阅读说明：本技术 聚丙烯的制备工艺 (Preparation process of polypropylene ) 是由 D·布丽塔 于 2020-04-01 设计创作，主要内容包括：本发明提供了一种用于制备含有着色剂的丙烯聚合物的工艺,包括：(i)形成(a)ZN催化剂组分和(b)着色剂的固体混合物(a/b),ZN催化剂组分包括Mg、Ti、卤素和内电子给体化合物,着色剂包括至少一种颜料；混合物的重量比(b)∶(a)为0.01∶1至0.4∶1；(ii)将混合物a/b进料到聚合反应器中并使反应器经受聚合条件以产生丙烯聚合物。如果b∶a的重量比和在聚合中混合物形成和使用之间经过和天数符合所提供的指导,则可以获得具有令人满意的产率和良好的光学和化学性质的聚合物。(The present invention provides a process for preparing a propylene polymer containing a colorant comprising: (i) forming a solid mixture (a/b) of (a) a ZN catalyst component comprising Mg, Ti, halogen and an internal electron donor compound and (b) a colourant, the colourant comprising at least one pigment; the weight ratio of the mixture (b) to the mixture (a) is 0.01: 1 to 0.4: 1; (ii) the mixture a/b is fed to a polymerization reactor and the reactor is subjected to polymerization conditions to produce a propylene polymer. If the weight ratio of b: a and the passage and number of days between the formation and use of the mixture in the polymerization correspond to the guidelines provided, polymers having satisfactory yields and good optical and chemical properties can be obtained.)

1. A process for preparing a colorant-containing propylene polymer comprising:

(i) forming a solid dry mixture (a-b) of (a) a ZN catalyst component comprising Mg, Ti, halogen and an internal electron donor compound, and (b) a colorant comprising at least one pigment; the weight ratio of the mixture (b) to the mixture (a) is 0.01: 1 to 0.4: 1;

(ii) feeding the mixture (a-b) to a polymerization reactor and subjecting the reactor to polymerization conditions to produce the propylene polymer,

the process is characterized in that the b: a weight ratio and the time in days elapsed between the formation and the use of the mixture in the polymerization fall from the equation y of 3+0.832x^-1，17Below the curve defined, where y is the time in days elapsed between formation and use of the mixture in the polymerization, and x is the weight ratio of (b) to (a).

2. The process according to claim 1, wherein the ZN catalyst has a spherical regular morphology and is prepared by reacting Ti halide with MgCl comprising the formula₂(R¹OH)_nWherein R is C₁-C₈Alkyl, and n is 2 to 6.

3. The process according to claim 1, wherein in the ZN catalyst component the amount of Mg is in the range of 8 to 30 wt% and the amount of Ti is in the range of 0.5 to 8 wt% relative to the total weight of solid catalyst component.

4. A process according to claim 3, wherein the electron donor compound is selected from esters, ethers, amines, silanes, carbamates and ketones or mixtures thereof.

5. Process according to claim 4, in which the electron donor compound is chosen from 1, 3-diethers of formula (I)

Wherein R is^IAnd R^IIStraight-chain or different and hydrogen or also forming one or more cyclic structuresBranched chain C₁-C₁₈A hydrocarbyl group; r^IIIThe radicals, equal to or different from each other, being hydrogen or C₁-C₁₈A hydrocarbyl group; r^IVThe radicals, equal to or different from each other, having the same general formula as R^IIIThe same meaning, except that it cannot be hydrogen; r^ITo R^IVEach of the groups may contain a heteroatom selected from halogen, N, O, S, and Si.

6. Process according to claim 4, wherein the final amount of electron donor compound in the solid catalyst component may be from 0.5 to 30 wt%.

7. The process of claim 1, wherein the pigment is black or blue.

8. The process according to claim 7, wherein the pigment is organic and is selected from copper phthalocyanines.

9. The process of claim 7, wherein the pigment is inorganic and is selected from ultramarine and carbon black.

10. The process of claim 1, wherein the colorant (b) is used in an amount such that the weight ratio (b) to (a) ranges from 0.01: 1 to 0.30: 1.

11. The process of claim 10, wherein the colorant is used in an amount such that the weight ratio (b) to (a) ranges from 0.01: 1 to 0.20: 1.

12. The process according to claim 1, wherein the solid dry mixture is prepared using a closed apparatus equipped with an internal rotating tool, or by using a closed rotating tool in which components a) and b) are mixed without using a liquid medium.

13. The process according to claim 1, wherein the mixture (a-b) is fed to a polymerization reactor together with an alkyl-Al compound selected from the trialkyl aluminum compounds and optionally an external electron donor compound.

14. The process according to claim 13, wherein the external donor is present and is selected from formula R_a ⁵R_b ⁶Si(OR⁷)_cWherein a and b are integers of 0 to 2, c is an integer of 1 to 3 and the sum of (a + b + c) is 4; r⁵、R⁶And R⁷Is an alkyl, cycloalkyl or aryl group having 1 to 18 carbon atoms, optionally containing heteroatoms.

15. The process according to claim 1, wherein the amount of colorant in the final propylene polymer is from 0.3 to 10 ppm.

Technical Field

The present invention relates to a polymerization process for preparing propylene polymers containing colored compounds. The polymer thus obtained has an optimal visual appearance.

Background

Polyolefins such as polypropylene can be prepared into articles that can be made attractive by using so-called additive packages. In addition to conventional stabilizers, the package may include clarifying agents for increasing clarity and coloring agents for imparting more or less intense color.

The additives described above may be added in the form of an "additive-package" pre-blend, which may also contain one or more of the following: an antioxidant; acid scavengers, slip agents, light stabilizers, optical brighteners and UV light absorbers.

Sometimes, the colorant (which may be in the form of a masterbatch premixed with the polymer) is added during or just prior to the forming process. Relatively high colorant loadings of 500-1000 parts per million (ppm) can be mixed and well dispersed into the plastic in this manner. The traditional process is to make bright-colored plastic articles of everyday use with a high degree of color.

It is more difficult to adequately disperse the additive into the plastic or polymer at very low additive concentration levels. For example, the additive can be dispersed into the polymer at very low loading levels by several steps of serial dilution. Thus, the application of additives in the range of a few ppm involves discrete steps, which are necessarily time consuming in polymer manufacturing applications.

On the other hand, the addition of small amounts of colorants to polyolefins, especially to propylene polymers, can improve visual appearance. EP 1989252 describes a process for dispersing small amounts of a colorant into a polymer, in particular polypropylene, which process comprises forming a first blend between the colorant and a clarifying agent. The first blend thus obtained is then added to the molten polymer, possibly together with additional stabilizers, and then extruded.

Although the dispersion results may be good, this method has the problem of requiring an additional mixing stage, and the fact that a clarifying agent needs to be used even if the optical properties are not strictly required.

Us patent 10,030,121 describes a process for the preparation of UHMWPE, wherein a pigment pre-dispersed in a slurry is mixed with a ZN catalyst and the mixture thus obtained is contacted with ethylene to polymerize it. The pigment is used in an amount such that its final amount in the polymer is in the range of 50ppm to 5000 ppm. This technique may have several disadvantages. For example, if not used immediately after their preparation, the suspensions must be stored and effective and burdensome measures must be taken due to the flammability of the hydrocarbon diluents. In addition, when the catalyst is to be fed to the reactor in dry form, a further stage of diluent removal is required.

US 2016/289422 describes forming a catalyst by combining a catalyst precursor mixture with a colorant mixture and immediately injecting the resulting product n into the I polymerization reactor.

Although small amounts of colorant can be dispersed in this manner, it introduces the problem of new and unknown catalyst aging characteristics derived from the presence of the colorant. This will seriously affect the possible commercial use of the colorant/catalyst mixture, since it is common industrial practice to store the catalyst for widely varying periods of time before use. Once used after the storage time, the catalyst performance and therefore the polymerization process will no longer be reliable.

Therefore, there is a need for a method of effectively dispersing a small amount of a colorant into a propylene polymer in a manner that does not burden the polymer processing and does not deteriorate the catalyst performance while maintaining smooth handling and reliability of the entire polymerization process.

Disclosure of Invention

The present invention provides a process for preparing a propylene polymer containing a colorant comprising:

(i) forming a solid mixture (a-b) of (a) a ZN catalyst component comprising Mg, Ti, halogen and an internal electron donor compound and (b) a colourant, the colourant comprising at least one pigment; weight ratio of mixture (b): (a) from 0.01: 1 to 0.4: 1;

(ii) feeding the mixture (a-b) to a polymerization reactor and subjecting the reactor to polymerization conditions to produce a propylene polymer,

the process is characterized in that the b: a weight ratio and the time in days elapsed between the formation and the use of the mixture in the polymerization fall within the range defined by the equation y 3+0.832x^-1，17Below the defined curve, wherein y is the time in days elapsed between formation and use of the mixture in the polymerization, and x is (b): (a) the weight ratio.

ZN solid catalyst component a) may have a granular, spherical, irregular or spherical regular morphology. Preferably, it has a spherical regular morphology.

Granular or other irregular catalyst particles can be produced by reacting Ti halide with a catalyst of the formula MgX_n(OR)_2-nWherein X is Cl or C₁-C₁₀A hydrocarbon group, R is C₁-C₈Alkyl and n is 0 to 2. This reaction produces MgCl consisting essentially of a Ti compound immobilized thereon₂Solid particles of composition.

Catalyst components having regular morphology can be prepared by reacting Ti halides with MgCl of the formula₂(R¹OH)_nWherein R is C₁-C₈Alkyl, preferably ethyl, and n is 2 to 6.

Preferably, the amount of Mg in the solid catalyst component is from 8 to 30 wt%, more preferably from 10 to 25 wt%, relative to the total weight of the solid catalyst component.

Preferably, the amount of Ti is from 0.5 to 8 wt%, more preferably from 0.7 to 5 wt%, in particular from 1 to 3.5 wt%, relative to the total weight of the solid catalyst component.

The titanium atom preferably belongs to the formula Ti (OR2)_nX_4-nWherein n is 0 to 4; x is halogen, R²Is a hydrocarbon group having 1 to 10 carbon atoms, preferably an alkyl group. Among them, particularly preferred are titanium compounds having at least one Ti-halogen bond, such as titanium tetrahalides or haloalcoholates. A preferred specific titanium compound is TiCl₄And Ti (OEt) Cl₃。

The catalyst component also comprises an electron donor compound (internal donor). Preferably, it is selected from esters, ethers, amines, silanes, carbamates and ketones or mixtures thereof.

The internal donor is preferably selected from alkyl and aryl esters of optionally substituted aromatic mono-or polycarboxylic acids, for example esters of benzoic and phthalic acid, and esters of aliphatic acids selected from malonic, glutaric, maleic and succinic acid. Specific examples of such esters are n-butyl phthalate, diisobutyl phthalate, di-n-octyl phthalate, ethyl benzoate and p-ethoxyethyl benzoate. Furthermore, diesters as disclosed in WO 2010/078494 and US 7,388,061 may be used. Of this class, 2, 4-pentanediol dibenzoate derivatives and 3-methyl-5-tert-butylcatechol dibenzoate are particularly preferred. Furthermore, the internal donor may be selected from diol derivatives selected from the group consisting of dicarbamates, monoester monocarbamates and monocarbonate monoesters. Furthermore, 1, 3 diethers of formula:

r, R therein^I、R^II、R^III、R^IVAnd R^VAre identical or different from one another, are hydrogen or a hydrocarbon radical having 1 to 18 carbon atoms, and R^VIAnd R^VIIAre the same or different from each other, have the same general formula as R-R^VThe same meaning, except that they cannot be hydrogen; R-R^VIIOne or more of the groups may be linked to form a ring. Particularly preferred is the compound wherein R^VIAnd R^VIIIs selected from C₁-C₄1, 3-diethers of alkyl groups.

Mixtures of the above donors may also be used. Specific mixtures are those composed of esters of succinic acid and 1, 3-diethers, as disclosed in WO 2011/061134.

In general, the final amount of electron donor compound in the solid catalyst component may be from 0.5 to 30% by weight, preferably from 1 to 20% by weight.

The preparation of the solid catalyst component is carried out according to several methods. One method comprises the preparation of a magnesium or chlorohydrin at a temperature of about 80 ℃ to 120 ℃ in the presence of an electron donor compound (particularly according to U.S. patent No.)4,220,554 prepared chlorohydrate) with an excess of TiCl₄The reaction between them.

According to a preferred method, the solid catalyst component may be prepared by reacting a compound of formula Ti (OR)²) m-yXy, where m is the valence of titanium, y is a number from 1 to m, and R²Having the same meaning as previously specified, preferably TiCl₄Wherein the magnesium chloride is derived from MgCl₂·pR³Adducts of OH, wherein p is a number from 0.1 to 6, preferably from 2 to 3.5, R³Is a hydrocarbon group having 1 to 18 carbon atoms. The adduct may suitably be prepared in spherical form by mixing the alcohol and the magnesium chloride in the presence of an inert hydrocarbon immiscible with the adduct, operating at the melting temperature of the adduct (100 to 130 ℃) under stirring conditions. The emulsion is then rapidly quenched, causing the solidification of the adduct in the form of spherical particles. Examples of spherical adducts prepared according to this method are described in U.S. Pat. No.4,399,054 and U.S. Pat. No.4,469,648. The adduct thus obtained can be directly reacted with the Ti compound or it can be previously submitted to a thermal controlled dealcoholation (at a temperature ranging from about 80 to 130 ℃) to obtain an adduct in which the number of moles of alcohol is lower than 3, preferably from 0.1 to 2.5. The reaction with the Ti compound can be carried out by suspending the adduct (dealcoholated or as such) in cold TiCl₄(about 0 ℃) in a reaction vessel; the mixture is then heated at 80 to 130 ℃ and held at this temperature for 0.5 to 2 hours. With TiCl₄The treatment of (c) may be performed one or more times. The electron-donor compound is preferably used in TiCl₄Added during the treatment. The preparation of spherical catalyst components is described, for example, in European patent applications EP-A-395083, EP-A-553805, EP-A-553806, EPA 601525 and WIPO patent application publication WO 98/44009.

The colorant b) comprises at least one pigment. In some embodiments, the colorant may be a mixture containing a dye. In further embodiments, the colorant may include a dye in combination with one or more pigments.

The pigments may be organic or inorganic. The organic pigments according to the invention contain at least one C-H bond in their structure. In contrast, inorganic pigments are pigments that do not contain a C-H bond in their structure.

Preferably, the pigments used according to the invention have a black or blue colour.

Preferred pigments are those based on carbon Black, such as carbon Black (Cabot Black), phthalocyanine metal derivatives such as copper phthalocyanine, ultramarine (inorganic) and quinacridone based pigments. Among them, copper phthalocyanine is particularly preferable.

Preferably, the amount of colorant used in step (i) is such that the weight ratio colorant b)/catalyst component a) is from 0.01: 1 to 0.30: 1, more preferably from 0.01: 1 to 0.25: 1, especially from 0.01: 1 to 0.20: 1.

The solid catalyst component a) and the colorant b) can be mixed using available techniques for mixing solids, taking care to prevent the components from coming into contact with contaminants such as oxygen and water.

Typically, solid dry mixtures can be prepared using a closed apparatus equipped with an internal rotating means, such as a mechanical stirrer, or by using a closed rotating means in which components a) and b) are mixed without the use of a liquid medium.

The mixing time may be 5 minutes to 24 hours, preferably 30 minutes to 4 hours. The temperature at which mixing takes place may be in a range such that the mixing temperature is not close to the melting or degradation point of the solids a) and b) -in particular, the mixing temperature may suitably be in the range of 0 to 80 ℃. Preferably, the mixing is carried out at room temperature (about 23 ℃ to about 25 ℃).

After mixing, the solid mixture can be used immediately for polymerization, or it can be stored for a period of time corresponding to the equation y 3+0.832x^-1，17Wherein y is the time in days elapsed between formation and use of the mixture in the polymerization, and x is (b): (a) the weight ratio.

In one embodiment of the invention, the process is carried out as follows: in step (i), the weight ratio (b): (a) is in the range of from 0.01: 1 to 0.25: 1, and in step (ii), the mixture (a-b) is fed to the polymerization reactor over a maximum number of days of from 7 to 65.

In general, the activity of the solid catalyst mixture (a-b), expressed as Kg of polymer per g of feed mixture, is lower than that of the component (a) alone, and can range from 30 to 100 Kg of polymer per g of catalyst. This is due at least in part to the thinning effect provided by the pigment. Therefore, to take this effect into account, the polymerization activity of the solid mixture always refers to the amount of component (a) of the mixture. However, it is also clear that the colorant may lead to accelerated aging of the catalyst. In particular, it has been noted that if the time elapsed from preparation to use exceeds the value given by the equation for a given weight ratio, the catalyst performance decreases to such an extent that the catalyst activity becomes too low and the plant productivity is affected. Preferably, the propylene polymer of the present invention is characterized in that the amount of colorant is from 0.2 to 15ppm, preferably from 0.3 to 10ppm, in particular from 0.3 to 8ppm, relative to the weight of the propylene polymer. These propylene polymers may allow the production of objects with improved visual appearance. This is shown by the fact that: the yellowness index of the polymer is reduced relative to a polymer without the colorant. If the catalyst provides unexpectedly too low a polymerization activity, the final amount of colorant may become too high, imparting too significant coloration to the polymer. In this case, the final object may not exhibit the desired visual appearance. However, taking into account the guidance given by the above equation ensures that the catalyst activity is maintained at a satisfactory level to give a suitable final amount of colorant, while maintaining interesting values of polymer properties such as stereoregularity (measured by xylene insolubility) and bulk density (which is directly related to polymer morphology).

The solid mixture of the invention is used in polymerization together with an alkylaluminum cocatalyst and optionally an external electron donor compound.

The alkylaluminum compound is preferably chosen among the trialkylaluminum compounds such as, for example, triethylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum. It is also possible to use trialkylaluminums with alkylaluminum halides, alkylaluminum hydrides or alkylaluminum sesquichlorides such as AlEt₂Cl and Al₂Et₃Cl₃A mixture of (a).

Preferred external electron-donor compounds comprise silicon compounds, ethers, esters, such as ethyl 4-ethoxybenzoate, amines, heterocyclic compounds, in particular 2, 2, 6, 6-tetramethylpiperidine, ketonesAnd 1, 3-diethers. Another preferred class of external donor compounds is that of the formula R_a ⁵R_b ⁶Si(OR⁷)_cWherein a and b are integers of 0 to 2, c is an integer of 1 to 3, and the sum of (a + b + c) is 4; r⁵、R⁶And R⁷Is an alkyl, cycloalkyl or aryl group having 1 to 18 carbon atoms optionally containing heteroatoms. Particularly preferred are methylcyclohexyldimethoxysilane, diphenyldimethoxysilane, methyl-tert-butyldimethoxysilane, dicyclopentyldimethoxysilane, 2-ethylpiperidinyl-2-tert-butyldimethoxysilane and 1, 1, 1, -trifluoropropyl-2-ethylpiperidinyl-dimethoxysilane (1, 1, 1, trifluropropyl-2-ethylpiperidinyl-dimethoxysilane) and 1, 1, 1, -trifluoropropyl-methyldimethoxysilane (1, 1, 1, trifluropropyl-methyl-dimethoxysilane). The external electron donor compound is used in such an amount that the molar ratio between the organoaluminium compound and said electron donor compound is between 5 and 500; preferably 7 to 400; and more preferably 10 to 200.

Optionally, a prepolymerization step may be carried out before the main polymerization step. The prepolymerization step can be carried out in a first reactor selected from a loop reactor or a continuous stirred tank reactor. The prepolymerization can be carried out in the gas phase or in the liquid phase. Preferably in the liquid phase. The liquid medium comprises liquid alpha-olefin monomer, optionally with the addition of an inert hydrocarbon solvent. The hydrocarbon solvent may be aromatic, such as toluene, or aliphatic, such as propane, hexane, heptane, isobutane, cyclohexane and 2, 2, 4-trimethylpentane. The amount of hydrocarbon solvent, if any, is less than 40 wt%, preferably less than 20 wt%, relative to the total amount of alpha-olefins. Preferably, the prepolymerization step is carried out in the absence of an inert hydrocarbon solvent.

The average residence time in the reactor may be from 2 to 40 minutes, preferably from 10 to 25 minutes. The temperature ranges from 10 ℃ to 50 ℃, preferably from 20 ℃ to 40 ℃. The use of these conditions allows obtaining a preliminary polymerization degree in the preferred range of 60 to 800g/g of the solid catalyst component, preferably 150 to 500g/g of the solid catalyst component.

The slurry comprising prepolymerized catalyst is withdrawn from the prepolymerization reactor and fed to the reactor where the main polymerization step takes place.

The main polymerization stage can be carried out in gas phase or liquid phase. The gas-phase process can be carried out in a fluidized or stirred fixed-bed reactor or in a gas-phase reactor comprising two interconnected polymerization zones, one of which operates under fast fluidization conditions and the other in which the polymer flows under the action of gravity. The liquid phase process may be in slurry, solution or bulk (liquid monomer). The latter technique is most preferred and can be carried out in various types of reactors, such as a continuous stirred tank reactor, a loop reactor or a plug flow reactor. The polymerization can be carried out at a temperature of from 20 to 120 c, preferably from 40 to 85 c. When the polymerization is carried out in the gas phase, the operating pressure may be from 0.5 to 10MPa, preferably from 1 to 5 MPa. In the bulk polymerization, the operating pressure may be from 1 to 6MPa, preferably from 1.5 to 4 MPa. Preferably, the main polymerization stage is carried out by reacting in liquid monomer, preferably in a loop reactor, optionally with ethylene and/or C₄-C₁₀Propylene is polymerized in a mixture of alpha-olefins to obtain a crystalline propylene polymer.

Hydrogen can be used as a molecular weight regulator. The propylene polymer obtained in this stage has a xylene insolubility preferably higher than 90%, more preferably higher than 95%, according to the isotactic pentad content (with C over the whole polymer)¹³-NMR determination) higher than 93%, preferably higher than 95%. The values of the melt flow rate according to ISO 1133(230 ℃, 2.16Kg) can vary within a wide range from 0.01 to 300g/10min, in particular 0.1250g/10 min. The bulk density of the polymer may be from 0.40 to 0.50g/cm³。

In the case of the production of heterophasic propylene copolymers (also known as impact copolymers), the second polymerization stage is carried out in a different reactor to produce the propylene/ethylene copolymer. The second stage may be carried out in a conventional fluidized bed gas phase reactor in the presence of the polymeric material and the catalyst system from the preceding polymerization step. The polymerization mixture was discharged from the first reactor to a gas-solid separator and subsequently fed to a fluidized bed gas phase reactor operating under conventional temperature and pressure conditions.

The polymer produced in the second stage is preferably an ethylene copolymer containing from 15 to 75% by weight of C₃-C₁₀Alpha-olefins, optionally containing small proportions of dienes, are at least 60% xylene soluble at room temperature. Preferably, the alpha-olefin is selected from propylene or butene-1 and its content is preferably in the range of 20 to 70 wt%.

The final propylene polymer obtained by the process of the present invention can be obtained in a reactor grade having melt flow rate values according to ISO 1133(230 ℃, 2.16Kg) of from 0.01 to 100g/10min, preferably from 0.1 to 70 and more preferably from 0.2 to 60. It may be chemically degraded, if desired, to achieve a final MFR value suitable for the selected application.

The propylene polymers thus obtained may also be added with additives used in the art, such as antioxidants, light stabilizers, heat stabilizers, clarifiers and nucleating agents.

In particular, the addition of nucleating agents may bring about an improvement in the physico-mechanical properties, such as tensile modulus in the range of 800 to 1800MPa, tensile strength at yield in the range of 20 to 50MPa and transparency.

Typical examples of nucleating agents are p-tert-butylbenzoate, dibenzylidene sorbitol derivatives and talc.

The nucleating agent is preferably added to the composition of the present invention in an amount of 0.05 to 2% by weight, more preferably 0.1 to 1% by weight, relative to the total weight. Nucleation can be seen by increasing the crystallization temperature of the polymer. On the other hand, the colorants used according to the invention may also provide the same effect. In particular, it has been observed that small amounts of copper phthalocyanine used as a colorant also have a nucleating effect by increasing the crystallization temperature to 120 ° to 125 ℃.

Among the clarifying agents, dibenzylidene sorbitol derivatives are preferred.

These are sold in granular form. Compounds such as 1, 3-O-2, 4-bis (3, 4-dimethylbenzylidene) sorbitol (hereinafter referred to as "DMDBS"), are available under the trade name DMDBS3988 is available from Milliken and Company asPolypropylene provides nucleation and clarification properties. Other DBS-based clarifying compounds may be used, including those substituted with other groups on the sorbitol portion of the molecule or on the benzene ring portion of the molecule. Other clarifier compounds may be used, such as bis [2, 2' -methylenebis- (4, 6-di-tert-butylphenyl) phosphate]Aluminum (from Palmaroll SAS, France, as "NA-21^TM"commercially available").

The polymers thus obtained can be used to prepare finished products according to conventional techniques such as injection moulding, extrusion blow moulding, injection stretch blow moulding and thermoforming.

Examples

Data for propylene polymer materials were obtained according to the following method:

xylene soluble fraction

2.5g of polymer and/250 mL of xylene were introduced into a glass flask equipped with a refrigerator and a magnetic stirrer. The temperature was raised to the boiling point of the solvent in 30 minutes. The solution thus obtained was then kept under reflux and stirred for a further 30 minutes. The closed flask was then kept in an ice-water bath for 30 minutes and in a thermostatic water bath at 25 ℃ for 30 minutes. The solid thus obtained was filtered on quick filter paper and the filtered liquid was divided into two 100ml aliquots. A 100ml aliquot of the filtered liquid was poured into a pre-weighed aluminum container which was heated on a hot plate under a stream of nitrogen to remove the solvent by evaporation. The container was then held on an oven at 80 ℃ under vacuum until a constant weight was obtained. The residue was weighed to determine the percentage of xylene soluble polymer.

Melt Flow Rate (MFR)

Measured according to ISO 1133(230 ℃, 2.16Kg)

Yellowness index

The determination of the Yellowness Index (YI) is obtained by directly measuring the X, Y and Z trichromatic coordinates on the pellets using a trichromatometer capable of assessing the deviation of the colour of the object from a preset standard white to yellow in the dominant wavelength range between 570nm and 580 nm. The geometry of the instrument should allow for viewing of the reflected light of the two rays that impinge on the sample at an angle of 45 deg. at an angle of 90 deg. to each other, according to the CIE standard, from "illuminant C". After calibration, the pellets to be tested were placed in a glass container to obtain the X, Y, Z coordinates and the yellowness index was calculated according to the following formula:

YI＝100*(1.274976795*X-1.058398178*Z)/Y

examples

General procedure for propylene polymerization

A 4 liter steel autoclave equipped with a stirrer, pressure gauge, thermometer, catalyst feed system, monomer feed line and thermostatted jacket was purged with a stream of nitrogen at 70 ℃ for 1 hour. A solution containing 75ml of anhydrous hexane, 0.6g of triethylaluminium (AlEt)₃5.3mmol) and 0.006 to 0.010g of a suspension of the solid catalyst component previously associated with 10% by weight of total AlEt₃And an amount of dicyclopentyldimethoxysilane such that the molar ratio of Al/dicyclopentyldimethoxysilane in the glass pot was 20, for 5 minutes. The autoclave was closed and the required amount of hydrogen (4500cc) was added. Then, 1.2kg of liquid propylene was fed under stirring. The temperature was raised to 70 ℃ in about 10 minutes and polymerization was carried out at this temperature for 2 hours. At the end of the polymerization, the unreacted propylene bis-recovery polymer was removed and dried under vacuum at 70 ℃ for 3 hours. The resulting polymer was weighed and characterized.

General procedure for the preparation of MgCl2 · (EtOH) m adduct.

Preparation of microspheroidal MgCl according to the method described in example 2 of U.S. Pat. No.4,399,054₂·2.8C₂H₅And (5) OH. The resulting adduct has an average particle size of 25 μm.

Example 1 (comparative)

Preparing a solid catalyst component containing 9, 9-bis (methoxymethyl) fluorene.

1.0L of TiCl was added at room temperature under a nitrogen atmosphere₄Into a 2.0L round bottom glass reactor equipped with a mechanical stirrer, cooler and thermometer. After cooling to-5 ℃ 13.2g of MgCl were introduced with stirring₂And EtOH microspheresComplexes (prepared as disclosed in the general procedure). The temperature was then raised from-5 ℃ to 40 ℃ and when this temperature was reached, 9, 9-bis (methoxymethyl) fluorene was used as internal electron donor introduced in an amount to yield a Mg/9, 9-bis (methoxymethyl) fluorene molar ratio of 6.

At the end of the addition, the temperature was raised to 100 ℃ and held at this value for 30 minutes. After this time, the stirring was stopped and the solid product was allowed to settle. The supernatant was then siphoned off, leaving 300cm in the reactor³While maintaining the temperature at 75 ℃. After removal of the supernatant, fresh TiCl was added₄And an additional amount of donor such that the Mg/9, 9-bis (methoxymethyl) fluorene molar ratio is 20. The entire slurry mixture was then heated at 109 ℃ and held at this temperature for 30 minutes. The stirring is interrupted; the solid product was allowed to settle and the supernatant liquid was siphoned off while maintaining the temperature at 109 ℃. Repeatedly on fresh TiCl₄(1L total volume) and the mixture was kept stirring at 109 ℃ for 15 minutes, then the supernatant was siphoned off.

The solid was washed five times (5X 1.0L) with anhydrous isohexane at 50 ℃ and once (1.0L) at room temperature

Finally the solid was dried in vacuo, weighed and analyzed.

The catalyst comprises the following components: mg is 12.5 wt%; 3.7 wt% of Ti; i.d. ═ 20.7 wt%.

The catalyst thus obtained was used for propylene polymerization according to the general procedure described above. The results are shown in Table 1.

Example 2 and comparative examples 3 to 5

A colorant/solid catalyst component dry mixture was prepared at a weight ratio of 0.2

Into a 50cc vessel were introduced 3g of the catalyst component prepared as in example 1 and 0.6g of copper phthalocyanine. The solids were mixed for 30 minutes and then discharged. Several aliquots of the mixture were tested at different times in the propylene polymerization according to the general procedure described above. The conditions and results are shown in table 1.

Examples 6 to 7 and comparative examples 8 to 9

A colorant/solid catalyst component dry mixture was prepared at a weight ratio of 0.1

Into a 50cc vessel were introduced 3g of the catalyst component prepared as in example 1 and 0.3g of copper phthalocyanine. The solids were mixed for 60 minutes and then discharged. Several aliquots of the mixture were tested at different times in the propylene polymerization according to the general procedure described above. The conditions and results are shown in table 1.

Examples 10 to 12 and comparative example 13

A colorant/solid catalyst component dry mixture was prepared at a weight ratio of 0.05

Into a 50cc vessel were introduced 3g of the catalyst component prepared as in example 1 and 0.15g of copper phthalocyanine. The solids were mixed for 120 minutes and then discharged. Several aliquots of the mixture were tested at different times in the propylene polymerization according to the general procedure described above. The conditions and results are shown in table 1.

Examples 14 to 16.

A colorant/solid catalyst component dry mixture was prepared at a weight ratio of 0.025

Into a 10cc vessel were introduced 3g of the catalyst component as prepared in example 1 and 0.075g of copper phthalocyanine. The solids were mixed for 60 minutes and then discharged. Several aliquots of the mixture were tested at different times in the propylene polymerization according to the general procedure described above. The conditions and results are shown in table 1 below.

TABLE 1

nd is not measured.