymerisation process of the present invention, the catalyzer of propene/but-1-ene polymerization includes but are not limited to Ziegler-Natta catalyst.The Ziegler-Natta catalyst used is by open in a large number, preferably have the catalyzer of high stereoselective, the Ziegler-Natta catalyst of high stereoselective described herein refers to the catalyzer can prepared isotactic index and be greater than the propene polymer of 95%.This type of catalyzer, usually containing ingredient of solid catalyst A, is preferably the solid catalyst active ingredient of titaniferous; Organo-aluminium compound cocatalyst component B; External electron donor component C.
The operational this kind of specific examples containing active solid catalyst component A is disclosed in Chinese patent CN85100997, CN93102795.0, CN98126383.6, CN98111780.5, CN98126385.2, CN99125566.6, CN99125567.4, CN00109216.2, CN02100900.7.Described catalyzer can directly use, and also can add after pre-complexing and/or prepolymerization.Catalyzer described in Chinese patent CN85100997, CN93102795.0, CN98111780.5 and CN02100900.7, has advantage especially for high melt strength, propylene preparation method of the present invention.
Invention cocata lysts B component is organo-aluminium compound, preferred alkyl aluminum compound, more preferably trialkylaluminium, as: triethyl aluminum, triisobutyl aluminium, three n-butylaluminum etc., the wherein ratio of solids containing titanium catalyst component and organo-aluminium compound cocatalyst component, with Al/Ti mass ratio range for 10 ~ 500: 1.
According to the requirement to different molecular weight fraction, in different reactor, add the external electron donor with different qualities (different hydrogen response).Particularly, in first stage i.e. the first reactor, the present invention needs the propene polymer preparing high molecular weight block, and in order to make this fraction have higher molecular weight, have selected one and have lower hydrogen response external electron donor, it is as R
1 nsi (OR
2)
4-nshown in, R in formula
1identical or different, be C
3-C
6branching or the aliphatic group of ring-type, preferred R
1for cyclopentyl, sec.-propyl or cyclohexyl; R
2for C
1-C
3straight chain aliphatic, such as methyl, ethyl or propyl group; N is 1 or 2, is preferably 2.Particular compound is as dicyclopentyl dimethoxyl silane, diisopropyl dimethoxy silane, Dicyclohexyldimethoxysilane, second, isobutyl dimethoxy silane etc.Preferably wherein the first external electron donor is dicyclopentyl dimethoxyl silane and/or diisopropyl dimethoxy silane.
The MFR value of first stage resulting polymers controls at 0.01-0.3g/10min, according to actual needs, the hydrogen that usual selection does not add molecular weight regulator at the first reactor or adds minute quantity (being less than or equal to 300ppmV) makes molecular weight regulator, to obtain the fraction of high molecular.
On the basis of first stage polyreaction resultant, add the polyreaction that the second external electron donor component and molecular weight regulator (hydrogen) carry out subordinate phase, and the MFR value controlling final polymkeric substance controls as 0.2-10g/10min.
The general formula of the second external electron donor component is R
3 nsi (OR
4)
4-n, in formula, n is 0 or 1 or 2.R in general formula
3and R
4for identical or different C
1-C
3straight chain aliphatic, such as methyl, ethyl or propyl group; Specifically can include but are not limited to tetramethoxy-silicane, tetraethoxysilane, trimethylmethoxysilane, trimethylethoxysilane, dimethyldimethoxysil,ne, dimethyldiethoxysilane etc.The general formula of the second external electron donor component or be R
5r
6si (OR
7)
2, R in general formula
7for C
1-C
3straight chain aliphatic, R
5for C
1-C
3straight chain aliphatic, such as methyl, ethyl or propyl group, R
6for C
3-C
6branching or the aliphatic group of ring-type; Particular compound is as methylcyclohexyl dimethoxy silane.Wherein preferably the second external electron donor is tetraethoxysilane and/or Cyclohexylmethyldimethoxysilane.
The polyreaction of the different steps described in polymerization process of the present invention can be carried out respectively in different reactors.A concrete embodiment is: the polyreaction of first stage is carried out in the first reactor, and the polyreaction of subordinate phase is carried out in the second reactor.Add in the first reactor: a kind of be main ingredient with magnesium, titanium, halogen and internal electron donor ingredient of solid catalyst A, a kind of organoaluminum B component, the first external electron donor component C, under the condition of basic no hydrogen, carry out the copolymerization of propene/but-1-ene, gained polymerisate introduces the second reactor, add the second external electron donor component, under certain hydrogen exists, carry out the copolymerization of further propene/but-1-ene.
In the first reactor, three kinds of described catalyst components can directly join in the first reactor, after the pre-complexing also can known altogether through industry and/or prepolymerization, then join in the first reactor.Wherein the form of the reactor of pre-complex reaction can be various, its objective is and make catalyst components can obtain fully effective mixing, can be continuous stirred tank reactor, annular-pipe reactor, one section of pipeline containing static mixer, even also can be the pipeline that one section of material is in turbulence state.
The temperature-controllable of pre-complexing is between-10 ~ 60 DEG C, and preferred temperature is 0 ~ 30 DEG C.The time controling of pre-complexing is at 0.1 ~ 180min, and the preferred time is 5 ~ 30min.
Process or the catalyzer without pre-complexing can also carry out optionally prepolymerization process.Prepolymerization can be carried out continuously under liquid-phase bulk condition, also can carry out in inert solvent discontinuous.Pre-polymerization reactor can be continuous stirred tank, annular-pipe reactor etc.Prepolymerized temperature-controllable is between-10 ~ 60 DEG C, and preferred temperature is 0 ~ 40 DEG C.Prepolymerized multiple controls at 0.5 ~ 1000 times, and preferred multiple is 1.0 ~ 500 times.
Described polyreaction in propylene liquid phase, or can be carried out in the gas phase, or adopts liquid-gas combination technique to carry out.When carrying out liquid polymerization, polymerization temperature is 0 ~ 150 DEG C, with 40 ~ 100 DEG C as well; Polymerization pressure should higher than the saturated vapour pressure of propylene under corresponding polymerization temperature.When vapour phase polymerization, polymerization temperature is 0 ~ 150 DEG C, with 40 ~ 100 DEG C as well; Polymerization pressure can be normal pressure or higher, and preferred pressure is 1.0 ~ 3.0MPa (gauge pressure, lower same).
Polymerization can be carry out continuously, also may be carried out batchwise.Successive polymerization can be Liquid-phase reactor or the Gas-phase reactor of two or more series connection, Liquid-phase reactor can be annular-pipe reactor or stirred-tank reactor, Gas-phase reactor can be horizontal type agitated bed reactor or vertical mixing bed bioreactor or fluidized-bed reactor etc., and above Liquid-phase reactor and Gas-phase reactor also can at random matched combined.Propene/but-1-ene copolymerization of the present invention preferably carries out in the annular-pipe reactor of two or more series connection.
Resulting polymers of the present invention can use equipment to carry out extruding pelletization, usually adds the additive that this technical field uses, as oxidation inhibitor, photostabilizer, thermo-stabilizer, tinting material and filler etc. during granulation.
Propene/but-1-ene copolymerization of the present invention, preferably wherein the polypropylene productivity ratio of first stage and subordinate phase is 30: 70 ~ 70: 30, is more preferably 40: 60 ~ 60: 40.
Propene/but-1-ene copolymerization of the present invention, preferred described butylene adds in two stages, and wherein first stage butylene add-on is that butylene adds 60 ~ 40% of total amount, and subordinate phase butylene add-on is that butylene adds 40 ~ 60% of total amount.
In the preparation method of polymkeric substance of the present invention, when adding two reactors or the periodical operation of series connection by adjustment, the external electron donor consumption of different steps, kind and hydrogen and butylene add-on, do not need with special catalyst; Compare to the method adding hydrogen concentration adjustment molecular weight distribution in prior art by means of only difference, the present invention can use the hydrogen of less amount, namely more economical means high performance product can be prepared, propene/but-1-ene random copolymerization high melt strength, propylene optical property and toughness are all better than common homo-polypropylene, and fusing point is lower than common homo-polypropylene; While improving product optical property, hexane extractable (hexane extractable is proportional with xylene soluble content) is but obviously less compared with propylene/ethylene copolymer, mainly can be used for preparation medical treatment, health field foaming product, biaxially oriented film, articles thermoformed therefrom and blow-molded article.
Polymerization process of the present invention not only can obtain the propene polymer compared with wide molecular weight distribution, and its maximum feature is that " very high molecular weight block " content is higher, the content of " low molecular weight fraction " also can ensure to be greater than a certain amount of simultaneously, make the melt strength of gained propene polymer have like this to improve significantly, also assures that the processing characteristics that polymkeric substance is superior simultaneously.
A kind of preparation method with the multipolymer of the propene/but-1-ene of high fondant-strength that the present invention is concrete, it is characterized in that, in the annular-pipe reactor of two series connection, carry out two benches propene/but-1-ene copolymerization, wherein, first stage: under Ziegler-Natta catalyst exists, under the polymerization temperature of 50 ~ 100 DEG C, under hydrogen content is less than or equal to 300ppmV condition, carry out polyreaction, the MFR of resulting polymers controls as 0.01-0.3g/10min, described Ziegler-Natta catalyst is composed of the following components: a kind of with magnesium, titanium, halogen and internal electron donor are the ingredient of solid catalyst A of main ingredient, a kind of organoaluminum B component, dicyclopentyl dimethoxyl silane C, ratio wherein between component A and B component counts 1: 10 ~ 500 (weight ratios) with titanium aluminum ratio, the ratio of B component and component C is 10 ~ 150: 1 (weight ratio), subordinate phase: on the basis of first stage resultant of reaction, hydrogen adds tetraethoxysilane and proceeds propene/but-1-ene copolymerization under existing, the amount of the organoaluminum component added by the first stage is determined, fills into tetraethoxysilane, makes itself and organoaluminum ratio be 1: 1 ~ 50 (weight ratios), the MFR of final polymkeric substance controls as 0.2-10g/10min.
The present invention is also corresponding provides a kind of multipolymer with the propene/but-1-ene of high fondant-strength, and it has following feature:
A (), at 230 DEG C, MFR during load 2.16kg is 0.2-10g/10min;
(b) molecular weight distribution M
w/ M
n=6-20;
C content that () molecular weight is greater than 5,000,000 fractions is more than or equal to 0.8wt%;
(d) M
z+1/ M
nbe more than or equal to 70;
(e) butene content 0.1wt% ~ 15wt%.
In order to improve the melt strength of polymkeric substance, the molecular weight improving polymkeric substance is necessary, but in order to ensure that product has good processing characteristics (extrusion performance), in certain molecular-weight average (namely certain MFR) scope, the distribution controlling its molecular weight is very crucial.In this polymkeric substance, need that there is a certain amount of " very high-molecular weight polymer " fraction on the one hand, and on the other hand, need that again there is relatively large " low-molecular weight polymer " fraction, i.e. a kind of molecular weight distribution of relative broad range.
As everyone knows, polymer is not made up of the compound of unimodal molecular weight, even the polymer of a kind of " purely ", the mixture of the polymeric homologue that, molecular weight identical by chemical constitution is not etc. yet, structure is different formed.The characteristic of this high molecular molecular weight heterogeneity (i.e. molecular size range differ, uneven), is just called the polymolecularity of molecular weight.The high molecular molecular weight generally recorded is all molecular-weight average.The molecular-weight average of polymkeric substance is identical, but dispersiveness is not necessarily identical.Usually, people use gel permeation chromatograph to measure the molecular weight distribution of polymkeric substance, can obtain number-average molecular weight, weight-average molecular weight, Z-average molecular weight or (Z+1)-average molecular weight by molecular weight distribution curve.High molecular weight block, to the weighted of these Molecular weight Averages, is the trend increased successively, i.e. M
n< M
w< M
z< M
z+1.Usually, people adopt M
w/ M
nrepresent the molecular weight distribution of polymkeric substance, M
nnear the low-molecular-weight part of polymkeric substance, namely low molecular weight part is to M
naffect larger; M
wthe part of high molecular in polymkeric substance, namely high molecular weight moieties is to M
waffect larger.There is good over-all properties/processing characteristics, generally by the molecular weight distribution M of propene polymer to make polypropylene
w/ M
ncontrol within 6-20.
But the present inventor is found by repetition test, only control M
w/ M
nthese data, can not meet the demand that the present invention prepares high fondant-strength, also " very high-molecular weight polymer fraction " must be controlled just can reach object of the present invention quantitatively in certain scope.Particularly preferably " very high-molecular weight polymer fraction " and " low-molecular weight polymer fraction " is controlled all quantitatively in certain scope.Consider due to a small amount of " very high molecular weight block " not remarkably influenced M
w, but M can be affected significantly
z+1.And relatively large " low-molecular weight polymer fraction " is to M
nimpact is comparatively large, therefore, in propene polymer of the present invention, ensures M
z+1/ M
nit is very important for being more than or equal to 70.
In the multipolymer of the propene/but-1-ene of the invention described above, preferably, the fraction content that molecular weight is greater than 5,000,000 is more than or equal to 1.0wt%, more preferably, is more than or equal to 1.5wt%.Preferably, the content that molecular weight is less than the fraction of 50,000 is more than or equal to 15.0wt%, is less than or equal to 40wt%; More preferably be more than or equal to 17.5wt%, be less than or equal to 30%.M
z+1/ M
nbe preferably more than or equal 80.Butene content 0.5wt% ~ 10wt% in preferred copolymer.
Preferably, the multipolymer of this propene/but-1-ene is at 230 DEG C, and MFR during load 2.16kg is 1.6-6g/10min; More preferably its MFR is 2.5-6g/10min.
In addition, the present invention, by the control to each molecular weight fraction, can obtain the polymkeric substance that dispersion index PI is 6.0-20.0, is preferably 9.0-16.0.
Inventive polymers compared with prior art, has higher melt strength, is greater than 0.8 newton, even can more than 2.2 newton; Its optical property and toughness are better than common homo-polypropylene, and fusing point is lower than common homo-polypropylene; While improving product optical property, hexane extractable (hexane extractable is proportional with xylene soluble content) is but obviously less compared with propylene/ethylene copolymer, mainly can be used for preparation medical treatment, health field foaming product, biaxially oriented film, articles thermoformed therefrom and blow-molded article.
Embodiment
To be described the present invention by specific embodiment below, but it is only explain instead of limit the present invention.
In embodiment, polymkeric substance relevant data obtains by following testing method:
1) detection of heat-drawn wire: detect according to ASTM D648-07.
2) melt strength: adopt the Rheoten melt strength instrument that German Geottfert Werkstoff Pruefmaschinen company produces.This instrument comprises the contrary roller of a pair sense of rotation, polymkeric substance is after single screw extrusion machine fusion plastification, the circular hole die turned to through 90 ° is again extruded, being clamped in employing between two rollers waits acceleration accelerated manner by uniaxial extension, drawing force measures by measure force element, to the maximal force recorded during melt fracture and so-called melt strength from stretching.
3) melt flow rate (MFR) (MFR) is by ISO1133,230 DEG C, measures under 2.16kg load.
4) molecular weight polydispersity index PI: with U.S. Rheometric Scientific Inc sell model be that the rheometer of ARES (senior rheometer expanding system) is at 190 DEG C, the viscosity of certain frequency scope working sample and modulus value, the pattern of sample clamp is flat.Molecular weight polydispersity index PI=10
5/ G, G are " storage modulus (G ') frequency curve " and " out-of-phase modulus (G ")-frequency curve " modulus value of point of intersection.Before test, resin sample is molded into the thin slice of 2mm at 200 DEG C.
5) molecular weight distribution (M
w/ M
n, M
z+1/ M
n): adopt Polymer Laboratories company of Britain to produce molecular weight and the molecular weight distribution of the IR5 detector coupling working sample of PL-GPC 220 gel permeation chromatograph and Polymer Char company of Spain product, chromatographic column is 3 series connection Plgel, 10 μm of MIXED-B posts, solvent and moving phase are 1,2,4-trichlorobenzene is (containing 0.3g/1000ml oxidation inhibitor 2,6-dibutyl paracresol), column temperature 150 DEG C, flow velocity 1.0ml/min.
6) resin stretched intensity is pressed ASTM D638-00 and is measured.
7) resin modulus in flexure is pressed ASTM D790-97 and is measured.
8) IZOD notched Izod impact strength is pressed ASTM D256-00 and is measured.
9) intrinsic viscosity: the Y501C intrinsic viscosity analyser adopting VISCOTEK company of the U.S., measures by ASTM D 5225-1998 method.Solvent is perhydronaphthalene, probe temperature 135 DEG C.
10) solubles content: adopt the CRYSTEX instrument of PolyChar company of Spain to record, solvent is trichlorobenzene.Its result cold xylene solvend Data correction of the polymkeric substance recorded according to ASTM D5492-2006 standard.
11) butene content: the butene content on Nicdet Magna-IR760 in working sample, is put in sample between two KBr salt sheets, warms, be pressed into film, measure under normal temperature under being placed in infrared lamp.Characteristic peak optical density(OD) is obtained by baseline method.With 1gA1152/A723 the propylene that nuclear-magnetism obtains divided and mole be compared to figure, obtain quantitation curves: 1g A
1152/ A
721=0.0212C
3-1.1121, utilize this equation, infrared analysis is carried out to sample, just can carry out quantitatively the segment composition of multipolymer.
12) fusing point: measure by DSC method, polyacrylic dsc analysis carries out on Perkin-ElmerDSC-7, first the polypropylene specimen of about 5mg is raised to 200 DEG C with the speed of 10 DEG C/min, maintain 5min, eliminate thermal history, then drop to 50 DEG C with identical speed, record Tc Tc, be warmed up to 200 DEG C with 10 DEG C/min speed again, record fusing point Tm.
13) mist degree: test according to GB 2410 method.
14) hexane extractable: test according to GB/T 5009.58-2003 method.
Embodiment 1:
Polyreaction is carried out on a set of polypropylene pilot plant.Its major equipment comprises prepolymerization reactor, first ring pipe reactor and the second annular-pipe reactor.Polymerization process and step as follows:
(1) prepolymerization:
Primary Catalysts (the solid catalyst active ingredient of titaniferous) adopts the method that in Chinese patent CN93102795, embodiment 1 describes to obtain, its Ti content: 2.4wt%, Mg content 18.0wt%, n-butyl phthalate content: 13wt%.
Primary Catalysts, promotor (triethyl aluminum), the first external electron donor (dicyclopentyl dimethoxyl silane, DCPMS) through 10 DEG C, after 20min pre-contact, add prepolymerization reactor continuously and carry out prepolymerization, prepolymerization is carried out under propylene liquid-phase bulk environment, temperature is 15 DEG C, the residence time is about 4min, and under this condition, the pre-polymerization multiple of catalyzer is about 120-150 times.The triethyl aluminum flow entering prepolymerization reactor is 6.33g/hr, and bicyclopentyl dimethoxy silane flow is 0.33g/hr, and Primary Catalysts flow is about 0.5g/hr.
(2) copolymerization of propene/but-1-ene:
Pre-polymerization rear catalyst enters in the annular-pipe reactor of two series connection, completes the copolymerization of propene/but-1-ene in annular-pipe reactor.Wherein the butylene add-on of the first endless tube is 5mol%, and the butylene add-on of the second endless tube is 4mol%.Two loop po lymerisation temperature of reaction 70 DEG C, reaction pressure 4.0MPa.The processing condition of gate ring pipe reactor, make the productivity ratio of first, second endless tube be about 45: 55.
Not hydrogenation in the charging of first ring pipe reactor, the density of hydrogen < 10ppmV that on-line chromatograph detects, adds a certain amount of hydrogen in the second annular-pipe reactor charging, and the density of hydrogen that on-line chromatograph detects is 4500ppmV.
Because these catalyst components directly enter first ring pipe reactor after prepolymerization, first ring pipe reactor no longer includes other charging any except propylene and butylene, therefore, in first ring pipe reactor, triethyl aluminum/dicyclopentyl dimethoxyl silane (Al/Si-I) is 19.0 (weight ratios) than the ratio be in catalyst prepolymer.
In the second annular-pipe reactor, add the tetraethoxysilane (TEOS) into 0.67g/hr, therefore, in the second annular-pipe reactor, triethyl aluminum/tetraethoxysilane (Al/Si-II) is than being 9.4 (weight ratios).Concrete technology condition is in table 1.
Go out after propylene and butylene from the second endless tube polymkeric substance out through flash separation, remove the activity of catalyst in reactor through wet nitrogen, polymkeric substance, through heat drying, obtains polymer powders.
Is added IRGAFOS 168 additive of 0.1wt%, IRGANOX 1010 additive of 0.2wt% and the calcium stearate of 0.05wt% in the powder that polymerization is obtained, use twin screw extruder granulation.Gained pellet is carried out performance test by existing relevant ASTM standard.
Embodiment 2:
With embodiment 1, just become 25mol% in the butylene add-on of first ring pipe reactor; The butylene add-on of the second annular-pipe reactor is adjusted to 20mol%; Meanwhile, the amounts of hydrogen in the second annular-pipe reactor is adjusted to 8500ppmv.
Comparative example 1:
With embodiment 2, just Al/Si is adjusted to 10; Second reactor no longer adds external electron donor; The hydrogen feed concentration of the second annular-pipe reactor is adjusted to 10000ppmv.
The concrete technology parameter of each embodiment and comparative example, resulting polymers analytical results and polymer physics performance list in table 1 ~ 4.
Table 1. embodiment polymerization process condition
Table 2. embodiment polymers analysis results (1)
Table 3. embodiment polymers analysis results (2)
In table: F280z is the polypropylene that China petroleum Chemicals Co., Ltd. Town Hai Lian Hua branched Corporation produces
Table 4. embodiment polymer physics performance
Data from form, comparative example 1 does not add the high external electron donor of a hydrogen response in subordinate phase reaction, its polypropylene product small molecular amount is inadequate, and the melting index of product is low, and extrusion performance (processing characteristics) is very poor and limit its use.
In addition, in actual production, the density of hydrogen (10000ppm) that in comparative example 1, subordinate phase uses reaches capacity high level substantially; Under non-critical operational condition, in reactor, hydrogen can not infinitely increase, when density of hydrogen is greater than 10000ppm, not only can cause damage to appliance arrangement, in subsequent propylene, hydrogen removes also very difficult, finally, follow and cause density of hydrogen in the first reactor uncontrollable at low level with carrying hydrogen in propylene.Therefore, propene polymer can not be made to meet the particular product performance parameters described in the present invention by controlling merely density of hydrogen.
Claims (6)
1. a preparation method for the propene/but-1-ene copolymer of high fondant-strength, is characterized in that, in the reactor of plural serial operation, carries out the propene/but-1-ene copolymerization of more than two benches, wherein:
First stage: under Ziegler-Natta catalyst exists, under the polymerization temperature of 50 ~ 100 DEG C, carry out propene/but-1-ene copolymerization, the MFR of resulting polymers controls as 0.01-0.3g/10min, and described Ziegler-Natta catalyst comprises the first external electron donor component;
Subordinate phase: on the basis of first stage resultant of reaction, hydrogen adds the second external electron donor component and proceeds propene/but-1-ene copolymerization under existing;
The MFR of final polymkeric substance controls as 0.2-10g/10min;
Wherein, the first external electron donor is dicyclopentyl dimethoxyl silane and/or diisopropyl dimethoxy silane, and the second external electron donor is tetraethoxysilane and/or Cyclohexylmethyldimethoxysilane;
All add butylene in each stage, the ratio of each stage butylene add-on is determined according to the load in each stage;
In first stage, Ziegler-Natta catalyst is composed of the following components: a kind of be main ingredient with magnesium, titanium, halogen and internal electron donor ingredient of solid catalyst A, a kind of organoaluminum B component, the first external electron donor component C; Ratio wherein between component A and B component counts 1:10 ~ 500 (weight ratio) with titanium aluminum ratio; Ratio between B component and component C is 10 ~ 150:1 (weight ratio); In subordinate phase, the ratio between organoaluminum component and the second external electron donor component of filling into is 1 ~ 50:1 (weight ratio);
In the first phase, hydrogen content is less than or equal to 300ppmV;
MFR presses ISO1133,230 DEG C, measures under 2.16kg load.
2. preparation method according to claim 1, in the first stage, adjusts the consumption of the first external electron donor component, makes itself and organoaluminum ratio be 1:15 ~ 100 (weight ratios); In subordinate phase, the amount of the organoaluminum component added by the first stage is determined, fills into the second external electron donor component, makes itself and organoaluminum ratio be 1:2 ~ 20 (weight ratios).
3. preparation method according to claim 1, wherein the productivity ratio of first stage and subordinate phase is 30:70 ~ 70:30.
4. preparation method as claimed in any of claims 1 to 3, wherein, described butylene adds in two stages, and first stage butylene add-on is that butylene adds 60 ~ 40% of total amount, and subordinate phase butylene add-on is that butylene adds 40 ~ 60% of total amount.
5. utilize the propene/but-1-ene copolymer that preparation method as claimed in any of claims 1 to 4 makes, it has following characteristics:
A (), at 230 DEG C, MFR during load 2.16kg is 0.2-10g/10min;
(b) molecular weight distribution M
w/ M
n=6-20;
C content that () molecular weight is greater than 5,000,000 fractions is more than or equal to 0.8wt%;
(d) M
z+1/ M
nbe more than or equal to 70;
E () butene content is 0.1wt% ~ 15wt%.
6. propene/but-1-ene copolymer according to claim 5, it has following characteristics:
A (), at 230 DEG C, MFR during load 2.16kg is 1.6-6g/10min;
(b) molecular weight distribution M
w/ M
n=6-20;
C content that () molecular weight is greater than 5,000,000 fractions is more than or equal to 1.0wt%;
(d) M
z+1/ M
nbe more than or equal to 80;
E () butene content is 0.5wt% ~ 10wt%;
F content that () molecular weight is less than 50,000 fractions is more than or equal to 17.5wt%, is less than or equal to 30%;
G the dispersion index PI of () polymkeric substance is 9.0-16.0.
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| CN105622809B (en) * | 2014-10-31 | 2019-03-22 | 中国石油化工股份有限公司 | A kind of preparation method of the impact polypropylene of low VOC content |
| CN106674721B (en) * | 2015-11-06 | 2019-08-20 | 中国石油化工股份有限公司 | A kind of high fondant-strength impact polypropylene expanded bead and preparation method thereof |
| CN108659150B (en) * | 2017-03-30 | 2020-01-10 | 中国科学院化学研究所 | Application of organosilane, polypropylene and preparation method of polypropylene |
| CN108659151B (en) * | 2017-03-30 | 2020-01-10 | 中国科学院化学研究所 | Application of organosilane, polypropylene and preparation method of polypropylene |
| CN108164624B (en) * | 2017-11-24 | 2020-06-16 | 新疆天利高新石化股份有限公司 | Method for preparing propylene-butylene copolymer with high butylene content in situ by aid of nano powder |
| CN108484810B (en) * | 2018-05-04 | 2020-08-21 | 江苏煦和新材料有限公司 | Method for preparing high-melt-strength polypropylene |
| KR20240038800A (en) | 2021-08-04 | 2024-03-25 | 차이나 페트로리움 앤드 케미컬 코포레이션 | Flexible polypropylene modified insulating material, manufacturing method and application thereof |
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| CN1091748A (en) * | 1993-03-29 | 1994-09-07 | 中国石油化工总公司 | The spherical catalyst of for olefines polymerization |
| CN102020733A (en) * | 2009-09-10 | 2011-04-20 | 中国石油化工股份有限公司 | Multiphase copolymerization polypropylene production process |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1091748A (en) * | 1993-03-29 | 1994-09-07 | 中国石油化工总公司 | The spherical catalyst of for olefines polymerization |
| CN102020733A (en) * | 2009-09-10 | 2011-04-20 | 中国石油化工股份有限公司 | Multiphase copolymerization polypropylene production process |
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