CA1247816A - Lightly crosslinked linear olefinic polymer foams and process for making - Google Patents
Lightly crosslinked linear olefinic polymer foams and process for makingInfo
- Publication number
- CA1247816A CA1247816A CA000495177A CA495177A CA1247816A CA 1247816 A CA1247816 A CA 1247816A CA 000495177 A CA000495177 A CA 000495177A CA 495177 A CA495177 A CA 495177A CA 1247816 A CA1247816 A CA 1247816A
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- CA
- Canada
- Prior art keywords
- cross
- foam
- linear
- linking agent
- linking
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Classifications
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J9/00—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof
- C08J9/0066—Use of inorganic compounding ingredients
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J9/00—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof
- C08J9/0014—Use of organic additives
Abstract
ABSTRACT
A substantially closed-celled linear poly-olefin foam is made by melt processing under pressure a linear polyolefin together with a volatile blowing agent and a cross-linking agent and then expanding the polymer. Suitable cross-linking agents, includ-ing azido and vinyl functional silanes, organic peroxides, multifunctional vinyl monomers, and oxygen, increase the melt tension and melt viscosity of the polymer by lightly cross-linking the polymer with itself to enable the production of foams having improved properties in comparison with branched polyolefin foams.
A substantially closed-celled linear poly-olefin foam is made by melt processing under pressure a linear polyolefin together with a volatile blowing agent and a cross-linking agent and then expanding the polymer. Suitable cross-linking agents, includ-ing azido and vinyl functional silanes, organic peroxides, multifunctional vinyl monomers, and oxygen, increase the melt tension and melt viscosity of the polymer by lightly cross-linking the polymer with itself to enable the production of foams having improved properties in comparison with branched polyolefin foams.
Description
.~ 78~
LIGHTLY CROSSLINKED LINEAR OLEFI~IC
POLYMER FOAMS AND PROCESS FOR MAKING
This invention relates to lightly cross-linked linear olefinic polymer foam materials and processes for the preparation thereof.
Closed-cell branched ethylenic polymer foams may be manufac-tured by the process of extrusion foaming, wherein a normally solid thermoplastic ethylenic polymer resin, such as low density poly-ethylene, is melt processed and mixed under pressure with a volatile blowing agent to form a flowable gel.
The gel is then passed through a shaping orifice or die op ning into a zone of lower pressure. As the pressure is lowered, the volatile constituent of the gel vaporizes forming cells in the resin structure, which cools to a cellular foam material.
Linear olefinic polymers such as. linear low density polyethylene, high density polyethylene, and polypropylene have several properties which make the use of these polymers in foams desirable. For example, these linear olefinic polymers have a higher modulus of elasticity, greater toughness, higher heat distortion temperature, and lower permeability to blowin~ agents than other branched olefins. However, 31,339-F -1-
LIGHTLY CROSSLINKED LINEAR OLEFI~IC
POLYMER FOAMS AND PROCESS FOR MAKING
This invention relates to lightly cross-linked linear olefinic polymer foam materials and processes for the preparation thereof.
Closed-cell branched ethylenic polymer foams may be manufac-tured by the process of extrusion foaming, wherein a normally solid thermoplastic ethylenic polymer resin, such as low density poly-ethylene, is melt processed and mixed under pressure with a volatile blowing agent to form a flowable gel.
The gel is then passed through a shaping orifice or die op ning into a zone of lower pressure. As the pressure is lowered, the volatile constituent of the gel vaporizes forming cells in the resin structure, which cools to a cellular foam material.
Linear olefinic polymers such as. linear low density polyethylene, high density polyethylene, and polypropylene have several properties which make the use of these polymers in foams desirable. For example, these linear olefinic polymers have a higher modulus of elasticity, greater toughness, higher heat distortion temperature, and lower permeability to blowin~ agents than other branched olefins. However, 31,339-F -1-
2 ~ Z~78~
previous attempts to produce low density foams of these linear olefins by an extrusion process have been unsuccessful. Linear polyolefins, when foamed by an extrusion process suffer from small foam cross-~section, high levels of open cells, flow instability,and a narrow ranye of foaming temperatures.
The exact cause of problems of foaminy linear polyol-efins i5 not believed to be known.
However, it is generally believed that poor melt strength together with a sharp change in melt viscosity near the transition temperature makes extrusion foaming of linear polyolefins difficult.
With these properties, it is difficult to control bubble expansion during extrusion and under con-lS ditions of h@at and high shear stresses. Thisresults in many broken bubbles (open cells) during expansion and consequent poor foams.
Previous efforts to cure these problems with the foamability of linear polyolefins have centered around blending a linear polyolefin with another olefin polymer having good extrusion foam-ability. For example, Park et al, U.S. Patent No. 4,226,946, blended a linear polyethylene with a low density branched polyethylene to improve extru-sion foamability of the linear polyethylene. Watanabeet al, U.S. Patent No. 4,102,829, blended an ionomer resin with a linear polyethyle~e for the same purpose.
However, such known methods offer only partial solutions because of one or more deficiencies in the range of operating parameters, cost of materials, and final foam properties.
31,339-F -2-i _3_ ~2~7~6 It is also known that relatively lightly to moderately cross-linked thermoplastic polymers have melt properties that are suitable :Eor foam expansion. However, such cross-linked polymers are difficult to process on conventiona:L melt pro-cessing apparatus such as extruders because of flow instability. ~he prior art has general:Ly not utilized cross-linked polymers on such apparatus because shear degradation of the pol~ner occurs during melt processing and extrusion.
Accordingly, there is a need in the art for linear olefinic polymer compositions and pro-cesses which can be utili.zed to foam or expand such polymers in conventional melt processing apparatus.
The present invention meets that need by providing a process for the preparation of a lightly cross-linked linear olefinic pol~mer foam having a substantially closed-cell structure. The term "linear olefinic polymer" as used in this specifi-cation includes both polymers and copolymers of linear olefins such as linear low density poly-ethylene (LLDPE), high density polyethylene (HDPE) and polypropylene (PP), as well as polystyrene (PS).
In one aspect the present invention con-cerns a process or preparing a lightly cross-linked linear polyolefin foam having a substantially closed--cell structure, comprising the steps of:
a) melt blending under pressure at least one linear polyolefin selected from the group con-sisting of LLDPE, HDPE, PP and PS together with a 31,339-F -3-~2~78:L6 blowing agent and a sufficient amount o a cross-linking agent selected from the group consisting of azido functional silanes, vinyl functional silanes, organic peroxides, multifunctional vinyl monomers, and oxygen, to form a flowable admixture, and, (b) extruding said admixture through a die to a zone of lower pressure and activating said ~lowing agent to expand at least one linear polyolefin to form said lightly cross-linked foam. ~ -The cross-linking agent in step ~a) can be a~mixed together with the blowing agent and the linear polyolefin or can be added after a flowable admixture of the linear polyolefin and the blowing agent is formed in an amount sufficient to initiate cross--linking of -the linear polyolefin and increase the pressure of the admixture to at least 400 psig (2758 kPa).
In another aspect the present invention concerns a lightly cross-linked linear polyolefin foams prepared according to the aforementioned process.
A linear olefinic polymer or blend of linear olefinic polymers is melt processed in a conventional manner by feeding, melting, and metering it in a conven-tional melt processing apparatus such as an extruder.
A volatile blowing agent and cross~linking agent are mixed with the linear olefinic pol~ner und~er pressure to form a flowable gel or admixture. The cross-linking agent is added in an amount which is sufficient to initiate cross-linking and raise the pressure of the gel or admixture at the die opening to approximately 31,339-F -4-_5- ~Z4~
400 (2759 kPa) or above but insufficient to cause melt fracture of the polymer to occur. "Melt fracture" is a term used in the art to describe a melt flow instability of a polymer as it is extruded through cl die which flow instability causes voids and/or other irregularities in the final produc-t. Suitable cross-linking agents have been found to include azido and vinyl functional-silanes, organic peroxides, multifunctional vinyl monomers, and oxygen.
As the flowable gel or admixture is extruded through the die, opening to a zone of lower pressure, the volatile blowing agent activates to expand the linear olefinic polymer to a substantially closed-cell foam structure which is lightly cross-linked to itself.
Foams having densities of betwen 0.6 and 15 pounds per cubic oot (pcf) (9.6 and 240.3 kg/m3) may be produced.
The linear olefinic polymer foams have excellent dimen-sional stability and higher compressive strengths and heat distortion temperatures than branched low density polyethylene foams of the same density.
The linear oleinic polymer foams of the present invention may be produced using conventional melt processing equipment by extrusion and injection molding. The compositions are useful as structural foams, cross-linked jackets for cables and wires, thermocollapse resistant films, and cross-linked poly-.
olefin sheet for polyolefin foam production 31,339-F -5_ -6~
In another aspect the present invention concerns expandable linear olefinic polymer composi-tion comprising at least one-linear polyolefin selected from the group consisting of LLDPE, HDPE, PP and PS, a blowing agent, and a cross-linking agent selected from the group consisting of azido functional silanes, vinyl functional silanes, organic peroxides, multifunctional vinyl monomers, and oxygen.
Brief Description of the Drawings Figure 1 is a graph of die pressure versus die gap for a linear low density polyethylene (having a melt index of 1.0 and a density of 0.935 g/cm3) foam cross~linked with an azido silane and using FC-12 (dichlorodifluoromethane) as a blowing agent; open and filled symbols indicate good and poor foams, respectively;
Figure 2 is a graph of die pressure versus die gap for an 80/20 by weight blend of linear low density polye-thylene (1.0 melt index, 0.935 g/cm3 density) and polystyrene (average molecular weight of 200,0C0) foam cross-linked with an azido silane and using a 95/5 by weight blend of FC-12 and ethanal as a blowing agent; filled symbols indicate pre-foaming;
Figure 3 is a graph of die pressure versusdie gap for a linear low density polyethylene (1.0 melt index, 0.935 g~cm3 density) foam cross-linked with dicumyl pero~ide; filled sy~bols indicate prefoaming;
31,339-~ -6-_7~ 7~6 Figure 4 is a graph of the thermocollapse resistance (percent volume retention versus tempera-ture) for linear low density polyethylene (2.3 melt index, 0.935 g/cm3 densi-ty) foams cross-linked with different levels of an azido silane and using a 80/20 by weight blend of FC-12 and ethanol as a blowing agent;
: Figure 5 is a graph of heat distortion characteristics (percent volume re-tention versus temperature) for a series of linear olefinic polymer foams cross-linked with an azido silane;
Figure 6 is a graph of compressive strengths of linear olefinic polymer foams made with a linear low density polyethylene having a melt index of l.0 and a density of 0.935 g/cm3 compared with a low density polyethylene foam (2.3 melt index, 0.923 g/cm3 density); and Figure 7 is a graph of compressive strengths of linear olefinic polymer foams and a low density polyethylene foamO
The process of the present invention per-mits the production of a low density foam material having a substantially closed-cell structure from a linear olefinic polymer or blend of linear olefinic polymers by an extrusion process. Examples of linear olefinic polymers which can be used include linear low density polyethylene, high density poly-ethylene, polypropylene, polystyrene, and blends thereof. Copolymers of linear olefins may also be utilized. Such linear olefinic polymers have been, 31,339-F -7--8~ 7~
heretofore, difficult to expand by conventional melt processing apparatuses into suitable foamed materials.
Blowing agents useful in the practice of the present invention are well-known and may comprise solids which decompose into gaseous products at extrusion temperatures or volatile liquids. A
preferred class of blowing agents is the group of halogenated hydrocarbon compounds having from 1 to 4 carbon atoms. Dichlorodifluoromethane (FC-12) is most preferred as it is inexpensive and readily available. When halogenated hydrocarbon compounds are used as the blowing agent, there can be from 0.013 to 0.50 gram mole, and preferably 0.040 to 0.30 gram mole of such blowing agent per 100 parts of linear olefinic polymer resin in the flowable gel or admixture. Although use of a single blowing agent is preferred, mixtures of two or more of such blowing agents may also be used.
The blowing agent is compounded into the flowabl~ gel in proportions to make the desired degree of expansion in the resulting foamed cellular product to make products having foamed densities down to 0.6 pcf (9.6 kg/m3). Depending on the amount of blowing agent added, the resulting oamed materials may have densities from 0.6 to 15.0 pcf (9.6 to 240 kg/m3).
Cross-linking agents useful in the prac-tice of the present invention include azido and vinyl functional silanes, organic peroxides, multi-functional vinyl monomers, and oxygen. The cross--linking agents of the present invention are added to 31,339-F -8--9~ 47E3~6 the olefinic polymer gel with the blowing agent and serve to light~y cross-link the linear olefinic polymer with itself. This cross-linking increases the mel-t tension and melt viscosity of the polymer gel, while permitting the polymer to remain flowable.
This light cross-linking of the polymer also per-mits pressure to build up in the extruder to 400 psig (2758 kPa) or above without prefoaming which is important in producing a closed cellular struc tured foam.
An important aspect of the present invention is the control of the amount of cross-linking agent to the polymer gel. TOQ much cross linking agent causes melt fracture and poor foam ~uality. Too little cross-linking agent does not provide good foamability. The cross-linked melt must remain flowable without suffering serve melt fracture and should contain less than 10 percent gels by dissolution test i~ boiling xylene. In terms of melt index 20 (ASTM D~1238 Condition N 190C, 10 Kg), the lightly cross-linked polymer melt should have a melt index greater than 0.1.
While all of the cross-linking agents utilized in the present invention are useful for producing linear olefinic polymer foams, the most preferred cross-linking agents are the azido func-- tional silanPs of the general formula R R'SiY2, in which R represents an azido functional radical attached to silicon through a silicon to carbon bond and composed of carbon, hydrogen, optionally sulfur and oxygen, each Y represents a hydrolyzable organic radical, and R' represents a monovalent 31,339~F -9-~47~
54693-36g6 hydrocarbon radical or a hydrolyzable organic radicalO
While not wi~hing to be bound by any particular mechanism, it is believed that the azido silane cross-linking agent acts via two separate mechanisms, one of which forms reversible cross-linked bonds. In this reversible reaction, the azido silane compound grafts onto an olefinic polymer through a nitrine insertion reaction. Cross-linking develops through hydrolysis of the silanes to silanols followed by condensation of silanols to siloxanes. This reaction mechanism is explained more ~ully in my commonly assigned U.S.
Patent No. 4,694,025 which issued on September 15, 1987.
Since the condensation reaction of silanols to siloxanes is cataly~ed by the presence of certain metal catalysts such as dibutyl tin dilaurate or butyl tin maleate, it is preferred that when azido silanes are 2~ used as the cross-linking agent in the present invention, that a small amount of such catalysts also be added to the polymer melt. The cross-linking reaction is self-controlled in the extruder by the presence of a gaseous reaction product, namely an alcohol, which limits the reaction. However, the cross-linking reaction proceeds during foam expansion at the exit of the die as the alcohol diffuses into the gaseous phase with the volatile blowing agent.
In this manner, cross-linking of the polymer gel in the extruder is controlled so that the gel remains flowable until it exits the die to a zone of lower pressure. There, the cross-linking reaction proceeds, which stabilizers gas 31,339-F -10-~2~71 3~6 bubble and cell formation as the olefinic polymer is expanded. Because the degree of cross~linking in the extruder can be controlled, a greater proportion of azido silane cross-linking agent may be added and, a higher degree of cross-linking in resultant polymer foam may be obtained. Accordingly, the resultant polymer, cross-linked by azido silanes, may no longer be flowable and may contain a large amount of gels.
Suitable azido-functional silane compounds include the group of azido trialkoxysilanes such as 2-(trimethoxysilyl) ethyl phenyl sulfonyl azide (com-mercially available from Petrarch Systems, Inc., Bristol, Pennsylvania) and (triethoxy silyl)hexyl sulfonyl azide (commercially available as Azcup D-98 from Hercules, Inc., Wilmington, Delaware). The azido functional silane cross-linking agent is added in an amount between 0.01 to 2.0 parts per hundred (pph), by weight, of linear olefinic polymer. An especially preferred range of addition is between 0.02 to 1.0 pph of azido silane cross-linking agent.
Other suitable silane cross-linking agents useful in the practice of the present invention include vinyl functional alkoxy silanes such as vinyl trimethoxy silane and vinyl triethoxy silane. These silane cross--linking agents may be represented by the general formula RR'SiY2 in which R represents a vinyl functional radical attached to silicon through a silicon carbon bond and composed of carbon, hydrogen, and optionally oxygen or nitrogen, each Y represents a hydrolyzable organic radical, and ~' represents a hydrocarbon radical or Y.
Further examples of such silanes are found in U.S.
Patent No. 3~646,155.
previous attempts to produce low density foams of these linear olefins by an extrusion process have been unsuccessful. Linear polyolefins, when foamed by an extrusion process suffer from small foam cross-~section, high levels of open cells, flow instability,and a narrow ranye of foaming temperatures.
The exact cause of problems of foaminy linear polyol-efins i5 not believed to be known.
However, it is generally believed that poor melt strength together with a sharp change in melt viscosity near the transition temperature makes extrusion foaming of linear polyolefins difficult.
With these properties, it is difficult to control bubble expansion during extrusion and under con-lS ditions of h@at and high shear stresses. Thisresults in many broken bubbles (open cells) during expansion and consequent poor foams.
Previous efforts to cure these problems with the foamability of linear polyolefins have centered around blending a linear polyolefin with another olefin polymer having good extrusion foam-ability. For example, Park et al, U.S. Patent No. 4,226,946, blended a linear polyethylene with a low density branched polyethylene to improve extru-sion foamability of the linear polyethylene. Watanabeet al, U.S. Patent No. 4,102,829, blended an ionomer resin with a linear polyethyle~e for the same purpose.
However, such known methods offer only partial solutions because of one or more deficiencies in the range of operating parameters, cost of materials, and final foam properties.
31,339-F -2-i _3_ ~2~7~6 It is also known that relatively lightly to moderately cross-linked thermoplastic polymers have melt properties that are suitable :Eor foam expansion. However, such cross-linked polymers are difficult to process on conventiona:L melt pro-cessing apparatus such as extruders because of flow instability. ~he prior art has general:Ly not utilized cross-linked polymers on such apparatus because shear degradation of the pol~ner occurs during melt processing and extrusion.
Accordingly, there is a need in the art for linear olefinic polymer compositions and pro-cesses which can be utili.zed to foam or expand such polymers in conventional melt processing apparatus.
The present invention meets that need by providing a process for the preparation of a lightly cross-linked linear olefinic pol~mer foam having a substantially closed-cell structure. The term "linear olefinic polymer" as used in this specifi-cation includes both polymers and copolymers of linear olefins such as linear low density poly-ethylene (LLDPE), high density polyethylene (HDPE) and polypropylene (PP), as well as polystyrene (PS).
In one aspect the present invention con-cerns a process or preparing a lightly cross-linked linear polyolefin foam having a substantially closed--cell structure, comprising the steps of:
a) melt blending under pressure at least one linear polyolefin selected from the group con-sisting of LLDPE, HDPE, PP and PS together with a 31,339-F -3-~2~78:L6 blowing agent and a sufficient amount o a cross-linking agent selected from the group consisting of azido functional silanes, vinyl functional silanes, organic peroxides, multifunctional vinyl monomers, and oxygen, to form a flowable admixture, and, (b) extruding said admixture through a die to a zone of lower pressure and activating said ~lowing agent to expand at least one linear polyolefin to form said lightly cross-linked foam. ~ -The cross-linking agent in step ~a) can be a~mixed together with the blowing agent and the linear polyolefin or can be added after a flowable admixture of the linear polyolefin and the blowing agent is formed in an amount sufficient to initiate cross--linking of -the linear polyolefin and increase the pressure of the admixture to at least 400 psig (2758 kPa).
In another aspect the present invention concerns a lightly cross-linked linear polyolefin foams prepared according to the aforementioned process.
A linear olefinic polymer or blend of linear olefinic polymers is melt processed in a conventional manner by feeding, melting, and metering it in a conven-tional melt processing apparatus such as an extruder.
A volatile blowing agent and cross~linking agent are mixed with the linear olefinic pol~ner und~er pressure to form a flowable gel or admixture. The cross-linking agent is added in an amount which is sufficient to initiate cross-linking and raise the pressure of the gel or admixture at the die opening to approximately 31,339-F -4-_5- ~Z4~
400 (2759 kPa) or above but insufficient to cause melt fracture of the polymer to occur. "Melt fracture" is a term used in the art to describe a melt flow instability of a polymer as it is extruded through cl die which flow instability causes voids and/or other irregularities in the final produc-t. Suitable cross-linking agents have been found to include azido and vinyl functional-silanes, organic peroxides, multifunctional vinyl monomers, and oxygen.
As the flowable gel or admixture is extruded through the die, opening to a zone of lower pressure, the volatile blowing agent activates to expand the linear olefinic polymer to a substantially closed-cell foam structure which is lightly cross-linked to itself.
Foams having densities of betwen 0.6 and 15 pounds per cubic oot (pcf) (9.6 and 240.3 kg/m3) may be produced.
The linear olefinic polymer foams have excellent dimen-sional stability and higher compressive strengths and heat distortion temperatures than branched low density polyethylene foams of the same density.
The linear oleinic polymer foams of the present invention may be produced using conventional melt processing equipment by extrusion and injection molding. The compositions are useful as structural foams, cross-linked jackets for cables and wires, thermocollapse resistant films, and cross-linked poly-.
olefin sheet for polyolefin foam production 31,339-F -5_ -6~
In another aspect the present invention concerns expandable linear olefinic polymer composi-tion comprising at least one-linear polyolefin selected from the group consisting of LLDPE, HDPE, PP and PS, a blowing agent, and a cross-linking agent selected from the group consisting of azido functional silanes, vinyl functional silanes, organic peroxides, multifunctional vinyl monomers, and oxygen.
Brief Description of the Drawings Figure 1 is a graph of die pressure versus die gap for a linear low density polyethylene (having a melt index of 1.0 and a density of 0.935 g/cm3) foam cross~linked with an azido silane and using FC-12 (dichlorodifluoromethane) as a blowing agent; open and filled symbols indicate good and poor foams, respectively;
Figure 2 is a graph of die pressure versus die gap for an 80/20 by weight blend of linear low density polye-thylene (1.0 melt index, 0.935 g/cm3 density) and polystyrene (average molecular weight of 200,0C0) foam cross-linked with an azido silane and using a 95/5 by weight blend of FC-12 and ethanal as a blowing agent; filled symbols indicate pre-foaming;
Figure 3 is a graph of die pressure versusdie gap for a linear low density polyethylene (1.0 melt index, 0.935 g~cm3 density) foam cross-linked with dicumyl pero~ide; filled sy~bols indicate prefoaming;
31,339-~ -6-_7~ 7~6 Figure 4 is a graph of the thermocollapse resistance (percent volume retention versus tempera-ture) for linear low density polyethylene (2.3 melt index, 0.935 g/cm3 densi-ty) foams cross-linked with different levels of an azido silane and using a 80/20 by weight blend of FC-12 and ethanol as a blowing agent;
: Figure 5 is a graph of heat distortion characteristics (percent volume re-tention versus temperature) for a series of linear olefinic polymer foams cross-linked with an azido silane;
Figure 6 is a graph of compressive strengths of linear olefinic polymer foams made with a linear low density polyethylene having a melt index of l.0 and a density of 0.935 g/cm3 compared with a low density polyethylene foam (2.3 melt index, 0.923 g/cm3 density); and Figure 7 is a graph of compressive strengths of linear olefinic polymer foams and a low density polyethylene foamO
The process of the present invention per-mits the production of a low density foam material having a substantially closed-cell structure from a linear olefinic polymer or blend of linear olefinic polymers by an extrusion process. Examples of linear olefinic polymers which can be used include linear low density polyethylene, high density poly-ethylene, polypropylene, polystyrene, and blends thereof. Copolymers of linear olefins may also be utilized. Such linear olefinic polymers have been, 31,339-F -7--8~ 7~
heretofore, difficult to expand by conventional melt processing apparatuses into suitable foamed materials.
Blowing agents useful in the practice of the present invention are well-known and may comprise solids which decompose into gaseous products at extrusion temperatures or volatile liquids. A
preferred class of blowing agents is the group of halogenated hydrocarbon compounds having from 1 to 4 carbon atoms. Dichlorodifluoromethane (FC-12) is most preferred as it is inexpensive and readily available. When halogenated hydrocarbon compounds are used as the blowing agent, there can be from 0.013 to 0.50 gram mole, and preferably 0.040 to 0.30 gram mole of such blowing agent per 100 parts of linear olefinic polymer resin in the flowable gel or admixture. Although use of a single blowing agent is preferred, mixtures of two or more of such blowing agents may also be used.
The blowing agent is compounded into the flowabl~ gel in proportions to make the desired degree of expansion in the resulting foamed cellular product to make products having foamed densities down to 0.6 pcf (9.6 kg/m3). Depending on the amount of blowing agent added, the resulting oamed materials may have densities from 0.6 to 15.0 pcf (9.6 to 240 kg/m3).
Cross-linking agents useful in the prac-tice of the present invention include azido and vinyl functional silanes, organic peroxides, multi-functional vinyl monomers, and oxygen. The cross--linking agents of the present invention are added to 31,339-F -8--9~ 47E3~6 the olefinic polymer gel with the blowing agent and serve to light~y cross-link the linear olefinic polymer with itself. This cross-linking increases the mel-t tension and melt viscosity of the polymer gel, while permitting the polymer to remain flowable.
This light cross-linking of the polymer also per-mits pressure to build up in the extruder to 400 psig (2758 kPa) or above without prefoaming which is important in producing a closed cellular struc tured foam.
An important aspect of the present invention is the control of the amount of cross-linking agent to the polymer gel. TOQ much cross linking agent causes melt fracture and poor foam ~uality. Too little cross-linking agent does not provide good foamability. The cross-linked melt must remain flowable without suffering serve melt fracture and should contain less than 10 percent gels by dissolution test i~ boiling xylene. In terms of melt index 20 (ASTM D~1238 Condition N 190C, 10 Kg), the lightly cross-linked polymer melt should have a melt index greater than 0.1.
While all of the cross-linking agents utilized in the present invention are useful for producing linear olefinic polymer foams, the most preferred cross-linking agents are the azido func-- tional silanPs of the general formula R R'SiY2, in which R represents an azido functional radical attached to silicon through a silicon to carbon bond and composed of carbon, hydrogen, optionally sulfur and oxygen, each Y represents a hydrolyzable organic radical, and R' represents a monovalent 31,339~F -9-~47~
54693-36g6 hydrocarbon radical or a hydrolyzable organic radicalO
While not wi~hing to be bound by any particular mechanism, it is believed that the azido silane cross-linking agent acts via two separate mechanisms, one of which forms reversible cross-linked bonds. In this reversible reaction, the azido silane compound grafts onto an olefinic polymer through a nitrine insertion reaction. Cross-linking develops through hydrolysis of the silanes to silanols followed by condensation of silanols to siloxanes. This reaction mechanism is explained more ~ully in my commonly assigned U.S.
Patent No. 4,694,025 which issued on September 15, 1987.
Since the condensation reaction of silanols to siloxanes is cataly~ed by the presence of certain metal catalysts such as dibutyl tin dilaurate or butyl tin maleate, it is preferred that when azido silanes are 2~ used as the cross-linking agent in the present invention, that a small amount of such catalysts also be added to the polymer melt. The cross-linking reaction is self-controlled in the extruder by the presence of a gaseous reaction product, namely an alcohol, which limits the reaction. However, the cross-linking reaction proceeds during foam expansion at the exit of the die as the alcohol diffuses into the gaseous phase with the volatile blowing agent.
In this manner, cross-linking of the polymer gel in the extruder is controlled so that the gel remains flowable until it exits the die to a zone of lower pressure. There, the cross-linking reaction proceeds, which stabilizers gas 31,339-F -10-~2~71 3~6 bubble and cell formation as the olefinic polymer is expanded. Because the degree of cross~linking in the extruder can be controlled, a greater proportion of azido silane cross-linking agent may be added and, a higher degree of cross-linking in resultant polymer foam may be obtained. Accordingly, the resultant polymer, cross-linked by azido silanes, may no longer be flowable and may contain a large amount of gels.
Suitable azido-functional silane compounds include the group of azido trialkoxysilanes such as 2-(trimethoxysilyl) ethyl phenyl sulfonyl azide (com-mercially available from Petrarch Systems, Inc., Bristol, Pennsylvania) and (triethoxy silyl)hexyl sulfonyl azide (commercially available as Azcup D-98 from Hercules, Inc., Wilmington, Delaware). The azido functional silane cross-linking agent is added in an amount between 0.01 to 2.0 parts per hundred (pph), by weight, of linear olefinic polymer. An especially preferred range of addition is between 0.02 to 1.0 pph of azido silane cross-linking agent.
Other suitable silane cross-linking agents useful in the practice of the present invention include vinyl functional alkoxy silanes such as vinyl trimethoxy silane and vinyl triethoxy silane. These silane cross--linking agents may be represented by the general formula RR'SiY2 in which R represents a vinyl functional radical attached to silicon through a silicon carbon bond and composed of carbon, hydrogen, and optionally oxygen or nitrogen, each Y represents a hydrolyzable organic radical, and ~' represents a hydrocarbon radical or Y.
Further examples of such silanes are found in U.S.
Patent No. 3~646,155.
3 1 , 3 3 9 -F
4~6 Suitable organic peroxide cross-linking agents include dicumyl peroxide, commercially available under the Trademark DICUP R from Hercules, Inc., Wilmington, Delaware. The organic peroxide cross-linking agents are preferably added in an amount between 0.001 to 0.5 pph, and most preferably between 0.005 to 0.1 pph, of line-ar olefinic polymer. Suitable multifunctional vinyl monomer cross~linking agents for the present invèntion include trimethylolpropane triacrylate ~TMPTA) and pentaerythritol triacrylate (PETA), both commercially available from Celanese Corp. The multifunctional vinyl monomer cross-linking agents are preferably added in an amount between 0.01 to 2.0 pph, and most preferably between 0.1 to 1.0 pph, of linear olefinic polymer. Additionally, it has been found that the introduction of oxygen will initiate self-cross--linking of linear olefinic polymers by a free radical mechanism.
The cross-linking of linear olefinic polymers by organic peroxides, multifunctional vinyl monomers, and oxygen is believed to take place via a free radical mechanism in which tertiary hydrogens on the polymer are removed. ~owever, since this type of reaction is irreversible, the amounts of cross-linking agent added should be closely controlled to prevent over-cross--linking of the polymer resulting in melt fracture.
. In accordance with the process of the present invention, olefinic polymer foams may be made on con-ventional melt processing apparatus such as by con-tinuous extrusion from a screw-type extruder. Such an extruder typically comprises a series of sequential zones including a feed zone, compression and melt zone, 31,339-F -12-1~47~
metering zone, and mixing zone. The barrel of the extruder may be provided with conventional electric heaters for zoned temperature control.
An inlet, such as a straight-through injec-tion nozzle, is provided for adding a mixture of fluidblowing agent and cross~linking agent under pressure to the polymer in the extruder barrel between the metering and mixing ~ones. Cross-linking agent is pumped, in a ..
controllable manner, into the stream of fluid blowing agent upstream of the injection nozzle. The hlowing agent and cross-linking agent are co.npounded into the starting polymer in a conventional manner to form a flowable g~l or admixture, preferably in a continuous manner. Thus, khe polymer, blowing agent, and cross-linking agent may be combined in the mixing zone of anextruder using heat to plastify the polymer resin, pressure to maintain the blowing agent in a liquid state, and mechanical mixing to obtain thorough mixing.
The discharge end of the mixing zone of the extruder is connected, through a cooling and tempera-ture control zone, to a die orifice. The hot polymer gel is cooled and then passed through the die orifice into a zone of lower pressure ~e.g., normal ambient air atmosphere) where the blowing agent is activated and the polymer gel expands to a lower density, cellular mass. As the foamed extrusion forms, it is conducted away from the die and allowed to cool and harden.
In practice, the temperature of the feed zone is maintained at 160C to 200C, preferably 180C, the temperature of the melting, metering, and mixing zones are maintained at 190C to 230C, preferably 210C ,and 31,339-F -13-~2~7~
the tempera-ture in the cooling and temperature control ~zone is maintained at 100C to 140C, preferably 120C.
The temperature of the polymer gel as it expands through the die orifice is preferably just above the temperature at which solid polymer would crystallize out of the gel and will vary depending upon the particular olefinic polymer utilized.
The resulting linear~olefinic polymer foams comprise substantially closed-cell structures and are flexible to bending and shaping. The foams have excel-lent dimensional stability ana high compressive strengths and heat distortion temperatures than branched low density polyethylene foams having an equivalent foam density.
As is conventional, finely divided solid materials such as talc, calcium silicate, zinc stearate, and the like can advantageously be incorporated with the polymer gel prior to expansion. Such finely divided materials aid in controlling the size of the cells and may be employed in amounts up to five percent by weight of the polymer. Numerous fillers, pigments, lubricants, and the like well-known in the art can also be incor~
porated as desired. Antio~idants may be added to retard or suppress the cross-linking reaction. In such an instance where antioxidant is present in or added to the polymer gel, an additional amount of cross-linking agent may be required to achieve the desired degree of cross-linking.
The specific working examples that follow are intended to illustrate -the invention but are not to be - taken as limiting the scope thereof. In the examples, 31,339-F -14--15- ~2~7~
parts and percentages are by weigh~ unless otherwise specified or required by the context.
Example 1 The apparatus used in this and other examples was 1-1/4 inch (3.17 cm) screw type extruder having two additional zones for mixing and cooling at the end of usual sequential zones for ieeding, melting, and metering.
- An opening for blowing agent injection was provided on the extruder barrel between the metering and mixing zones. A small syrin~e-type pump was connected to the blowing agent stxeam fo; injection of cross-linking agent. At the end of the cooling zone there was attached a die orifice having an opening of rectangular shape. The height of the opening, called die gap hereinafter, was adjustable while its width was fixed at 0.25 inch (0.63 cm).
A granular linear low density polyethylene (LLDPE~, having 1.0 melt index (ASTM D-1238-79 Con-dition E) and 0.935 g/cm3 density was uniformly mixed with 0.1 pph dibutyl tin dilaurate condensation cata-lyst (commercially available under the designation T-12, from M&T Chemical Inc.) and 0.1 pph talcum powder.
The mixture was fed into the extruder at an essentially uniform rate of about 10 pounds per hour (12.6 x 10 kgJs). FC-12 blowing agent (dichlorodifluoromethane) was injected into the extruder at a rate of 19.9 pph.
The temperatures maintained at the extruder zones were:
170C at feeding zone, 220C at melting and metering zone, and 220C at mixing zone. The temperature of the cooling zone was adjusted so that the gel could be cooled down to 123C throughout the tests. For each test, the die gap was varied to.determine its effect on 31,339-F -15-7~6 foam appearance. A predetermined amoun-t of an azido functional silane was injected into the extruder to determine its effect on foaming performance.
The test results are summarized in Table I
and Figure l. As can be seen from Figure 1, a key to successful foam extrusion of a linear low density -polyolefin is the ability to build the die pressure to - approximately 400 psig (2758 kPa) or above. This ~ - -appears to be an approximate line of demarcation between good and poor foams in appearance.
Without addition of azido silane, the LLDPE
foam partially collapsed at a larger die gap. The die had to be closed to 0.06 inch (0.15 cm) to substantially prevent the foam from collapsing. At this small die gap, the foam had a very small cross-section, a high level of open ceils, a high density, some voids in the cross-section, and ripple on the edges. The foam was not of satisfactory quality. When 0.05 pph of an azido silane was added, the foam quality improved dramatically with the pressure increased both at the die and extruder discharge. At a die gap as large as 0.110 inch (0.28 cm), a good ~uality foam having a larger cross-section, low density, and low open cell content was achieved.
The foam strand was straight with no sign of flow instability. The foam looked even better at 0.075 pph silane level. Excellent ~uality foam was produced at a die gap as large as 0.145 inch l0.37 cm). At 0.10 pph silane level, an even larger cross-sectioned foam was achieved. The foam looked good but there developed a slight sign of over-cross-linking as exhibited by a slightly higher level of open cells.
31,339 F -16-` 17 ~247~
The LLDPE foams thus produced with low cost FC-12 blowing agent had good dimensional stability during aging. This feature is remarkable in that a foam produced from a branched chain low density poly-ethylene using the same blowing agent shrinks as muchas 30 percent during aging. The LLDPE foams also had a heat distortion temppera-ture of 115C-, which is 15C -higher than that for a typical low density polyethylene foam (LDPE). The heat distortion temperature is the highest temperature at which a foam shrinks no more than 5 percent in volume during one hour aging.
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31, 339-F -19-Example 2 The tests in this example employed the same apparatus, polymer composition, and operation conditions as in Example 1. An 80/20 mixture of FC-12/ethanol was used as thè blowing agent in order to ~ee the effect of alcohol on the cross-linking.
The tests results are set forth in Table II.
In this example, which is not a part of the present invention, but rather a part of the subject matter of U.S. Patent No. ~,694,025 which issued on September 15, 1987, referred to abo~e, it is shown that alcohol suppressed line pressure~ for formulations cross-linked with an azido functional silane.
Although not as dramatic as in Example 1, the effects of silane were evident in one or more areas of foaming performance. Good quality foams were obtained at the silane levels of 0.1 to 0.15 pph. At a 0.25 pph silane level, the foam strand ~ractured ~ignifying over-cross-linking. As shown in Figure 4, the foams made with 0.15 and 0.25 pph silane showed some thermo--collapse resistance during oven aging tests. That is, these foams retained over 50 percent of their original volume during aging in 130C oven for one hour while the control (Test Na. 1 ) and those containing a lower level of silane collapsed totally during the test.
3 Example 3 The same apparatus, polymer, and operating procedure as in Example 1 were also employed in this example. A small amount (0.05 pph) of organotin catalyst (T-12) was added to all formulations is this 31,339-F -20-~2~7l3~
example. The talc level was varied from 0.1 to 0.7 pph for cell size control. A 90/10 by weight mixture of FC-12/MeC12 was used as the blowing agent. A prede-termined amount of an azido functional silane was mixed in the blowing agent. The extruder zones were main-tained at 170C, 200C, and 200C for feeding zone, melting and metering zone and mixing zone, respectively.
The gel temperature was maintained at 128C. The die gap wàs fixed at 0.100 inch (2.54 mm) for ~all tests except for Test No. 5 ln which the foam appearance at O.200 inch (5.08 mm) die gap was also observed. Also in Test No. 5, a small amount (1.0 pph) of methanol was mixed in to determine its effect. The test results are given in Table III.
Without the crosslinking agent, the foam was of poor quality with small cross-section, some voids, rough skin, and rippled edges in spite of its substan tially closed-cell structure. When a small amount (0.125 pph) of an azido functional silane was added, an excellent quality foam was obtained. At the silane level of 0.15 pph, melt fracture developed. Cutting the level of nucleator did not improve foam quality.
When the alcohol-containing blowing agent was injected, the melt fracture disappeared and an excellent quality foam of large cross-section was obtained. The die could be opened as wide as 0.200 inch (5.08 mm) withou-t incurring prefoaming although more open cells developed in the foam. Te LLDPE foams produced in this example showed good dimensional stability during ambient aging and a high heat distortion temperature of 115C.
31,339 F -21--22~ '78~6 Example 4 The apparatus used in this example and its operating procedure were the same as used in Example 1.
A high density linear polyethylene (HDPE~ having 0.6 melt index (ASTM D-1238-79 Condition E) and 0.963 g/cm3 density was used in this example. The polymer ~ranules were mixed with 0.05 pph talc and 0.05 pph organotin catalyst (T-12). The mixture was fed into the extruder at 10 pounds per hour (12.60 x 10 4-kg/s~.- Extruder zones were maintained at 160C, 200C and 200C for feeding, melting and metering, and mixing zone, respectively. The gel temperature was fixed at 132C for all test~. The test results are set forth in Table IV.
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The cross-linking of linear olefinic polymers by organic peroxides, multifunctional vinyl monomers, and oxygen is believed to take place via a free radical mechanism in which tertiary hydrogens on the polymer are removed. ~owever, since this type of reaction is irreversible, the amounts of cross-linking agent added should be closely controlled to prevent over-cross--linking of the polymer resulting in melt fracture.
. In accordance with the process of the present invention, olefinic polymer foams may be made on con-ventional melt processing apparatus such as by con-tinuous extrusion from a screw-type extruder. Such an extruder typically comprises a series of sequential zones including a feed zone, compression and melt zone, 31,339-F -12-1~47~
metering zone, and mixing zone. The barrel of the extruder may be provided with conventional electric heaters for zoned temperature control.
An inlet, such as a straight-through injec-tion nozzle, is provided for adding a mixture of fluidblowing agent and cross~linking agent under pressure to the polymer in the extruder barrel between the metering and mixing ~ones. Cross-linking agent is pumped, in a ..
controllable manner, into the stream of fluid blowing agent upstream of the injection nozzle. The hlowing agent and cross-linking agent are co.npounded into the starting polymer in a conventional manner to form a flowable g~l or admixture, preferably in a continuous manner. Thus, khe polymer, blowing agent, and cross-linking agent may be combined in the mixing zone of anextruder using heat to plastify the polymer resin, pressure to maintain the blowing agent in a liquid state, and mechanical mixing to obtain thorough mixing.
The discharge end of the mixing zone of the extruder is connected, through a cooling and tempera-ture control zone, to a die orifice. The hot polymer gel is cooled and then passed through the die orifice into a zone of lower pressure ~e.g., normal ambient air atmosphere) where the blowing agent is activated and the polymer gel expands to a lower density, cellular mass. As the foamed extrusion forms, it is conducted away from the die and allowed to cool and harden.
In practice, the temperature of the feed zone is maintained at 160C to 200C, preferably 180C, the temperature of the melting, metering, and mixing zones are maintained at 190C to 230C, preferably 210C ,and 31,339-F -13-~2~7~
the tempera-ture in the cooling and temperature control ~zone is maintained at 100C to 140C, preferably 120C.
The temperature of the polymer gel as it expands through the die orifice is preferably just above the temperature at which solid polymer would crystallize out of the gel and will vary depending upon the particular olefinic polymer utilized.
The resulting linear~olefinic polymer foams comprise substantially closed-cell structures and are flexible to bending and shaping. The foams have excel-lent dimensional stability ana high compressive strengths and heat distortion temperatures than branched low density polyethylene foams having an equivalent foam density.
As is conventional, finely divided solid materials such as talc, calcium silicate, zinc stearate, and the like can advantageously be incorporated with the polymer gel prior to expansion. Such finely divided materials aid in controlling the size of the cells and may be employed in amounts up to five percent by weight of the polymer. Numerous fillers, pigments, lubricants, and the like well-known in the art can also be incor~
porated as desired. Antio~idants may be added to retard or suppress the cross-linking reaction. In such an instance where antioxidant is present in or added to the polymer gel, an additional amount of cross-linking agent may be required to achieve the desired degree of cross-linking.
The specific working examples that follow are intended to illustrate -the invention but are not to be - taken as limiting the scope thereof. In the examples, 31,339-F -14--15- ~2~7~
parts and percentages are by weigh~ unless otherwise specified or required by the context.
Example 1 The apparatus used in this and other examples was 1-1/4 inch (3.17 cm) screw type extruder having two additional zones for mixing and cooling at the end of usual sequential zones for ieeding, melting, and metering.
- An opening for blowing agent injection was provided on the extruder barrel between the metering and mixing zones. A small syrin~e-type pump was connected to the blowing agent stxeam fo; injection of cross-linking agent. At the end of the cooling zone there was attached a die orifice having an opening of rectangular shape. The height of the opening, called die gap hereinafter, was adjustable while its width was fixed at 0.25 inch (0.63 cm).
A granular linear low density polyethylene (LLDPE~, having 1.0 melt index (ASTM D-1238-79 Con-dition E) and 0.935 g/cm3 density was uniformly mixed with 0.1 pph dibutyl tin dilaurate condensation cata-lyst (commercially available under the designation T-12, from M&T Chemical Inc.) and 0.1 pph talcum powder.
The mixture was fed into the extruder at an essentially uniform rate of about 10 pounds per hour (12.6 x 10 kgJs). FC-12 blowing agent (dichlorodifluoromethane) was injected into the extruder at a rate of 19.9 pph.
The temperatures maintained at the extruder zones were:
170C at feeding zone, 220C at melting and metering zone, and 220C at mixing zone. The temperature of the cooling zone was adjusted so that the gel could be cooled down to 123C throughout the tests. For each test, the die gap was varied to.determine its effect on 31,339-F -15-7~6 foam appearance. A predetermined amoun-t of an azido functional silane was injected into the extruder to determine its effect on foaming performance.
The test results are summarized in Table I
and Figure l. As can be seen from Figure 1, a key to successful foam extrusion of a linear low density -polyolefin is the ability to build the die pressure to - approximately 400 psig (2758 kPa) or above. This ~ - -appears to be an approximate line of demarcation between good and poor foams in appearance.
Without addition of azido silane, the LLDPE
foam partially collapsed at a larger die gap. The die had to be closed to 0.06 inch (0.15 cm) to substantially prevent the foam from collapsing. At this small die gap, the foam had a very small cross-section, a high level of open ceils, a high density, some voids in the cross-section, and ripple on the edges. The foam was not of satisfactory quality. When 0.05 pph of an azido silane was added, the foam quality improved dramatically with the pressure increased both at the die and extruder discharge. At a die gap as large as 0.110 inch (0.28 cm), a good ~uality foam having a larger cross-section, low density, and low open cell content was achieved.
The foam strand was straight with no sign of flow instability. The foam looked even better at 0.075 pph silane level. Excellent ~uality foam was produced at a die gap as large as 0.145 inch l0.37 cm). At 0.10 pph silane level, an even larger cross-sectioned foam was achieved. The foam looked good but there developed a slight sign of over-cross-linking as exhibited by a slightly higher level of open cells.
31,339 F -16-` 17 ~247~
The LLDPE foams thus produced with low cost FC-12 blowing agent had good dimensional stability during aging. This feature is remarkable in that a foam produced from a branched chain low density poly-ethylene using the same blowing agent shrinks as muchas 30 percent during aging. The LLDPE foams also had a heat distortion temppera-ture of 115C-, which is 15C -higher than that for a typical low density polyethylene foam (LDPE). The heat distortion temperature is the highest temperature at which a foam shrinks no more than 5 percent in volume during one hour aging.
31,339 F -17-7~
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31, 339-F -19-Example 2 The tests in this example employed the same apparatus, polymer composition, and operation conditions as in Example 1. An 80/20 mixture of FC-12/ethanol was used as thè blowing agent in order to ~ee the effect of alcohol on the cross-linking.
The tests results are set forth in Table II.
In this example, which is not a part of the present invention, but rather a part of the subject matter of U.S. Patent No. ~,694,025 which issued on September 15, 1987, referred to abo~e, it is shown that alcohol suppressed line pressure~ for formulations cross-linked with an azido functional silane.
Although not as dramatic as in Example 1, the effects of silane were evident in one or more areas of foaming performance. Good quality foams were obtained at the silane levels of 0.1 to 0.15 pph. At a 0.25 pph silane level, the foam strand ~ractured ~ignifying over-cross-linking. As shown in Figure 4, the foams made with 0.15 and 0.25 pph silane showed some thermo--collapse resistance during oven aging tests. That is, these foams retained over 50 percent of their original volume during aging in 130C oven for one hour while the control (Test Na. 1 ) and those containing a lower level of silane collapsed totally during the test.
3 Example 3 The same apparatus, polymer, and operating procedure as in Example 1 were also employed in this example. A small amount (0.05 pph) of organotin catalyst (T-12) was added to all formulations is this 31,339-F -20-~2~7l3~
example. The talc level was varied from 0.1 to 0.7 pph for cell size control. A 90/10 by weight mixture of FC-12/MeC12 was used as the blowing agent. A prede-termined amount of an azido functional silane was mixed in the blowing agent. The extruder zones were main-tained at 170C, 200C, and 200C for feeding zone, melting and metering zone and mixing zone, respectively.
The gel temperature was maintained at 128C. The die gap wàs fixed at 0.100 inch (2.54 mm) for ~all tests except for Test No. 5 ln which the foam appearance at O.200 inch (5.08 mm) die gap was also observed. Also in Test No. 5, a small amount (1.0 pph) of methanol was mixed in to determine its effect. The test results are given in Table III.
Without the crosslinking agent, the foam was of poor quality with small cross-section, some voids, rough skin, and rippled edges in spite of its substan tially closed-cell structure. When a small amount (0.125 pph) of an azido functional silane was added, an excellent quality foam was obtained. At the silane level of 0.15 pph, melt fracture developed. Cutting the level of nucleator did not improve foam quality.
When the alcohol-containing blowing agent was injected, the melt fracture disappeared and an excellent quality foam of large cross-section was obtained. The die could be opened as wide as 0.200 inch (5.08 mm) withou-t incurring prefoaming although more open cells developed in the foam. Te LLDPE foams produced in this example showed good dimensional stability during ambient aging and a high heat distortion temperature of 115C.
31,339 F -21--22~ '78~6 Example 4 The apparatus used in this example and its operating procedure were the same as used in Example 1.
A high density linear polyethylene (HDPE~ having 0.6 melt index (ASTM D-1238-79 Condition E) and 0.963 g/cm3 density was used in this example. The polymer ~ranules were mixed with 0.05 pph talc and 0.05 pph organotin catalyst (T-12). The mixture was fed into the extruder at 10 pounds per hour (12.60 x 10 4-kg/s~.- Extruder zones were maintained at 160C, 200C and 200C for feeding, melting and metering, and mixing zone, respectively. The gel temperature was fixed at 132C for all test~. The test results are set forth in Table IV.
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The effect of an azido silane on the foaming was even more dramatic during the tests in this example. Without silane, a good foam could not be produced, but with 0.15 pph silane excellent quality substantially closed-cell foam was achieved. The foams expanded by low cost FC-12 blowing agent showed excellent dimensional stability during ambient aging with shrinkage no more than 3 percent. This is a remarkable improvement over a LDPE foam made with FC-12 blowing agent. The heat distortion temperature of the HDPE foams was 125C which is 25C higher than that of typical LPDE foam.
Example 5 In this example, the same apparatus, operating conditions, and polymer composition were used, as in Example 4, except for gel temperature and blowing agent. The gel temperature was maintained at 130C
and a 90/10 mixture of FC-12/EtOH was used as the blowing agent. The test results are presented in Table V.
Again, the silane cross-linking agent aided in foam processing and alcohol suppressed development of cross-linking in the extrusion line. At a low silane level, improvements were seen in one or more performance areas. For example, even at 0.05 pph silane level, foam density dropped significantly from the control. At 0.15 pph silane level, good quality foams were produced with a noticeable increase in the die pressure. Interestingly, the pressure at extruder discharge increased little at this silane level. This is an advantage in foam 31,339-F -29-~30~ 78P6 extrusion process since a high die pressure prevents prefoaming but a low extruder discharge pressure faci-litates polymer extrusion. The trend indicates that the alcohol~containing blowing agent called for a silane level higher than 0.15 pph for the optimum results.
Example 6 - The apparatus used in this example was the same as in Example 1. A Hercules Porofax 6523 poly-propylene resin having 4.0 melt index ~ASTM D-1738 Condition L) was u~-d. The polymer was mixed with 0.1 pph talc and 0.05 pph organotin catalyst (T-12) and fed into the extruder at a uniform rate of 10 pounds per hour (12.60 x 104 kg/s). A 90/10 by weight mixture of FC-12 and methylene chloride was injected into the extruder at a rate of 27.8 pph. Extruder zones were maintained at 180C, 200C and 210C for feeding, melting and metering, and mixing zone, respectively.
The gel temperature was kept at an essentially constant level of 146C. The data are summarized in Table VI.
In this example also, addition of an azido functional silane improved foam processability of polypropylene.
The polypropylene foams did not shrink at all during aging and had a heat distortion temperature as high as 165C.
Exam~le 7 The same apparatus used in Example l was used in this example. The polymer feedstock employed ln this example was an 80/20 mixture o a linear Iow density polyethylene that was used in Example 1 and a polystyrene having weight average molecular weight of 200,000.
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31, 339-F -36-_37~ 6 Two granular polymers were blended by use of a tumbler, mixer with 0.1 pph talc and 0.05 pph organo-tin catalys-t (T-1~) and fed to the extruder at an essentially uniform rate of 10 pounds per hour (12.6 x 104 kg/s). A 95/5 by weight mixture of FC-12/ethanol was injected into the extruder at a rate of approxi-mately 21.0 pph.- Extruder zones were maintained at 145C, 195C and 205C, respectively, for feeding, melting and metering; and mixing zone, respectively.
The gel was cooled down to an essentially uniform temperature of 122C. The test results are seen in Table VII and Figure 2.
This particular polymer blend provided reason-ably good foam without cross-linking when the die gap was closed down to 0.050 inch (1.27 mm). The foam had a small cross~section and a relatively high level of open cells. At a laryer die gap, foam collapsed par-tially. Foam improved progressively with the azido functional silane level. At a silane level of 0.15 pph or higher, superb-looking foams were obtained having a lower density, lar~er cross-section, and lower open cell content. At a silane level as high as 0.25 pph, there was no sign of over-cross~linking. Again, a die pressure of approximately 400 psig (2758 kPa) was the line o demarcation between good and poor foams.
The foams thus produced also had excellent dimensional stability during aging without suffering any shrinkage. The heat distortion temperature of the blend foam was llO~C.
31,339-F -37--38- ~247~6-Exam~le 8 The apparatus, operatlng procedure, and polymer used in this example were the same as in Example 1.
Polymer granules were adhered with 0.05 pph talc by use of a wetting agent and fed into the extruder.
FC-12 blowing agent was injected into the extruder at an essentially uniform rate of 19.7 pph. A predeter-mined amount of dicumyl peroxidf (Dicup R (Trademark), from Hercules Inc.) was injected into the blowing agent stream in 10 percent by weight solution in methylene chloride. Extruder zone temperatures were maintained at 140C, 180C, and 200C, respectively. The gel was cooled down to an essentially uniform temperature of 124C. The resultant data are given in Table VIII and are illustrated in Figure 3.
The control LLDPE foam was not satisfactory.
Addition of a small amount (0.0054 pph) of dicumyl peroxide improved foam processability and quality. The best result was obtained at a peroxide level of 0.01 pph. Excellent quality foams were produced at a wide range of die gaps. When the peroxide level was raised to 0.0123 pph, symptoms of over-cross-linking developed.
At a high peroxide level, the foam strand fractured.
Again, a die pressure of approximately 400 psig (2758 kPa) was the line of demarcation between good and poor foams. - -Example 9 A Brabender Plasti-corder (Trademark of C. W.
Brabender Instrumen-ts, Inc.) mixing head having 60 ml capacity was employed in this example in order to show 31,339-F -38-_39_ ~4~
that a multi-vinyl functional monomer could be used as a cross-linking agent in accordance with this invention.
The Brabender mixer was heated to an essen-tially constant temperature of 200C. A linear low density polyethylene used in Example 1 was used in all tests of this example. Approximately 40 g of the granular polyethylene was put in the mixer with its blades rotating at a constant speed cf 30 rpm. The opening of the mixer was continuously purged with nitrogen in most tests e~cept otherwise specified. The tor~ue was continuously recorded on a strip chart. The torque reached an essentially steady state in 5 to 10 minutes.
After 10 minutes mixing, there was added a predetermined amount of cross-linking agent selected from Dicup R dicumyl peroxide by Hercules Inc. and trimethylolpropane triacrylate ~TMPTA) made by Celanese Chemical Co. Dicup R was fed in 20 percent solution in methyl~ne chlorid~. Kneading was continued until the torque peaked out. Melt index of the cross-linked material was determined.
As shown in Table IX, dicumyl peroxide is an effective cross-linking agent. The torque rose 18 percent at the peroxide level of 0.02 pph. The level of peroxide was determined rather excessive in Example 8. A similar increase in torque was achieved by 0.3 to 0.4 pph TMPTA in nitrogen atmosphere. From this result, it is inferred that a multivinyl monomer may be used as a cross-linking agent for improving extrusion oamability of a linear polyolefin polymer.
31,339-F -39--40~ 7~
Example 10 The Brabender mixer was also used in this example. Several linear low density polyethylenes and a high density polyethylene having 6.2 melt index (ASTM
D-1238-79 Condition E) and 0.963 g/cm3 density were evaluated for self-crosslinking in air atmosphere. In each test, approximately 40 g of polymer was charged in the mixer with its blades rotating at a constant speed of 3~ rpm. The test data are set fo~rth in Table X.
All linear low density polyethylenes gained more than enough torgue for improvement in extrusion ~oamability during kneading in the mixer. The induc-tion time for torque rise was mostly shorter than 30 minutes. The induction time became shorter and the maximum torque rise was greater at a higher temperature.
In inert atmosphere, the torque did not rise appreciably.
Antioxidant delayed cross-linking but did not s-top its development. From the results of the tests, it is inferred that melt kneading of a linear polyethylene in the presence of oxygen is another way of lightly cross -linking the polymer for extrusion foaming. A vented extruder could be used for this purpose.
Example 11 The apparatus used in this example was the same as Example 1. A granular polystyrene, polystyrene with a weight average molecular weight of 200,000, was uniformly mixed with a small amount of dibutyl tin dilaurate condensation catalyst (T-12, available from M
& T Chemicals, Inc.), barium stearate and talcum powder.
The mixture was fed into the extruder at an essentially uniform rate of 10 pounds per hour (12.60 x 10 4 kg/s).
A premixed blowing agent was injec-ted into the extruder 31,339-F -40--41- ~47~
at a predetermined rate. Blowing agents used in this example were a 50/50 by weight mixture of fluorocarbon 12 (FC-12) and methyl chloride (MeCl) for Text No. 1 and a 70/30 by weight mixture of fluorocarbon 12 and fluorocarbon ll (FC-11) for the other tests. An.azido functional silane, 2-(trimethoxysily ethylphenylsulfonyl) azide (CT2905 distributed by Petrarch Systems, Inc.~, was injected to the blowing agent stream at a uniform ~ predetermined rate. The extruder zones were maintained at 170C, la~C and 200C for feeding, melting, metering, and mixing zone, respectively. The temperature of the cooling zone was adjusted so that the gel could be cooled down to a uniform temperature for optimum foam expansion.
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Cross-linkin~ Agent Peak Melt Level Environment Time Torque Ratio Index Test Type (pph) Gas (min) (Peak/Initial) (dg/min) No ~1) (2) (3) ~4) (5) (6) -~ N2 20 1.00 7.19 2 Dicup R 0.01 - N 12 1.03 5.94 0.02 N2 12 1.18 4.50 0.03 N2 ` 14 1.2B- 2.62 0.04 N 12 1.37 2.32 0.05 N22 14 1.47 1.76 0.06 N2 14 1.59 1.07 0.08 N2 12 1.81 0.93 0.10 N2 12 2.06 0.24 3 TMPTA 0.1 N2 12 1.01 5.77 0.15 N 20 1.08 5.29 0.2 N2 30 1.07 4.73 0.3 N 25 1.15 2.73 0.4 N2 27 1.19 2.54 0.5 N 14 2.29 1.17 0.5 A2r 20 1.98 ND
ND = not determined (1) = Dicup R = dicumyl peroxide manufactured by Hercules, Inc.
TMPTA = trimethyolpropane triacrylate made by Celanese Chemical Co.
(2) = parts of cross-linking agent mixed in per hundred parts of polymer (33 = N2 The opening of Brabender mixer was blanketed nitrogen Alr = No nitrogen blanketing.
(4) = time from the start of a test to when the torque reached the maximum (5) = the maximum torque divided by the torque immediately before the cross-linking agent was added.
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The effect of an azido silane on the foaming was even more dramatic during the tests in this example. Without silane, a good foam could not be produced, but with 0.15 pph silane excellent quality substantially closed-cell foam was achieved. The foams expanded by low cost FC-12 blowing agent showed excellent dimensional stability during ambient aging with shrinkage no more than 3 percent. This is a remarkable improvement over a LDPE foam made with FC-12 blowing agent. The heat distortion temperature of the HDPE foams was 125C which is 25C higher than that of typical LPDE foam.
Example 5 In this example, the same apparatus, operating conditions, and polymer composition were used, as in Example 4, except for gel temperature and blowing agent. The gel temperature was maintained at 130C
and a 90/10 mixture of FC-12/EtOH was used as the blowing agent. The test results are presented in Table V.
Again, the silane cross-linking agent aided in foam processing and alcohol suppressed development of cross-linking in the extrusion line. At a low silane level, improvements were seen in one or more performance areas. For example, even at 0.05 pph silane level, foam density dropped significantly from the control. At 0.15 pph silane level, good quality foams were produced with a noticeable increase in the die pressure. Interestingly, the pressure at extruder discharge increased little at this silane level. This is an advantage in foam 31,339-F -29-~30~ 78P6 extrusion process since a high die pressure prevents prefoaming but a low extruder discharge pressure faci-litates polymer extrusion. The trend indicates that the alcohol~containing blowing agent called for a silane level higher than 0.15 pph for the optimum results.
Example 6 - The apparatus used in this example was the same as in Example 1. A Hercules Porofax 6523 poly-propylene resin having 4.0 melt index ~ASTM D-1738 Condition L) was u~-d. The polymer was mixed with 0.1 pph talc and 0.05 pph organotin catalyst (T-12) and fed into the extruder at a uniform rate of 10 pounds per hour (12.60 x 104 kg/s). A 90/10 by weight mixture of FC-12 and methylene chloride was injected into the extruder at a rate of 27.8 pph. Extruder zones were maintained at 180C, 200C and 210C for feeding, melting and metering, and mixing zone, respectively.
The gel temperature was kept at an essentially constant level of 146C. The data are summarized in Table VI.
In this example also, addition of an azido functional silane improved foam processability of polypropylene.
The polypropylene foams did not shrink at all during aging and had a heat distortion temperature as high as 165C.
Exam~le 7 The same apparatus used in Example l was used in this example. The polymer feedstock employed ln this example was an 80/20 mixture o a linear Iow density polyethylene that was used in Example 1 and a polystyrene having weight average molecular weight of 200,000.
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31, 339-F -36-_37~ 6 Two granular polymers were blended by use of a tumbler, mixer with 0.1 pph talc and 0.05 pph organo-tin catalys-t (T-1~) and fed to the extruder at an essentially uniform rate of 10 pounds per hour (12.6 x 104 kg/s). A 95/5 by weight mixture of FC-12/ethanol was injected into the extruder at a rate of approxi-mately 21.0 pph.- Extruder zones were maintained at 145C, 195C and 205C, respectively, for feeding, melting and metering; and mixing zone, respectively.
The gel was cooled down to an essentially uniform temperature of 122C. The test results are seen in Table VII and Figure 2.
This particular polymer blend provided reason-ably good foam without cross-linking when the die gap was closed down to 0.050 inch (1.27 mm). The foam had a small cross~section and a relatively high level of open cells. At a laryer die gap, foam collapsed par-tially. Foam improved progressively with the azido functional silane level. At a silane level of 0.15 pph or higher, superb-looking foams were obtained having a lower density, lar~er cross-section, and lower open cell content. At a silane level as high as 0.25 pph, there was no sign of over-cross~linking. Again, a die pressure of approximately 400 psig (2758 kPa) was the line o demarcation between good and poor foams.
The foams thus produced also had excellent dimensional stability during aging without suffering any shrinkage. The heat distortion temperature of the blend foam was llO~C.
31,339-F -37--38- ~247~6-Exam~le 8 The apparatus, operatlng procedure, and polymer used in this example were the same as in Example 1.
Polymer granules were adhered with 0.05 pph talc by use of a wetting agent and fed into the extruder.
FC-12 blowing agent was injected into the extruder at an essentially uniform rate of 19.7 pph. A predeter-mined amount of dicumyl peroxidf (Dicup R (Trademark), from Hercules Inc.) was injected into the blowing agent stream in 10 percent by weight solution in methylene chloride. Extruder zone temperatures were maintained at 140C, 180C, and 200C, respectively. The gel was cooled down to an essentially uniform temperature of 124C. The resultant data are given in Table VIII and are illustrated in Figure 3.
The control LLDPE foam was not satisfactory.
Addition of a small amount (0.0054 pph) of dicumyl peroxide improved foam processability and quality. The best result was obtained at a peroxide level of 0.01 pph. Excellent quality foams were produced at a wide range of die gaps. When the peroxide level was raised to 0.0123 pph, symptoms of over-cross-linking developed.
At a high peroxide level, the foam strand fractured.
Again, a die pressure of approximately 400 psig (2758 kPa) was the line of demarcation between good and poor foams. - -Example 9 A Brabender Plasti-corder (Trademark of C. W.
Brabender Instrumen-ts, Inc.) mixing head having 60 ml capacity was employed in this example in order to show 31,339-F -38-_39_ ~4~
that a multi-vinyl functional monomer could be used as a cross-linking agent in accordance with this invention.
The Brabender mixer was heated to an essen-tially constant temperature of 200C. A linear low density polyethylene used in Example 1 was used in all tests of this example. Approximately 40 g of the granular polyethylene was put in the mixer with its blades rotating at a constant speed cf 30 rpm. The opening of the mixer was continuously purged with nitrogen in most tests e~cept otherwise specified. The tor~ue was continuously recorded on a strip chart. The torque reached an essentially steady state in 5 to 10 minutes.
After 10 minutes mixing, there was added a predetermined amount of cross-linking agent selected from Dicup R dicumyl peroxide by Hercules Inc. and trimethylolpropane triacrylate ~TMPTA) made by Celanese Chemical Co. Dicup R was fed in 20 percent solution in methyl~ne chlorid~. Kneading was continued until the torque peaked out. Melt index of the cross-linked material was determined.
As shown in Table IX, dicumyl peroxide is an effective cross-linking agent. The torque rose 18 percent at the peroxide level of 0.02 pph. The level of peroxide was determined rather excessive in Example 8. A similar increase in torque was achieved by 0.3 to 0.4 pph TMPTA in nitrogen atmosphere. From this result, it is inferred that a multivinyl monomer may be used as a cross-linking agent for improving extrusion oamability of a linear polyolefin polymer.
31,339-F -39--40~ 7~
Example 10 The Brabender mixer was also used in this example. Several linear low density polyethylenes and a high density polyethylene having 6.2 melt index (ASTM
D-1238-79 Condition E) and 0.963 g/cm3 density were evaluated for self-crosslinking in air atmosphere. In each test, approximately 40 g of polymer was charged in the mixer with its blades rotating at a constant speed of 3~ rpm. The test data are set fo~rth in Table X.
All linear low density polyethylenes gained more than enough torgue for improvement in extrusion ~oamability during kneading in the mixer. The induc-tion time for torque rise was mostly shorter than 30 minutes. The induction time became shorter and the maximum torque rise was greater at a higher temperature.
In inert atmosphere, the torque did not rise appreciably.
Antioxidant delayed cross-linking but did not s-top its development. From the results of the tests, it is inferred that melt kneading of a linear polyethylene in the presence of oxygen is another way of lightly cross -linking the polymer for extrusion foaming. A vented extruder could be used for this purpose.
Example 11 The apparatus used in this example was the same as Example 1. A granular polystyrene, polystyrene with a weight average molecular weight of 200,000, was uniformly mixed with a small amount of dibutyl tin dilaurate condensation catalyst (T-12, available from M
& T Chemicals, Inc.), barium stearate and talcum powder.
The mixture was fed into the extruder at an essentially uniform rate of 10 pounds per hour (12.60 x 10 4 kg/s).
A premixed blowing agent was injec-ted into the extruder 31,339-F -40--41- ~47~
at a predetermined rate. Blowing agents used in this example were a 50/50 by weight mixture of fluorocarbon 12 (FC-12) and methyl chloride (MeCl) for Text No. 1 and a 70/30 by weight mixture of fluorocarbon 12 and fluorocarbon ll (FC-11) for the other tests. An.azido functional silane, 2-(trimethoxysily ethylphenylsulfonyl) azide (CT2905 distributed by Petrarch Systems, Inc.~, was injected to the blowing agent stream at a uniform ~ predetermined rate. The extruder zones were maintained at 170C, la~C and 200C for feeding, melting, metering, and mixing zone, respectively. The temperature of the cooling zone was adjusted so that the gel could be cooled down to a uniform temperature for optimum foam expansion.
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Cross-linkin~ Agent Peak Melt Level Environment Time Torque Ratio Index Test Type (pph) Gas (min) (Peak/Initial) (dg/min) No ~1) (2) (3) ~4) (5) (6) -~ N2 20 1.00 7.19 2 Dicup R 0.01 - N 12 1.03 5.94 0.02 N2 12 1.18 4.50 0.03 N2 ` 14 1.2B- 2.62 0.04 N 12 1.37 2.32 0.05 N22 14 1.47 1.76 0.06 N2 14 1.59 1.07 0.08 N2 12 1.81 0.93 0.10 N2 12 2.06 0.24 3 TMPTA 0.1 N2 12 1.01 5.77 0.15 N 20 1.08 5.29 0.2 N2 30 1.07 4.73 0.3 N 25 1.15 2.73 0.4 N2 27 1.19 2.54 0.5 N 14 2.29 1.17 0.5 A2r 20 1.98 ND
ND = not determined (1) = Dicup R = dicumyl peroxide manufactured by Hercules, Inc.
TMPTA = trimethyolpropane triacrylate made by Celanese Chemical Co.
(2) = parts of cross-linking agent mixed in per hundred parts of polymer (33 = N2 The opening of Brabender mixer was blanketed nitrogen Alr = No nitrogen blanketing.
(4) = time from the start of a test to when the torque reached the maximum (5) = the maximum torque divided by the torque immediately before the cross-linking agent was added.
(6) = melt index of the kneaded polymer determined per ASTM D~1238-79 condition N.
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At a fixed die opening for a given blowing agent system where all formulations provided good quality foams, both pxessures at -the die and extruder discharge were recorded and samples were taken. The foam samples were aged for about one month at ambient temperature prior to property determination and secondary foaming tests.
~ ~ Secondary foaming was conducted both by - -atmospheric steam and by hot air. Foam slugs of 0.25 inches (6.35 mm) thickness were slided out of foam strands and aged for about one day at ambient temperature prior to secondary expansions. After exposure to atmospheric steam for varying lengths of time, foam specimens were aged at ambient temperature while their weights and volumes were monitored. Highly expanded foam specimens shrank when taken out of steam but recovered to the final steady state volumes in about two days. Expansion tests in hot air were conducted similarly with the exception that expansion or shrinkage of a foam specimen in the oven was permanent not need-ing ambient aging for volume recovery.
Table XIA shows that incorporation of an azido functional silane gradually raises both the die pressure and the extruder discharge pressure.
Other noticable effects of silane include enlarge-ment in çell size and cross-sectional size which .
are desirable in foam extrusion.
The remarkable effect of silane on steam expandability of extruded polystyrene foam is seen in Table XIB. Addition of silane enhances both the rate 31,339-F -47-~2a~713~i .
and extent of foam expansion in steam. At the silane level of 0.2 pph, the foam expands about twice as much as the control to an expansion ratio e~ceeding 280 in two hours. At this long exposure to steam, the control and one with a low level (0.05 pph) of silane suffered thermal collapse;
the expansion ratios~are lower than those at one hour exposure.
~ . .
The type of blowing agent also has a sig-nificant effect on steam expandability of the extruded polystyrene foams. The foam expanded with FC-12/MeCl blowing agent shows expansions lower than one half of that made with FC-12/FC-11 blowing agent. Loss of methyl chloride during aging is one probable cause of the relatively poorer performance of the FC-12/-MeCl blown foam. FC-11, having a high solubility in polystyrene, effectively plasticizes polystyrene for faster and greater expansion.
The effect of crosslinking is also seen in hot air expansion tests. As Table XIC shows, foams lightly crosslinked with an azido functional silane expaned more and withstand hot air lonyer than the control. For example, a foam crosslinked wi-th 0.15 pph or higher level of azido silane keeps expanding during 90 minutes exposure to 100C air while the control collapses within 60 minutes at the same temperature. Although less pronounced, the cross~linking effect persists at a lower level of silane as well.
30 Example_12 The apparatus and its operating procedure used for tests in this example are the same as in 31,339-F -48-Example 1. The polymer feedstock employed for tests in this example was a 50/50 by weight blend of poly-styrene with Mw 200,000 and polystyrene with Mw 300,000. Approximately 0.05 pph T-12, 0.1 pph barium stearate and 0.1 pph talcum powder were mixed in -the granular blend of two polystyrenes and fed into the extruder at a uniform rate of 10 pounds per hour (12.60 x 10 4 kg/s). In test 1, there was used a 50/50 by weight mixture of FC-12 and methyl chloride 10 as the expanding agent and a 70/30 mixture of FC-12 and FC-11 in the rest of the tests. The level O F
azido silane cross-linking agent was varied up to 0.45 pph. The extruder zones were maintained at about 170C, 200C and 200C for feeding, melting, metering, and mixing zone, respectively. The tempera-ture of the cooling zone was adjusted so that the gel could reach an essentially uniform temperature of 135C.
When the operating condition reached an essentially steady state, the effects of die opening on foam appearance and line pressure were studied.
Foam samples were taken both at the threshold die gap for prefoaming and at a fixed die gap for a given blowing agent system. Property determina-tion and secondary foaming tests were conducted asdescribed in Example 11.
In general, silane cross-linking has a similar effect on this polymer blend. As shown in Tables XIIA, XIIB and XIIC, azido functional silane increased die pressure and cell size permitting achievement of a larger foam cross-section and greater expansion in both steam and hot air. The die may be opened wider at an azido functional 31,339-F -49-_50_ 12~7~6 silane level 0.25 pph or higher. For this polymer blend also, the type OL expanding agent has a pronounced effect on steam expandability. FC-12/~
FC-11 is superior to FC-12/MeCl blowing agent. This is ascribed to the low permeability and high solubility of FC-11 in polystyrene.
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31 ,.339-F -59--Example 13 The apparatus used in this example was the same as used in the other examples of this invention. As "S" shaped die orifice for Dow Pelaspan-PacTU loose-fill packing was attached at the discharge end of the extruder replacing the gap-adjustable die used in the other examples.
A 60/40 by weight mixture of polystyrene with Mw 200,aoo and polystyrene with Mw 300,000 was mixed with 1.2 pph fire retardant made by Dow Chemical Co.
(FR-651), 0.02 pph magnesium oxide and 0.02 pph calcium ~tearate by the use oP a small amount of wetting agent.
For tests incorporating azido silane, a small amount oP
wetting agent. For tests incorporating azido silane, a smal} amount oP (0.05 pph) of dibutyl tin dilaurate (T-12) was additionally mixed ln. The mixture was fed into the extruder at a uniform rate of about 10 pounds per hour (12.6 x 10~4 kg/s). A predetermined amount of azido functional silane was premixed in the blowing agent and injected into the extruder. A 95/5 by weight mixture o~ FC-11 and methylene chloride was the blowing 2~ agent used for Test 1 and 2 and small amount of methanol was mixed to the blowing agent for Test 3.
The extruder zones were maintained at 160C, 180C and 200C for feeding, melting and metering, and mixing zone, respectively. The temperature of the cooling zone was adjusted so that the extruder strand could become essentially free of voids upon quenching in cold water. The solid strand was cut to granules oP
approximately 1/4 inch (6.35 mm~ in length. The granules were about 5/16 inch (7.9 mm) in width and about 3/32 inch (2.4 mm) in thickness.
31~339-F -60-.. ....
-61~ ~2~7~
The as-extruded granules were annealed in 65C water for about 30 minutes and aged in ambient air for one day prior to steam expansion tests. The granules were expanded by atmospheric steam for 10 minutes and .then aged for a day. This first expansion was followed by the second, third and fourth expansion in a day interval between the-expansions. Expansion times were 10, l and 1 minutes for the second, third and fourth expansion, respectively. Foam densities were determined after the foams were aged for one day after each expansion.
As shown in Table XIII, addition of an azido silane results in a slight increase in the line pressure and leads to lower foam densities.
The expanded material cross-linked with azido silane not only showed lower densities after each expansion but better appearance after third and fourth expan-sions. The control (Test l) developed splits and cracks on the surface but the cross-linked materials showed few such deficiencies.
Example 14 The heat distortion temperature of foams was tested by aging them in a convective oven for one hour. Figure 5 illustrates the results of the tests. A control branched low density polyethylene (LDPE) foam with no azido silane cross-linking showed substantial heat distortion at between 105C and 110C. The heat distortion temperatures of foam - produced from polypropylene (PP), high density poly-ethylene (XDPE), and linear low density polyethylene ~LLDPE) are 165C, 125C, and 115C, respectively.
Blending in 20 percent polystyrene (PS) slightly 31,339-F -61--62~ ~2~7~
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aJ X _I C~l ~ ~ C l C') ~ ~ ~9 t- 00 31, 339-F -62--63~ 7~6 reduces the heat distortion temperature of linear low density polyethylene. On the other hand, incor-porating as much as 40 percent L~PE does not cause a drop in the heat dis~or-tion temperature of the linear low density polyethylene. All of the linear olefinic polymer oams cross-linked with azido silanes would be serviceable at temperature higher than -that with a branched low density polyethylene foam.
Example 15 As shown in Figures 6 and 7, and also in Table XVI below, the toughness and strength of the linear polyolefins are also well reflected in their foam properties. A 1.64 pounds per cubic foot (pcf) (26.27 kg/m3~ densith LLDPE foam out-performs an equivalent density LDPE foam in all strength categories. The LLDPE foam was twice as strong and twice as tough as the LDPE foam. The 1.64 pcf (26.27 kg/m3) density LLDPE foam almost matches a much higher density (2.53 pcf) (40.53 kg/m3) LDPE foam in compressive strength and actually outperformed the LDPE foam in tensile properties.
The heat distortion temperature of the LL~PE foams were 10C to 15C higher than that of the LDPE foam.
Foams made from high density polyethylene and polypropylene also reflect superior compressive strengths and heat distortion temperatures in com-parison to the LDPE foam.
31,339-F -63--64- ~Z~7~6 s~
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31, 339-F -64--65- 1~478~
Exam~le 16 The apparatus used in this exampl~ and its operating procedure were the same as used in Example 1.
A linear low density polyethylene having a 1.0 melt index and 0.935 gm/cm3 density was used in this example.
The polymPr granules were mixed with 0.05 pph talc and 0.05 pph organotin catalyst (T-12~; A dichlorodi-fluoromethane (FC-12) blowing agent was added at the : rate of 1-.82 to 1.88 lb/hr (2.29 x 10 4 to 2.37 -- -kg/s). As the cross-linking agent, a viny'trimethoxy silane (VTMO) was injected into the blowing agent stream in the amounts indicated in Table XVI. The extruder zones were maintained at 160C, 180C~
and 200C for feeding, melting and metering, and mixing, respectively. The gel temperature was fixed at 125C for all tests. The test results are set forth in Table XVI.
As can be seen, the control sample with no cross~linking agent collapsed at larger die open-ings. Only at the smallest die opening was a satis-factory foam produced; however, this foam had a very small cross-section and some open cells. The addition of VTMO as the cross-linking agent permitted the use of wider die openings resulting in good foams having larger cell and cross-sectional sizes while exhibiting a very low open cell content.
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31, 339-F -67--68- ~2~'78~6 Example 17 The apparatus, procedure, polymer, additives, and blowing agent used in this example were the same as used in Example 16. As the cross-lin.king agent, a 30:1 by weight mixture of vinyltrimethoxy silane and dicumyl peroxides was injected into the blowing agent stream in -the amounts indicated in Table XVII.
As can be seen, the VTMO/peroxide mixture was ~uite effective an~ produced excellent quality foams having large cell and cross-sectional sizes and very low open cell content.
31,339-F -68--69~ 7Z3~6 o O J~ l o r~ c~l r~ ~ t ~ r ~ ~.
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At a fixed die opening for a given blowing agent system where all formulations provided good quality foams, both pxessures at -the die and extruder discharge were recorded and samples were taken. The foam samples were aged for about one month at ambient temperature prior to property determination and secondary foaming tests.
~ ~ Secondary foaming was conducted both by - -atmospheric steam and by hot air. Foam slugs of 0.25 inches (6.35 mm) thickness were slided out of foam strands and aged for about one day at ambient temperature prior to secondary expansions. After exposure to atmospheric steam for varying lengths of time, foam specimens were aged at ambient temperature while their weights and volumes were monitored. Highly expanded foam specimens shrank when taken out of steam but recovered to the final steady state volumes in about two days. Expansion tests in hot air were conducted similarly with the exception that expansion or shrinkage of a foam specimen in the oven was permanent not need-ing ambient aging for volume recovery.
Table XIA shows that incorporation of an azido functional silane gradually raises both the die pressure and the extruder discharge pressure.
Other noticable effects of silane include enlarge-ment in çell size and cross-sectional size which .
are desirable in foam extrusion.
The remarkable effect of silane on steam expandability of extruded polystyrene foam is seen in Table XIB. Addition of silane enhances both the rate 31,339-F -47-~2a~713~i .
and extent of foam expansion in steam. At the silane level of 0.2 pph, the foam expands about twice as much as the control to an expansion ratio e~ceeding 280 in two hours. At this long exposure to steam, the control and one with a low level (0.05 pph) of silane suffered thermal collapse;
the expansion ratios~are lower than those at one hour exposure.
~ . .
The type of blowing agent also has a sig-nificant effect on steam expandability of the extruded polystyrene foams. The foam expanded with FC-12/MeCl blowing agent shows expansions lower than one half of that made with FC-12/FC-11 blowing agent. Loss of methyl chloride during aging is one probable cause of the relatively poorer performance of the FC-12/-MeCl blown foam. FC-11, having a high solubility in polystyrene, effectively plasticizes polystyrene for faster and greater expansion.
The effect of crosslinking is also seen in hot air expansion tests. As Table XIC shows, foams lightly crosslinked with an azido functional silane expaned more and withstand hot air lonyer than the control. For example, a foam crosslinked wi-th 0.15 pph or higher level of azido silane keeps expanding during 90 minutes exposure to 100C air while the control collapses within 60 minutes at the same temperature. Although less pronounced, the cross~linking effect persists at a lower level of silane as well.
30 Example_12 The apparatus and its operating procedure used for tests in this example are the same as in 31,339-F -48-Example 1. The polymer feedstock employed for tests in this example was a 50/50 by weight blend of poly-styrene with Mw 200,000 and polystyrene with Mw 300,000. Approximately 0.05 pph T-12, 0.1 pph barium stearate and 0.1 pph talcum powder were mixed in -the granular blend of two polystyrenes and fed into the extruder at a uniform rate of 10 pounds per hour (12.60 x 10 4 kg/s). In test 1, there was used a 50/50 by weight mixture of FC-12 and methyl chloride 10 as the expanding agent and a 70/30 mixture of FC-12 and FC-11 in the rest of the tests. The level O F
azido silane cross-linking agent was varied up to 0.45 pph. The extruder zones were maintained at about 170C, 200C and 200C for feeding, melting, metering, and mixing zone, respectively. The tempera-ture of the cooling zone was adjusted so that the gel could reach an essentially uniform temperature of 135C.
When the operating condition reached an essentially steady state, the effects of die opening on foam appearance and line pressure were studied.
Foam samples were taken both at the threshold die gap for prefoaming and at a fixed die gap for a given blowing agent system. Property determina-tion and secondary foaming tests were conducted asdescribed in Example 11.
In general, silane cross-linking has a similar effect on this polymer blend. As shown in Tables XIIA, XIIB and XIIC, azido functional silane increased die pressure and cell size permitting achievement of a larger foam cross-section and greater expansion in both steam and hot air. The die may be opened wider at an azido functional 31,339-F -49-_50_ 12~7~6 silane level 0.25 pph or higher. For this polymer blend also, the type OL expanding agent has a pronounced effect on steam expandability. FC-12/~
FC-11 is superior to FC-12/MeCl blowing agent. This is ascribed to the low permeability and high solubility of FC-11 in polystyrene.
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31 ,.339-F -59--Example 13 The apparatus used in this example was the same as used in the other examples of this invention. As "S" shaped die orifice for Dow Pelaspan-PacTU loose-fill packing was attached at the discharge end of the extruder replacing the gap-adjustable die used in the other examples.
A 60/40 by weight mixture of polystyrene with Mw 200,aoo and polystyrene with Mw 300,000 was mixed with 1.2 pph fire retardant made by Dow Chemical Co.
(FR-651), 0.02 pph magnesium oxide and 0.02 pph calcium ~tearate by the use oP a small amount of wetting agent.
For tests incorporating azido silane, a small amount oP
wetting agent. For tests incorporating azido silane, a smal} amount oP (0.05 pph) of dibutyl tin dilaurate (T-12) was additionally mixed ln. The mixture was fed into the extruder at a uniform rate of about 10 pounds per hour (12.6 x 10~4 kg/s). A predetermined amount of azido functional silane was premixed in the blowing agent and injected into the extruder. A 95/5 by weight mixture o~ FC-11 and methylene chloride was the blowing 2~ agent used for Test 1 and 2 and small amount of methanol was mixed to the blowing agent for Test 3.
The extruder zones were maintained at 160C, 180C and 200C for feeding, melting and metering, and mixing zone, respectively. The temperature of the cooling zone was adjusted so that the extruder strand could become essentially free of voids upon quenching in cold water. The solid strand was cut to granules oP
approximately 1/4 inch (6.35 mm~ in length. The granules were about 5/16 inch (7.9 mm) in width and about 3/32 inch (2.4 mm) in thickness.
31~339-F -60-.. ....
-61~ ~2~7~
The as-extruded granules were annealed in 65C water for about 30 minutes and aged in ambient air for one day prior to steam expansion tests. The granules were expanded by atmospheric steam for 10 minutes and .then aged for a day. This first expansion was followed by the second, third and fourth expansion in a day interval between the-expansions. Expansion times were 10, l and 1 minutes for the second, third and fourth expansion, respectively. Foam densities were determined after the foams were aged for one day after each expansion.
As shown in Table XIII, addition of an azido silane results in a slight increase in the line pressure and leads to lower foam densities.
The expanded material cross-linked with azido silane not only showed lower densities after each expansion but better appearance after third and fourth expan-sions. The control (Test l) developed splits and cracks on the surface but the cross-linked materials showed few such deficiencies.
Example 14 The heat distortion temperature of foams was tested by aging them in a convective oven for one hour. Figure 5 illustrates the results of the tests. A control branched low density polyethylene (LDPE) foam with no azido silane cross-linking showed substantial heat distortion at between 105C and 110C. The heat distortion temperatures of foam - produced from polypropylene (PP), high density poly-ethylene (XDPE), and linear low density polyethylene ~LLDPE) are 165C, 125C, and 115C, respectively.
Blending in 20 percent polystyrene (PS) slightly 31,339-F -61--62~ ~2~7~
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aJ X _I C~l ~ ~ C l C') ~ ~ ~9 t- 00 31, 339-F -62--63~ 7~6 reduces the heat distortion temperature of linear low density polyethylene. On the other hand, incor-porating as much as 40 percent L~PE does not cause a drop in the heat dis~or-tion temperature of the linear low density polyethylene. All of the linear olefinic polymer oams cross-linked with azido silanes would be serviceable at temperature higher than -that with a branched low density polyethylene foam.
Example 15 As shown in Figures 6 and 7, and also in Table XVI below, the toughness and strength of the linear polyolefins are also well reflected in their foam properties. A 1.64 pounds per cubic foot (pcf) (26.27 kg/m3~ densith LLDPE foam out-performs an equivalent density LDPE foam in all strength categories. The LLDPE foam was twice as strong and twice as tough as the LDPE foam. The 1.64 pcf (26.27 kg/m3) density LLDPE foam almost matches a much higher density (2.53 pcf) (40.53 kg/m3) LDPE foam in compressive strength and actually outperformed the LDPE foam in tensile properties.
The heat distortion temperature of the LL~PE foams were 10C to 15C higher than that of the LDPE foam.
Foams made from high density polyethylene and polypropylene also reflect superior compressive strengths and heat distortion temperatures in com-parison to the LDPE foam.
31,339-F -63--64- ~Z~7~6 s~
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31, 339-F -64--65- 1~478~
Exam~le 16 The apparatus used in this exampl~ and its operating procedure were the same as used in Example 1.
A linear low density polyethylene having a 1.0 melt index and 0.935 gm/cm3 density was used in this example.
The polymPr granules were mixed with 0.05 pph talc and 0.05 pph organotin catalyst (T-12~; A dichlorodi-fluoromethane (FC-12) blowing agent was added at the : rate of 1-.82 to 1.88 lb/hr (2.29 x 10 4 to 2.37 -- -kg/s). As the cross-linking agent, a viny'trimethoxy silane (VTMO) was injected into the blowing agent stream in the amounts indicated in Table XVI. The extruder zones were maintained at 160C, 180C~
and 200C for feeding, melting and metering, and mixing, respectively. The gel temperature was fixed at 125C for all tests. The test results are set forth in Table XVI.
As can be seen, the control sample with no cross~linking agent collapsed at larger die open-ings. Only at the smallest die opening was a satis-factory foam produced; however, this foam had a very small cross-section and some open cells. The addition of VTMO as the cross-linking agent permitted the use of wider die openings resulting in good foams having larger cell and cross-sectional sizes while exhibiting a very low open cell content.
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31, 339-F -67--68- ~2~'78~6 Example 17 The apparatus, procedure, polymer, additives, and blowing agent used in this example were the same as used in Example 16. As the cross-lin.king agent, a 30:1 by weight mixture of vinyltrimethoxy silane and dicumyl peroxides was injected into the blowing agent stream in -the amounts indicated in Table XVII.
As can be seen, the VTMO/peroxide mixture was ~uite effective an~ produced excellent quality foams having large cell and cross-sectional sizes and very low open cell content.
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31 ,339-F -70-
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31 ,339-F -70-
Claims (12)
1. A process for preparing a lightly cross-linked linear polyolefin foam having a substantially closed-cell structure, comprising the steps of:
a) melt blending under pressure at least one linear polyolefin selected from the group consisting of LLDPE, HDPE, PP and PS together with a blowing agent and sufficient amount of a cross-linking agent selected from the group consisting of azido functional silanes, vinyl functional silanes, organic peroxides, multi-functional vinyl monomers, and oxygen, to form a flowable admixture, and, b) extruding said admixture through a die to a zone of lower pressure and activating said blowing agent to expand at least one said linear polyolefin to form said lightly cross -linked foam.
a) melt blending under pressure at least one linear polyolefin selected from the group consisting of LLDPE, HDPE, PP and PS together with a blowing agent and sufficient amount of a cross-linking agent selected from the group consisting of azido functional silanes, vinyl functional silanes, organic peroxides, multi-functional vinyl monomers, and oxygen, to form a flowable admixture, and, b) extruding said admixture through a die to a zone of lower pressure and activating said blowing agent to expand at least one said linear polyolefin to form said lightly cross -linked foam.
2. The process of Claim 1 in which the pressure at said die is at least 400 psig (2758 kPa).
3. The process of Claim 1 in which said cross-linking agent is 2-(trimethoxysilyl ethyl phenyl sulfonyl) azide, and a catalyst which catalyzes the condensation of silanols is added with the cross--linking agent.
4. The process of Claim 1 in which said cross-linking agent is dicumyl peroxide.
5. The process of Claim 1 in which said cross linking agent is trimethylolpropane triacrylate.
6. The process of Claim 1 in which said crosslinking agent is vinyl trimethoxy silane.
7. The process of Claim 1 wherein in step a) said cross-linking agent is added after a flowable admixture of said at least one linear poly-olefin and said blowing agent is formed in an amount sufficient to initiate cross-linking of said at least one linear polyolefin and increase the pressure of said admixture to at least 400 psig (2758 kPa).
8. The process of Claim 1 in which said cross-linking agent is from 0.01 to 2.0 pph of an azido functional silane, and a catalyst which cata-lyzes the condensation of silanols is added.
9. The process of Claim 1 in which said cross-linking agent is from 0.001 to 0.5 pph of an oxganic peroxide.
10. The process of Claim 1 in which said cross-linking agent is from 0.01 to 2.0 pph of a multifunctional vinyl monomer.
11. A lightly cross-linked linear poly-olefin foam having a substantially closed-cell structure when prepared according to the process of Claim 1 or Claim 7.
12. An expandable linear olefinic polymer composition comprising at least one linear polyolefin selected from the group consisting of LLDPE, EDPE, PP
and PS, a blowing event, and a cross-linking agent selected from the group consisting of azido functional silanes, vinyl functional silanes, organic peroxides, multifunctional vinyl monomers, and oxygen.
and PS, a blowing event, and a cross-linking agent selected from the group consisting of azido functional silanes, vinyl functional silanes, organic peroxides, multifunctional vinyl monomers, and oxygen.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US06/672,001 US4714716A (en) | 1984-11-16 | 1984-11-16 | Lightly crosslinked linear olefinic polymer foams and process for making |
| US672,001 | 1984-11-16 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1247816A true CA1247816A (en) | 1989-01-03 |
Family
ID=24696749
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000495177A Expired CA1247816A (en) | 1984-11-16 | 1985-11-13 | Lightly crosslinked linear olefinic polymer foams and process for making |
Country Status (11)
| Country | Link |
|---|---|
| US (1) | US4714716A (en) |
| EP (1) | EP0181637B1 (en) |
| JP (2) | JPS61126701A (en) |
| AT (1) | ATE71640T1 (en) |
| BR (1) | BR8505760A (en) |
| CA (1) | CA1247816A (en) |
| DE (1) | DE3585207D1 (en) |
| DK (1) | DK526285A (en) |
| ES (1) | ES8706176A1 (en) |
| FI (1) | FI81819C (en) |
| NO (1) | NO166234C (en) |
Families Citing this family (83)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4694025A (en) * | 1984-11-16 | 1987-09-15 | The Dow Chemical Company | Alcohol control of lightly crosslinked foamed polymer production |
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-
1984
- 1984-11-16 US US06/672,001 patent/US4714716A/en not_active Expired - Fee Related
-
1985
- 1985-11-13 CA CA000495177A patent/CA1247816A/en not_active Expired
- 1985-11-14 DE DE8585114456T patent/DE3585207D1/en not_active Expired - Fee Related
- 1985-11-14 AT AT85114456T patent/ATE71640T1/en not_active IP Right Cessation
- 1985-11-14 DK DK526285A patent/DK526285A/en not_active Application Discontinuation
- 1985-11-14 BR BR8505760A patent/BR8505760A/en not_active IP Right Cessation
- 1985-11-14 EP EP85114456A patent/EP0181637B1/en not_active Expired - Lifetime
- 1985-11-15 NO NO854575A patent/NO166234C/en unknown
- 1985-11-15 ES ES548924A patent/ES8706176A1/en not_active Expired
- 1985-11-15 JP JP60255144A patent/JPS61126701A/en active Pending
- 1985-11-15 FI FI854509A patent/FI81819C/en not_active IP Right Cessation
-
1986
- 1986-10-06 JP JP61236387A patent/JPS6390544A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| FI81819B (en) | 1990-08-31 |
| ATE71640T1 (en) | 1992-02-15 |
| DE3585207D1 (en) | 1992-02-27 |
| NO854575L (en) | 1986-05-20 |
| US4714716A (en) | 1987-12-22 |
| FI81819C (en) | 1990-12-10 |
| EP0181637A2 (en) | 1986-05-21 |
| JPS6390544A (en) | 1988-04-21 |
| NO166234B (en) | 1991-03-11 |
| BR8505760A (en) | 1986-08-12 |
| EP0181637B1 (en) | 1992-01-15 |
| NO166234C (en) | 1991-06-19 |
| FI854509A0 (en) | 1985-11-15 |
| ES8706176A1 (en) | 1987-06-01 |
| ES548924A0 (en) | 1987-06-01 |
| DK526285D0 (en) | 1985-11-14 |
| EP0181637A3 (en) | 1988-05-25 |
| JPS61126701A (en) | 1986-06-14 |
| DK526285A (en) | 1986-05-17 |
| FI854509A (en) | 1986-05-17 |
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