Reduction in VOC and FOG values of filled heterophasic polypropylene by separate aeration of individual polyolefin components

Abstract

A process for reducing the volatile and semi-volatile organic content (VOC and FOG values) of a heterophasic polypropylene composition, the heterophasic polypropylene composition comprising (i) at least 15 wt.-% of at least a first heterophasic polypropylene; (ii) less than 15 wt.-% of at least one elastomeric polyolefin, (iii) at least one filler; (iv) optionally polyethylene; and (v) optionally further polyolefins to below 100 g/g (VOC, VDA 278 October 2011) and below 390 g/g (FOG, VDA 278 October 2011), the process involving aerating the first heterophasic polypropylene and each further polyolefin component that is present in an amount of at least 15 wt.-% relative to the total weight of the heterophasic polypropylene composition, before extruding these aerated components with the at least one elastomeric polyolefin and the at least one filler and the optional polyethylene and/or optional further polyolefin(s).

Claims

1. A process for reducing the volatile and semi-volatile organic content (VOC and FOG values) of a heterophasic polypropylene composition, the heterophasic polypropylene composition comprising: i) at least 15 wt. % of at least a first heterophasic polypropylene; ii) less than 15 wt. % of at least one elastomeric polyolefin; iii) at least one filler; iv) optionally polyethylene; and v) optionally further polyolefins to below 100 g/g (VOC, VDA 278 October 2011) and below 390 g/g (FOG, VDA 278 October 2011), the process comprising the steps of: a) aerating the first heterophasic polypropylene through steps a1) to a5) as a substrate: a1) providing an aeration vessel having at least one inlet for aeration gas, at least one outlet for exhaust gas, an inlet for the substrate at the top of the aeration vessel, an outlet for the substrate at the bottom of the aeration vessel; wherein the substrate is present as a packed bed; a2) initiating a counter-current flow of the substrate and aeration gas a3) by; feeding a substrate showing a VOC value of greater than 100 g/g and an FOG value of greater than 390 g/g (VOC and FOG values according to VDA 278 October 2011), into said aeration vessel from the top, feeding the aeration gas into said aeration vessel via the at least one inlet at the bottom; withdrawing the exhaust gas via the outlet for exhaust gas; a4) maintaining said aeration gas flow for an aeration time of less than 12 hours; a5) withdrawing an aerated substrate having a VOC value of below 100 g/g and an FOG value of below 390 g/g (VOC and FOG values according to VDA 278 October 2011) via the outlet at the bottom of the aeration vessel; b) repeating steps a1) to a5) for the respective aeration of each further substrate that is present in an amount of at least 15 wt. % relative to the total weight of the heterophasic polypropylene composition, such that all substrates which are individually present in an amount of at least 15 wt. % relative to the total weight of the heterophasic polypropylene composition are aerated; c) extruding the withdrawn first heterophasic polypropylene and any further aerated substrates with the at least one elastomeric polyolefin and the at least one filler and the optional polyethylene and/or optional further polyolefin(s) if present to afford the heterophasic polypropylene composition having a VOC value below 100 g/g (VDA 278 October 2011) and a FOG value below 390 g/g (VDA 278 October 2011), wherein the at least one elastomeric polyolefin and the at least one filler are not aerated.

2. The process according to claim 1, wherein the combined first heterophasic polypropylene and any further aerated polyolefin components make up 50 to 90 wt. % of the heterophasic polypropylene composition.

3. The process according to claim 1, wherein the aeration gas is air.

4. The process according to claim 1, wherein the process is continuous.

5. The process according to claim 1, wherein the raw first heterophasic polypropylene and any further polyolefin components to be aerated are provided in pellet form, and the pellets have a diameter D in the range of 2.5 mm up to 5 mm.

6. The process according to claim 4, wherein the pellets are pre-heated before being added to the aeration vessel.

7. The process according to claim 1, wherein the temperature of the aeration gas is from 100 C. to 140 C.

8. The process according to claim 1, whereby the exhaust gas is subjected to a purification step and then recycled back into the inlet for the aeration gas.

9. The process according to claim 1, wherein the exhaust gas optionally passes a heat exchanger before being discharged into the atmosphere.

10. The process according to claim 1, wherein the aeration vessel is cylindrical, or conical, or cylindrical with a cone shaped bottom portion.

11. The process according to claim 1, wherein the heterophasic polypropylene composition comprises in addition to components (i) to (v) at least one slip agent as component (vi).

12. The process according to claim 1, wherein the heterophasic polypropylene composition comprises in addition to components (i) to (v) at least one slip agent as component (vi), and wherein the slip agent is selected from the group of fatty acid amides.

Description

BRIEF DESCRIPTION OF THE FIGURES

(1) FIG. 1 shows the VOC content of the inventive and comparative examples

(2) FIG. 2 shows the FOG content of the inventive and comparative examples

DETAILED DESCRIPTION OF THE INVENTION

(3) The Process

(4) The invention is primarily concerned with a process for reducing the volatile and semi-volatile organic content (VOC and FOG values) of a heterophasic polypropylene composition, the heterophasic polypropylene composition comprising (i) at least 15 wt.-% of at least a first heterophasic polypropylene; (ii) less than 15 wt.-% of at least one elastomeric polyolefin, (iii) at least one filler; (iv) optionally polyethylene; and (v) optionally further polyolefins
to below 100 g/g (VOC, VDA 278 October 2011) and below 390 g/g (FOG, VDA 278 October 2011),
the process comprising the steps of a) aerating the first heterophasic polypropylene through steps a1) to a5) wherein the polyolefin of said steps is the first heterophasic polypropylene: a1) providing an aeration vessel having at least one inlet for aeration gas, at least one outlet for exhaust gas, an inlet for a polyolefin at the top of the aeration vessel, an outlet for the polyolefin at the bottom of the aeration vessel; wherein the polyolefin is present as a packed bed; a2) initiating a counter-current flow of the polyolefin and aeration gas a3) by feeding the raw polyolefin showing a VOC value of greater than 100 g/g and an FOG value of greater than 390 g/g (VOC and FOG values according to VDA 278 October 2011), into said aeration vessel from the top feeding the aeration gas into said aeration vessel via the at least one inlet at the bottom; withdrawing the exhaust gas via the outlet for exhaust gas; a4) maintaining said aeration gas flow for an aeration time of less than 24 hours; a5) withdrawing the aerated polyolefin having a VOC value of below 100 g/g and an FOG value of below 390 g/g (VOC and FOG values according to VDA 278 October 2011) via the outlet at the bottom of the aeration vessel; b) repeating steps a1) to a5) for the respective aeration of each further polyolefin component that is present in an amount of at least 15 wt.-% relative to the total weight of the heterophasic polypropylene composition, such that all polyolefin components that are individually present in an amount of at least 15 wt.-% relative to the total weight of the heterophasic polypropylene composition are aerated; c) extruding the withdrawn first heterophasic polypropylene and any further aerated polyolefin components with the at least one elastomeric polyolefin and the at least one filler and the optional polyethylene and/or optional further polyolefin(s) if present to afford the heterophasic polypropylene composition having a VOC value below 100 g/g (VDA 278 October 2011) and a FOG value below 390 g/g (VDA 278 October 2011).

(5) The effect of the invention is a more efficient reduction of VOC and FOG values than would be achieved by aeration of pellets of the final blended heterophasic polypropylene composition.

(6) Whilst it is trivial that a reduction of the mass to be treated will speed up the process, i.e. increase space-time yield, other factors combine to enhance the increase in space-time yield. By selecting only the components that are the chief contributors to the overall FOG and VOC content of the composition, said overall values can be reduced to a satisfactory level without the need for aeration of other components. Whilst the resultant FOG and VOC values of the composition will be higher than in case that every component were aerated, the values are still more than satisfactory for the composition to be used in the manufacture of inter alia automobile articles. The improvement in space-time yield as result of the process outweighs the reduced effect of the degassing.

(7) The improvement in space-time yield has obvious economic advantages, as aeration for relatively short time periods requires less energy to supply heated gas. Additionally, less space is required for silos to house the polymer composition than for longer aeration processes, wherein larger amounts of the polymer composition must be stored for longer periods of time during the aeration process.

(8) The process of the invention as given above defines that each polyolefin fraction which makes up at least 15 wt.-% of the heterophasic polypropylene composition is aerated through steps a1) to a5). Since the at least one elastomeric polyolefin is present in less than 15 wt.-%, this means that both it and the filler (which may be present in at least 15 wt.-% but is not a polyolefin) are not aerated.

(9) It is preferred that the total mass of polyolefins to be aerated is not so high as to minimize the efficiency gains of the process of the invention, but similarly not so low as to mean that the reduction in VOC and FOG values is insufficient for use in, for example, automobile interiors. Suitably the total mass of the compounds to be aerated makes up 50 to 90 wt.-% of the heterophasic polypropylene composition.

(10) Should it be necessary, it is also theoretically possible to further improve the efficiency by tailoring the degassing properties to each individual component, rather than to the most sticky component, as must be done when the composition is aerated as a whole.

(11) In addition, the aeration process of the current invention also has advantages in terms of maintaining the structural properties of the heterophasic polypropylene composition and maintaining the scratch resistance of the polypropylene material while also leading to low levels of VOCs and FOGs. It is believed that aerating for extremely long periods of time with a low temperature gas, or using a gas with a temperature of greater than 140 C. would lead to deterioration of the properties of the polypropylene material, for example deterioration of the scratch resistance properties of the polypropylene.

(12) Furthermore, the process according to the present invention does not lead to a significant loss of slip-agent meaning that if the heterophasic polypropylene composition is used for injection moulding to produce polypropylene articles, it is easily released from the mould and no polypropylene is left stuck to the mould surface.

(13) Heterophasic Polypropylene Composition

(14) The heterophasic polypropylene composition of the invention comprises (i) at least 15 wt.-% of at least a first heterophasic polypropylene; (ii) less than 15 wt.-% of at least one elastomeric polyolefin, (iii) at least one filler; (iv) optionally polyethylene; and (v) optionally further polyolefins

(15) The properties of the first heterophasic polypropylene are not particularly limited.

(16) The MFR.sub.2 may for example be from 0.1 to 200 g/10 min, more preferably from 1.0 to 150 g/10 min. The density may be from 850 to 930 g/cm.sup.3, more preferably from 860 to 910 g/cm.sup.3.

(17) Examples of suitable heterophasic polypropylenes include but are not limited to BG055AI, BF970MO, BJ400HP, ED007HP, EF015AE and EG050AE, commercially available from Borealis AG, Austria. The heterophasic polypropylene may also be a virgin reactor-made heterophasic polypropylene.

(18) The at least one elastomeric polyolefin is similarly not particularly limited.

(19) Suitable elastomeric polyolefins are often copolymers of ethylene with -olefin comonomers, for example octene.

(20) Examples of suitable elastomeric polyolefins include Engage 7220, Engage 8100, Engage 8200 and Engage 8401 from Dow Chemical, USA, as well as Queo 8201, Queo 8203 and Queo 8210 from Borealis AG, Austria. The at least one elastomeric polyolefin may also be a virgin reactor-made elastomeric polyolefin.

(21) The at least one filler is selected from the group of natural or synthetic non-thermoplastic fillers or reinforcement. Preferably the at least one filler is a mineral filler. It is appreciated that the at least one filler is a phyllosilicate, mica or wollastonite. Even more preferred the at least one filler is selected from the group consisting of mica, wollastonite, kaolinite, smectite, montmorillonite and talc. The most preferred at least one filler is talc.

(22) The optional polyethylene is usually (when present) in the form of a masterbatch formulation for the addition of various additives and stabilizers. The optional additives of the heterophasic polypropylene composition are well-known in the art, and may include (but are not restricted to) the group of antioxidants, pigments, nucleating agents and specific additives for enhancing UV stability and/or scratch resistance. Additives known to improve the scratch resistance of polypropylene compounds include erucamide, stearate and glycerol monostearate amongst others.

(23) The further polyolefins are not limited, and can, for example, be further heterophasic polypropylenes as described above.

(24) The melting temperature (Tm) of the raw first heterophasic polypropylene and all further polyolefin components to be aerated is preferably greater than 150 C., more preferably greater than 160 C. Following aeration there may be a negligible change in the melting point (T.sub.m) of the polypropylene composition, such as e.g. a less than 10% reduction in melting point (T.sub.m) value, or a less than 5% reduction in melting point value, or a less than 2.5% reduction in melting point value. The melting temperature (T.sub.m) of the individual components following aeration are, therefore, each greater than 150 C., preferably greater than 160 C. Without wishing to be bound by any theory, it is believed that the aeration process according to the present invention does not lead to a substantial change in the properties of the individual components, such as e.g. T.sub.m, and therefore there would be no substantial change in the properties of the final heterophasic polypropylene composition of the invention relative to an identical heterophasic polypropylene composition in which no individual component has undergone aeration.

(25) The individual aerated components of the heterophasic polypropylene composition of the invention may show FOG values of 500 g/g or less, preferably 450 g/g or less, more preferably 400 g/g or less, and most preferably of 380 g/g or less. In addition, the individual aerated components that result from the inventive process according to steps a1) to a5) may show VOC values of 150 g/g or less, preferably of 100 g/g or less, more preferably of 80 g/g or less, and most preferably of 60 g/g or less. (Both VOC and FOG values according to VDA 278 October 2011)

(26) In certain embodiments, the inventive process leads to a reduction in VOC values (VDA 278 October 2011) of the aerated components of the heterophasic polypropylene composition, relative to said aerated components prior to aeration, of greater than 50%, preferably greater than 60%, more preferably of greater than 70%.

(27) In certain embodiments, the inventive process leads to a reduction in FOG values (VDA 289 October 2011) of the aerated components of the heterophasic polypropylene composition, relative to said aerated components prior to aeration, of greater than 10%, preferably greater than 20%, more preferably greater than 30%.

(28) In certain such embodiments, the inventive process leads to a reduction, relative to said aerated components prior to aeration, in VOC values (VDA 278 October 2011) of the aerated components of the polypropylene composition of greater than 50%, and a reduction in FOG values (VDA 278 October 2011) of greater than 10%, more preferably a reduction of greater than 60% and 20% respectively, most preferably a reduction in VOC values (VDA 278 October 2011) of the aerated components of the polypropylene composition of greater than 70%, and a reduction in FOG values (VDA 278 October 2011) of greater than 30%.

(29) The heterophasic polypropylene composition of the invention may show FOG values of 390 g/g or less, preferably 380 g/g or less, and most preferably of 370 g/g or less. In addition, the heterophasic polypropylene compositions that result from the inventive process may show VOC values of 100 g/g or less, preferably of 90 g/g or less. (Both VOC and FOG values according to VDA 278 October 2011).

(30) In certain embodiments, the inventive process leads to a reduction in VOC values (VDA 278 October 2011) of the heterophasic polypropylene composition, relative to a comparative heterophasic polypropylene composition in which none of the components have undergone aeration, of greater than 30%, preferably greater than 40%, more preferably of greater than 50%.

(31) In certain embodiments, the inventive process leads to a reduction in FOG values (VDA 289 October 2011) of the heterophasic polypropylene composition, relative to a comparative heterophasic polypropylene composition in which none of the components have undergone aeration, of greater than 10%, preferably greater than 30%, more preferably greater than 20%, most preferably greater than 30%.

(32) In certain such embodiments, the inventive process leads to a reduction, relative to a comparative heterophasic polypropylene composition as described above, in VOC values (VDA 278 October 2011) of the polypropylene composition of greater than 30%, and a reduction in FOG values (VDA 278 October 2011) of greater than 10%, more preferably a reduction of greater than 40% and 20% respectively, most preferably a reduction in VOC values (VDA 278 October 2011) of the polypropylene composition of greater than 50%, and a reduction in FOG values (VDA 278 October 2011) of greater than 30%.

(33) The process according to the present invention, furthermore, does not lead to depletion of slip agents such as e.g. erucamide. During polypropylene production, slip agents are often added to the polypropylene blend in order to reduce the coefficient of friction of these polypropylene materials. The most popular slip agents used by industry are from the chemical group of fatty acid amides, such as e.g. erucamide. When a slip agent is mixed with a polypropylene polymer melt, it is absorbed into the amorphous regions of the polypropylene polymer.

(34) Upon cooling, the slip agent becomes incompatible with the polypropylene material because of the different surface energies of the two materials and migrates to the material surface.

(35) The rate of migration depends on the difference between the surface energies of the polypropylene and the slip agent (the larger the difference, the faster the migration). This initially leads to the formation of a monolayer on the polymer surface, followed by the deposition of subsequent layers when new molecules of the slip agent arrive on the surface leading to the formation of a double layer. Because of weak bonding between the layers of fatty acid amides, materials produced from polypropylene containing fatty acid amides will slide over each other with ease. The presence of a layer of slip agent also reduces the friction at the surface of the polypropylene composition. This property is also important, for example, when producing injection-moulded articles, as slip agents can be used to help aid the release of injection-moulded articles from a mould. Fatty acid amides come to the surface of polypropylene articles, when the polypropylene cools; therefore, reducing the coefficient of friction between the polypropylene article and the mould. This means that with relatively little force the polypropylene article can be removed from the mould and that no polypropylene sticks to the mould on release of the moulded article. Many slip agents in particular fatty acid amides, such as e.g. erucamide are relatively volatile and, therefore, care is required to prevent these materials escaping during processing steps in polymer production. The process according to the current invention does not lead to depletion of slip agents in particular fatty acid amides, such as e.g. erucamide. Therefore, the process according to the present invention allows the advantageous removal of volatile and semi-volatile substances, without stripping out slip agents from the polypropylene composition. Thus, in the process according to the present invention, the polypropylene composition preferably contains at least one slip agent, more preferably at least one slip agent selected from the group of fatty acid amides, most preferably erucamide.

(36) Aeration Gas Flow

(37) In the process according to the present invention, the polyolefin, preferably in the form of pellets, is preferably subjected to a warm gas-stream.

(38) The present invention preferably provides a process, wherein the total normalised volumetric airflow used is from 1 to 5 Nm.sup.3/kg such as at least about 1.5 Nm.sup.3/kg, preferably at least about 2 Nm.sup.3/kg, such as around 2.6 Nm.sup.3/kg.

(39) According to the present invention, the gas input is at the bottom of the aeration vessel, resulting in a gas flow from bottom to top through the bed of the polyolefin composition. In the present invention, the gas inlet may preferably be selected from the group of: a nozzle, a series of nozzles, a gas distribution ring and a gas distribution plate.

(40) The process according to the present invention comprises a step of optionally subjecting the gas downstream of the aeration vessel to a means for removing the hydrocarbons. Preferably, these means are selected from one or more catalytic oxidation units, one or more carbon absorption columns (drums) and/or any conventional exhaust treatment known in the art. Even more preferably, these means are carbon absorption columns (drums). Preferably, when the aeration gas is air and/or nitrogen, it can be emitted into the atmosphere after removal of hydrocarbons. Additionally, the aeration gas can be treated and re-circulated back into the aeration vessel.

(41) Moreover, the heat still contained in the discharged gas can be transferred to the gas used for aeration via heat exchangers known in the art, if the gas taken from the environment has a temperature lower than the temperature needed for the process.

(42) In the process according to present invention, the exhaust gas is preferably discharged into the atmosphere. Alternatively, but less preferably the exhaust gas is used again after separation of the volatile and semi-volatile substances.

(43) Aeration Process

(44) The present invention preferably provides an aeration process, which is operated for less than 24 hours, preferably less than 12 hours, more preferably less than 10 hours, most preferably from 3 to 9 hours. Generally, the aeration time is inversely proportional to the gas temperature, meaning that a compromise must be reached to avoid the pellets melting and sticking together. Typical values for the temperature and residence time for polypropylene according to EP 1 671 773 A1 are from 80 to 110 C. for a period of from 10 to 50 hours. It is believed that the reduction in VOC values reaches a plateau following extended aeration times of greater than five hours in the conditions described here; in contrast, for FOG values there is a weaker dependence on aeration time in the period from 0 to 5 hours. It is believed that this is due to slow diffusion of higher molecular weight alkanes (C.sub.16-C.sub.32), which contribute greatly to FOG values, in contrast to the rapid diffusion of C.sub.25 which are considered for VOC values.

(45) In the process according to the present invention, the polyolefin is preferably not mixed or moved throughout the treatment by mechanical means. Consequently, during the aeration process the polyolefin composition is effectively stationary (apart from its vertical transit through the aeration vessel). Therefore, the present invention preferably excludes processes where the polymer composition is agitated during aeration; these processes do not fall under the scope of this invention, such as fluidised bed processes. Absence of mechanical mixing and similar measures such as re-filling or the like is particularly advantageous since the creation of fines is avoided. In addition, the filling degree is higher without the need for mechanical stirring or the need to transfer the polyolefin composition into another treatment vessel/silo.

(46) The present invention optionally provides a process, wherein the pellets are pre-heated before being added to the aeration vessel, such as being pre-heated to at least 40 C., more preferably pre-heated to temperatures of from 80 C. to 100 C. before being added to the aeration vessel.

(47) As the specific heat capacity of the polyolefin composition together with the mass of the polyolefin composition is significant compared to the specific heat capacity of the gas together with the mass of the gas, one has to be attentive that the gas stream temperatures are met for the inlet and the outlet of the aeration. Thus, if the polyolefin composition is provided at relatively low temperatures in a silo, a pre-heating step will be necessary. The pre-heating can also naturally be effected by the gas-stream and the temperatures as specified above. However, during such pre-heating the temperature at the outlet will be lower as the heat is transferred to the polyolefin composition.

(48) The polyolefin composition is optionally pre-heated before the start of the aeration time to speed up the process. Generally, any heating measures known in the prior art can be used for pre-heating. The polyolefin composition may be pre-heated to temperatures of 40 C. or more, preferably 50 C. or more.

(49) Pre-heating could also be considered as not letting the pellets cool down, which are produced, extruded and pelletized shortly beforehand. Such pellets normally have a temperature of about 40 C. or higher, preferably 50 C. or higher. Hence, the production process of the polyolefin composition and the process of the current invention can be carried out as an integrated process.

(50) In contrast, the present invention may provide a process in which the polyolefin composition is not pre-heated before being added to the aeration vessel and in which the polyolefin is simply warmed by the flow of heated aeration gas in the silo. Without wishing to be bound by any theory, it is believed that with a rather small pellet size (diameter of ca. 3.5 mm), the composition reaches the desired aeration temperature rapidly after being added to the aeration vessel.

(51) The aeration vessel used in the process of the present invention is not particularly limited and in principle, any commercially available aeration vessel or aeration silo may be used; in addition, customised aeration vessels, which have been specifically constructed for the purpose of aeration, may be used.

(52) For shortening the pre-heating phase, avoiding energy loss during aeration and/or also increased homogeneity over the cross-section, the use of an isolated treatment vessel, preferentially an isolated silo is preferred. The silo may for example be a steel silo. Furthermore, the silo may be cylindrically or conically shaped.

(53) Products and Articles

(54) An aspect of the present invention also relates to products obtainable by the processes described above and to articles produced therewith. Polypropylene is a versatile material that is easily processable and which finds a number of applications in the automobile industry e.g. for injection moulded components such as, e.g., dashboards or car door interior articles. Polypropylene compositions are also used as the covering for blister packaging.

(55) All preferred ranges and embodiments as described above also hold for these products and articles and are incorporated by reference herewith.

(56) Experimental Part

(57) The following Examples are included to demonstrate certain aspects and embodiments of the invention as described in the claims. It should be appreciated by those of skill in the art, however, that the following description is illustrative only and should not be taken in any way as a restriction of the invention.

(58) Test Methods

(59) Sample Preparation

(60) VOC values, FOG values and TVOC values were measured as described below, after sample preparation consisting of injection moulding plaques in the acc. EN ISO 19069-2:2016. These plaques were packed in aluminium-composite foils immediately after production and the foils were sealed.

(61) For the thermodesorption analysis according to VDA 278 (October 2011) the samples were stored uncovered at room temperature (23 C. max.) for 7 days directly before the commencement of the analysis.

(62) Regarding the VDA 277 (January 1995) measurements, no additional uncovered storage or other conditioning took place. Instead, the injection moulded plaques were cut and ground in a Retsch SM-2000 mill.

(63) In both cases (VDA 277 and VDA 278), the production date of the injection moulded plaques, the time when the sample arrived in the lab as well as the analysis date were recorded.

(64) VOC and FOC acc VDA278

(65) VOC Value

(66) is determined according to VDA 278 October 2011 from injection moulded plaques. VDA 278 October 2011, Thermal Desorption Analysis of Organic Emissions for the Characterization of Non-Metallic Materials for Automobiles, VDA Verband der Automobilindustrie. 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.

(67) FOG Value

(68) is determined according to VDA 278 October 2011 from injection moulded plaques. According to the VDA 278 October 2011 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 having a boiling point in the boiling range of n-Alkanes C16 to C32 are determined and analyzed.

(69) Melt Flow Rate (MFR.sub.2)

(70) The melt flow rates were measured with a load of 2.16 kg (MFR.sub.2) at 230 C. The melt flow rate is the quantity of polymer in grams which the test apparatus standardized to ISO 1133 extrudes within 10 minutes at a temperature of 230 C. under a load of 2.16 kg.

(71) Xylene Cold Soluble Fraction (XCS wt %)

(72) The xylene cold soluble fraction (XCS) is determined at 23 C. according to ISO 6427.

(73) Polymer-Puncture Plaque-Instrumented

(74) Puncture energy is determined in the instrumented falling weight test according to ISO 6603-2 using injection moulded plaques of 60601 mm and a test speed of 2.2 m/s, clamped, lubricated striker with 20 mm diameter. The reported puncture energy results from an integral of the failure energy curve measured at (60601 mm).

(75) Diameter D

(76) A sieve analysis according to ISO 3310 was performed. The sieve analysis involved a nested column of sieves with wire mesh screen with the following sizes: >20 m, >32 m, >63 m, >100 m, >125 m, >160 m, >200 m, >250 m, >315 m, >400 m, >500 m, >710 m, >1 mm, >1.4 mm, >2 mm, >2.8 mm, >4 mm. The samples were poured into the top sieve which has the largest screen openings. Each lower sieve in the column has smaller openings than the one above (see sizes indicated above). At the base is the receiver. The column was placed in a mechanical shaker. The shaker shook the column. After the shaking was completed the material on each sieve was weighed. The weight of the sample of each sieve was then divided by the total weight to give a percentage retained on each sieve. The particle size distribution and the characteristic median particle size d50 was determined from the results of the sieve analysis according to ISO 9276-2.

EXAMPLES

(77) Resin Composition

(78) The following components were blended to form a filled heterophasic polypropylene composition.

(79) TABLE-US-00001 TABLE 1 Filled heterophasic polypropylene composition to be aerated. Component Wt.-% HECO 1 29.32 HECO 2 17.6 HECO 3 15.0 EP 1 6.0 Talc 17.0 CB 4.5 PE 8.0 PP 1.2 Epoxy resin 0.4 Erucamide 0.23 Nucleating agent NA-21 0.2 Cyasorb UV 3808PP5 0.2 Irganox 1076 FD 0.15 Richfos 168 0.1 chalk 0.1 HECO 1: Commercial heterophasic propylene copolymer BJ400HP of Borealis AG, Austria, having a melt flow rate MFR.sub.2 (230 C.) of 100 g/10 min and a content of xylene cold solubles (XCS) of 14 wt.-%. HECO 2: Commercial heterophasic propylene copolymer EF015AE of Borealis AG, Austria, having a melt flow rate MFR.sub.2 (230 C.) of 18 g/10 min and a content of xylene cold solubles (XCS) of 31 wt.-%. HECO 3: Commercial heterophasic propylene copolymer ED007HP of Borealis AG, Austria, having a melt flow rate MFR.sub.2 (230 C.) of 7 g/10 min and a content of xylene cold solubles (XCS) of 25 wt.-%. EP: Commercial elastomeric ethylene-octene copolymer Engage 8200 of Dow Chemical, USA having a melt flow rate MFR.sub.2 (190 C.) of 5 g/10 min and a density of 870 kg/m.sup.3. Talc: Commercial talc Jetfine 3 CA of Imerys, UK. PE: Commercial high-density polyethylene BorPure MB7541 of Borealis having a melt flow rate MFR.sub.2 (190 C.) or 4 g/10 min and a density of 954 kg/m.sup.3. PP: Commercial propylene homopolymer HA001A-B1 of Borealis having a melt flow rate MFR.sub.2 (230 C.) of 0.6 g/10 min. Epoxy resin: Commercial bisphenol-based medium molecular weight solid epoxy resin NPES-902 of Nan Ya Plastics Corporation, Taiwan.

(80) Compounding was performed in a Coperion W&P ZSK40 twin screw extruder in a temperature range of 220-240 C. followed by solidification of the resulting melt strand in a water bath and pelletization.

(81) Comparative Example 1 (CE1)

(82) CE1 represents the resin composition as described above, in which neither the individual components nor the final composition have been subjected to aeration.

(83) Comparative Example 2 (CE2)

(84) CE2 represents the resin composition as described above, in which the final composition has been subjected to aeration subsequent to compounding.

(85) Aeration was carried out in an insulated cylindrically shaped silo with dimensions of 1.5 m.sup.3. The pellets had a median particle size d50 of 3.5 mm (ISO 3310, evaluation according to ISO 9276-2).

(86) The pellets were at room temperature (ca. 25 C.) before being subjected to aeration i.e. a pre-heating step was not applied.

(87) The aeration process was carried out for 7 hours at a temperature of 140 C. A gas flow rate of 260 m.sup.3/h was used. This corresponds to a normalised gas flow of 2.6 Nm.sup.3/kg. The pellets were not mixed or agitated during the process and instead simply moved vertically through the silo at a speed of 100 kg/h.

(88) The process was carried out on a 1000 kg scale. In a cylindrical silo of 1.5 m.sup.3. A relative flow rate of polypropylene composition pellets of 100 kg/h was maintained throughout the aeration process.

(89) Inventive Example 1 (IE1)

(90) IE1 represents the resin composition as described above, in which HECO 1, HECO 2 and HECO 3 have been subjected to aeration individually prior to the compounding step in which the resin composition as described is blended.

(91) The aeration conditions for the individual components are identical to those described above for CE2.

(92) The VOC and FOG values obtained for HECO 1, HECO 2, HECO 3 and each final composition are given in Table 2. The values in parentheses are the VOC and FOG values for the unaerated individual HECO components.

(93) TABLE-US-00002 TABLE 2 Volatile organic and semi-volatile organic condensable contents of the resin components and final composition under differing aeration regimes. % reduction % reduction Example VOC (g/g) FOG (g/g) of VOC of FOG HECO 1 48 (197) 369 (630) 76% 41% HECO 2 56 (196) 377 (632) 71% 40% HECO 3 32 (131) 274 (394) 76% 30% CE1 205 545 CE2 42 283 80% 48% IE1 85 363 59% 33%

(94) As can be seen from the data in Table 2, whilst the reduction of VOC and FOG values is higher for CE2 than for IE1, the efficiency (i.e. space-time yield) of IE1 is improved. In the process of IE1 only approx. 62% of the composition has been aerated, whilst the reduction of VOC content is 73.6% as high as for CE2 (i.e. 59%/80%) and the reduction of the FOC content is 69.5% as effective.

(95) As discussed previously, this improved space-time yield has obvious economic advantages, as aeration for relatively short time periods requires less energy to supply heated gas. Additionally, less space is required for silos to house the polymer composition than for longer aeration processes, wherein larger amounts of the polymer composition must be stored for longer periods of time during the aeration process.

(96) Further improvements could be envisaged if the aeration of each individual component were optimized separately, rather than general conditions used for each resin.