Title of Invention	"A PROCESS FOR PREPARATION OF CREEP RESISTANT POLYPROPYLENE"
Abstract	The invention relates to a process for the preparation of a polypropylene for e.g. pipe, profile and moulding applications, containing from 1.0 to 10.0% by weight of ethylene or C4-C10-α-olefin repeating units and having a MFR2 value of between 0.05 and 0.40 g/10 min by polymerizing propylene and ethylene in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound and the cocatalyst component of -which comprises an organoahrnunium compound, and hydrogen as a molecular weight regulating agent, to give said polypropylene. The creep-resistance of the polypropylene is unproved by performing the process by means of me following steps: . (a) copolymerizfflg propylene and ethylene into a random copolymer at 40 to 110*C using: a catalyst system of the above-mentioned type; a portion of ethylene orC4-C10-α-olefin leading to 1.0 to 10.0% by weight of ethylene repeating units in said random copolymer; and no or a minimal amount of hydrogen leading to a MFRjo value of between 0.01 and 5.0 g/10 min for said random copolymer, if this step is performed first, or to a MFR2 value for said polypropyleneof between 0.05 and 0.40 g/10 mm, if this step is performed after step(b);the poportion of random copolymer of this step being from 20 to 80% b weight of said polypropylene, (b) polymerizing propylene at 40 to 110°C using: a catalyst system of the above- mentioned type; no or arnuuinal portion of ethylene leading to 0.0 to 1.0% by weight of cthylene repeating units in the polymer resulting from this step; and an amount of hydrogen leading to a MFR2 value of between 30 and 300 g/10 min for said polymer, if this step is performed first, or to a MFR2 value for said poly¬ propylene of between O.OS and 0.40 g/10 min, if mis step is performed after step (a); the proportion of polymer of this step being from 80 to 20% by weight of said polypropylene. The polypropylene can be elastomer modified byi (c) providing an elastomer, the proportion of which is from 5 to 40% by weight of said polypropylene. In this case the MFR2 value of the polypropylene can be from 0.05 to 50 g/10 min.

Title of Invention

"A PROCESS FOR PREPARATION OF CREEP RESISTANT POLYPROPYLENE"

Abstract

The invention relates to a process for the preparation of a polypropylene for e.g. pipe, profile and moulding applications, containing from 1.0 to 10.0% by weight of ethylene or C4-C10-α-olefin repeating units and having a MFR2 value of between 0.05 and 0.40 g/10 min by polymerizing propylene and ethylene in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound and the cocatalyst component of -which comprises an organoahrnunium compound, and hydrogen as a molecular weight regulating agent, to give said polypropylene. The creep-resistance of the polypropylene is unproved by performing the process by means of me following steps: . (a) copolymerizfflg propylene and ethylene into a random copolymer at 40 to 110*C using: a catalyst system of the above-mentioned type; a portion of ethylene orC4-C10-α-olefin leading to 1.0 to 10.0% by weight of ethylene repeating units in said random copolymer; and no or a minimal amount of hydrogen leading to a MFRjo value of between 0.01 and 5.0 g/10 min for said random copolymer, if this step is performed first, or to a MFR2 value for said polypropyleneof between 0.05 and 0.40 g/10 mm, if this step is performed after step(b);the poportion of random copolymer of this step being from 20 to 80% b weight of said polypropylene, (b) polymerizing propylene at 40 to 110°C using: a catalyst system of the above- mentioned type; no or arnuuinal portion of ethylene leading to 0.0 to 1.0% by weight of cthylene repeating units in the polymer resulting from this step; and an amount of hydrogen leading to a MFR2 value of between 30 and 300 g/10 min for said polymer, if this step is performed first, or to a MFR2 value for said poly¬ propylene of between O.OS and 0.40 g/10 min, if mis step is performed after step (a); the proportion of polymer of this step being from 80 to 20% by weight of said polypropylene. The polypropylene can be elastomer modified byi (c) providing an elastomer, the proportion of which is from 5 to 40% by weight of said polypropylene. In this case the MFR2 value of the polypropylene can be from 0.05 to 50 g/10 min.

Full Text	New piping-grade polypropylene composition The invention relates to a process for the preparation of rigid polypropylene for e.g. pipe, fiber, profile and moulding applications, containing from 1.0 to 10.0% by weight of ethylene repeating units and having a MFR2 value of between 0.05 and 0.40 g/10 min, by polymerizing propylene and ethylene or a C4-CiQ-a-olefin in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound and the cocatalyst component of which comprises an organoaluminium compound, and hydrogen as a molecular weight regulating agent, to give said polypropylene. The invention also relates to a process for the preparation of elastomer modified polypropylene for e.g. pipe, fiber, profile and moulding applications, containing from 1.0 to 30% by weight of ethylene or a C4-C10-α-olefin repeating units and having a MFR2 value of between 0,05 and 50 g/10 min, by polymerizing propylene and ethylene or a C4-C10-α-olefin in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound and the cocatalyst com¬ponent of which comprises an organoaluminium compound, and hydrogen as a molecular weight regulating agent, as well as providing an elastomer component, to give said elastomer modified polypropylene. Finally, the invention also relates to a creep-resistant polypropylene made by the above processes and its use-By Melt Flow Rate (MFR) is meant the weight of a polymer extruded through a standard cylindrical die at a standard temperature in a laboratory rheometer carrying a standard piston and load. Thus MFR is a measure of the melt viscosity of a polymer and hence also of its molecular weight. The smaller the MFR, the larger is the molecular weight. It is frequently used for characterizing a polyolefins, e.g. polypropylene, where the standard conditions MFRmi are: temperature 230°C; die dimensions 9.00 mm in length and 2.095 mm in diameter; load of the piston, 2,16 kg (mi=2), 5.0 kg (mi=5), 10.0 kg (mi=10), 21.6 kg (mi-21). See Alger, M.S.M., Polymer Science Dictionary, Elsevier 1990, p. 257. The standard generally used are ISO 1133 C4, ASTM D 1238 and DIN 53735.By Flow Rate Ratio (FRR) is meant the ratio between the Melt Flow Rate (MFR) measured at a standard temperature and with standard die dimensions using a heavy load and the melt flow rate measured at the same temperature with the same die dimensions using a light load. Usually, for propylene polymers are used nominal loads 10.0 kg and 2.16 kg (ISO 1133 C4). The larger the value of the FRR, the broader the molecular weight distribution. Polypropylene copolymer has many characteristics which makes it desirable for applications like pipes, fittings, moulded articles, foams etc. Polypropylene as piping material is mainly used in non-pressure applications (pipe and fittings) and profiles. There is a small volume used for pressure pipe, mainly hot water and industrial pipes. The good thermal resistance of polypropylene compared to other polyolefins is utilized for the pipe applications. All three main types of propylene polymer, i.e. homopolymers, random copolymers and block copolymers are used. Homopolymevs give the pipe good rigidity but the impact and creep properties are not very good. The block copolymers give good impact properties but the creep properties are like homopolymers due to the homoporymer matrix. Propylene ethylene random copolymers are used for pressure pipe applications for hot water and industrial pipes. The propylene-ethylene random copolymers for pressure pipes are today produced with high yield Ziegler-Natta catalysts in processes (bulk or gas phase) giving a material having a relatively narrow molecular weight distribution (MWD * Mv/Mn) of about 5, corresponding to a FRR (MFRio/MFRa) of 13-17. The molecular weight (Mw) of the pipe material with melt flow rate (MFR2) of 0.1-0.4 is about 600 000 - 1 000 000. This high molecular weight and the narrow MWD cause problems in compounding and extrusion of pipes. The proccssability of such materials is difficult due to the low shear sensitivity causing unwanted degradation of the material and melt fracture, which is seen as uneven surface and thickness variations of the pipes. In addition the conventional propylene random copolymer pipe materials produced in one phase have not strength enough for the short and long term properties (notch resistance and creep) needed for good pressure pipes. The processability of the conventional propylene random copolymers can be improved by broadening the MWD using multi-stage polymerization processes. In multi-stage polymerization the MWD of the polymer can be broadened by pro¬ducing different molecular weight polymers in each stage. The MWD of polymer becomes broader when lower molecular weight polymer is reactor-blended into the higher molecular weight polymer adjusting the final MFR by choosing the right molecular weight and the reactor split in each stage. The molecular weight of the polymer in each step can be controlled by hydrogen which acts as a chain transfer agent. Reactor temperature may be also used for controlling the molecular weight of polymer in each step. Multi-stage polymerization is disclosed e.g. in patent application JP-91048, but the process concerns film grade polypropylene with a final MFR2 of about 1.5. When the processability is improved by producing broader MWD propylene random copolymer, also the amount of low molecular fraction is increased if the comonomer feeds are the same in each stage. The taste and odour are adversely affected. By using a concept invented with high yield TiCl4 catalyst it is possible to produce pipe material having improved mechanical and pipe properties and also a good extrudability. The improved strength properties of the material come from a very high molecular weight fraction of Mw k 2000000 g/moi and totally novel comonomer distribution together with a broad molecular weight distribution, hi another embodiment of the invention, an elastomer is provided within this propylene product for increased impact strength. The embodiment of the invention relating to a non-elastomeric polypropylene product is essentially characterized by what is said in the characterizing part of claim 1. Thus the invented concept is based on the idea of producing a broad MWD and a high molecular weight propylene random copolymer and improved comonomer distribution using high yield catalysts in two or several reactors at different reaction conditions. The comonomers incorporated in long chains as described in this invention destroy the regularity of the chains leading to the more homogenous distribution of the essential tie-chains and entanglements needed for creep properties and toughness in pipe materials. The low molecular weight fraction contains no or minimal portion of ethylene repeating units in the polymer. Together with the high molecular weight random copolymer fraction this fraction is improving the processability. The no or low ethylene content fraction gives the total polymer the stiffness needed for rigid materials e.g. pipes, profiles and moulding applications. A homopolymer or a minirandom copolymer (ethylene 2% has a stiffness of The problem with the uneven comonomer distribution with high yield TiCl4 catalysts is solved in a way that the amount of comonomer is split between the reactors. To the reactor where the high molecular weight propylene polymer is pro¬duced is fed more essentially all, comonomer compared to the reactor where the low molecular PP i produced. Higher amounts of comonomer can be fed because the solubility of the high molecular weight polymer is lower. The final comonomer content is adjusted by controlling the comonomer feed into the reactor. The intervals given in this publication always include both limits thereof. Thus one embodiment of the present invention relates to a process for the preparation of polypropylene for e.g. pipe, fiber, profile and moulding applications. Such a grade of polypropylene has from 1.0 to 10.0% by weight of etbylene or a C4-C10-α-otefra repeating units and has a MFR2 value of between 0.10 and 0.40 g/10 min. The preparation takes place by polymerizing propylene and ethylene or a C4-C10-α-olefin in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound, and a cocatalyst component of which comprises an organoaluminium compound, optionally an external electron donor and hydrogen as a molecular weight regulating agent It has been found that extremely creep-resistant polypropylene can be prepared by applying the following steps in any mutual order: (a) copolymerizrag propylene and ethylene or aC4-C10-α-olefin into a random copolymer at 40 to 110°C using: a catalyst system of the above-mentioned type; a portion of ethylene or C4-C10-α-olefin leading to 1,0 to 10.0% by weight of ethylene or C4-C10-α-otefin repeating units in said random copolymer; and no or a minimal amount of hydrogen leading to a MFR10 value of between 0.01 and 5.0 g/10 min for said random copolymer, if this step is performed first, or to a MFR2 value for said polypropylene of between 0.05 and 0.40 g/10 rain, if this step is performed after step (b); the proportion of random copolymer of this step being from 20 to 80% by weight of said polypropylene, (b) polymerizing propylene at 40 to 110°C using: a catalyst system of the above- mentioned type; no or a minimal portion of ethylene leading to 0,0 to 1.0% by weight of ethylene repeating units in the polymer resulting from this step; and an amount of hydrogen leading U> a MTR2 value of between 20 and 1000 g/10 mio fnr said polymer, if this step is performed first, or to a MFR2 value for said poly¬ propylene of between 0.05 and 0.40 g/10 min, if this step is performed after step (a); the proportion of polymer of this step being from 80 to 20% by weight of said polypropylene. In step (a) a very high molecular weight random copoiymer of propylene and ethylene is prepared, which gives the polypropylene its extremely high shape-resistance, fai step (b), essentially homopolymeric low molecular weight poly¬propylene is prepared, which gives the product good melt-processing properties and improved stiffness. In the process of me invention the order of steps (a) and (b) can freely be chosen. It is, however, preferable to perform step (a) before step (b). Although, different catalyst systems of the above mentioned type can be used in steps (a) and (b), it is preferable to use the same catalyst system for both steps. According to a preferable embodiment, the catalyst system is added to step (a) and the same catalyst system is then used both in step (a) and (b). Steps (a) and (b) can be performed in reactors, which may be of any type con¬ventionally used for propylene polymerization and copolymerization, preferentially a loop (CSTR) or gas phase reactor, but it is most preferable to perform one of steps (a) and (b) in a loop (CSTR) reactor and the other step in a gas phase reactor, whereby any reaction medium used and unreactive reagents are removed at least partly between step (a) and step (b). In such a case the procatalyst (also called catalyst in the art), cocatalyst and external donor are fed to the loop reactor. The reaction medium and unreacted reagents such as H2 or comonomer can be removed by known methods between the steps. It is also preferable to adjust the proportion of copoiymer resulting from step (a) and the MFR values of step (a) and step (b) so that the FRR value (MFRio/MFR2), which is also a measure of the molecular weight distribution, of said polypropylene is between 10 and 100, most preferably between 20 and 50. The catalyst used hi the present process for the preparation of polypropylene can be any suitable catalyst, which consists of a procatalyst, which is a reaction product of at least tetravalent titanium compound and a magnesium halide compound, and a cocatalyst, which comprises an organoaluminium compound, an optionally external electron donor compound. Preferentially, said catalyst system has been prepared by: (i) providing a procatalyst by reacting a magnesium halide compound, chosen from magnesium chloride, its complex with ethanol and other derivatives of magnesium chloride, with titanium tetrachloride and optionally with an internal donor, exemplified by the dialkyl phthalates, (ii) providing as cocatalyst an organoaluminium compound chosen from trialkyl aluminium exemplified by triethyl aluminium, dialkyl aluminium chloride, alkyl aluminium sesquichloride, optionally (iii) providing as at least one external donor an ester of an aromatic acid exempli¬fied by methyl p-methyl benzoate, or an organosilicon compound exemplified by alkoxy silanes or blends thereof, and, optionally (iv) prepolymerizing a small amount of olefin by contacting the olefin with said procatalyst, cocatalyst and, optionally, the external donor. hi step (a) of the present process, a portion of ethylene is preferably used, which leads to 1.0 to 7.0% by weight of ethylene units in the random copolymer resulting from this step. Further in step (a) preferably no or a minimal amount of hydrogen is used, which leads to a MFRio value of between 0.05 and 2.0 g/min for the random copolymer resulting from mis step, if the step is performed first. Also, the proportion of random copolymer resulting from step (a) is preferably from 40 to 80% by weight of said polypropylene. Thus it can be said, that the polypropylene prepared by the process of the invention contains preferably more random copolymer than low molecular weight homopolymer or minirandom copolymer. In step (b), low molecular weight essentially homopolymeric propylene is produced. The molecular weight is adjusted by means of hydrogen. If the hydrogen amount is too high, the molecular weight will be too low and the product will be useless as pipe, profile or moulding material. In step (b) an amount of hydrogen is preferably used, which leads to a MFR2 value of between 30 and 500 g/10 min for the polymer resulting from this step, if it performed first. As it was said before, too much ethylene units in the low molecular weight component leads to difficulties in retaining good stiffness properties of the product. Thus, in step (b) no or a minimal amount of ethylene is used, which preferably leads to 0.0 to 0.5% by weight of ethylene repeating units in the polymer resulting from this step. Prefel'ably, the low molecular weight homopolymer fraction is smaller that the high molecular weight random copolymer fraction, i.e. the proportion nf polymer resulting from step (b) is from 60 to 20% by weight of said polypropylene. According to another embodiment of the present invention, the invention relates to a process for the preparation of elastomer modified polypropylene for e.g. pipe, fiber, film, foam, profile and moulding applications. Such a grade of polypropylene has from 1.0 to 30% by weight of ethylene or a C4-C10-α-olefin repeating units and has a MFR2 value of between 0.05 and 50 g/10 min. The preparation takes place by polymerizing propylene and ethylene or a C4-C10-α-olefin in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound, and a cocatalyst component of which comprises an organoaluminium compound, and hydrogen as a molecular weight regulating agent, as well as providing an elastomer component. It has been found that extremely creep-resistant polypropylene can be prepared by applying the following steps: (a) copolymerizing propylene and ethylene into a random copolymer at 40 to 110'C using: a catalyst system of the above-mentioned type; a portion of ethylene or C4-C10-α-olefin leading to 1.0 to 10.0% by weight of ethylene or C4-C10-α- olefin repeating units in said random copolymer; and no or a minimal amount of hydrogen leading to a MFR10 value of between 0.01 and 5.0 g/10 min for said random copolymer, if this step is performed first, or to a MFR2 value for said poly¬ propylene of between 0.05 and 50 g/10 min, if this step is performed after step (b); the proportion of random copolymer of this step being from 20 to 80% by weight of said polypropylene, (b) polymerizing propylene at 40 to 110°C using: a catalyst system of the above- mentioned type; no or a minimal portion of ethylene leading to 0.0 to 1.0% by weight of ethylene repeating units in the polymer resulting from this step; and an amount of hydrogen leading to a MFR2 value of between 20 and 1000 g/10 min for said polymer, if this step is performed first, or to a MFR2 value for said poly¬ propylene of between 0.05 and 50 g/10 min, if this step is performed after step (a); the proportion of polymer of this step being from 80 to 20% by weight of said polypropylene, and (c) providing a rubbery copolymer (elastomer) the proportion of which is from 5 to 40% by weight of said polypropylene. In step (a) a very high molecular weight random copolymer of propylene and ethylene is prepared, which gives the polypropylene its extremely high shape-resistance. In step (b), essentially homopolymeric low molecular weight poly¬propylene is prepared, which gives the product good melt-processing properties and improved stiffness. In step (c), the provided rubbeiy copolymet gives better impact resistance, In the process of the invention the order of steps (a) and (b) can freely be chosen. It isr however, preferable to perform step (a) before step (b). Although different catalyst systems of the above mentioned type can be used in steps (a) and (b), it is preferable to use the same catalyst system for both steps. According to a preferable embodiment, the catalyst system is added to step (a) and the same catalyst system is then used both in step (a) and (b). Steps (a) and (b) can be performed in reactors, which may be of any type con¬ventionally used for propylene polymerization and copolymerization preferentially a loop (CSTR) or gas phase reactor, but it is most preferable to perform one of steps (a) and (b) in a loop (CSTR) reactor and the other step in a gas phase reactor, whereby any reaction medium used and unreactive reagents are removed at least partly between step (a) and step (b). In such a case the procatalyst (also called catalyst in the art), cocatalyst and external donor is fed to the loop reactor. The reaction medium and uweacted reagents such as H2 or comonomer can be removed by known methods between the steps. Preferably, steps (a) and (b) are performed so that said polypropylene has a MFR2 value of between 0.1 and 12 g/10 min. It is also preferable to adjust the proportion of copolyraer resulting from step (a) and the MFR values of step (a) and step (b) so that the FRR value (MFRio/MFR2)7 which is also a measure of the molecular weight distribution, of said polypropylene is between 10 and 100, most preferably between 20 and 50. The catalyst used in the present process for the preparation of polypropylene can be any suitable catalyst, which consists of a procatalyst, which is a reaction product of at least tetravalent titanium compound and a magnesium halide compound, and a cocatalyst, which comprises an organoaluminium compound, an optionally external electron donor compound. Preferentially, said catalyst system has been prepared by: (i) providing a procatalyst by reacting a magnesium halide compound, chosen from magnesium chloride, its complex with ethanol and other derivatives of magnesium chloride, with titanium tetrachloride and optionally with an internal donor, exemplified by the dialkyl phthalates, (ii) providing as cocatalyst an organoaluminium compound chosen from trialkyl aluminium exemplified by triethyl aluminium, dialkyl aluminium chloride, alkyl aluminium sesquichlonde, optionally (iii) providing as at least one external donor an ester of an aromatic acid exempli¬fied by methyl p-methyl benzoate, or an organosilicon compound exemplified by alkoxy silanes or blends thereof, and, optionally (iv) prepolymerizing a small amount of olefin by contacting the olefin with said procatalyst, cocatalyst and, optionally, the external donor. In step (a) of the present process, a portion of ethylene or a C4-Cio-a-olefin is preferably used, which leads to 1.0 to 7.0% by weight of ethylene or a C4-Cjo-a-olefin units in the random copolymer resulting from this step. Further in step (a) preferably no or a minimal amount of hydrogen is used, which leads to a MFRjQ value of between 0.05 and 2.0 g/min for the random copolymer resulting from this step, if the step is performed first. Also, the proportion of random copolymer resulting from step (a) is preferably from 40 to 80% by weight of said poly¬propylene. Thus it can be said, that the polypropylene prepared by the process of the invention contains preferably more random copolymer than low molecular weight homopolymer or minirandora copolymer. In step (b), low molecular weight essentially homopolymeric or minirandom (having little comonomer) propylene is produced. The molecular weight is adjusted by means of hydrogen. If the hydrogen amount is too high, the molecular weight will be too low and the product will be useless as pipe, profile or moulding material. In step (b) an amount of hydrogen is preferably used, which leads to a MFR 2 value of between 30 and 500 g/10 min for the polymer resulting from this step, if it performed first. As it was said before, too much ethylene units in the low molecular weight component leads to difficulties in retaining the stiffness properties of the product. Thus, in step (b) no or a minimal amount of ethylene is used, which preferably leads to 0.0 to 0.5% by weight of ethylene repeating units in the polymer resulting from this step. Preferably, the low molecular weight homopolymer fraction is smaller that the high molecular weight random copolymer fraction, Le. the proportion of polymer resulting from step (b) ia from 60 to 20?4 by weight of said polypropylene. The step (c) of providing an elastomer preferably follows steps (a) and (b) and, most preferentially, the order of steps is (a) => (b) => (c). The step (c) of providing an elastomer can be performed in two ways. According to the first and more preferable way, said elastomer is provided by copolymerizing at least propylene and ethylene into an elastomer. The conditions for the copolymerizatkm are within the limits of conventional EPM production conditions such as they are disclosed e.g. in Encyclopedia of Polymer Science and Engineering, Second Edition, Vol. 6, p. 545-558. A rubbery product is formed if the ethylene repeating unit content in the polymer is within a certain interval. Thus, preferentially, in step (c), ethylene and propylene are copolymerized into an elastomer in such a ratio that the copolymer step (c) contains from 10 to 70% by weight of ethylene units. Most preferably, the ethylene unit content is from 30 to 50% by weight of the copolymeric propylene/ethylene elastomer. According to preferable embodiments of the invention, the following conditions are independently chosen for the three step process: a temperature in step (c) of between 40 and 90°C, said catalyst system is added to step (a) and used in both steps (a), (b) and (c), step (a) is performed in a loop (CSTR) reactor and steps (b) and (c) are performed in two separate gas phase reactors, the added comonomer portion is adjusted so that the proportion of ethylene repeating units after steps (a) and (b) is from 1 to 4% by weight and the proportion of ethylene repeating units after steps (a), (b) and (c) is from 5 to 15% by weight, in step (c), ethylene and propylene are copolymerized into an elastomer in a molar ratio ethylene/propylene of between 30/70-50/50. According to another embodiment of the claimed process, the elastomer in step (c) is provided by adding a ready-made or natural elastomer to the reaction product of steps (a) and (b), most preferably an impact modified heterophasic polypropylene having from 15 to 50% by weight of a propylene-ethylene elastomeric copolymer. As polypropylene for pipe, profile and moulding applications has not before been prepared with such a good shape preservance, the invention also relates to an extremely creep-resistant polypropylene for said applications. The creep resistance can be measured by registering the deflection of the material during 500-1000 h using 7.3 ar 6.5 MP& load at 60°C. This new material ehows a creep level of I/*? to 1/2 of regular PP (pipe grade) material comparable to e.g. the PP material of comparative example 9, This is a sensational result and can open new application in e.g. piping. According to one embodiment of the invention, the creep-resistant polypropylene has been made according to the above described process for its preparation. According to another embodiment of the invention, the use of the above mentioned polypropylene is claimed, which use is directed to pipes, profiles, moulded articles and foams, fibres and films. In addition to ethylene and propylene, the process and the polypropylene according to the invention can contain from 0.0 to 10.0% by weight of any other olefin such as butene-1, 4-raethyl-pentene-l, hexene-1, octene-1 and decene-1 or combinations of them. The stiffness of this material is higher than that for materials produced with about the same comonomer content in several reactors or in only one reactor without loosing the impact. That is seen best when comparing the embodiment examples I to 10 with comparative examples 1 to 3 which are produced in the same conditions but with different ethylene feed splits. The entanglements and tie-chains of the high molecular fraction in the material give the material better pipe properties especially higher tensile strength tensile modulus charpy impact strength, and lower creep under load. The invented copolymers give also longer time to failure at same hoop stress levels in standard pipe pressure tests than the conventionally produced random pipe material. The invention is in the following illuminated by the following examples and comparative examples. Examples The following tests and preparations were made: Mechanical tests from 4 mm compression moulded plaques. The specimens were according to ISO 527. Tensile strength according to ISO 527 (cross head speed - 50 mm/min). Tensile modules according to ISO 527 (cross head speed = 1 mm/rain). Charpy, notched impact according to ISO 179/leA. Creep test is a Borealis tensile-creep-method for ranking of pipe materials. In the method a constant stress is applied to a specimen (a modified ISO dumb bell =120 mm long, thickness = 2 mm). The test temperature = 60°C (oven) and the stress = 7.3 mPa (for PP materials). The increase of strain with time is recorded 500 to 1000 h. The creep is defined as the elongation at 100 h in mm units corresponding to stiffness and the slope between 100 h and 400 h in angle units. This creep resistance test method is comparable to e.g. ISO 899-1, DIN 53444 and ASTM2990. Example 1 Preparation and properties of high MW very broad MWD two-stage random homo-PPcopolymer The PP copolyraers were produced in a pilot plant having a loop reactor and a fluid bed gas phase reactor connected in series. The catalyst, cocatalyst and donor were fed to the loop reactor. The reaction medium of loop was flashed away before the solid polymer containing the active catalyst entered to the gas phase. The prepolymerized MgCl2-supported Ti catalyst (prepared according to patent US 5,234,879, included by reference) was used in the polymerization. Cocatalyst was triethyl aluminium (TEA) and external donor dicyclopentanedimethoxysilane (DCPDMS). Al/Ti mole ratio was 150 and Al/donor mole ratio 5. In the first stage (loop reactor) was produced high MW propylene-ethylene random copolymer, and die polymerization was continued in the second stage (gas phase reactor) which produced low MW homo-PP. The polymerization temperature used in both stages was 70°C. The production rate was 6 kg/h for the first stage and 4 kg/h for the second stage, which means a production split of 60/40. The MFR:s of the first stage and final product were adjusted with separate hydrogen feeds. More detailed properties of the material produced in each stage are shown in Table 1. trample 2 Preparation and properties of moderately broad MWD two-stage random homo-PP copolymer The polymer was polymerized as in example I, except that the production split was 80/20 and the MW of the random PP produced in the first stage was adjusted slightly lower with hydrogen feed. More detailed properties of the material pro¬duced in each stage are shown in Table 1. pxample 3 Preparation and properties of very broad MWD two-stage random minirandotn-PP copolymer The polymer was polymerized as in Example 1, except that the production split was 61/39, and instead of homo-PP the second stage produced propylene-ethylene random copolymer containing 0,5 w-% ethylene. More detailed properties of the material produced in each stage are shown in Table 1. Example A Preparation and properties of broad MWD two stage homo-random-PP copolymer The polymer was polymerized as in Example 1, except that the first stage (loop reactor) produced low MW homo-PP and the second stage high MW propylene-ethylene random copolymer containing about 4 xv-% ethylene. The production split was 41/59. More detailed properties of the material produced in each stage are shown in Table 1. gxarople 5 Preparation and properties of moderately broad MWD two-stage random homo-PP copolymer with another catalyst and higher ethylene content random-PP The polymer was polymerized as in Example 1, except that the catalyst was pre¬pared according to patent US 4,784,983, included by reference, and the high MW random-PP produced in the first stage had higher ethylene content and slightly lower MW. More detailed properties of the material produced in each stage are shown in Table 1. Preparation and properties of medium broad MWD two-stage random homo-PP copolyrner The polymer was polymerized as in Example 1, except that the production split was 59/41, the MW of the random-PP produced in the first stage was adjusted slightly lower and that as external donor, cyclohexyl methyl dimethoxy silane was used. More detailed properties of the material produced in each stage are shown in Table 1. Example? Preparation and properties of moderately broad MWD two-stage random homo-PP copolymer with a higher amount of me homopolymer produced The polymer was polymerized as in Example 1, except that the production split was 42/58. More detailed properties of the material produced in each stage are shown in Table 1. Example 8 Preparation and properties of moderately broad MWD two-stage random homo-PP copolymer with a lower ethylcne content random PP copolymer The polymer was polymerized as in Example I, except that the high MW random PP produced in the first stage had lower ethylene content and the production split was 50/50. More detailed properties of the material produced in each stage are shown in Table 1 Example 9 Preparation and properties of broad MWD two-stage homo-random PP copolymer The polymer was polymerized as in Example 1, except that the first stage (loop reactor) produced low MW homo-PP and the second stage high MW propylene-1-butene-ethylene random copolymer containing about 1.1 w-% 1-butene and 0.6 w-% ethylene. The production split was 50/50. More detailed properties of the material produced in each stage are shown in Table 1. Example 10 Preparation and properties of broad MWD three-stage impact modified random homo-PP copolymer The PP copolymers were produced in a pilot plant having a loop reactor and two fluid bed gas phase reactors connected in series. The catalyst, cocatatyst and donor were fed to the loop reactor. The reaction medium of loop was flashed away before the solid polymer containing the active catalyst entered to the first gas phase. The prepolymerized MgCl2-supported Ti catalyst (prepared according to patent US 5,234,879, included by reference) was used in the polymerization. Cocatalyst was triethyl aluminium (TEA) and external donor cyclohexyl methyl dimethoxy silane. In the first stage (loop reactor) was produced high MW propylene-ethylene random copolymer. The polymerization was continued in the second stage (gas phase reactor) which produced low MW horao-PP, and the third stage (gas phase) produced rubbery ethylene-propylene copolymer. The ethylene/propylene mole ratio in the third stage was 30/70. The production split of the stages in weight fractions was 57/26/17. The polymerization temperature used in all stages was 70°C. The MFR:s measured after the polymerization stages were adjusted with separate hydrogen feeds. More detailed properties of the material produced in each stage are shown in Table 2. Example 11 Preparation and properties of broad MWD three-stage impact modified random homo-PP copolymer having smaller fraction of homo-PP and larger fraction of rubbery copolymer The polymer was polymerized as in Example 7, except that the production split was 63/12/25 and the MW of the random-PP produced in the loop reactor was adjusted lower with small hydrogen feed. The ethylene/propylene mole ratio in the third stage was 36/64. More detailed properties of the material produced in each stage are shown in Table 2. Example 12 Preparation and properties of broad MWD three-stage impact modified random-PP copolymer, with low ethylene random-PP made in the second stage The polymer was polymerized as in Example 8, except that the production split was 58/29/13, and instead of homo-PP the second stage produced low MW propylene-ethylene random copolymer containing 0.5 w-% ethylene. More detailed properties of the material produced in each stage are shown in Table 2. Example 13 Preparation and properties of broad MWD three-stage impact modified homo-random-PP copolymer The polymer was polymerized as in Example 9, except that the first stage (loop reactor) produced low MW homo-PP and the second stage (gas phase reactor) produced high MW propylene-ethylene random copolymer containing about 4 w-% ethylene, and the third stage (gas phase reactor) produced rubbery ethylene-propylene copolymer. The ethylene/propylene mole ratio in the third stage was 33/67. The production split was 36/48/15. As an external donor, dicyclopentane-dimethoxysilane (DCPDMS) was used. More detailed properties of the material produced in each stage are shown in Table 2. Example 14 Preparation and properties of broad MWD two-stage random homo-PP copolymer which is impact modified with melt blended PP block copolymer The polymer composition is a melt blended mixture of 67 w-% of PP random copolymer made according to example 2 and 33 w-% of a impactmodified hetero-phasic PP (MFR2 1.5 g/10 min) having 15 w-% of rubbery propylene-ethylene copolymer. More detailed properties of the material produced in each stage are shown in Table 2, Comparative example 1 Preparation and properties of moderately broad MWD two-stage random-PP copolymer with higher ethylene content of the low MW phase The polymer was polymerized as in Example 3, except that the ethylene content of the low MW polymer produced in the second stage was higher, and the MW of the polymer produced in the fust stage was slightly lower. The external donor was cyclohexylmethyl dimethoxysilane. The production split was 60/40. More detailed properties of the material produced in each stage are shown in Table 1. Comparative example 2 The following material was tested: Borealis commercial PP-pipe grade, RA130E, which is used for hot water pressure pipes. Comparative example 3 Preparation and properties of impact modified low ethylene random-PP copolymer The PP copolymers were produced in a pilot plant having a loop reactor and a fluid bed gas phase reactor connected in series. The catalyst, cocatalyst and donor were fed to the loop reactor. The reaction medium of loop was flashed away before the solid polymer containing the active catalyst entered to the gas phase. The poly¬merization temperature used in both reactors was 70°C. The prepolymerized MgCl2-supported Ti catalyst (prepared according to patent US 5,234,879, included by reference) was used in the polymerization. Cocatalyst was triethyl aluminium (TEA) and external donor dicyclopentanedimethoxysilane (DCPDMS). In the first stage (loop reactor) was produced propylene-ethylene random copolymer of 4% ethylene, and the polymerization was continued in the second stage (gas phase reactor) which produced rubbery propylene-ethylene copolymer. The ethylene/propylene mole ratio in the third stage was 35/65. The production rate in the first stage was 11 kg/h and in the second stage 2.1 kg/h, which means a production split of 84/16. The MFR:s of the first stage and final product were adjusted with separate hydrogen feeds. (Table Removed) More detailed properties of the material produced in each stage are shown in Table 2, Comparative example 4 Preparation and properties of impact-modified propylene-ethylene random copolymer with higher MW of me rubbery phase The polymer was polymerized as in comparative Example 3, except that the rubbery propylene-ethylene copolymer was produced without any hydrogen feed to the gas phase reactor. More detailed properties of the material produced in each stage are shown in Table 2. (Table Removed) 1. A process for the preparation of polypropylene for e.g. pipe, fiber, profile and moulding applications, containing from 1.0 to 10.0% by weight of ethyletie or C4-C10-α-olefm repeating units and having a MFR2 value of between 0.05 and 0.40 g/10 min, by polymerizing propylene and ethylene or a C4-C10-α-olefin in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound and the cocatalyst component of which comprises an organoaluminium compound, optionally an external donor and hydrogen as a molecular weight regulating agent, to give said polypropylene, characterized in that it is a process for the preparation of creep-resistant polypropylene which comprises the following steps in any mutual order: (a) copolymerizing propylene and ethylene or a C4-C10-α-olcfin into a random copolymer at 40 to 110°C using: a catalyst system of the above-mentioned type; a portion of ethylene or C4-C10-α-olefin leading to 1.0 to 10.0% by weight of ethylene or C4-C10-α--olefin repeating units in said random copolymer; and no or a minimal amount of hydrogen leading to a MFR10value of between 0.01 and 5.0 g/10 min for said random copolymer, if this step is performed first, or to a MFR2 value for said polypropylene of between 0.05 and 0.40 g/10 min, if this step is performed after step (b); the proportion of random copolymer of this step being from 20 to 80% by weight of said polypropylene, (b) polymerizing propylene at 40 to 1 10°C using: a catalyst system of the above- mentioned type; no or a minimal portion of ethylene leading to 0.0 to 1.0% by weight of ethylene repeating units in the polymer resulting from this step; and an amount of hydrogen leading to a MFR2 value of between 20 and 1000 g/10 min, for said polymer, if this step is performed first, or to a MFR2 value for said poly¬ propylene of between 0.05 and 0.40 g/10 min, if this step is performed after step (a); the proportion of polymer of this step being from 80 to 20% by weight of said polypropylene. 2. Process according to Claim 1, characterized in that the ordar of steps is 3. Process according to Claim 2, characterized in that said catalyst sysrtfeHto is added to step (a) and the same catalyst system is then used both m step (zftttd (V). 4. Process according to Claim 1, 2 or 3, characterized in that step (a) is per¬ formed In a loop (CSTR) leaului juid alep (b) is performed in (PgNhtthase reactor, whereby any reaction medium used and any unreacted reagents are removed at least partly between step (a) and step (b). 5. Process according to any preceding claim, characterized in that the proportion of copolymer resulting from step (a) and the MFR values of step (a) and step (b) are such that the FRR value (= MFR10/MFR2) of said polypropylene is between 10 and 100, preferentially between 20 and 50. 6. Process according to any preceding claim, characterized in that said catalyst system has been prepared by: (i) providing a procatalyst by reacting a magnesium halide compound, chosen from magnesium chloride, its complex with ethanol and other derivatives of magnesium chloride, with titanium tetrachloride and optionally with an internal donor, exemplified by the diatkyl phthalates, (ii) providing as cocatalyst an organoahuninhrai compound chosen from trialkyl aluminium exemplified by triethyl aluminium, dialkyl aluminium chloride, alkyl aluminium sesquichloride, optionally (iii) providing as at least one external donor an ester of an aromatic acid exempli¬fied by methyl p-methyl benzoate, or an organosilicon compound exemplified by alkoxy silanes or blends thereof, and, optionally (iv) prepolymerizing a small amount of olcfin by contacting the olefin with said procatalyst, cocatalyst and, optionally, the external donor. 7. Process according to any preceding claim, characterized in that in step (a), a portion of ethylene is used, which leads to 1.0 to 7.0% by weight of ethylene units in the random copolymer resulting from this step. 8. Process according to any preceding claim, characterized in that in step (a), no or a minimal amount of hydrogen is used, which leads to a MFR10 value of between 0.05 and 2,0 g/10 min for the random copolymer resulting from this step, if the step is performed first. 9. Process according to any preceding claim, characterized in that the pro¬ portion of random copolymer resulting from step (a) is from 40 to 80% by weight of said polypropylene. 10. Process according to any preceding claim, characterized in that in step (b), no or a minimal amount of ethylene is used, which leads to 0.0 to 0.5% by weight of ethylene repeating units in the polymer resulting from this step. 11. Process according to any preceding claim, characterized in that in step (b), an amount of hydrogen is used, which leads to a MFR2 value of between 30 and 500 g/10 min for the polymer resulting from this step, if it is performed first. 12. Process according to any preceding claim, characterized in that the proportion of polymer resulting from step (b) is from 60 to 20% by weight of said poly¬ propylene. 13. A process for the preparation of elastomer modified polypropylene for e.g. pipe, fiber, film, profile and moulding applications, containing from 1.0 to 30% by weight of ethylene or C4C10-α-olefin repeating units and having a MFR2 value of between 0.05 and 50 g/10 min, by polymerizing propylene and ethylene or a C4- C10-α-olefin in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound and the cocatalyst component of which comprises an organoaluminium compound, and hydrogen as a molecular weight regulating agent, as well as providing an elastomer component, to give said elastomer modified polypropylene, characterized in that it is a process for the preparation of creep-resistant and stiff polypropylene which comprises the following steps: (a) copolymerizing propylene and ethylene or a C4-Cio-a-olcfin into a random copolymer at 40 to 110°C using: a catalyst system of the above-mentioned type; a portion of ethylene or C4C10-α--olefin leading to 1.0 to 10.0% by weight of ethylene or C4C10-α-olefin repeating units in said random copolymer; and no or a minimal amount of hydrogen leading to a MFR10 value of between 0.01 and 5.0 g/10 min for said random copolymer, if this step is performed first, or to a MFR2 value for said polypropylene of between 0.05 and 50 g/10 min, if this step is performed after step (b); the proportion of random copolymer of this step being from 20 to 80% by weight of said polypropylene, (b) polymerizing propylene at 40 to 110°C using: a catalyst system of the above- mentioned type; no or a minimal portion of ethylene leading to 0.0 to 1.0% by weight of ethylene repeating units in the polymer resulting from this step; and an amount of hydrogen leading to a MFK2 value of between 20 and 1000 g/10 min for said polymer, if this step is performed first, or to a MFR2 value for said poly¬ propylene of between 0.05 and 50 g/10 min, if this step is performed after step (a); the proportion of polymer of this step being from 80 to 20% by weight of said polypropylene, and (c) providing a rubbery copolymer (elastomer), the proportion of which is from 5 to 40% by weight of said polypropylene, to give said elastomer modified polypropylene. 14. Process according to Claim 13, characterized in that the order of steps (a) and (b) is (a)=»(b). 15. Process according to Claim 13 or 14, characterized in that said catalyst system is added to step (a) and the same catalyst system is then used both in step (a) and (b). 16. Process according to Claim 13, 14 or 15, characterized in that step (a) is per¬ formed in a loop (CSTR) reactor and step (b) is performed in a gas phase reactor, whereby any reaction medium used and any unreacted reagents are removed at least partly between step (a) and step (b). 17. Process according to any of claims 13 to 16, characterized in that the pro¬ portion of copolymer resulting from step (a) and the MFR values of step (a) and step (b) are such that the FRR value (= MFR10/MFR.2) of said polypropylene is between 10 and 100, preferentially between 20 and 50, 18. Process according to any of claims 13 to 17, characterized in that said catalyst system has been prepared by: (i) providing a procatalyst by reacting a magnesium halide compound, chosen from magnesium chloride, its complex with ethanol and other derivatives of magnesium chloride, with titanium tetrachloride and optionally with an internal donor, exemplified by the dialkyl phthalates, (u) providing as cocatalyst an organoaluminium compound chosen from trialkyl aluminium exemplified by triethyl aluminium, dialkyl aluminium chloride, alkyl aluminium sesquichloride, optionally (iii) providing as at least one external donor an ester of an aromatic acid exempli¬fied by methyl p-methyl benzoate, or an organosilicon compound exemplified by alkoxy silanes or blends thereof, and, optionally (iv) prepolymerizing a small amount of olefin by contacting the olefin with said procatalyst, cocatalyst and, optionally, the external donor. 19. Process according to any of claims 13 to 18, characterized in that in step (a), a portion of ethylene is used, which leads to 1.0 to 7.0% by weight of ethylene units in the random copolymcr resulting from this step, 20. Process according to any of claims 13 to 19, characterized in that in step (a), no or a minimal amount of hydrogen is used, which leads to a MFR^o value of between 0.05 and 2.0 g/10 min for the random copolymer resulting from this step, if the step is performed first. 21. Process according to any of claims 13 to 20, characterized in that the pro¬ portion of random copolyraer resulting from step (a) is from 40 to 80% by weight of said elastomer modified polypropylene. 22. Process according to any of claims 13 to 21, characterized in that in step (b), no or a minimal amount of ethylene is used, which leads to 0 0 to 0.5% by weight of ethylene repeating units in the polymer resulting from this step. 23. Process according to any of claims 13 to 22, characterized in that in step (b), an amount of hydrogen is used, which leads to a MFR2 value of between 30 and 500 g/10 min for the polymer resulting from this step, if it is performed first. 24. Process according to any of claims 13 to 23, characterized in that the pro¬ portion of polymer resulting from step (b) is from 60 to 20% by weight of said elastomer modified polypropylene. 25. A process according to any of claims 13 to 24, characterized in mat step (c) follows steps (a) and (b), preferably in the order (a)=>(b)=>(c). 26. A process according to any of claims 13 to 25, characterized in that in step (c), said elastomer is provided by copolymerizing at least propylene and ethylene into an elastomer. 27. A process according to Claim 26, characterized in that in step (c), ethylene and propylene are copolymerized into an elastomer in such a ratio, that Hie copolymer of step (c) contains from 10 to 70% by weight of ethylene units. 28. A process according to Claim 26 or 27, characterized in that the following conditions are independently chosen for the three-step process: a temperature in step (c) of between 40 and 90°C, said catalyst system is added to step (a) and used in both steps (a), (b) and (c), step (a) is performed in a loop (CSTR) reactor and steps (b) and (c) arc per¬formed in two separate gas phase reactors, the added comonomer portion is adjusted so that the proportion of ethylene repeating units after steps (a) and (b) is from 1 to 4% by weight and the proportion of ethylene repeating units after steps (a), (b) and (c) is from 5 to 15% by weight, in step (c), ethylene and propylene are copolymerized into an elastomer in a molar ratio ethylcne/piopylene of between 3 0/70-50/50. A process according to any of claims 13 to 25, characterized in that in step (c), the elastomer is provided by adding a ready made or natural elastomer to the reaction product of steps (a) and (b). 29. A process according to Claim 29, characterized in that in step (c), the added ready made elastomer is an impact modified polyolefin. 30. A process according to any of claims 13 to 30, characterized in that in step (c) said impact modified polyolefin is an impact-modified heterophasic poly¬ propylene having from 5 to 30% by weight of a propylene-emylene elastomeric copolymer. 31. Creep-resistant polypropylene for e.g. pipe, profile and moulding applications, characterized in that it shows a creep level of 1/5 to 1/2 of regular PP material measured by tensile creep method. 32. Creep-resistant polypropylene according to Claim 32, characterized in that it has been prepared by a process according to one of claims 1 to 31. 33. The use of a creep resistant polypropylene according to Claim 32 or 33 pipes, fibre, film, profiles, moulded articles and foams. 34. . A process for the preparation of polypropylene for e.g. pipe, fiber, profile and moulding applications substantially as hereinbefore described with reference to the foregoing Examples. 35. Creep-resistant polypropylene for e.g. pipe, profile and moulding applications substantially as hereinbefore described with reference to the foregoing Examples.

Full Text

New piping-grade polypropylene composition
The invention relates to a process for the preparation of rigid polypropylene for e.g. pipe, fiber, profile and moulding applications, containing from 1.0 to 10.0% by weight of ethylene repeating units and having a MFR2 value of between 0.05 and 0.40 g/10 min, by polymerizing propylene and ethylene or a C4-CiQ-a-olefin in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound and the cocatalyst component of which comprises an organoaluminium compound, and hydrogen as a molecular weight regulating agent, to give said polypropylene.
The invention also relates to a process for the preparation of elastomer modified polypropylene for e.g. pipe, fiber, profile and moulding applications, containing from 1.0 to 30% by weight of ethylene or a C4-C10-α-olefin repeating units and having a MFR2 value of between 0,05 and 50 g/10 min, by polymerizing propylene and ethylene or a C4-C10-α-olefin in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound and the cocatalyst com¬ponent of which comprises an organoaluminium compound, and hydrogen as a molecular weight regulating agent, as well as providing an elastomer component, to give said elastomer modified polypropylene.
Finally, the invention also relates to a creep-resistant polypropylene made by the above processes and its use-By Melt Flow Rate (MFR) is meant the weight of a polymer extruded through a standard cylindrical die at a standard temperature in a laboratory rheometer carrying a standard piston and load. Thus MFR is a measure of the melt viscosity of a polymer and hence also of its molecular weight. The smaller the MFR, the larger is the molecular weight. It is frequently used for characterizing a polyolefins, e.g. polypropylene, where the standard conditions MFRmi are: temperature 230°C; die dimensions 9.00 mm in length and 2.095 mm in diameter; load of the piston, 2,16 kg (mi=2), 5.0 kg (mi=5), 10.0 kg (mi=10), 21.6 kg (mi-21). See Alger, M.S.M., Polymer Science Dictionary, Elsevier 1990, p. 257. The standard generally used are ISO 1133 C4, ASTM D 1238 and DIN 53735.By Flow Rate Ratio (FRR) is meant the ratio between the Melt Flow Rate (MFR) measured at a standard temperature and with standard die dimensions using a heavy load and the melt flow rate measured at the same temperature with the same die dimensions using a light load. Usually, for propylene polymers are used nominal loads 10.0 kg and 2.16 kg (ISO 1133 C4). The larger the value of the FRR, the broader the molecular weight distribution.
Polypropylene copolymer has many characteristics which makes it desirable for applications like pipes, fittings, moulded articles, foams etc. Polypropylene as piping material is mainly used in non-pressure applications (pipe and fittings) and profiles. There is a small volume used for pressure pipe, mainly hot water and industrial pipes. The good thermal resistance of polypropylene compared to other polyolefins is utilized for the pipe applications. All three main types of propylene polymer, i.e. homopolymers, random copolymers and block copolymers are used. Homopolymevs give the pipe good rigidity but the impact and creep properties are not very good. The block copolymers give good impact properties but the creep properties are like homopolymers due to the homoporymer matrix. Propylene ethylene random copolymers are used for pressure pipe applications for hot water and industrial pipes.
The propylene-ethylene random copolymers for pressure pipes are today produced with high yield Ziegler-Natta catalysts in processes (bulk or gas phase) giving a material having a relatively narrow molecular weight distribution (MWD * Mv/Mn) of about 5, corresponding to a FRR (MFRio/MFRa) of 13-17. The molecular weight (Mw) of the pipe material with melt flow rate (MFR2) of 0.1-0.4 is about 600 000 - 1 000 000. This high molecular weight and the narrow MWD cause problems in compounding and extrusion of pipes. The proccssability of such materials is difficult due to the low shear sensitivity causing unwanted degradation of the material and melt fracture, which is seen as uneven surface and thickness variations of the pipes. In addition the conventional propylene random copolymer pipe materials produced in one phase have not strength enough for the short and long term properties (notch resistance and creep) needed for good pressure pipes.
The processability of the conventional propylene random copolymers can be improved by broadening the MWD using multi-stage polymerization processes. In multi-stage polymerization the MWD of the polymer can be broadened by pro¬ducing different molecular weight polymers in each stage. The MWD of polymer becomes broader when lower molecular weight polymer is reactor-blended into the higher molecular weight polymer adjusting the final MFR by choosing the right
molecular weight and the reactor split in each stage. The molecular weight of the polymer in each step can be controlled by hydrogen which acts as a chain transfer agent. Reactor temperature may be also used for controlling the molecular weight of polymer in each step. Multi-stage polymerization is disclosed e.g. in patent application JP-91048, but the process concerns film grade polypropylene with a final MFR2 of about 1.5.
When the processability is improved by producing broader MWD propylene random copolymer, also the amount of low molecular fraction is increased if the comonomer feeds are the same in each stage. The taste and odour are adversely affected.
By using a concept invented with high yield TiCl4 catalyst it is possible to produce pipe material having improved mechanical and pipe properties and also a good extrudability. The improved strength properties of the material come from a very high molecular weight fraction of Mw k 2000000 g/moi and totally novel comonomer distribution together with a broad molecular weight distribution, hi another embodiment of the invention, an elastomer is provided within this propylene product for increased impact strength.
The embodiment of the invention relating to a non-elastomeric polypropylene product is essentially characterized by what is said in the characterizing part of claim 1. Thus the invented concept is based on the idea of producing a broad MWD and a high molecular weight propylene random copolymer and improved comonomer distribution using high yield catalysts in two or several reactors at different reaction conditions. The comonomers incorporated in long chains as described in this invention destroy the regularity of the chains leading to the more homogenous distribution of the essential tie-chains and entanglements needed for creep properties and toughness in pipe materials.
The low molecular weight fraction contains no or minimal portion of ethylene repeating units in the polymer. Together with the high molecular weight random copolymer fraction this fraction is improving the processability. The no or low ethylene content fraction gives the total polymer the stiffness needed for rigid materials e.g. pipes, profiles and moulding applications.
A homopolymer or a minirandom copolymer (ethylene 2% has a stiffness of The problem with the uneven comonomer distribution with high yield TiCl4 catalysts is solved in a way that the amount of comonomer is split between the reactors. To the reactor where the high molecular weight propylene polymer is pro¬duced is fed more essentially all, comonomer compared to the reactor where the low molecular PP i produced. Higher amounts of comonomer can be fed because the solubility of the high molecular weight polymer is lower. The final comonomer content is adjusted by controlling the comonomer feed into the reactor. The intervals given in this publication always include both limits thereof.
Thus one embodiment of the present invention relates to a process for the preparation of polypropylene for e.g. pipe, fiber, profile and moulding applications. Such a grade of polypropylene has from 1.0 to 10.0% by weight of etbylene or a C4-C10-α-otefra repeating units and has a MFR2 value of between 0.10 and 0.40 g/10 min. The preparation takes place by polymerizing propylene and ethylene or a C4-C10-α-olefin in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound, and a cocatalyst component of which comprises an organoaluminium compound, optionally an external electron donor and hydrogen as a molecular weight regulating agent
It has been found that extremely creep-resistant polypropylene can be prepared by applying the following steps in any mutual order:
(a) copolymerizrag propylene and ethylene or aC4-C10-α-olefin into a random
copolymer at 40 to 110°C using: a catalyst system of the above-mentioned type; a
portion of ethylene or C4-C10-α-olefin leading to 1,0 to 10.0% by weight of
ethylene or C4-C10-α-otefin repeating units in said random copolymer; and no or a
minimal amount of hydrogen leading to a MFR10 value of between 0.01 and 5.0
g/10 min for said random copolymer, if this step is performed first, or to a MFR2
value for said polypropylene of between 0.05 and 0.40 g/10 rain, if this step is
performed after step (b); the proportion of random copolymer of this step being
from 20 to 80% by weight of said polypropylene,
(b) polymerizing propylene at 40 to 110°C using: a catalyst system of the above-
mentioned type; no or a minimal portion of ethylene leading to 0,0 to 1.0% by
weight of ethylene repeating units in the polymer resulting from this step; and an
amount of hydrogen leading U> a MTR2 value of between 20 and 1000 g/10 mio fnr
said polymer, if this step is performed first, or to a MFR2 value for said poly¬
propylene of between 0.05 and 0.40 g/10 min, if this step is performed after step (a);
the proportion of polymer of this step being from 80 to 20% by weight of said polypropylene.
In step (a) a very high molecular weight random copoiymer of propylene and ethylene is prepared, which gives the polypropylene its extremely high shape-resistance, fai step (b), essentially homopolymeric low molecular weight poly¬propylene is prepared, which gives the product good melt-processing properties and improved stiffness.
In the process of me invention the order of steps (a) and (b) can freely be chosen. It is, however, preferable to perform step (a) before step (b). Although, different catalyst systems of the above mentioned type can be used in steps (a) and (b), it is preferable to use the same catalyst system for both steps. According to a preferable embodiment, the catalyst system is added to step (a) and the same catalyst system is then used both in step (a) and (b).
Steps (a) and (b) can be performed in reactors, which may be of any type con¬ventionally used for propylene polymerization and copolymerization, preferentially a loop (CSTR) or gas phase reactor, but it is most preferable to perform one of steps (a) and (b) in a loop (CSTR) reactor and the other step in a gas phase reactor, whereby any reaction medium used and unreactive reagents are removed at least partly between step (a) and step (b). In such a case the procatalyst (also called catalyst in the art), cocatalyst and external donor are fed to the loop reactor. The reaction medium and unreacted reagents such as H2 or comonomer can be removed by known methods between the steps.
It is also preferable to adjust the proportion of copoiymer resulting from step (a) and the MFR values of step (a) and step (b) so that the FRR value (MFRio/MFR2), which is also a measure of the molecular weight distribution, of said polypropylene is between 10 and 100, most preferably between 20 and 50.
The catalyst used hi the present process for the preparation of polypropylene can be any suitable catalyst, which consists of a procatalyst, which is a reaction product of at least tetravalent titanium compound and a magnesium halide compound, and a cocatalyst, which comprises an organoaluminium compound, an optionally external electron donor compound.
Preferentially, said catalyst system has been prepared by:
(i) providing a procatalyst by reacting a magnesium halide compound, chosen from magnesium chloride, its complex with ethanol and other derivatives of magnesium chloride, with titanium tetrachloride and optionally with an internal donor, exemplified by the dialkyl phthalates,
(ii) providing as cocatalyst an organoaluminium compound chosen from trialkyl aluminium exemplified by triethyl aluminium, dialkyl aluminium chloride, alkyl aluminium sesquichloride, optionally
(iii) providing as at least one external donor an ester of an aromatic acid exempli¬fied by methyl p-methyl benzoate, or an organosilicon compound exemplified by alkoxy silanes or blends thereof, and, optionally
(iv) prepolymerizing a small amount of olefin by contacting the olefin with said procatalyst, cocatalyst and, optionally, the external donor.
hi step (a) of the present process, a portion of ethylene is preferably used, which leads to 1.0 to 7.0% by weight of ethylene units in the random copolymer resulting from this step. Further in step (a) preferably no or a minimal amount of hydrogen is used, which leads to a MFRio value of between 0.05 and 2.0 g/min for the random copolymer resulting from mis step, if the step is performed first. Also, the proportion of random copolymer resulting from step (a) is preferably from 40 to 80% by weight of said polypropylene. Thus it can be said, that the polypropylene prepared by the process of the invention contains preferably more random copolymer than low molecular weight homopolymer or minirandom copolymer.
In step (b), low molecular weight essentially homopolymeric propylene is produced. The molecular weight is adjusted by means of hydrogen. If the hydrogen amount is too high, the molecular weight will be too low and the product will be useless as pipe, profile or moulding material. In step (b) an amount of hydrogen is preferably used, which leads to a MFR2 value of between 30 and 500 g/10 min for the polymer resulting from this step, if it performed first.
As it was said before, too much ethylene units in the low molecular weight component leads to difficulties in retaining good stiffness properties of the product. Thus, in step (b) no or a minimal amount of ethylene is used, which preferably leads to 0.0 to 0.5% by weight of ethylene repeating units in the polymer resulting from this step. Prefel'ably, the low molecular weight homopolymer fraction is smaller that the high molecular weight random copolymer fraction, i.e. the proportion nf polymer resulting from step (b) is from 60 to 20% by weight of said polypropylene.
According to another embodiment of the present invention, the invention relates to a process for the preparation of elastomer modified polypropylene for e.g. pipe, fiber, film, foam, profile and moulding applications. Such a grade of polypropylene has from 1.0 to 30% by weight of ethylene or a C4-C10-α-olefin repeating units and has a MFR2 value of between 0.05 and 50 g/10 min. The preparation takes place by polymerizing propylene and ethylene or a C4-C10-α-olefin in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound, and a cocatalyst component of which comprises an organoaluminium compound, and hydrogen as a molecular weight regulating agent, as well as providing an elastomer component.
It has been found that extremely creep-resistant polypropylene can be prepared by applying the following steps:
(a) copolymerizing propylene and ethylene into a random copolymer at 40 to
110'C using: a catalyst system of the above-mentioned type; a portion of ethylene
or C4-C10-α-olefin leading to 1.0 to 10.0% by weight of ethylene or C4-C10-α-
olefin repeating units in said random copolymer; and no or a minimal amount of
hydrogen leading to a MFR10 value of between 0.01 and 5.0 g/10 min for said
random copolymer, if this step is performed first, or to a MFR2 value for said poly¬
propylene of between 0.05 and 50 g/10 min, if this step is performed after step (b);
the proportion of random copolymer of this step being from 20 to 80% by weight of
said polypropylene,
(b) polymerizing propylene at 40 to 110°C using: a catalyst system of the above-
mentioned type; no or a minimal portion of ethylene leading to 0.0 to 1.0% by
weight of ethylene repeating units in the polymer resulting from this step; and an
amount of hydrogen leading to a MFR2 value of between 20 and 1000 g/10 min for
said polymer, if this step is performed first, or to a MFR2 value for said poly¬
propylene of between 0.05 and 50 g/10 min, if this step is performed after step (a);
the proportion of polymer of this step being from 80 to 20% by weight of said
polypropylene, and
(c) providing a rubbery copolymer (elastomer) the proportion of which is from 5
to 40% by weight of said polypropylene.
In step (a) a very high molecular weight random copolymer of propylene and ethylene is prepared, which gives the polypropylene its extremely high shape-resistance. In step (b), essentially homopolymeric low molecular weight poly¬propylene is prepared, which gives the product good melt-processing properties and
improved stiffness. In step (c), the provided rubbeiy copolymet gives better impact resistance,
In the process of the invention the order of steps (a) and (b) can freely be chosen. It isr however, preferable to perform step (a) before step (b). Although different catalyst systems of the above mentioned type can be used in steps (a) and (b), it is preferable to use the same catalyst system for both steps. According to a preferable embodiment, the catalyst system is added to step (a) and the same catalyst system is then used both in step (a) and (b).
Steps (a) and (b) can be performed in reactors, which may be of any type con¬ventionally used for propylene polymerization and copolymerization preferentially a loop (CSTR) or gas phase reactor, but it is most preferable to perform one of steps (a) and (b) in a loop (CSTR) reactor and the other step in a gas phase reactor, whereby any reaction medium used and unreactive reagents are removed at least partly between step (a) and step (b). In such a case the procatalyst (also called catalyst in the art), cocatalyst and external donor is fed to the loop reactor. The reaction medium and uweacted reagents such as H2 or comonomer can be removed by known methods between the steps.
Preferably, steps (a) and (b) are performed so that said polypropylene has a MFR2 value of between 0.1 and 12 g/10 min.
It is also preferable to adjust the proportion of copolyraer resulting from step (a) and the MFR values of step (a) and step (b) so that the FRR value (MFRio/MFR2)7 which is also a measure of the molecular weight distribution, of said polypropylene is between 10 and 100, most preferably between 20 and 50.
The catalyst used in the present process for the preparation of polypropylene can be any suitable catalyst, which consists of a procatalyst, which is a reaction product of at least tetravalent titanium compound and a magnesium halide compound, and a cocatalyst, which comprises an organoaluminium compound, an optionally external electron donor compound.
Preferentially, said catalyst system has been prepared by:
(i) providing a procatalyst by reacting a magnesium halide compound, chosen
from magnesium chloride, its complex with ethanol and other derivatives of
magnesium chloride, with titanium tetrachloride and optionally with an internal donor, exemplified by the dialkyl phthalates,
(ii) providing as cocatalyst an organoaluminium compound chosen from trialkyl aluminium exemplified by triethyl aluminium, dialkyl aluminium chloride, alkyl aluminium sesquichlonde, optionally
(iii) providing as at least one external donor an ester of an aromatic acid exempli¬fied by methyl p-methyl benzoate, or an organosilicon compound exemplified by alkoxy silanes or blends thereof, and, optionally
(iv) prepolymerizing a small amount of olefin by contacting the olefin with said procatalyst, cocatalyst and, optionally, the external donor.
In step (a) of the present process, a portion of ethylene or a C4-Cio-a-olefin is preferably used, which leads to 1.0 to 7.0% by weight of ethylene or a C4-Cjo-a-olefin units in the random copolymer resulting from this step. Further in step (a) preferably no or a minimal amount of hydrogen is used, which leads to a MFRjQ value of between 0.05 and 2.0 g/min for the random copolymer resulting from this step, if the step is performed first. Also, the proportion of random copolymer resulting from step (a) is preferably from 40 to 80% by weight of said poly¬propylene. Thus it can be said, that the polypropylene prepared by the process of the invention contains preferably more random copolymer than low molecular weight homopolymer or minirandora copolymer.
In step (b), low molecular weight essentially homopolymeric or minirandom (having little comonomer) propylene is produced. The molecular weight is adjusted by means of hydrogen. If the hydrogen amount is too high, the molecular weight will be too low and the product will be useless as pipe, profile or moulding material. In step (b) an amount of hydrogen is preferably used, which leads to a MFR 2 value of between 30 and 500 g/10 min for the polymer resulting from this step, if it performed first.
As it was said before, too much ethylene units in the low molecular weight component leads to difficulties in retaining the stiffness properties of the product. Thus, in step (b) no or a minimal amount of ethylene is used, which preferably leads to 0.0 to 0.5% by weight of ethylene repeating units in the polymer resulting from this step. Preferably, the low molecular weight homopolymer fraction is smaller that the high molecular weight random copolymer fraction, Le. the proportion of polymer resulting from step (b) ia from 60 to 20?4 by weight of said polypropylene.
The step (c) of providing an elastomer preferably follows steps (a) and (b) and, most preferentially, the order of steps is (a) => (b) => (c).
The step (c) of providing an elastomer can be performed in two ways. According to the first and more preferable way, said elastomer is provided by copolymerizing at least propylene and ethylene into an elastomer. The conditions for the copolymerizatkm are within the limits of conventional EPM production conditions such as they are disclosed e.g. in Encyclopedia of Polymer Science and Engineering, Second Edition, Vol. 6, p. 545-558. A rubbery product is formed if the ethylene repeating unit content in the polymer is within a certain interval. Thus, preferentially, in step (c), ethylene and propylene are copolymerized into an elastomer in such a ratio that the copolymer step (c) contains from 10 to 70% by weight of ethylene units. Most preferably, the ethylene unit content is from 30 to 50% by weight of the copolymeric propylene/ethylene elastomer.
According to preferable embodiments of the invention, the following conditions are independently chosen for the three step process:
a temperature in step (c) of between 40 and 90°C,
said catalyst system is added to step (a) and used in both steps (a), (b) and (c),
step (a) is performed in a loop (CSTR) reactor and steps (b) and (c) are performed in two separate gas phase reactors,
the added comonomer portion is adjusted so that the proportion of ethylene repeating units after steps (a) and (b) is from 1 to 4% by weight and the proportion of ethylene repeating units after steps (a), (b) and (c) is from 5 to 15% by weight,
in step (c), ethylene and propylene are copolymerized into an elastomer in a molar ratio ethylene/propylene of between 30/70-50/50.
According to another embodiment of the claimed process, the elastomer in step (c) is provided by adding a ready-made or natural elastomer to the reaction product of steps (a) and (b), most preferably an impact modified heterophasic polypropylene having from 15 to 50% by weight of a propylene-ethylene elastomeric copolymer.
As polypropylene for pipe, profile and moulding applications has not before been prepared with such a good shape preservance, the invention also relates to an extremely creep-resistant polypropylene for said applications. The creep resistance can be measured by registering the deflection of the material during 500-1000 h using 7.3 ar 6.5 MP& load at 60°C. This new material ehows a creep level of I/*? to 1/2 of regular PP (pipe grade) material comparable to e.g. the PP material of
comparative example 9, This is a sensational result and can open new application in e.g. piping.
According to one embodiment of the invention, the creep-resistant polypropylene has been made according to the above described process for its preparation. According to another embodiment of the invention, the use of the above mentioned polypropylene is claimed, which use is directed to pipes, profiles, moulded articles and foams, fibres and films.
In addition to ethylene and propylene, the process and the polypropylene according to the invention can contain from 0.0 to 10.0% by weight of any other olefin such as butene-1, 4-raethyl-pentene-l, hexene-1, octene-1 and decene-1 or combinations of them.
The stiffness of this material is higher than that for materials produced with about the same comonomer content in several reactors or in only one reactor without loosing the impact. That is seen best when comparing the embodiment examples I to 10 with comparative examples 1 to 3 which are produced in the same conditions but with different ethylene feed splits. The entanglements and tie-chains of the high molecular fraction in the material give the material better pipe properties especially higher tensile strength tensile modulus charpy impact strength, and lower creep under load. The invented copolymers give also longer time to failure at same hoop stress levels in standard pipe pressure tests than the conventionally produced random pipe material.
The invention is in the following illuminated by the following examples and comparative examples.
Examples
The following tests and preparations were made:
Mechanical tests from 4 mm compression moulded plaques. The specimens were
according to ISO 527.
Tensile strength according to ISO 527 (cross head speed - 50 mm/min).
Tensile modules according to ISO 527 (cross head speed = 1 mm/rain).
Charpy, notched impact according to ISO 179/leA.
Creep test is a Borealis tensile-creep-method for ranking of pipe materials. In the
method a constant stress is applied to a specimen (a modified ISO dumb bell =120
mm long, thickness = 2 mm). The test temperature = 60°C (oven) and the stress =
7.3 mPa (for PP materials).
The increase of strain with time is recorded 500 to 1000 h.
The creep is defined as the elongation at 100 h in mm units corresponding to
stiffness and the slope between 100 h and 400 h in angle units.
This creep resistance test method is comparable to e.g. ISO 899-1, DIN 53444 and
ASTM2990.
Example 1
Preparation and properties of high MW very broad MWD two-stage random homo-PPcopolymer
The PP copolyraers were produced in a pilot plant having a loop reactor and a fluid bed gas phase reactor connected in series. The catalyst, cocatalyst and donor were fed to the loop reactor. The reaction medium of loop was flashed away before the solid polymer containing the active catalyst entered to the gas phase.
The prepolymerized MgCl2-supported Ti catalyst (prepared according to patent US 5,234,879, included by reference) was used in the polymerization. Cocatalyst was triethyl aluminium (TEA) and external donor dicyclopentanedimethoxysilane (DCPDMS). Al/Ti mole ratio was 150 and Al/donor mole ratio 5.
In the first stage (loop reactor) was produced high MW propylene-ethylene random copolymer, and die polymerization was continued in the second stage (gas phase reactor) which produced low MW homo-PP. The polymerization temperature used in both stages was 70°C. The production rate was 6 kg/h for the first stage and 4 kg/h for the second stage, which means a production split of 60/40. The MFR:s of the first stage and final product were adjusted with separate hydrogen feeds.
More detailed properties of the material produced in each stage are shown in Table 1.
trample 2
Preparation and properties of moderately broad MWD two-stage random homo-PP copolymer
The polymer was polymerized as in example I, except that the production split was 80/20 and the MW of the random PP produced in the first stage was adjusted slightly lower with hydrogen feed. More detailed properties of the material pro¬duced in each stage are shown in Table 1.
pxample 3
Preparation and properties of very broad MWD two-stage random minirandotn-PP copolymer
The polymer was polymerized as in Example 1, except that the production split was 61/39, and instead of homo-PP the second stage produced propylene-ethylene random copolymer containing 0,5 w-% ethylene. More detailed properties of the material produced in each stage are shown in Table 1.
Example A
Preparation and properties of broad MWD two stage homo-random-PP copolymer
The polymer was polymerized as in Example 1, except that the first stage (loop reactor) produced low MW homo-PP and the second stage high MW propylene-ethylene random copolymer containing about 4 xv-% ethylene. The production split was 41/59. More detailed properties of the material produced in each stage are shown in Table 1.
gxarople 5
Preparation and properties of moderately broad MWD two-stage random homo-PP copolymer with another catalyst and higher ethylene content random-PP
The polymer was polymerized as in Example 1, except that the catalyst was pre¬pared according to patent US 4,784,983, included by reference, and the high MW random-PP produced in the first stage had higher ethylene content and slightly lower MW. More detailed properties of the material produced in each stage are shown in Table 1.
Preparation and properties of medium broad MWD two-stage random homo-PP copolyrner
The polymer was polymerized as in Example 1, except that the production split was 59/41, the MW of the random-PP produced in the first stage was adjusted slightly lower and that as external donor, cyclohexyl methyl dimethoxy silane was used. More detailed properties of the material produced in each stage are shown in Table 1.
Example?
Preparation and properties of moderately broad MWD two-stage random homo-PP copolymer with a higher amount of me homopolymer produced
The polymer was polymerized as in Example 1, except that the production split was 42/58. More detailed properties of the material produced in each stage are shown in Table 1.
Example 8
Preparation and properties of moderately broad MWD two-stage random homo-PP copolymer with a lower ethylcne content random PP copolymer
The polymer was polymerized as in Example I, except that the high MW random PP produced in the first stage had lower ethylene content and the production split was 50/50. More detailed properties of the material produced in each stage are shown in Table 1
Example 9
Preparation and properties of broad MWD two-stage homo-random PP copolymer
The polymer was polymerized as in Example 1, except that the first stage (loop reactor) produced low MW homo-PP and the second stage high MW propylene-1-butene-ethylene random copolymer containing about 1.1 w-% 1-butene and 0.6
w-% ethylene. The production split was 50/50. More detailed properties of the material produced in each stage are shown in Table 1.
Example 10
Preparation and properties of broad MWD three-stage impact modified random homo-PP copolymer
The PP copolymers were produced in a pilot plant having a loop reactor and two fluid bed gas phase reactors connected in series. The catalyst, cocatatyst and donor were fed to the loop reactor. The reaction medium of loop was flashed away before the solid polymer containing the active catalyst entered to the first gas phase.
The prepolymerized MgCl2-supported Ti catalyst (prepared according to patent US 5,234,879, included by reference) was used in the polymerization. Cocatalyst was triethyl aluminium (TEA) and external donor cyclohexyl methyl dimethoxy silane.
In the first stage (loop reactor) was produced high MW propylene-ethylene random copolymer. The polymerization was continued in the second stage (gas phase reactor) which produced low MW horao-PP, and the third stage (gas phase) produced rubbery ethylene-propylene copolymer. The ethylene/propylene mole ratio in the third stage was 30/70. The production split of the stages in weight fractions was 57/26/17. The polymerization temperature used in all stages was 70°C. The MFR:s measured after the polymerization stages were adjusted with separate hydrogen feeds.
More detailed properties of the material produced in each stage are shown in Table 2. Example 11
Preparation and properties of broad MWD three-stage impact modified random homo-PP copolymer having smaller fraction of homo-PP and larger fraction of rubbery copolymer
The polymer was polymerized as in Example 7, except that the production split was 63/12/25 and the MW of the random-PP produced in the loop reactor was adjusted lower with small hydrogen feed. The ethylene/propylene mole ratio in the third
stage was 36/64. More detailed properties of the material produced in each stage are shown in Table 2.
Example 12
Preparation and properties of broad MWD three-stage impact modified random-PP copolymer, with low ethylene random-PP made in the second stage
The polymer was polymerized as in Example 8, except that the production split was 58/29/13, and instead of homo-PP the second stage produced low MW propylene-ethylene random copolymer containing 0.5 w-% ethylene. More detailed properties of the material produced in each stage are shown in Table 2.
Example 13
Preparation and properties of broad MWD three-stage impact modified homo-random-PP copolymer
The polymer was polymerized as in Example 9, except that the first stage (loop reactor) produced low MW homo-PP and the second stage (gas phase reactor) produced high MW propylene-ethylene random copolymer containing about 4 w-% ethylene, and the third stage (gas phase reactor) produced rubbery ethylene-propylene copolymer. The ethylene/propylene mole ratio in the third stage was 33/67. The production split was 36/48/15. As an external donor, dicyclopentane-dimethoxysilane (DCPDMS) was used. More detailed properties of the material produced in each stage are shown in Table 2.
Example 14
Preparation and properties of broad MWD two-stage random homo-PP copolymer which is impact modified with melt blended PP block copolymer
The polymer composition is a melt blended mixture of 67 w-% of PP random copolymer made according to example 2 and 33 w-% of a impactmodified hetero-phasic PP (MFR2 1.5 g/10 min) having 15 w-% of rubbery propylene-ethylene copolymer. More detailed properties of the material produced in each stage are shown in Table 2,
Comparative example 1
Preparation and properties of moderately broad MWD two-stage random-PP copolymer with higher ethylene content of the low MW phase
The polymer was polymerized as in Example 3, except that the ethylene content of the low MW polymer produced in the second stage was higher, and the MW of the polymer produced in the fust stage was slightly lower. The external donor was cyclohexylmethyl dimethoxysilane. The production split was 60/40. More detailed properties of the material produced in each stage are shown in Table 1.
Comparative example 2
The following material was tested: Borealis commercial PP-pipe grade, RA130E, which is used for hot water pressure pipes.
Comparative example 3
Preparation and properties of impact modified low ethylene random-PP copolymer
The PP copolymers were produced in a pilot plant having a loop reactor and a fluid bed gas phase reactor connected in series. The catalyst, cocatalyst and donor were fed to the loop reactor. The reaction medium of loop was flashed away before the solid polymer containing the active catalyst entered to the gas phase. The poly¬merization temperature used in both reactors was 70°C.
The prepolymerized MgCl2-supported Ti catalyst (prepared according to patent US 5,234,879, included by reference) was used in the polymerization. Cocatalyst was triethyl aluminium (TEA) and external donor dicyclopentanedimethoxysilane (DCPDMS).
In the first stage (loop reactor) was produced propylene-ethylene random copolymer of 4% ethylene, and the polymerization was continued in the second stage (gas phase reactor) which produced rubbery propylene-ethylene copolymer. The ethylene/propylene mole ratio in the third stage was 35/65. The production rate in the first stage was 11 kg/h and in the second stage 2.1 kg/h, which means a production split of 84/16. The MFR:s of the first stage and final product were adjusted with separate hydrogen feeds.

(Table Removed)
More detailed properties of the material produced in each stage are shown in Table
2,
Comparative example 4
Preparation and properties of impact-modified propylene-ethylene random copolymer with higher MW of me rubbery phase
The polymer was polymerized as in comparative Example 3, except that the rubbery propylene-ethylene copolymer was produced without any hydrogen feed to the gas phase reactor. More detailed properties of the material produced in each stage are shown in Table 2.
(Table Removed)

1. A process for the preparation of polypropylene for e.g. pipe, fiber, profile and moulding applications, containing from 1.0 to 10.0% by weight of ethyletie or C4-C10-α-olefm repeating units and having a MFR2 value of between 0.05 and 0.40 g/10 min, by polymerizing propylene and ethylene or a C4-C10-α-olefin in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound and the cocatalyst component of which comprises an organoaluminium compound, optionally an external donor and hydrogen as a molecular weight regulating agent, to give said polypropylene, characterized in that it is a process for the preparation of creep-resistant polypropylene which comprises the following steps in any mutual order:
(a) copolymerizing propylene and ethylene or a C4-C10-α-olcfin into a random
copolymer at 40 to 110°C using: a catalyst system of the above-mentioned type; a
portion of ethylene or C4-C10-α-olefin leading to 1.0 to 10.0% by weight of
ethylene or C4-C10-α--olefin repeating units in said random copolymer; and no or a
minimal amount of hydrogen leading to a MFR10value of between 0.01 and 5.0
g/10 min for said random copolymer, if this step is performed first, or to a MFR2
value for said polypropylene of between 0.05 and 0.40 g/10 min, if this step is
performed after step (b); the proportion of random copolymer of this step being
from 20 to 80% by weight of said polypropylene,
(b) polymerizing propylene at 40 to 1 10°C using: a catalyst system of the above-
mentioned type; no or a minimal portion of ethylene leading to 0.0 to 1.0% by
weight of ethylene repeating units in the polymer resulting from this step; and an
amount of hydrogen leading to a MFR2 value of between 20 and 1000 g/10 min, for
said polymer, if this step is performed first, or to a MFR2 value for said poly¬
propylene of between 0.05 and 0.40 g/10 min, if this step is performed after step (a);
the proportion of polymer of this step being from 80 to 20% by weight of said
polypropylene.
2. Process according to Claim 1, characterized in that the ordar of steps is
3. Process according to Claim 2, characterized in that said catalyst sysrtfeHto is
added to step (a) and the same catalyst system is then used both m step (zftttd (V).
4. Process according to Claim 1, 2 or 3, characterized in that step (a) is per¬
formed In a loop (CSTR) leaului juid alep (b) is performed in (PgNhtthase reactor,
whereby any reaction medium used and any unreacted reagents are removed at least partly between step (a) and step (b).
5. Process according to any preceding claim, characterized in that the proportion
of copolymer resulting from step (a) and the MFR values of step (a) and step (b) are
such that the FRR value (= MFR10/MFR2) of said polypropylene is between 10 and
100, preferentially between 20 and 50.
6. Process according to any preceding claim, characterized in that said catalyst
system has been prepared by:
(i) providing a procatalyst by reacting a magnesium halide compound, chosen from magnesium chloride, its complex with ethanol and other derivatives of magnesium chloride, with titanium tetrachloride and optionally with an internal donor, exemplified by the diatkyl phthalates,
(ii) providing as cocatalyst an organoahuninhrai compound chosen from trialkyl aluminium exemplified by triethyl aluminium, dialkyl aluminium chloride, alkyl aluminium sesquichloride, optionally
(iii) providing as at least one external donor an ester of an aromatic acid exempli¬fied by methyl p-methyl benzoate, or an organosilicon compound exemplified by alkoxy silanes or blends thereof, and, optionally
(iv) prepolymerizing a small amount of olcfin by contacting the olefin with said procatalyst, cocatalyst and, optionally, the external donor.
7. Process according to any preceding claim, characterized in that in step (a), a
portion of ethylene is used, which leads to 1.0 to 7.0% by weight of ethylene units
in the random copolymer resulting from this step.
8. Process according to any preceding claim, characterized in that in step (a), no
or a minimal amount of hydrogen is used, which leads to a MFR10 value of
between 0.05 and 2,0 g/10 min for the random copolymer resulting from this step, if
the step is performed first.
9. Process according to any preceding claim, characterized in that the pro¬
portion of random copolymer resulting from step (a) is from 40 to 80% by weight of
said polypropylene.
10. Process according to any preceding claim, characterized in that in step (b), no
or a minimal amount of ethylene is used, which leads to 0.0 to 0.5% by weight of
ethylene repeating units in the polymer resulting from this step.
11. Process according to any preceding claim, characterized in that in step (b), an
amount of hydrogen is used, which leads to a MFR2 value of between 30 and 500
g/10 min for the polymer resulting from this step, if it is performed first.
12. Process according to any preceding claim, characterized in that the proportion
of polymer resulting from step (b) is from 60 to 20% by weight of said poly¬
propylene.
13. A process for the preparation of elastomer modified polypropylene for e.g.
pipe, fiber, film, profile and moulding applications, containing from 1.0 to 30% by
weight of ethylene or C4C10-α-olefin repeating units and having a MFR2 value of
between 0.05 and 50 g/10 min, by polymerizing propylene and ethylene or a C4-
C10-α-olefin in the presence of a catalyst system, the procatalyst component of which is a reaction product of at least a tetravalent titanium compound and a magnesium halide compound and the cocatalyst component of which comprises an organoaluminium compound, and hydrogen as a molecular weight regulating agent, as well as providing an elastomer component, to give said elastomer modified polypropylene, characterized in that it is a process for the preparation of creep-resistant and stiff polypropylene which comprises the following steps:
(a) copolymerizing propylene and ethylene or a C4-Cio-a-olcfin into a random
copolymer at 40 to 110°C using: a catalyst system of the above-mentioned type; a
portion of ethylene or C4C10-α--olefin leading to 1.0 to 10.0% by weight of
ethylene or C4C10-α-olefin repeating units in said random copolymer; and no or a
minimal amount of hydrogen leading to a MFR10 value of between 0.01 and 5.0
g/10 min for said random copolymer, if this step is performed first, or to a MFR2
value for said polypropylene of between 0.05 and 50 g/10 min, if this step is
performed after step (b); the proportion of random copolymer of this step being
from 20 to 80% by weight of said polypropylene,
(b) polymerizing propylene at 40 to 110°C using: a catalyst system of the above-
mentioned type; no or a minimal portion of ethylene leading to 0.0 to 1.0% by
weight of ethylene repeating units in the polymer resulting from this step; and an
amount of hydrogen leading to a MFK2 value of between 20 and 1000 g/10 min for
said polymer, if this step is performed first, or to a MFR2 value for said poly¬
propylene of between 0.05 and 50 g/10 min, if this step is performed after step (a);
the proportion of polymer of this step being from 80 to 20% by weight of said
polypropylene, and
(c) providing a rubbery copolymer (elastomer), the proportion of which is from 5
to 40% by weight of said polypropylene, to give said elastomer modified
polypropylene.
14. Process according to Claim 13, characterized in that the order of steps (a) and
(b) is (a)=»(b).
15. Process according to Claim 13 or 14, characterized in that said catalyst
system is added to step (a) and the same catalyst system is then used both in step (a)
and (b).
16. Process according to Claim 13, 14 or 15, characterized in that step (a) is per¬
formed in a loop (CSTR) reactor and step (b) is performed in a gas phase reactor,
whereby any reaction medium used and any unreacted reagents are removed at least
partly between step (a) and step (b).
17. Process according to any of claims 13 to 16, characterized in that the pro¬
portion of copolymer resulting from step (a) and the MFR values of step (a) and
step (b) are such that the FRR value (= MFR10/MFR.2) of said polypropylene is
between 10 and 100, preferentially between 20 and 50,
18. Process according to any of claims 13 to 17, characterized in that said
catalyst system has been prepared by:
(i) providing a procatalyst by reacting a magnesium halide compound, chosen from magnesium chloride, its complex with ethanol and other derivatives of magnesium chloride, with titanium tetrachloride and optionally with an internal donor, exemplified by the dialkyl phthalates,
(u) providing as cocatalyst an organoaluminium compound chosen from trialkyl aluminium exemplified by triethyl aluminium, dialkyl aluminium chloride, alkyl aluminium sesquichloride, optionally
(iii) providing as at least one external donor an ester of an aromatic acid exempli¬fied by methyl p-methyl benzoate, or an organosilicon compound exemplified by alkoxy silanes or blends thereof, and, optionally
(iv) prepolymerizing a small amount of olefin by contacting the olefin with said procatalyst, cocatalyst and, optionally, the external donor.
19. Process according to any of claims 13 to 18, characterized in that in step (a),
a portion of ethylene is used, which leads to 1.0 to 7.0% by weight of ethylene units
in the random copolymcr resulting from this step,
20. Process according to any of claims 13 to 19, characterized in that in step (a),
no or a minimal amount of hydrogen is used, which leads to a MFR^o value of
between 0.05 and 2.0 g/10 min for the random copolymer resulting from this step, if
the step is performed first.
21. Process according to any of claims 13 to 20, characterized in that the pro¬
portion of random copolyraer resulting from step (a) is from 40 to 80% by weight of
said elastomer modified polypropylene.
22. Process according to any of claims 13 to 21, characterized in that in step (b),
no or a minimal amount of ethylene is used, which leads to 0 0 to 0.5% by weight of
ethylene repeating units in the polymer resulting from this step.
23. Process according to any of claims 13 to 22, characterized in that in step (b),
an amount of hydrogen is used, which leads to a MFR2 value of between 30 and
500 g/10 min for the polymer resulting from this step, if it is performed first.
24. Process according to any of claims 13 to 23, characterized in that the pro¬
portion of polymer resulting from step (b) is from 60 to 20% by weight of said
elastomer modified polypropylene.
25. A process according to any of claims 13 to 24, characterized in mat step (c)
follows steps (a) and (b), preferably in the order (a)=>(b)=>(c).
26. A process according to any of claims 13 to 25, characterized in that in step
(c), said elastomer is provided by copolymerizing at least propylene and ethylene
into an elastomer.
27. A process according to Claim 26, characterized in that in step (c), ethylene
and propylene are copolymerized into an elastomer in such a ratio, that Hie
copolymer of step (c) contains from 10 to 70% by weight of ethylene units.
28. A process according to Claim 26 or 27, characterized in that the following
conditions are independently chosen for the three-step process:
a temperature in step (c) of between 40 and 90°C,
said catalyst system is added to step (a) and used in both steps (a), (b) and (c),
step (a) is performed in a loop (CSTR) reactor and steps (b) and (c) arc per¬formed in two separate gas phase reactors,
the added comonomer portion is adjusted so that the proportion of ethylene repeating units after steps (a) and (b) is from 1 to 4% by weight and the proportion of ethylene repeating units after steps (a), (b) and (c) is from 5 to 15% by weight,
in step (c), ethylene and propylene are copolymerized into an elastomer in a molar ratio ethylcne/piopylene of between 3 0/70-50/50.
A process according to any of claims 13 to 25, characterized in that in step
(c), the elastomer is provided by adding a ready made or natural elastomer to the
reaction product of steps (a) and (b).
29. A process according to Claim 29, characterized in that in step (c), the added
ready made elastomer is an impact modified polyolefin.
30. A process according to any of claims 13 to 30, characterized in that in step
(c) said impact modified polyolefin is an impact-modified heterophasic poly¬
propylene having from 5 to 30% by weight of a propylene-emylene elastomeric
copolymer.
31. Creep-resistant polypropylene for e.g. pipe, profile and moulding applications,
characterized in that it shows a creep level of 1/5 to 1/2 of regular PP material
measured by tensile creep method.
32. Creep-resistant polypropylene according to Claim 32, characterized in that it
has been prepared by a process according to one of claims 1 to 31.
33. The use of a creep resistant polypropylene according to Claim 32 or 33
pipes, fibre, film, profiles, moulded articles and foams.
34. . A process for the preparation of polypropylene for e.g. pipe, fiber, profile
and moulding applications substantially as hereinbefore described with reference
to the foregoing Examples.
35. Creep-resistant polypropylene for e.g. pipe, profile and moulding
applications substantially as hereinbefore described with reference to the foregoing
Examples.

Documents:

993-del-1997-abstract.pdf

993-del-1997-claims.pdf

993-del-1997-correspondence-others.pdf

993-del-1997-correspondence-po.pdf

993-del-1997-description (complete).pdf

993-del-1997-form-1.pdf

993-del-1997-form-19.pdf

993-del-1997-form-2.pdf

993-del-1997-form-26.pdf

993-del-1997-form-4.pdf

993-del-1997-form-6.pdf

993-del-1997-petition-137.pdf

993-del-1997-petition-138.pdf

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Patent Number

232384

Indian Patent Application Number

993/DEL/1997

PG Journal Number

13/2009

Publication Date

27-Mar-2009

Grant Date

16-Mar-2009

Date of Filing

17-Apr-1997

Name of Patentee

BOREALIS A/S

Applicant Address

LYNGBY HOVEDGADE 96, DK-2800 LYNGBY, DENMARK.

Inventors:

#	Inventor's Name	Inventor's Address
1	HARKONEN, MIKA	VANGA MYLLYPOLKU 18C, FIN-01360 VANTAA, FINLAND
2	MALM, Bo	HARJUVIITA 16A 27, FIN-021140 ESPOO, FINLAND.
3	NYMARK, ANDERS	KAHDEKSANTOISTAMAENKUJA 5, FIN-06100 PORVOO, FINLAND.

PCT International Classification Number

C08F 297/06

PCT International Application Number

N/A

PCT International Filing date

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1	961722	1996-04-19	Finland