Patent Application
20230174759
The present invention is directed to a fiber reinforced composite comprising a polypropylene having very narrow molecular weight distribution (MWD) and glass fibers, to the manufacture of said fiber reinforced composite as well as to articles comprising said fiber reinforced composite.
Polypropylene is a material used in a wide variety of technical fields, and reinforced polypropylenes have in particular gained relevance in fields previously exclusively relying on non-polymeric materials, in particular metals. One particular example of reinforced polypropylenes are glass fibre reinforced polypropylene composites. Such materials enable tailoring of the properties of the composites by selecting the type of polypropylene, the amount of glass fibre and sometimes by selecting the type of compatibilizer used.
Accordingly, nowadays glass fibre reinforced polypropylene composites are a well-established materials for applications requiring high stiffness, heat deflection resistance and impact resistance (examples include automotive components with a load-bearing function in the engine compartment, support parts for polymer body panels, washing machine and dishwasher components). However, one drawback of the commercial available fibre reinforced polypropylene composites is their rather high emission caused by a rather high amount of oligomers obtained as side product in the polymerization process. Further, fibre reinforced polypropylene composites with rather high melt flow rate MFR2, is normally reached by visbreaking resp. controlled degradation of Ziegler-Natta produced polypropylene. Such material contains an even higher amount of emissions due to the degradation process and the residues of the initiator.
Accordingly, there is the need for glass fibre reinforced polypropylene composites being stiff, having rather high heat deflection resistance, being well processable and further having very low emissions.
The finding of the present invention is that the fibre reinforced polypropylene composite must comprise a polypropylene having very narrow molecular weight distribution and rather high melting temperature. Preferably, the polypropylene has been visbroken.
Accordingly the present invention is directed to a fiber reinforced polypropylene composite having a melt flow rate MFR2 (230° C., 2.16 kg) measured according to ISO 1133 in the range of 10 to 100 g/10 min, preferably in the range of 15 to 50 g/10 min, and comprising
The present invention is especially directed to a fiber reinforced polypropylene composite having a melt flow rate MFR2 (230° C., 2.16 kg) measured according to ISO 1133 in the range of 10 to 50 g/10 min, preferably in the range of 15 to 50 g/10 min, and consists of
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the propylene homopolymer [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the propylene homopolymer determined by gel permeation chromatography (GPC).
Preferred embodiments of the fiber reinforced composite are defined in the dependent claims of the invention.
The present invention is further directed to a process for the manufacture of the fiber reinforced composite as defined in the present invention comprising the steps of adding
Preferably, the polypropylene according to this invention is obtained by polymerizing propylene and optionally ethylene, more preferably only propylene, in the presence of the metallocene catalyst having the formula (I)
wherein each R1 are independently the same or can be different and are hydrogen or a linear or branched C1-C6 alkyl group, whereby at least on R1 per phenyl group is not hydrogen,
R′ is a C1-C10 hydrocarbyl group, preferably a C1-C4 hydrocarbyl group and more preferably a methyl group and
X independently is a hydrogen atom, a halogen atom, C1-C6 alkoxy group, C1-C6 alkyl group, phenyl or benzyl group
and subsequent the polypropylene has been visbroken.
It is preferred that for the above formula (I) X is chlorine, benzyl or a methyl group.
Preferably, both X groups of formula (I) are the same. The most preferred options for X of formula (I) are two chlorides, two methyl or two benzyl groups, especially two chlorides.
Furthermore, the invention is directed to an article, preferably automotive article, comprising at least 90 wt.-% of the fiber reinforced composite according to the present invention.
In the following, the invention is described in more detail.
The Fiber Reinforced Composite
The present invention is directed to a fiber reinforced composite comprising a polypropylene, glass fibers and a compatibilizer. The fiber reinforced composite is understood as known in the art. That is, the polypropylene forms the continuous phase in which the glass fibers are embedded. In case the glass fibers are short glass fibers, said fibers are dispersed in the polypropylene wherein the polypropylene acts as the continuous phase. The compatibilizer improves the adhesion between the non-polar polypropylene and the polar glass fibers.
Accordingly the present invention is directed to a fiber reinforced polypropylene composite having a melt flow rate MFR2 (230° C., 2.16 kg) measured according to ISO 1133 in the range of 10 to 100 g/10 min, preferably in the range of 15 to 50 g/10 min, and comprising
The polypropylene, the glass fibers as well as the compatibilizer are described in more detail below.
Beside the three components typical additives may be present which for instance are added to enhance the lifetime of the polypropylene, i.e. antioxidants (see definition of additives below).
Thus in a preferred embodiment the fiber reinforced composite according to this invention has a melt flow rate MFR2 (230° C., 2.16 kg) measured according to ISO 1133 in the range of 10 to 100 g/10 min, preferably in the range of 15 to 50 g/10 min, and comprises
The fiber reinforced composition preferably does not contain an elastomeric polymer. An elastomeric polymer is understood as a polymer which does not form a continuous phase within the polypropylene. In other words, an elastomeric polymer is dispersed in the polypropylene, i.e. forms inclusion in the polypropylene. A polymer containing an elastomeric polymer as inclusions as a second phase would by contrast be called heterophasic and is preferably not part of the present invention. The presence of second phases or the so-called inclusions are for instance visible by high resolution microscopy, like electron microscopy or atomic force microscopy, or by dynamic mechanical thermal analysis (DMTA). Specifically in DMTA the presence of a multiphase structure can be identified by the presence of at least two distinct glass transition temperatures.
Therefore in a specific embodiment the fiber reinforced composite according to this invention has a melt flow rate MFR2 (230° C., 2.16 kg) measured according to ISO 1133 in the range of 10 to 100 g/10 min, preferably in the range of 15 to 50 g/10 min, and consists of
The fiber reinforced composite according to this invention is especially featured by low emission. Accordingly it is preferred that the fiber reinforced composite has a VOC (volatile organic compounds) value determined according to VDA 278 October 2011 of below 6.0 μg/g, more preferably in the range of 0.05 to below 6.0 μg/g, still more preferably in the range of 0.05 to 3.0 μg/g.
Additionally or alternatively to the requirement of the previous paragraph the fiber reinforced composite has an FOG (low volatility or condensable organic compounds) value determined according to VDA 278 October 2011 of below 40 μg/g, more preferably in the range of 5 to 40 μg/g, still more preferably in the range of 10 to 30 μg/g.
It is further preferred that the fiber reinforced composite has a tensile modulus as determined on injection molded specimens according to ISO 527-1 at 1 mm/min in the range of 3600 to 7000 MPa, more preferably in the range of 3800 to 6800 MPa, like in the range of 4000 to 6600 MPa.
Additionally or alternatively to the requirement of the previous paragraph the fiber reinforced composite has an impact Charpy impact strength determined according to ISO 179-1eU at 23° C. in the range of 30.0 to 75.0 kJ/m2, more preferably in the range of 35.0 to 70.0 kJ/m2, like in the range of 40.0 to 65.0 kJ/m2.
In a very specific embodiment, the fiber reinforced composite has a heat deflection temperature HDT measured in accordance with ISO 75 B at a load of 0.46 MPa in the range from 146 to 160° C., more preferably in the range of 148 to 158° C., like in the range of 150 to 156° C.
The Polypropylene
The essential component of the present invention is the polypropylene, which needs to be carefully selected to reach the desired properties. Accordingly, the polypropylene according to this invention needs a specific melting temperature and a very narrow molecular weight distribution (MWD).
Accordingly, the polypropylene according to this invention has
Preferably the polypropylene of the previous paragraph complies with the inequation (I), more preferably with the inequation (II),
Tm/MWD>50 (I)
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the polypropylene [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the polypropylene determined by gel permeation chromatography (GPC).
More preferably the polypropylene according to this invention has
Typically the polypropylene according to this invention has
Tm/MWD>50 (I)
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the polypropylene [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the polypropylene determined by gel permeation chromatography (GPC).
It is especially preferred that the polypropylene is monophasic, i.e. does not comprise polymer components which are not miscible with each other as it is the case for heterophasic propylene copolymers. As stated above, in contrast to monophasic systems heterophasic systems comprise a continuous polymer phase, like a polypropylene, in which a further non-miscible polymer, like an elastomeric polymer, is dispersed as inclusions. Said polypropylene systems containing a polypropylene matrix and inclusions as a second polymer phase would by contrast be called heterophasic and is preferably not part of the present invention. The presence of second polymer phases or the so called inclusions are for instance visible by high resolution microscopy, like electron microscopy or atomic force microscopy, or by dynamic mechanical thermal analysis (DMTA). Specifically in DMTA the presence of a multiphase structure can be identified by the presence of at least two distinct glass transition temperatures.
Therefore in a preferred embodiment the polypropylene according to this invention is a monophasic polypropylene having
Tm/MWD>50 (I)
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the monophasic polypropylene [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the monophasic polypropylene determined by gel permeation chromatography (GPC).
More preferably the polypropylene according to this invention is a monophasic polypropylene having a
Tm/MWD>50 (I)
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the monophasic polypropylene [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the monophasic polypropylene determined by gel permeation chromatography (GPC).
It is especially preferred that the monophasic polypropylene is a propylene homopolymer. A propylene homopolymer cannot be per definition heterophasic as it just contains polymer chains of propylene. In other words a propylene homopolymer according to this invention is always a monophasic polymer.
Accordingly the monophasic polypropylene according to this invention is preferably a propylene homopolymer having
Tm/MWD>50 (I)
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the propylene homopolymer [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the propylene homopolymer determined by gel permeation chromatography (GPC).
Still more preferably the monophasic polypropylene is especially a propylene homopolymer having
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the propylene homopolymer [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the propylene homopolymer determined by gel permeation chromatography (GPC).
The polypropylene according to this invention has been produced in the presence of a specific metallocene catalyst as defined in more detail below. In contrast to polypropylenes produced in the presence of Ziegler-Natta catalysts, polypropylenes produced in the presence of metallocene catalysts are characterized by mis-insertions of monomer units during the polymerization process. Further, such polypropylene are featured by rather low xylene cold soluble (XCS) content. Therefore the polypropylene according to this invention has a certain amount of 2,1-regio defects and low amounts of xylene cold solubles. That is, the polypropylene according to this invention has 2,1 regio-defects in the range of 0.10 to 0.90%, more preferably in the range of 0.15 to 0.80%, determined by 13C-NMR spectroscopy or a xylene cold soluble (XCS) fraction measured according to ISO 16152 (25° C.) in the range of 0.05 to 1.00 wt.-%, more preferably in the range of 0.10 to 0.90 wt.-%. It is especially preferred that the polypropylene according to this invention has 2,1 regio-defects in the range of 0.10 to 0.90%, more preferably in the range of 0.15 to 0.80%, determined by 13C-NMR spectroscopy and a xylene cold soluble (XCS) fraction measured according to ISO 16152 (25° C.) in the range of 0.05 to 1.00 wt.-%, more preferably in the range of 0.10 to 0.90 wt.-%.
Therefore the present invention is especially directed to a polypropylene, more preferably to a monophasic polypropylene, having
It is especially preferred that the polypropylene, more preferably the monophasic polypropylene, of the previous paragraph complies with the inequation (I), more preferably with the inequation (II),
Tm/MWD>50 (I)
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the (monophasic) polypropylene [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the (monophasic) polypropylene determined by gel permeation chromatography (GPC).
More preferably, the polypropylene, still more preferably the monophasic polypropylene, according to this invention has
It is especially preferred that the polypropylene, more preferably the monophasic polypropylene, of the previous paragraph complies with the inequation (II)
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the (monophasic) polypropylene [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the (monophasic) polypropylene determined by gel permeation chromatography (GPC).
As mentioned above, it is especially preferred that the monophasic polypropylene is a propylene homopolymer. Accordingly, in a preferred embodiment the monophasic polypropylene being a propylene homopolymer has
It is especially preferred that the propylene homopolymer of the previous paragraph complies with the inequation (II)
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the propylene homopolymer [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the propylene homopolymer determined by gel permeation chromatography (GPC).
Still more preferably the monophasic polypropylene is a propylene homopolymer having
It is especially preferred that the monophasic polypropylene is a propylene homopolymer having
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the propylene homopolymer [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the propylene homopolymer determined by gel permeation chromatography (GPC).
Additionally it is preferred that the polypropylene visbroken. Visbreaking, or controlled degradation in a radical-induced process, is normally used to enhance the melt flow rate and thus to lower the molecular weight and molecular weight distribution. Typically, visbreaking of a polymer is obtained by the use of peroxides. Such degradation steps normally increase the emission values (in terms of VOC or FOG) due to undesired side reaction leading to an increased amount of oligomers as well as residues from the peroxide decomposition. It has now surprisingly been found, that the degradation of polypropylene produced in the presence of a metallocene catalyst does not show the undesired effect of enhanced emission values. In other words, the molecular weight distribution (MWD) can be further reduced by visbreaking (degradation) in case a polypropylene has been used having a certain amount of 2,1 regio-defects, i.e. have been produced in the presence of a metallocene catalyst.
Therefore, the present invention is especially directed to a visbroken polypropylene having
VR=MFR
2(FINAL)
/MFR
2(START)
wherein
“MFR2(FINAL)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the polypropylene after visbreaking
“MFR2(START)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the polypropylene before visbreaking.
More preferably, the visbroken polypropylene of the previous paragraph is a visbroken monophasic polypropylene.
Still more preferably the polypropylene is a visbroken polypropylene having
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the visbroken polypropylene [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the visbroken polypropylene determined by gel permeation chromatography (GPC),
optionally wherein still further
the visbreaking ratio (VR) is in the range of 2.5 to 20.0, wherein the visbreaking ratio (VR) is determined according to equation
VR=MFR
2(FINAL)
/MFR
2(START)
wherein
“MFR2(FINAL)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the polypropylene after visbreaking
“MFR2(START)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the polypropylene before visbreaking.
More preferably, the visbroken polypropylene of the previous paragraph is a visbroken monophasic polypropylene.
Still more preferably the polypropylene according to this invention is a visbroken polypropylene having
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the visbroken polypropylene [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the visbroken polypropylene determined by gel permeation chromatography (GPC),
wherein optionally the visbreaking ratio (VR) is in the range of 2.5 to 20.0 wherein the visbreaking ratio (VR) is determined according to equation
VR=MFR
2(FINAL)
/MFR
2(START)
wherein
“MFR2(FINAL)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the polypropylene after visbreaking
“MFR2(START)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the polypropylene before visbreaking.
More preferably, the visbroken polypropylene of the previous paragraph is a visbroken monophasic polypropylene.
As mentioned above, it is especially preferred that the monophasic polypropylene is a propylene homopolymer.
Accordingly it is preferred that the polypropylene is a visbroken propylene homopolymer having
VR=MFR
2(FINAL)
/MFR
2(START)
wherein
“MFR2(FINAL)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the propylene homopolymer after visbreaking
“MFR2(START)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the propylene homopolymer before visbreaking.
It is still more preferred that the polypropylene is a visbroken propylene homopolymer having
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the visbroken propylene homopolymer [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the visbroken propylene homopolymer determined by gel permeation chromatography (GPC),
optionally wherein further
the visbreaking ratio (VR) is in the range of 2.5 to 20.0, wherein the visbreaking ratio (VR) is determined according to equation
VR=MFR
2(FINAL)
/MFR
2(START)
wherein
“MFR2(FINAL)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the propylene homopolymer after visbreaking
“MFR2(START)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the propylene homopolymer before visbreaking.
It is in particular preferred that the polypropylene is produced in the presence of a specific metallocene catalyst and is subsequently visbroken. Accordingly, in a very specific embodiment of the present invention the polypropylene, more preferably the monophasic polypropylene, is produced by polymerizing propylene and optionally ethylene in the presence of the metallocene catalyst having the formula (I)
wherein each R1 are independently the same or can be different and are hydrogen or a linear or branched C1-C6 alkyl group, whereby at least on R1 per phenyl group is not hydrogen,
R′ is a C1-C10 hydrocarbyl group, preferably a C1-C4 hydrocarbyl group and more preferably a methyl group and X independently is a hydrogen atom, a halogen atom, C1-C6 alkoxy group, C1-C6 alkyl group, phenyl or benzyl group and subsequently the polypropylene is visbroken wherein optionally the visbreaking ratio (VR) is in the range of 2.5 to 20.0, wherein the visbreaking ratio (VR) is determined according to equation
VR=MFR
2(FINAL)
/MFR
2(START)
wherein
“MFR2(FINAL)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the polypropylene after visbreaking
“MFR2(START)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the polypropylene before visbreaking.
Hence it is especially preferred that the polypropylene is a visbroken poylpropylene having
VR=MFR
2(FINAL)
/MFR
2(START)
Preferably, the visbroken polypropylene of the previous paragraph complies with the inequation (II)
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the visbroken polypropylene [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the visbroken polypropylene determined by gel permeation chromatography (GPC).
In a special preferred embodiment the polypropylene is a visbroken monophasic polypropylene having
VR=MFR
2(FINAL)
/MFR
2(START)
Preferably the visbroken monophasic polypropylene of the previous paragraph complies with the inequation (II)
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the visbroken monophasic polypropylene [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the visbroken monophasic polypropylene determined by gel permeation chromatography (GPC).
As mentioned above the polypropylene according to this invention is preferably a propylene homopolymer. Thus, it is in particular preferred that the polypropylene is a propylene homopolymer, which is produced in the presence of the specific metallocene catalyst according to formula (I) and subsequently visbroken.
Hence, the polypropylene according to this invention is in particular a visbroken propylene homopolymer having
VR=MFR
2(FINAL)
/MFR
2(START)
More preferably the polypropylene is a visbroken propylene homopolymer having
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the visbroken propylene homopolymer [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the visbroken propylene homopolymer determined by gel permeation chromatography (GPC).
wherein still further
VR=MFR
2(FINAL)
/MFR
2(START)
In the following, the polymerization of the polypropylene is described in detail.
The polypropylene according to this invention can be produced in one reactor or in a reactor cascade of two or more reactors, preferably two reactors. The polymerization processes suitable for producing the polypropylene according to this invention are known in the state of the art. They comprise at least one polymerization stage, where polymerization is typically carried out in solution, slurry, bulk or gas phase. Typically, the polymerization process comprises additional polymerization stages or reactors. In one particular embodiment, the process contains at least one bulk reactor zone and optionally at least one gas phase reactor zone, each zone comprising at least one reactor and all reactors being arranged in cascade. In one particularly preferred embodiment, the polymerization process comprises at least one bulk reactor and optionally at least one gas phase reactor arranged in that order. The process may further comprise pre- and post-reactors. Pre-reactors comprise typically pre-polymerization reactors. In this kind of processes, the use of higher polymerization temperatures is preferred in order to achieve specific properties of the polymer. Typical temperatures in these processes are 70° C. or higher, preferably 75° C. or higher. The higher polymerization temperatures as mentioned above can be applied in some or all reactors of the reactor cascade.
A preferred multistage process is a “loop-gas phase”-process, such as developed by Borealis (known as BORSTAR@ technology) described e.g. in patent literature, such as in EP 0 887 379, WO 92/12182, WO 2004/000899, WO 2004/111095, WO 99/24478, WO 99/24479 or in WO 00/68315. A further suitable slurry-gas phase process is the Spheripol@ process of Basell.
As mentioned above the polypropylene according to this invention is especially obtained in a polymerization process using a metallocene catalyst having the formula (I)
wherein each R1 are independently the same or can be different and are hydrogen or a linear or branched C1-C6 alkyl group, whereby at least on R1 per phenyl group is not hydrogen,
R′ is a C1-C10 hydrocarbyl group, preferably a C1-C4 hydrocarbyl group and more preferably a methyl group and
X independently is a hydrogen atom, a halogen atom, C1-C6 alkoxy group, C1-C6 alkyl group, phenyl or benzyl group.
Most preferably, X is chlorine, benzyl or a methyl group. Preferably, both X groups are the same. The most preferred options are two chlorides, two methyl or two benzyl groups, especially two chlorides.
Specific preferred metallocene catalysts of the invention include: rac-anti-dimethylsilanediyl[2-methyl-4,8-bis-(4′-tert-butylphenyl)-1,5,6,7-tetrahydro-s-indacen-1-yl][2-methyl-4-(3′,5′-dimethyl-phenyl)-5-methoxy-6-tert-butylinden-1-yl]zirconium dichloride rac-anti-dimethylsilanediyl[2-methyl-4,8-bis-(3′,5′-dimethylphenyl)-1,5,6,7-tetrahydro-s-indacen-1-yl][2-methyl-4-(3′,5′-dimethylphenyl)-5-methoxy-6-tert-butylinden-1-yl]zirconium dichloride rac-anti-dimethylsilanediyl[2-methyl-4,8-bis-(3′,5′-dimethylphenyl)-1,5,6,7-tetrahydro-s-indacen-1-yl][2-methyl-4-(3′,5′-ditert-butyl-phenyl)-5-methoxy-6-tert-butylinden-1-yl]zirconium dichloride
or their corresponding zirconium dimethyl analogues.
The most preferred catalyst is rac-anti-dimethylsilanediyl[2-methyl-4,8-bis-(3′,5′-dimethylphenyl)-1,5,6,7-tetrahydros-indacen-1-yl][2-methyl-4-(3′,5′-dimethylphenyl)-5-methoxy-6-tert-butylinden-1-yl]zirconium dichloride
The ligands required to form the complexes and hence catalysts of the invention can be synthesised by any process and the skilled organic chemist would be able to devise various synthetic protocols for the manufacture of the necessary ligand materials. For Example WO2007/116034 discloses the necessary chemistry. Synthetic protocols can also generally be found in WO 2002/02576, WO 2011/135004, WO 2012/084961, WO 2012/001052, WO 2011/076780, WO 2015/158790 and WO 2018/122134. Especially reference is made to WO 2019/179959 in which the most preferred catalyst of the present invention is described. The examples section also provides the skilled person with sufficient direction.
To form an active catalytic species it is normally necessary to employ a cocatalyst as is well known in the art.
According to the present invention a cocatalyst system comprising a boron containing cocatalyst and/or an aluminoxane cocatalyst is used in combination with the above defined metallocene catalyst complex.
The aluminoxane cocatalyst can be one of formula (III):
where n is usually from 6 to 20 and R has the meaning below.
Aluminoxanes are formed on partial hydrolysis of organoaluminum compounds, for example those of the formula AlR3, AlR2Y and Al2R3Y3 where R can be, for example, C1-C10 alkyl, preferably C1-C5 alkyl, or C3-C10 cycloalkyl, C7-C12 arylalkyl or alkylaryl and/or phenyl or naphthyl, and where Y can be hydrogen, halogen, preferably chlorine or bromine, or C1-C10 alkoxy, preferably methoxy or ethoxy. The resulting oxygen-containing aluminoxanes are not in general pure compounds but mixtures of oligomers of the formula (111).
The preferred aluminoxane is methylaluminoxane (MAO). Since the aluminoxanes used according to the invention as cocatalysts are not, owing to their mode of preparation, pure compounds, the molarity of aluminoxane solutions hereinafter is based on their aluminium content.
According to the present invention, also a boron containing cocatalyst can be used instead of the aluminoxane cocatalyst or the aluminoxane cocatalyst can be used in combination with a boron containing cocatalyst.
It will be appreciated by the skilled man that where boron based cocatalysts are employed, it is normal to pre-alkylate the complex by reaction thereof with an aluminium alkyl compound, such as TIBA. This procedure is well known and any suitable aluminium alkyl, e.g. Al(C1-C6 alkyl)3 can be used. Preferred aluminium alkyl compounds are triethylaluminium, tri-isobutylaluminium, tri-isohexylaluminium, tri-n-octylaluminium and tri-isooctylaluminium.
Alternatively, when a borate cocatalyst is used, the metallocene catalyst complex is in its alkylated version, that is for example a dimethyl or dibenzyl metallocene catalyst complex can be used.
Boron based cocatalysts of interest include those of formula (IV)
BY3 (IV)
wherein Y is the same or different and is a hydrogen atom, an alkyl group of from 1 to about 20 carbon atoms, an aryl group of from 6 to about 15 carbon atoms, alkylaryl, arylalkyl, haloalkyl or haloaryl each having from 1 to 10 carbon atoms in the alkyl radical and from 6-20 carbon atoms in the aryl radical or fluorine, chlorine, bromine or iodine. Preferred examples for Y are methyl, propyl, isopropyl, isobutyl or trifluoromethyl, unsaturated groups such as aryl or haloaryl like phenyl, tolyl, benzyl groups, p-fluorophenyl, 3,5-difluorophenyl, pentachlorophenyl, pentafluorophenyl, 3,4,5-trifluorophenyl and 3,5-di(trifluoromethyl)phenyl. Preferred options are trifluoroborane, triphenylborane, tris(4-fluorophenyl)borane, tris(3,5-difluorophenyl)borane, tris(4-fluoromethylphenyl)borane, tris(2,4,6-trifluorophenyl)borane, tris(penta-fluorophenyl)borane, tris(tolyl)borane, tris(3,5-dimethyl-phenyl)borane, tris(3,5-difluorophenyl)borane and/or tris (3,4,5-trifluorophenyl)borane.
Particular preference is given to tris(pentafluorophenyl)borane.
However it is preferred that borates are used, i.e. compounds containing a borate 3+ ion. Such ionic cocatalysts preferably contain a non-coordinating anion such as tetrakis(pentafluorophenyl)borate and tetraphenylborate. Suitable counterions are protonated amine or aniline derivatives such as methylammonium, anilinium, dimethylammonium, diethylammonium, N-methylanilinium, diphenylammonium, N,N-dimethylanilinium, trimethylammonium, triethylammonium, tri-n-butylammonium, methyldiphenylammonium, pyridinium, p-bromo-N,N-dimethylanilinium or p-nitro-N,N-dimethylanilinium.
Preferred ionic compounds which can be used according to the present invention include:
Preference is given to triphenylcarbeniumtetrakis(pentafluorophenyl) borate, N,N-dimethylcyclohexylammoniumtetrakis(pentafluorophenyl)borate or N,N-dimethylbenzylammoniumtetrakis(pentafluorophenyl)borate.
It has been surprisingly found that certain boron cocatalysts are especially preferred. Preferred borates of use in the invention therefore comprise the trityl ion. Thus the use of N,N-dimethylammonium-tetrakispentafluorophenylborate and Ph3CB(PhF5)4 and analogues therefore are especially favoured.
According to the present invention, the preferred cocatalysts are alumoxanes, more preferably methylalumoxanes, combinations of alumoxanes with Al-alkyls, boron or borate cocatalysts, and combination of alumoxanes with boron-based cocatalysts.
Suitable amounts of cocatalyst will be well known to the skilled man.
The molar ratio of boron to the metal ion of the metallocene may be in the range 0.5:1 to 10:1 mol/mol, preferably 1:1 to 10:1, especially 1:1 to 5:1 mol/mol.
The molar ratio of Al in the aluminoxane to the metal ion of the metallocene may be in the range 1:1 to 2000:1 mol/mol, preferably 10:1 to 1000:1, and more preferably 50:1 to 500:1 mol/mol.
The catalyst can be used in supported or unsupported form, preferably in supported form. The particulate support material used is preferably an organic or inorganic material, such as silica, alumina or zirconia or a mixed oxide such as silica-alumina, in particular silica, alumina or silica-alumina. The use of a silica support is preferred. The skilled person is aware of the procedures required to support a metallocene catalyst.
Especially preferably, the support is a porous material so that the complex may be loaded into the pores of the support, e.g. using a process analogous to those described in WO94/14856 (Mobil), WO95/12622 (Borealis) and WO2006/097497.
The average particle size of the silica support can be typically from 10 to 100 μm. However, it has turned out that special advantages can be obtained if the support has an average particle size from 15 to 80 μm, preferably from 18 to 50 μm.
The average pore size of the silica support can be in the range 10 to 100 nm and the pore volume from 1 to 3 mL/g.
Examples of suitable support materials are, for instance, ES757 produced and marketed by PQ Corporation, Sylopol 948 produced and marketed by Grace or SUNSPERA DM-L-303 silica produced by AGC Si-Tech Co. Supports can be optionally calcined prior to the use in catalyst preparation in order to reach optimal silanol group content.
The use of these supports is routine in the art.
As mentioned above it is in particular preferred that the polypropylene is visbroken.
For visbreaking typically discontinuous and continuous kneaders, twin-screw extruders and single screw extruders with special mixing sections and co-kneaders are used.
The visbreaking may be carried out in any known manner, but typically the present invention envisages chemical visbreaking using a peroxide visbreaking agent. Typical visbreaking agents are 2,5-dimethyl-2,5-bis(tert.butyl-peroxy)hexane (DHBP) (for instance sold under the tradenames Luperox 101 and Trigonox 101), 2,5-dimethyl-2,5-bis(tert.butyl-peroxy)hexyne-3 (DYBP) (for instance sold under the tradenames Luperox 130 and Trigonox 145), dicumyl-per oxide (DCUP) (for instance sold under the tradenames Luperox DC and Perkadox BC), di-tert.butyl-peroxide (DTBP) (for instance sold under the tradenames Trigonox B and Luperox Di), tertbutyl-cumyl-peroxide (BCUP) (for instance sold under the tradenames Trigonox T and Luperox 801) and bis (tert.butylperoxy-isopropyl)benzene (DIPP) (for instance sold under the tradenames Perkadox 14S and Lupperox DC).
Suitable amounts of peroxide to be employed in accordance with the present invention are in principle known to the skilled person and can easily be calculated on the basis of the amount of the polypropylene to be subjected to visbreaking, the MFR2 (230° C.; 2.16 kg) value of the polypropylene to be subjected to visbreaking and the desired target MFR2 ((230° C.; 2.16 kg) of the final polypropylene. Accordingly, typical amounts of peroxide visbreaking agent are from 0.001 to 0.15 wt.-%, more preferably from 0.002 to 0.10 wt.-%, based on the amount of polypropylene employed.
During visbreaking, higher molar mass chains of the starting product are broken statistically more frequently than lower molar mass molecules, resulting in an overall decrease of the average molecular weight, decrease of the molecular weight distribution (MWD) and an increase in melt flow rate MFR2 (230° C.; 2.16 kg).
The second mandatory composition in the fiber reinforced composite are the glass fibers. The glass fibers can be any type of glass fibers like long glass fibers or short glass fibers. However it is especially preferred that the glass fibers are short glass fibers, also known as cut glass fibers or chopped glass strands.
The short glass fibers used in the fiber reinforced composite preferably have an average fiber length in the range of from 2.0 to 10.0 mm, more preferably in the range of 2.0 to 8.0 mm, still more preferably in the range of 2.0 to 5.0 mm.
It is further preferred that the short glass fibers used in the fiber reinforced composite preferably have an average diameter of from 5 to 20 μm, more preferably from 8 to 18 μm, still more preferably 8 to 15 μm.
Preferably, the short glass fibers have an aspect ratio, defined as the ratio between average fiber length and average fiber diameter, of 150 to 600, preferably of 200 to 500, more preferably 250 to 400. The aspect ratio is the relation between average length and average diameter of the fibers.
A further component present in the fiber reinforced composite is the competibilizer or also called coupling agent or adhesion promotor. As mentioned above the compatibilizer improves the adhesion between the non-polar polypropylene and the polar glass fibers.
The compatibilizer according to this invention is preferably a polar modified polypropylene. The polar modified polypropylene, like a polar modified propylene homopolymer or a polar modified copolymer, are highly compatible with the polypropylene of the fiber reinforced composite according to this invention.
In terms of structure, the polar modified polypropylenes are preferably selected from graft or block copolymers.
In this context, preference is given to polar modified polypropylenes containing groups deriving from polar compounds, in particular selected from the group consisting of acid anhydrides, carboxylic acids, carboxylic acid derivatives, primary and secondary amines, hydroxyl compounds, oxazoline and epoxides, and also ionic compounds.
Specific examples of the said polar compounds are unsaturated cyclic anhydrides and their aliphatic diesters, and the diacid derivatives. In particular, one can use maleic anhydride and compounds selected from C1 to C10 linear and branched dialkyl maleates, C1 to C10 linear and branched dialkyl fumarates, itaconic anhydride, C1 to C10 linear and branched itaconic acid dialkyl esters, maleic acid, fumaric acid, itaconic acid and mixtures thereof.
In a particular preferred embodiment of the present invention, the polar modified polypropylene is maleic anhydride grafted polypropylene, wherein the polypropylene is either a propylene-ethylene copolymer or a propylene homopolymer. It is especially preferred that the polar modified polypropylene is maleic anhydride grafted polypropylene, wherein the polypropylene is a propylene homopolymer.
The polar modified polypropylene, especially the maleic anhydride grafted polypropylene, can be produced in a simple manner by reactive extrusion of the polypropylene, for example with maleic anhydride in the presence of free radical generators (like organic peroxides), as disclosed for instance in EP 0 572 028.
The amounts of groups deriving from polar compounds, like the amount of maleic anydride, in the polar modified polypropylene, are from 0.1 to 5.0 wt. %, preferably from 0.5 to 4.0 wt. %, and more preferably from 0.5 to 3.0 wt. %.
Preferably the polar modified polypropylene, like the maleic anhydride grafted polypropylene, has a melt flow rate MFR2 (190° C., 2.16 kg) measured according to ISO 1133 of at least 50 g/10 min, more preferably of at least 80 g/10 min, yet more preferably in the range of 50 to 500 g/10 min, still yet more preferably in the range of 80 to 250 g/10 min.
Fiber reinforced composite according to this invention may in addition comprise additives. Typical additives are acid scavengers, antioxidants, colorants, light stabilizers, slip agents, anti-scratch agents, dispersing agents, processing aids, lubricants, pigments, and the like.
Such additives are commercially available and for example described in “Plastic Additives Handbook”, 6th edition 2009 of Hans Zweifel (pages 1141 to 1190).
Additives are typically provided in form of a masterbatch. A masterbatch is a composition in which an additive or an additive mixture in rather high amount is dispersed in a polymer. Accordingly, the term “additive” according to the present invention also includes carrier materials, in particular polymeric carrier materials, in which the “active additive” or “active additive mixture” is dispersed.
The reinforced fiber composite is produced as well known in the art. Accordingly the fiber reinforced composite is manufactured by a processes comprising the steps of adding
For the extruding, i.e. melt blending, the individual components of the composite a conventional compounding or blending apparatus, e.g. a Banbury mixer, a 2-roll rubber mill, Buss-co-kneader or a twin screw extruder may be used. The fiber reinforced composite recovered from the extruder/mixer is usually in the form of granules. These granules are then preferably further processed, e.g. by injection molding to generate articles and products of the inventive composite.
It is especially preferred that the fiber reinforced composite according to the present invention is prepared by melt blending the individual components in an extruder, preferably a twin screw extruder.
In particular, it is preferred that the fiber reinforced composite according to the present invention is obtained by a process comprising the steps of
VR=MFR
2(FINAL)
/MFR
2(START)
wherein
“MFR2(FINAL)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the polypropylene after visbreaking
“MFR2(START)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the polypropylene before visbreaking.
The present invention is further directed to an article, preferably an automotive article, comprising at least 90 wt.-%, more preferably at least 95 wt.-%, yet more preferably consist, of the fiber reinforced composite according to the present invention.
Especially preferred are automotive articles are dashboards and dashboard supports, bumper supports, load-bearing components of doors and tailgates, under-the-hood components like ventilators and battery carriers, and underbody protection elements.
Based on the information provided above the present invention is especially directed to the following embodiments.
In a preferred embodiment the fiber reinforced composite according to this invention has a melt flow rate MFR2 (230° C., 2.16 kg) measured according to ISO 1133 in in the range of 10 to 100 g/10 min, preferably in the range of 15 to 50 g/10 min, and comprises
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the propylene homopolymer [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the propylene homopolymer determined by gel permeation chromatography (GPC).
That is in a preferred embodiment the fiber reinforced composite according to this invention has a melt flow rate MFR2 (230° C., 2.16 kg) measured according to ISO 1133 in in the range of 10 to 50 g/10 min, preferably in the range of 15 to 50 g/10 min, and comprises
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the visbroken propylene homopolymer [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min) MWD is the molecular weight distribution (MWD) of the visbroken propylene homopolymer determined by gel permeation chromatography (GPC),
preferably wherein the visbreaking ratio (VR) is in the range of 2.5 to 20.0, wherein the visbreaking ratio (VR) is determined according to equation
VR=MFR
2(FINAL)
/MFR
2(START)
wherein
“MFR2(FINAL)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the propylene homopolymer after visbreaking
“MFR2(START)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the propylene homopolymer before visbreaking.
In a very specific embodiment, the fiber reinforced composite according to this invention has a melt flow rate MFR2 (230° C., 2.16 kg) measured according to ISO 1133 in in the range of 10 to 100 g/10 min, preferably in the range of 15 to 50 g/10 min, and comprises
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the propylene homopolymer [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the propylene homopolymer determined by gel permeation chromatography (GPC),
wherein still yet further
In a further very specific embodiment the fiber reinforced composite according to this invention has a melt flow rate MFR2 (230° C., 2.16 kg) measured according to ISO 1133 in in the range of 10 to 100 g/10 min, preferably in the range of 15 to 50 g/10 min, and comprises
51<Tm/MWD<80 (II)
wherein
Tm is the melting temperature of the visbroken propylene homopolymer [in ° C.] determined by DSC according to ISO 11357-3 (heating and cooling rate 10° C./min)
MWD is the molecular weight distribution (MWD) of the visbroken propylene homopolymer determined by gel permeation chromatography (GPC),
wherein still yet further
VR=MFR
2(FINAL)
/MFR
2(START)
wherein
“MFR2(FNAL)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the propylene homopolymer after visbreaking
“MFR2(START)” is melt flow rate MFR2 (230° C.; 2.16 kg) measured according to ISO 1133 of the propylene homopolymer before visbreaking.
In the following, the present invention is described by way of examples.
The following definitions of terms and determination methods apply for the above general description of the invention as well as to the below examples unless otherwise defined.
The melt flow rate (MFR2) is determined according to ISO 1133 and is indicated in g/10 min.
The MFR2 of polypropylene is determined at a temperature of 230° C. and under a load of 2.16 kg.
The Heat deflection temperature B (HDT B) was determined according to ISO 75 B at 0.45 MPa using 80×10×4 mm3 test bars injection molded in line with EN ISO 1873-2.
The amount of the polymer soluble in xylene is determined at 25.0° C. according to ISO 16152; 1th edition; 2005-07-01.
d) Melting Temperature Tm and Crystallization Temperature Tc
The melting temperature Tm is determined by differential scanning calorimetry (DSC) according to ISO 11357-3 with a TA-Instruments 2920 Dual-Cell with RSC refrigeration apparatus and data station. A heating and cooling rate of 10° C./min is applied in a heat/cool/heat cycle between +23 and +210° C. The crystallization temperature (Tc) is determined from the cooling step while melting temperature (Tm) and melting enthalpy (Hm) are being determined in the second heating step.
Tensile modulus and elongation at break are measured according to ISO 527-2 using injection molded specimens as described in EN ISO 1873-2 (1 B dog bone shape, 4 mm thickness).
The Charpy impact strength was measured according to ISO 179 1eU at +23° C. using injection molded bar test specimens of 80×10×4 mm3 prepared in accordance with EN ISO 1873-2.
Quantitative nuclear-magnetic resonance (NMR) spectroscopy was used to quantify the comonomer content of the polymers. Quantitative 13C{1H} NMR spectra were recorded in the solution-state using a Bruker Advance III 400 NMR spectrometer operating at 400.15 and 100.62 MHz for 1H and 13C respectively. All spectra were recorded using a 13C optimized 10 mm extended temperature probehead at 125° C. using nitrogen gas for all pneumatics. Approximately 200 mg of material was dissolved in 3 ml of 1,2-tetrachloroethane-d2 (TCE-d2) along with chromium-(III)-acetylacetonate (Cr(acac)3) resulting in a 65 mM solution of relaxation agent in solvent (Singh, G., Kothari, A., Gupta, V., Polymer Testing 28 5 (2009), 475). To ensure a homogenous solution, after initial sample preparation in a heat block, the NMR tube was further heated in a rotatary oven for at least 1 hour. Upon insertion into the magnet the tube was spun at 10 Hz. This setup was chosen primarily for the high resolution and quantitatively needed for accurate ethylene content quantification. Standard single-pulse excitation was employed without NOE, using an optimised tip angle, 1 s recycle delay and a bi-level WALTZ16 decoupling scheme (Zhou, Z., Kuemmerle, R., Qiu, X., Redwine, D., Cong, R., Taha, A., Baugh, D. Winniford, B., J. Mag. Reson. 187 (2007) 225; Busico, V., Carbonniere, P., Cipullo, R., Pellecchia, R., Severn, J., Talarico, G., Macromol. Rapid Commun. 2007, 28, 1128). A total of 6144 (6k) transients were acquired per spectra. Quantitative 13C{1H} NMR spectra were processed, integrated and relevant quantitative properties determined from the integrals using proprietary computer programs. All chemical shifts were indirectly referenced to the central methylene group of the ethylene block (EEE) at 30.00 ppm using the chemical shift of the solvent. This approach allowed comparable referencing even when this structural unit was not present. Characteristic signals corresponding to the incorporation of ethylene were observed Cheng, H. N., Macromolecules 17 (1984), 1950).
With characteristic signals corresponding to 2,1 erythro regio defects observed (as described in L. Resconi, L. Cavallo, A. Fait, F. Piemontesi, Chem. Rev. 2000, 100 (4), 1253, in Cheng, H. N., Macromolecules 1984, 17, 1950, and in W-J. Wang and S. Zhu, Macromolecules 2000, 33 1157) the correction for the influence of the regio defects on determined properties was required. Characteristic signals corresponding to other types of regio defects were not observed.
The comonomer fraction was quantified using the method of Wang et. al. (Wang, W-J., Zhu, S., Macromolecules 33 (2000), 1157) through integration of multiple signals across the whole spectral region in the 13C{1H} spectra. This method was chosen for its robust nature and ability to account for the presence of regio-defects when needed. Integral regions were slightly adjusted to increase applicability across the whole range of encountered comonomer contents.
For systems where only isolated ethylene in PPEPP sequences was observed the method of Wang et. al, was modified to reduce the influence of non-zero integrals of sites that are known to not be present. This approach reduced the overestimation of ethylene content for such systems and was achieved by reduction of the number of sites used to determine the absolute ethylene content to:
E=0.5(Sββ+Sβγ+Sβδ+0.5(Sαβ+Sαγ))
Through the use of this set of sites the corresponding integral equation becomes:
E=0.5(IH+IG+0.5(IC+ID))
using the same notation used in the article of Wang et. al. (Wang, W-J., Zhu, S., Macromolecules 33 (2000), 1157). Equations used for absolute propylene content were not modified.
The mole percent comonomer incorporation was calculated from the mole fraction:
E[mol %]=100*fE
The weight percent comonomer incorporation was calculated from the mole fraction:
E[wt %]=100*(fE*28.06)/((fE*28.06)+((1−fE)*42.08))
Number average molecular weight (Mn), weight average molecular weight (Mw) and the molecular weight distribution (Mw/Mn) were determined by Gel Permeation Chromatography (GPC) according to ISO 16014-4:2003 and ASTM D 6474-99. A PolymerChar GPC instrument, equipped with infrared (IR) detector was used with 3×Olexis and 1×Olexis Guard columns from Polymer Laboratories and 1,2,4-trichlorobenzene (TCB, stabilized with 250 mg/L 2,6-Di tert butyl-4-methyl-phenol) as solvent at 160° C. and at a constant flow rate of 1 mL/min. 200 μL of sample solution were injected per analysis. The column set was calibrated using universal calibration (according to ISO 16014-2:2003) with at least 15 narrow MWD polystyrene (PS) standards in the range of 0.5 kg/mol to 11 500 kg/mol. Mark Houwink constants for PS, PE and PP used are as described per ASTM D 6474-99. All samples were prepared by dissolving 5.0-9.0 mg of polymer in 8 mL (at 160° C.) of stabilized TCB (same as mobile phase) for 2.5 hours for PP or 3 hours for PE at max. 160° C. under continuous gentle shaking in the autosampler of the GPC instrument.
VOC values and FOG values were measured according to VDA 278 (October 2011; Thermal Desorption Analysis of Organic Emissions for the Characterization of Non-Metallic Materials for Automobiles, VDA Verband der Automobilindustrie) after sample preparation of injection moulding plaques according to EN ISO 19069-2:2016. These plaques were packed in aluminium-composite foils immediately after production and the foils were sealed.
According to the VDA 278 October 2011 the VOC value is defined as “the total of the readily volatile to medium volatile substances. It is calculated as toluene equivalent. The method described in this recommendation allows substances in the boiling/elution range up to n-pentacosane (C25) to be determined and analyzed.”
The FOG value is defined as “the total of substances with low volatility, which elute from the retention time of n-tetradecane (inclusive)”. It is calculated as hexadecane equivalent. Substances in the boiling range of n-alkanes “C14” to “C32” are determined and analysed.
Fogging was measured according to DIN 75201:2011-11, method B (gravimetric method) on compression-moulded specimens (diameter 80 mm+/−1 mm, thickness<1 cm) cut out from an injection-moulded plate. With this method, the mass of fogging condensate on aluminium foil in mg is determined by means of weighing of the foil before and after the fogging test. The term “fogging” refers to a fraction of volatile substances condensed on glass parts as e.g. the windscreen of a vehicle.
The average fibre diameter is determined according to ISO 1888:2006(E), Method B, microscope magnification of 1000.
The following metallocene complex has been used as described in WO 2019/179959:
A steel reactor equipped with a mechanical stirrer and a filter net was flushed with nitrogen and the reactor temperature was set to 20° C. Next silica grade DM-L-303 from AGC Si-Tech Co, pre-calcined at 600° C. (5.0 kg) was added from a feeding drum followed by careful pressuring and depressurising with nitrogen using manual valves. Then toluene (22 kg) was added. The mixture was stirred for 15 min. Next 30 wt.-% solution of MAO in toluene (9.0 kg) from Lanxess was added via feed line on the top of the reactor within 70 min. The reaction mixture was then heated up to 90° C. and stirred at 90° C. for additional two hours. The slurry was allowed to settle and the mother liquor was filtered off. The catalyst was washed twice with toluene (22 kg) at 90° C., following by settling and filtration. The reactor was cooled off to 60° C. and the solid was washed with heptane (22.2 kg). Finally MAO treated SiO2 was dried at 600 under nitrogen flow for 2 hours and then for 5 hours under vacuum (−0.5 barg) with stirring. MAO treated support was collected as a free-flowing white powder found to contain 12.2% Al by weight.
30 wt.-% MAO in toluene (0.7 kg) was added into a steel nitrogen blanked reactor via a burette at 20° C. Toluene (5.4 kg) was then added under stirring. The metallocene complex as described above under 2a) (93 g) was added from a metal cylinder followed by flushing with 1 kg toluene. The mixture was stirred for 60 minutes at 20° C. Trityl tetrakis(pentafluorophenyl) borate (91 g) was then added from a metal cylinder followed by a flush with 1 kg of toluene. The mixture was stirred for 1 h at room temperature. The resulting solution was added to a a stirred cake of MAO-silica support prepared as described above over 1 hour. The cake was allowed to stay for 12 hours, folled by drying under N2 flow at 60° C. for 2 h and additionally for 5 h under vacuum (−0.5 barg) under stirring stirring.
Dried catalyst was sampled in the form of pink free flowing powder containing 13.9% Al and 0.11% Zr.
A Ziegler-Natta catalyst system has been used
Mg alkoxide solution was prepared by adding, with stirring (70 rpm), into 11 kg of a 20 wt-% solution in toluene of butyl ethyl magnesium (Mg(Bu)(Et)), a mixture of 4.7 kg of 2-ethylhexanol and 1.2 kg of butoxypropanol in a 20 I stainless steel reactor. During the addition the reactor contents were maintained below 45° C. After addition was completed, mixing (70 rpm) of the reaction mixture was continued at 60° C. for 30 minutes. After cooling to room temperature 2.3 kg of the donor bis(2-ethylhexyl)citraconate was added to the Mg-alkoxide solution keeping temperature below 25° C. Mixing was continued for 15 minutes under stirring (70 rpm).
20.3 kg of TiCl4 and 1.1 kg of toluene were added into a 20 I stainless steel reactor. Under 350 rpm mixing and keeping the temperature at 0° C., 14.5 kg of the prepared Mg alkoxy compound was added during 1.5 hours. 1.7 I of Viscoplex® 1-254 and 7.5 kg of heptane were added and after 1 hour mixing at 0° C. the temperature of the formed emulsion was raised to 90° C., within 1 hour. After 30 minutes mixing was stopped catalyst droplets were solidified and the formed catalyst particles were allowed to settle. After settling (1 hour), the supernatant liquid was siphoned away. Then the catalyst particles were washed with 45 kg of toluene at 90° C. for 20 minutes followed by two heptane washes (30 kg, 15 min). During the first heptane wash the temperature was decreased to 50° C. and during the second wash to room temperature.
The thus obtained catalyst was used along with triethyl-aluminium (TEAL) as co-catalyst and dicyclo pentyl dimethoxy silane (D-donor) as donor. The ratio used was:
TEAL/Ti: 250 mol/mol
TEAL/Donor: 10 mol/mol
In a second step the propylene homopolymer HPP2 is produced by visbreaking HPP1 by using a co-rotating twin-screw extruder at 200-230° C. and using (tert.-butylperoxy)-2,5-dimethylhexane (Trigonox 101, distributed by Akzo Nobel, Netherlands) in an appropriate amount to achieve the target MFR2 as indicated in table 2.
The properties of the propylenes homopolymers are summarized in table 2.
The inventive examples IE1 and the comparative examples CE1 and CE2 were prepared by compounding on a co-rotating twin-screw extruder (ZSK 40 from Coperion) with an L/D ratio of 43. The following process parameters were used:
The polypropylene and the additives different from the short glass fibers were fed to the extruder and melt-kneaded in the 2nd barrel. A first kneading zone for mixing the polypropylene and the additives is located between the 3rd and 5th barrel. The short glass fibers were added in the 6th barrel using a side feeder. A second kneading zone for glass fibre dispersion is located between the 7th and 12th barrel.
The composites and their properties are summarized in Table 3.
As glass fibers the commercial product ECSO3T-480H of Nippon Electric Glass having an average fiber length of 3.0 mm and an average diameter of 10 μm.
The following combination of additives was used in compounding: 0.2 wt % of Tris (2,4-di-t-butylphenyl) phosphite (CAS-No. 31570-04-4, commercially available as Irgafos 168 from BASF AF, Germany), 0.1 wt % of Pentaerythrityl-tetrakis(3-(3′,5′-di-tert. butyl-4-hydroxyphenyl)-propionate (CAS-No. 6683-19-8, commercially available as Irganox 1010 from BASF AG, Germany) and 0.2 wt % of the carbon black masterbatch “Plasblak PPP6331” of Cabot Corporation, Germany.
Compatibilizer is the commercial maleic anhydride grafted polypropylene “Sconia TPPP 8112 GA” of BYK of having a maleic anhydrid content of 1.4 wt.-% and an MFR2 of more than 80 g/10 min.
| Number | Date | Country | Kind |
|---|---|---|---|
| 20176021.2 | May 2020 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2021/062991 | 5/17/2021 | WO |
