Classifications

• • D—TEXTILES; PAPER
  • D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
  • D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
  • D01F6/00—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof
  • D01F6/44—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from mixtures of polymers obtained by reactions only involving carbon-to-carbon unsaturated bonds as major constituent with other polymers or low-molecular-weight compounds
  • D01F6/46—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from mixtures of polymers obtained by reactions only involving carbon-to-carbon unsaturated bonds as major constituent with other polymers or low-molecular-weight compounds of polyolefins

Definitions

• the present invention relates to novel fibres comprising propylene copolymers. More particularly, the invention relates to fibres comprising heterophasic propylene copolymers, especially heterophasic propylene copolymers containing a propylene random copolymer and an ethylene rubber copolymer.
• polypropylene is widely used in many fibre and fabric applications. However, it is generally deficient in applications that require high softness. Such applications include nonwoven fabrics for disposable garments or diapers and also for furniture applications. For soft-end use fibre and fabric applications random copolymers have come into use since they can be processed into fibres and fabrics that exhibit improved softness and drape characteristics compared to fibres and fabrics made from propylene homopolymers.
• the propylene copolymers are described as being an "alloy" from a random propylene copolymer having an ethylene content of 1-5 wt% and a bipolymer having an ethylene content of 10-30 wt%.
• the propylene copolymer alloy is further described as having a single T g peak, this being an indication as to the miscibility of the random copolymer and the bipolymer.
• the miscibility of the random copolymer and the bipolymer is disclosed to be a prerequisite for spinnability.
• a fibre comprising a heterophasic propylene copolymer containing a) 80-99 wt% of a matrix phase comprising a propylene random copolymer with 0.2- 15 wt% of ethylene and/or at least one C 4 -C 8 ⁇ -olefin and b) 1-20 wt% of a disperse phase comprising an ethylene rubber copolymer with from 20 - 80 wt% ethylene and from 80 - 20 wt% of at least one C 3 -C 8 ⁇ -olefin, wherein the heterophasic copolymer has at least two T g peaks.
• the fibres of the present invention are characterised by a heterophasic propylene copolymer having at least two discernible T g peaks. Nevertheless, as will be further shown below, these heterophasic propylene copolymers are perfectly spinnable with high uptake speeds and the produced fibres are characterised by excellent softness.
• the ethylene content may range from 20 - 80 wt% preferably from 20 - 50 wt%, Accordingly, the C 3 -C 8 ⁇ -olefin content may range from 80 - 20 wt%, preferably from 80 - 50 wt%,
• the ethylene rubber copolymer is an ethylene propylene rubber (EPR).
• EPR ethylene propylene rubber
• EPR's are more cost-effective than ethylene rubbers with higher ⁇ -olefins and they can either be synthesised in the second step of a two-step process, where the first step synthesises the matrix polymer or they can be mixed with the matrix polymer in a separate melt blending step.
• the heterophasic propylene copolymer contains 2 - 15 wt%, preferably 5 - 12 wt% of the ethylene rubber copolymer. These concentration ranges for the ethylene rubber are preferred, because fibres from heterophasic propylene copolymer with the above amounts of ethylene rubber copolymer offer the best compromise as to spinnability and mechanical properties, which both in general decrease with higher rubber contents, and softness, which generally increases with higher rubber content.
• the heterophasic propylene copolymer has an MFR of from 0.1 - 50 g/10 min, preferably 2.5 - 30 g/10 min.
• the heterophasic propylene copolymer has an MFR of from 200 - 2000 g/10 min.
• the production of melt blown nonwoven fabrics of this invention requires MFR's in the range of from 200 - 2000 g/10 min.
• Heterophasic propylene copolymers having the desired MFR's may be obtained by vis- breaking the low-MFR polymer with e.g. peroxides, or they may be available directly from the polymerisation process by suitable choice of conditions.
• the fibres of the invention comprise a heterophasic propylene copolymer having an overall ethylene content of from 1.0 - 15.0 wt%.
• the heterophasic propylene copolymers of which the fibres of the invention are comprised preferably show two T g temperatures.
• the first of these glass transition temperatures preferably is in the range of from -15 to +5 °C, more preferably around 0 °C.
• This first T g temperature usually is attributed to the matrix phase and is influenced by the comonomer content of the matrix phase. In the case of ethylene as comonomer it is lower with higher ethylene contents.
• the second of these glass transition temperatures preferably is in the range of from -35 to -65 °C, more preferably from -40 to -60 °C and most preferably around -50 °C.
• the second T g usually is attributed to the rubber copolymer of the disperse phase and it is influenced by its molecular weight and its ethylene content.
• a particularly preferred embodiment refers to a fibre comprising a heterophasic propylene copolymer which contains 80 - 95 wt% of a matrix phase comprising a propylene random copolymer with from 1.0 - 15.0 wt% of ethylene and 5 - 20 wt% of a disperse phase comprising an ethylene propylene rubber with from 20 - 40 wt% of ethylene and 80- 60 wt% of propylene, the heterophasic propylene copolymer having an overall ethylene content of from 4.0 - 12.0 wt% and two distinct T g peaks.
• Fibres made from these heterophasic propylene copolymer are characterised by superior softness, and contrary to the disclosure of US 6,218,010, the heterophasic propylene copolymer has two T g peaks.
• the invention also refers to articles comprising fibres according to the invention.
• fabric articles include, but are not limited to: nonwoven fabrics for hygiene applications such as diapers, medical gowns and masks; woven fabrics for upholstery and clothing; ropes, twines, carpets.
• the heterophasic propylene copolymers may be used to produce fibres of the following types; continuous fibre, bulked continuous fibre, staple fibre, monofilament fibre, stretch tape, strapping; and nonwoven fabrics which are spunbonded, meltblown, or produced from staple fibre.
• the heterophasic propylene copolymers may be produced by multistage process polymerisation of propylene and ethylene and/or an ⁇ -olefin such as bulk polymerisation, gas phase polymerisation, slurry polymerisation, solution polymerisation or combinations thereof using conventional catalysts. Those processes are well known to one skilled in the art.
• a preferred process is a combination of bulk slurry loop reactor(s) and gas phase reactor(s).
• the matrix polymer can be made either in loop reactors or in a combination of loop and gas phase reactor.
• the polymer produced in this way is transferred into another reactor and the disperse phase is polymerised.
• this polymerisation step is done in a gas phase polymerisation.
• a suitable catalyst for the polymerisation of the heterophasic copolymer is any stereospecific catalyst for propylene polymerisation which is capable of polymerising and copolymerising propylene and comonomers at a temperature of 40 to 110 °C and at a pressure from 10 to 100 bar.
• Ziegler Natta catalysts as well as metallocene catalysts are suitable catalysts.
• heterophasic propylene copolymer may also be produced by mixing and melt blending a propylene random copolymer with an ethylene rubber copolymer.
• a heterophasic propylene copolymer prepared as explained above, may be subjected to a controlled rheology (CR) process well known in the art, whereby the copolymer is visbroken into a resin having a narrower molecular weight distribution and lower average molecular weight in order to facilitate fibre spinning.
• the molecular weight (MW) of the visbroken heterophasic copolymer determines the level of melt viscosity and the ultimate desirable physical properties of the fibre.
• the MFR of the visbroken copolymer as determined by the MFR test (ISO 1133) may vary within a wide range from fractional to about 2000 g/10 minutes.
• the CR process is preferably carried out by using organic peroxides, such as 2,5-dimethyl-2,5-di(tert-butylperoxy)hexane).
• organic peroxides such as 2,5-dimethyl-2,5-di(tert-butylperoxy)hexane.
• the compounds used in the CR process are added to the polymer and the polymer is , for example, visbroken during the extrusion step.
• the CR process may also convert the polymer granules to pellets for easier feeding into the fibre spinning extruder.
• Additives such as stabilizers, pigments, fillers, antioxidants, ultra-violet screening agents, nucleating agents, certain processing oils and the like may optionally be added; however, this should not be considered a limitation of the present invention.
• the heterophasic copolymer is then drawn to a fine diameter fibre by one of several well known in the art modifications of the basic melt-extrusion fibre process.
• This process consists of the steps of (1 ) continuously feeding the heterophasic copolymer to a melting screw extruder; (2) At the end of the screw, a spinning pump meters the melted polymer through a filter to a spinneret where the melted polymer is extruded under pressure through capillaries, typically at a rate of about 0.3-1.0 grams per hole per minute; the capillaries, depending upon the desired fibre product, may vary widely in number, size and shape; (3) solidifying the fibres by transferring the heat to a surrounding medium; and (4) winding of the solidified fibres onto packages.
• Further processing typically includes orienting the fibres by drawing them to many times their original length. Also, a variety of thermal and texturing treatments well known in the art may be employed, depending on the desired final properties of the fibre. Embodiments of the present invention fibres can be drawn into fine diameter fibres at generally high drawdown speed, without the individual fibres sticking together below the crystallization point.
• a particular embodiment of the present invention involves the use of the heterophasic copolymers for spunbonded fabrics.
• the spunbonding process is one which is well known in the art of fabric production. Generally, continuous fibres are extruded, laid on an endless belt, and then bonded to each other, and often times to a second layer such as a melt blown layer, often by a heated calander roll, or addition of a binder, or by a mechanical bonding system (entanglement) using needles or hydro jets.
• a typical spunbond process consists of a continuous filament extrusion, followed by drawing, web formation by the use of some type of ejector, and bonding of the web.
• the heterophasic copolymer is visbroken using peroxide into a resin having a narrower molecular weight distribution and about 25 MFR.
• the polymer granules are converted into pellets.
• the pelletised 25 MFR heterophasic copolymer resin is then fed into an extruder. In the extruder, the pellets simultaneously are melted and forced through the system by a heating melting screw.
• a spinning pump meters the melted polymer through a filter to a spinneret where the melted polymer is extruded under pressure through capillaries, at a rate of 0.3-1.0 grams per hole per minute.
• the spinneret contains up to 6000 capillaries per metre of die width, measuring 0.4-0.6 mm in diameter.
• the polymer is melted at about 30 °C - 120 °C above its melting point to achieve sufficiently low melt viscosity for extrusion.
• the fibres exiting the spinneret are quenched and drawn into fine fibres measuring 10 - 40 microns in diameter by cold air jets, reaching filament speeds of up to 5000 metres per minute.
• the solidified fibre is laid randomly on a moving belt to form a random netlike structure known in the art as web.
• the web is bonded to achieve its final strength using a heated textile calander known in the art as thermobond calander.
• the calander consists of two heated steel rolls; one roll is plain ant the other bears a pattern of raised points.
• the web is conveyed to the calander wherein a fabric is formed by pressing the web between the rolls at a bonding temperature of about 130 °C - 150 °C.
• Crystallisation temperatures are determined by DSC measurement according to ISO 3146 at a cooling rate of 10 K/min after a first heating to 200 °C.
• the shear thinning index SHI is calculated from the flow curve ⁇ ( ⁇ ) at 200 °C - which can be determined with a capillary rheometer according to ISO 11443 or calculated from the complex shear viscosity determined with a plate-plate rheometer according to ISO 6271-10 using the "Cox-Merz rule" relating the shear viscosity to the dynamic viscosity as described in W.P. Cox & E.H. Merz, J.Polym.Sci. 28(1958) 619-623.
• the SHI (0/50) is defined as the ratio between the zero shear viscosity ( ⁇ 0 ) and the viscosity at a stress ( ⁇ ) value of 50000 Pa.
• the shear thinning index is proportional to the broadness of the molecular weight distribution (MWD) of the polymer.
• the MWD curve shows two maxima or one maximum and a pronounced shoulder.
• the higher molecular weight tail will be limited in practice.
• the melt flow rates were measured with a load of 2.16 kg at 230 °C.
• the melt flow rate is that quantity of polymer in grams which the test apparatus standardised to ISO 1133 extrudes within 10 minutes at a temperature of 230 °C under a load of 2.16 kg.
• Ethylene content in propylene polymer was measured by Fourier transmission infrared spectroscopy (FTIR). A thin film of the sample (thickness approximately 250 ⁇ m) was prepared by hot-pressing. The area of -CH2- absorption peak (800 - 650 cm-1) was measured with Perkin Elmer FTIR 1600 - spectrometer. The method was calibrated by ethylene content data measured by 13 C NMR.
• FTIR Fourier transmission infrared spectroscopy
• xylene solubles fraction For the determination of the xylene solubles fraction, 2.0 g of polymer are dissolved in 250 ml p-xylene at 135 °C under agitation. After 30 ⁇ 2 min the solution is allowed to cool for 15 min at ambient temperature and then to settle for 30 min at 25 ⁇ 0.5 °C. The solution is filtered with filter paper into two 100 ml flasks.
• the tests are carried out in accordance with ISO 6721-2 on specimens of 60x10x1 mm cut from compression moulded plaques.
• a temperature range of at least -100 to +150 °C is covered, using a heating rate of 1 /min.
• the storage modulus G' and the tangent of the loss angle tan( ⁇ ) are the primary results of the tests; from tan( ⁇ ) the temperatures - peak position and peak broadness - of the various mobility transitions, such as the glass transition temperature T g , in the systems, which can be attributed to the phases present, can be determined.
• the mechanical properties of the fibres were determined on a Textechno Statimat M. according to ISO 5079.
• the gauge length used has been 100 mm for fibres and 200 mm for nonwoven, the speed was 100 m/min.
• the tensile test method which was used for nonwoven was Edana 20.2-89.
• Example 1 (invention, propylene/ethylene random heterophasic copolymer)
• a continuous multistage process was used.
• the process comprised a prepolymerisation step, a loop reactor and a fluidized bed gas phase reactor.
• the catalyst used was highly active, stereospecific transesterified MgCI 2 -supported Ziegler-Natta catalyst prepared according to US 5,234,879 at a titanisation temperature of 135 °C.
• the catalyst was contacted with a co-catalyst (triethylaluminium, TEAL), and an external donor (di-cyclopentyl dimethoxysilane) with the Al/Ti ratio of 200 and an Al/Donor ratio of 10, to yield a catalyst system.
• TEAL triethylaluminium
• an external donor di-cyclopentyl dimethoxysilane
• the catalyst system and propylene were fed into the prepolymerisation reactor which was operated at ca. 30 °C and ca. 30 bar.
• the prepolymerised catalyst was used in the subsequent polymerisation reactors.
• Propylene, ethylene and hydrogen and the prepolymerised catalyst were fed into the loop reactor which was operated as bulk reactor at a temperature of ca. 70 °C and a pressure of ca. 30 bar.
• the polymer slurry stream was fed from the loop reactor into the gas phase reactor which was operated at a temperature of ca. 70 °C and a pressure of ca. 20 bar. More propylene, ethylene and hydrogen were fed into the gas phase reactor to control the desired properties of the final polymer.
• the process comprised a prepolymerisation step and a loop reactor.
• the catalyst used was highly active, stereospecific transesterified MgCI 2 -supported Ziegler-Natta catalyst prepared according to US 5,234,879 at a titanisation temperature of 135 °C.
• the catalyst was contacted with a co-catalyst (triethylaluminium, TEAL), and an external donor (di-cyclopentyl dimethoxysilane) with the Al/Ti ratio of 200 and an Al/Donor ratio of 10, to yield a catalyst system.
• TEAL triethylaluminium
• an external donor di-cyclopentyl dimethoxysilane
• the catalyst system and propylene were fed into the prepolymerisation reactor which was operated at ca. 30 C and ca. 30 bar.
• the prepolymerised catalyst was used in the subsequent polymerisation reactors.
• Propylene, ethylene and hydrogen and the prepolymerised catalyst were fed into the loop reactor which was operated as bulk reactor at a temperature of ca. 70 °C and a pressure of ca. 30 bar.
• the product was degassed before being fed to an extruder for pelletisation.
• MFR Loop Melt Flow Rate of the matrix phase of the heterophasic copolymer
• XS Loop xylene soluble fraction of matrix phase of the heterophasic copolymer
• MFR end Melt Flow Rate of the heterophasic copolymer
• XS end xylene cold soluble fraction of the heterophasic copolymer
• C2 total total ethylene content of the heterophasic copolymer
• Polymer 3 is a controlled rheology material with final MFR 25 g/10 min
• Spinning trials have been performed on a Fourne long spin pilot line.
• the spinneret used has 52 holes, each having a diameter of 0.5 mm.
• the throughput per hole has been kept constant at 0.3 g/hole-min.
• Polymer 3 has been evaluated on a Reicofil 3.1 pilot line. It was run on a single beam at a melt temperature of 257 °C at the die and a throughput of 180 kg/m/h. Spinning stability was good and at a cabin pressure of 6916 Pa the filament titer was 1.6 denier. The mechanical properties obtained on a 17 g/m 2 web are listed in Table 2 below.
• the samples used for determining softness were yarns produced at 1000 m/min and

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