CA1224609A - Blown nylon film and process for the preparation thereof - Google Patents

Abstract

Abstract of the Disclosure The preparation of monolayer blown nylon films on equipment conventionally used in the manufacture of blown polyethylene film is facilitated by the intimate admixture of a minor proportion by weight of a random ethylene/ethylenically unsaturated carboxylic acid copolymer into the nylon resin composition from which said blown-nylon film is to be manufactured.

Description

, BLOWN NYLON FILM AND
PROCESS FOR THE PREPARATION THEREOF

In one aspect, the present invention relates to certain monolayer, biaxially oriented blown nylon film materials and to a process for the preparation thereof. In another aspect, the invention relates to a process for the preparation of such films on conven-tional polyethylene blown film equipment. In a further aspect, thi~ invention also relates to an improved process fox the preparation of blown monolayer nylon films on specially designed extrusion equipment which is conventionally used in the preparation of monolayer blown nylon films.

Polyamide resins, commonly referred to as nylon, and blends thereof with various other polymeric materials such as polyethylene, graft or random copolymers of ethylene with ethylenically unsaturated carhoxylic acids or anhydrides, ethylene/vinyl acetate copolymers, ethylene/alkyl acrylate copolymers and the like are well known in the art and have been proposed for use in the fabrication of a variety of thermoplastic articles - 20 such as, for example, various molded parts, and extruded J,, 30,661-E' -l~ .

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articles includiny fibers, filaments, tubing, bottles, films, sheets, wire coatings and the like. See, for example, British Patent 998,439; Brit;ish Patent 1,262,802;
British Patent 1,464,036; British Patent 1,552,352;
U.S. Patents 3,093,255; 3,250,823; 3,373,223; 3,373,224;
3,472,916; 3,668,274; 3,676,400; 3,6~1,216; 3,822,227;
3,845,163; 3,963,799; 3,997,625; 4,018,733; 4,03~,438;
4,086,295; 4,100,238; 4,105,709; 4,160,790; 4,174,358;
4,251,424; 4,261,473; 4,287,315; 4,305,865; and 4,321,336;
Japanese Patent J7 4049-179; EPO Application Number 27191; and published Japanese Patent Applications J5 0142-675; J5 4155-270; J5 4155-272; J5 4016-576;
- J5 5034-95~; J5 6004-652 and J5 6062-864.

Historically, certain features or character-istics of polyamide resins have tended to hinder the manufacture of polymer film structures therewith. For example, such resins typically have relatively low melt tension properties and relatively low melt viscosity at the temperatures involved in extrusion processing and particularly at high.rates of shear~ Such characteristics have been especially troublesome relative to the manufacture of blown polyamide film structures, particularly in the case of monolayer blown polyamide film structures. In particular, an extruded, molten web or mass of such polymer generally fails to have sufficient strength to suitably support a hot film bubble as is necessary in conventional blown film manufacturing operations.
Accordingly, it has been common practice in the past to resort to special processing techniques (e.g., cast film prepaxation followed by special tentering/stretching operations), special equipment design (e.g., special die designs), special extra high molecular weight poly-amide compositions, special multiple layered film 30,661-F -2-~2~ 9 --3~

structures and the like when the objective was to prepare a biaxially orient~d polyamide film structure.

In view of the foregoing, it would be highly desirable to provide a means fo-- improving the process-S ability o polyamide resin compositions and to therebyfacilitate and simplify the fabrication of biaxially oriented, blown film structures ther,efrom. Moreover, it would also be highly desirable to provide a means or process by which biaxially oriented monolayer polyamide film structures could be suitably prepared using con-ventional polyolefin blown film manufacturing equipment.

In accordance with the present invent'on, it has now been found that certain blends of a major proportion of a polyamide resin with a minor proportion of a random copolymer of ethylene with an ethylenically unsaturated carboxylic acid can be suitably processed into biaxially oriented, monolayer blown film structures on equipment conventionally employed to manufacture blown polyethylene film structures. In addition, it has also been found that the incorporation of a minor proportion of a random copolymer of ethylene with an ethylenically unsaturated carboxylic acid into a major proportion of a polyamide resin substantially improves the processability of said polyamide on other types of equipment used in the industry for the preparation of monolayer blown polyamide film structures. Accordingly, the present invention in one asp~ct is a process for the prepara-tion of a biaxially oriented monolayer poly-amide film structure which process comprises intimately admixiny from 1 to 50 parts by weight of a random ethylene/ethylenically unsaturated carboxylic acid copolymer with from 50 to 99 parts by weight of a 30,661-F -3-~,~2~

polyamide resin and fabricating said int:imate admixture into a monolayer blown film structure.

In another aspect, the present invention is an improvement in an extrusion proce.ss for the prepara-tion of a blown monolayer film of a polyamide composi-tion wherein said improvement comprises the intimate incorporation into said polyamide composition, either prior to or during the blown film ex-trusion of said composition, of a minor proportion by weight of a random copolymer of a major pxoportion by weight of ethylene with a minor proportion by weight of an ethylenically unsaturated carboxylic acid.

The polyamide film structures prepared in the foregoing fashion have excellent strength properties in both the machine and transverse directions as well as having ~xcellent oxygen barrier properties. In addition, the use of the subject polymer blends for blown film manufacturing purposes is particularly advantageous since said blends have been found to have a substantially broader "operating window" (i.e., in terms of suitable melt temperature operating ranges) than polyamide compositions not containing the indicated ethylene/-ethylenically unsaturated carboxylic acid copolymer component.

The polyamide resins which are employed in the practice of the present invention are well known in the art and are commonly referxed to as nylon resins.
Representative examples of such polyamide resins are described in U.S. Patents 2,071,250; 2,071,251; 2,130,523;
- 30 and 2,130,948. Such polyamide resins are typically derived by the polymexization of one or more saturated 30,661-F -4-dibasic acids such as, for example, oxalic acid, succinic acid, adipic acid, suberic acid, sebacic acid, etc., with one or more saturated diamines such as, for example, hydrazine, ethylene diamine, tetramethylene diamine, pentamethylene diamine, hexamethylene diamine, deca-methylene diamine, and the like; by the polymerization of one or more monoamino-monocarboxylic acids, or the cyclic lactams thereof, such as, for example, 6~amino-hexanoic acid, 11-aminoundecanoic acid, 12-aminostearic acid and the like; or by the interpolymerization of a mixture of one or more diamines, one or more dicarboxylic acids and one or moxe monoamino-monocarboxylic acids.

Preferred polyamide resins for use in the practice of the present invention include polycapro-lactam (nylon-6), polyhexamethylene adipamide (nylon-6,6), polyhexamethylene sebacamide (nylon-6,10), polyamino~
undecanoic acid`(nylon-ll), polyamino-dodecanoic acid (nylon-12) or mixtures thereof.

As has been previously noted, the aforementioned polyamide resin typically constitutes a major proportion by weight (i.e., from 50 to 99 weight percent) of the polymer blends employed in the practice of the present invention. Preferably said polyamide resin constitutes from 70 to 95 (most preferably from 75 to 90) weight percent of such polymer blends.

Random ethylene/ethylenically unsaturated carboxylic acid copolymers which are suitably employed in the practice of the present inven-tion include those which are derived from the addition polymerization of a monomer mixture comprising a major proportion by weight (e.g., from 65 to 99, preferably from 80 to 98 and most 30,661-F -5-~2~

preferably from 80 to 94, percent~by weight) of ethylene and a minor proportion by weight (e.g., from 1 to 35, preferably from 2 to 20 and most preferably from 6 to 20, percent by weight) o an ethylenically unsaturated carboxylic acid monomer. Specific examples of such suitable ethylenically unsaturated carboxylic acids (which term includes mono- and polybasic acids, acid anhydrides, and partial esters of polybasic acids, as well as the various metallic salts thereof) are acrylic acid, methacrylic acid, crotonic acid, fumaric acid, maleic acid, itaconic acid, maleic anhydride, monomethyl maleate, monoethyl maleate, monomethyl fumarate, monoethyl fumarate, tripropylene glycol monomethyl ether acid maleate, or ethylene glycol monophenyl ether acid maleate. The carboxylic acid monomer i5 preferably~
selected from ~ ethylenically unsaturated mono- and polycarboxylic acids and acid anhydrides having from 3 to 8 carbon atoms per molecule and partial esters of such polycarboxylic acid wherein the acid moiety has at least one carboxylic acid group and the alcohol moiety has from 1 to 20 carbon atoms. SuGh copolymers may ~
consist essentially of ethylene and one or more of such ethylenically unsaturated acid or anhydride comonomers or can also contain small amounts of other monomers copolymerizable with ethylene. Thus, the copolymer can contain minor propoxtions (e.g., from 0 to 20 weight percent, preferably from 0 to 10 weight percent) of other copolymerizable monomers, such as, for example, alkyl or hydroxyalkyl esters of ethylenically unsaturated monocarboxylic acids such as methyl methacrylate, ethyl acrylate, 2-hydroxyethyl acrylate,

2-ethylhexyl acrylate, isobutyl acrylate etc.; vinyl - esters of saturated carboxylic acids such as vinyl `acetate, vinyl propionate, vinyl butyrate and the like.

30,661-F -6- ~
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Random copolymers of the general type referred to above are readily known in the art as are various methods for the preparation of same.

Especially preferred ethylene/ethylenically S unsaturated carboxylic acid copolymers for use in the practice of the present in~ention are the normally solid random copolymers of a major proportion by weight of ethylene with from 2 to 15 (most preferably from 6 to 10~ welght percent of acrylic, methacrylic or crotonic (especially acrylic acid) such as those described in U.S. Patents 3,520,861 and 3,239,370 and the known ionomer salts thereof.

Preferably, the ethylene/ethylenically unsaturated carboxylic acid copolymers employed in the lS present invention are of a relatively high molecular weight as exempliied by their exhibiting a melt index of from 0.5 to 10 decigrams/minute (more preferably from 1 to 5 decigrams/minute) when measured pursuant to - ASTM D-1238 Condition E.
.
The aforementioned ethylene/ethylenically unsaturated carboxylic acid copolymer will typically constitute a minor proportion ~i.e., from 1 to 50 weight percent) of the polyamide blends of the present invention. Preferably said copolymer will constitute from 5 to 30 weight percent of said ~lends and most preferably said copolymer will be employed in an amount of from 10 to 25 weight percent in said polymer blends.

In the practice of the present invention, it has been found to be important to ensure that the aforementioned polyamide resin and ethylene/ethylenically 30,661-F -7-~:2~61D~
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unsaturated carboxylic acid copolymex components of the subject polymer blends be very thoroughly and intimately admixed prior to the actual fabricat:ion of a blown polymeric film structure therefrom. Accordingly, in those instances where the extrusion equipment to be employed in the actual film fabrication operation is one having relatively poor mixing efficiency or characteristics, then it is generally desirable and advantageous to melt preblend the starting polyamide and ethylene/unsaturated carboxylic acid copolymer components together in a separate melt-form mixing operation (e.g., in a separate mixing extruder) in advance of the actual film forming operation. On the other hand, in those instances where the extrusion equipment employed in the film fabrica-tion operation is itself of a type exhibiting ~ood mixing characteristics (e.g., by virtue of havin~ a relatively large length to diameter ratio, special screw configurations adapted for increased mixing efficiency etc.), then a separate preliminary melt blending/extrusion operation may not be necessary for adequate admixing of the subject polymer blends and simple dry blending of the individual blend components (e.g., in solid pellet, powder or flake form) in advance of the film extrusion operation may be all that is required in such instance.

In the actual blown film extrusion processing operation of the present invention, it has also been found to be advantageous and beneficial to operate the blown film extruder employed in a fashion which results in a temperature profile along the length of the barrel which decreases from a higher temperature at the feed end (or at some other intermediate upstream zone) of said extruder to a relatively lower temperature (but, 30,661-F -8-~22~

naturally, still above the softening or melting of the polymer blend being extruded) at the die end ~hereof.
Accordingly, the operation of said blown film extruder in such a fashion represents a particularly preferred embodiment of the present invention.

In addition to the foregoiny, it has also been found to be important in the practice of the present invention to operate the subject blown film extrusion line in a fashion such that the "frost line height" of the blown nylon film "bubble" is less than 76 cm (30 inches~, preferably less than 38 cm ~15 inches) from the extruder die. As will be well recognized by the skilled artisan, the magnitude of the a~orementi4ned "frost line height" will be a function of a variety of factors such as, for example, the temperature of the polymer melt as it exits the extruder die, the thickness of the polymer web forming the film bubble, the linear velocity of the molten polymer film web, the temperature and volumetric flow rate of any forced cooling gases (e.g., air) employed, the crystal-lization rate of the polymer-composition employed, and the like. In this regard, it has been found to be highly advantageous and preferable to employ a chilled gaseous cooling medium ~e.g., chilled air at a temperature below about 25C, preferably below 15C) to cool the nylon film bubble as it exits the extruder die. In addition, it has also been found that the incorporation of the ethylene/ethylenically unsaturated carboxylic acid copolymer component of the present invention serves to substantially and dramatically increase the crystallization rate of the resulting polyamide composition (i.e., relative to what it would be in the absence of said ethylene/ethylenically unsaturated carboxylic acid 30,661-F -9-copolymer component); thereby significantly facilitating the rapid crystallization thereof and t.hus substantially reducing the "fro~t line height" in the blown nylon film manufacturing operation of .concerll, Following their preparation, the biaxially oriented monolayer polyamide-ethylene/ethylenlcally unsaturated carboxylic acid copolymer blend films prepared in accordance with the present invention can be employed in the conventional fashion in the ~ariety of well known packaging applications which have heretofore ~een served by cast nylon film structures, ~ hy cast and tentered nylon film structures, by multi-; layered blown nylon film structures, and the like.

The practice of the present invention is further illustrated by reference to the following examples thereof in which all parts and percentages are to be understood as being on a by weight basis unless otherwise indicated.

Example 1 In this example, a twin screw Werner-Pfleiderer compounding extruder was employed to melt blend 100 parts of a nylon-6 resin ~marketed by Allied Chemical Company as Capron~8207F) with.10 parts of a random ethylene/acrylic acid copolymer containing about 9.5 25 weight percent of acrylic acid and having a melt index -of about 10 decigrams/minute as determined purs~ant to ASTM D-1238, Condition E. During said melt blending operation, the indicated twin screw extruder was operated with a temperature profile along its length which ; 30 gradually decreased from 420F (215.6C) at its feed end to 370F ~187.8C) at the die end and the resulting extrudate, in strand form, was cooled and pelletized.

30,661-F -10-~ p ~2;~

Following the above-noted melt blending and pelletizing operation, the resulting pelletized polymer blend was processed into a blown monolayer film structure using a 6.35 cm ~2l~2 lnch) diameter single screw NRM extruder having a length to diameter (L/D) ratio of 15:1 and utilizing the following operating conditions:

Adapter Temperature = 392F (200C) Die Temperature - 392F (200C) Gate Temperature = 425F (218.3C) Zone 4 Temperature - 425F t218.3C) Zone 3 Temperature = 425F (218.3C) Zone 2 Temperature = 400F (204.4~C) Zone l Temperature = 400F (204.4C) Melt Temperature = 422.6F (217C) Screw Speed = 200 rpm Current = 10 amperes Die Pressure = 1150 psi (80.5 kg/cmZ) Haul-Off Rate = 21 feet per minute (6.3 met) Cooling Air Temperature = 53.6F (12C) Layflat Width = 9 inches (23 cm) Thickness = 1.7 mils (0.0432 mm) Frostline Height = 10 inches (25.4 cm) Following its prepartion in the foregoing fashion, the resulting film was studied and tested to determine and evaluate the physical properties thereof.
The results o such testing and evaluations were as follows:

30,661-F -11-~;~2~9 Dart Impact Strengthl (grams) 308 Gardner Clarity2 (% transparency) 42.8 20 Gloss3 21.2 40 Gloss3 42.8 Haæe4 (%) 19.1 Elmendorf Tear5, Machine Direction (MD) (grams) 90 Transverse Direction (TD) (grams) 51 Tensile Strength6, MD (psi) 14,265 (999 ~g/cm2) TD (psi) 11,915 (834 kg/cm2) Tensile Yield6, MD (psi) 5,S00 ~ (385 kg/cm TD (psi) 5,070 (355 kg/cm2) Elongation6, MD (%) 430 TD (%) 410 2% Secant Modules7, MD (psi~ 105,500 (7385 kg/cm2) TD (psi) 100,900 (7063 kg/cm2) r7 Toughness', MD (lb/in3) 2,740 (75843 gm/cm3) TD (lb/in3) 2,212 (61228 gm/cm3) Oxygen Transmission, (cc-mils/- 3.20 100 in2-24 hr-30 atm) 30,661-F -12-AST~ D1003 52 6 ASTM D882, D638 Comparative Experiment An attempt was made to repeat the blown film preparation procedure of Example l using pure nylon-6 resin (Allied Chemical Company's Capron 8207F) in place of the nylon-6/EAA blend which had been employed in Example 1. Such a~tempt proved to be unsuccessful since the extruded polymer mass could not be sa~is-factorily strung up due to inadequate melt strength.

Examples 2-4 --~ The procedures of Example 1 were repeated using three different random ethylene/acrylic acid (EAA~ copolymers in place of the 9.5 weight percent acid, lO: melt index EAA copolymer which had been employed in Example l. More specifically, the polymer blend employed in Exampl`e 2 was composed of lO0 parts of Allied Chemical Company's Capron 8207F ilm extrusion grade nylon-6 resin and lO parts of a random ethylene/-acrylic acid copolymer having an acrylic acid contentof about 12 weight percent and a melt index of 0.8 decigrams per minute; the polymer blend employed in : Example 3 was composed of 100 parts of Allied's Capron 8207F nylon-6 resin and 10 parts of a random ethylene/-; 30 acrylic acid copolymer having an acrylic acid content ``` :

- 30,661-F -13-2 ~6 of about 6.5 weight percen~ and a melt index of about 2 decigrams/minute and the polymer blend employed in Example 4 was composed of lO0 parts of Allied's Capron 8207F nylon-6 resin and 10 parts of a random ethylene/-acrylic acid copolymer having an acrylic acid content o~ about 9.5 weight percent and a melt index Qf 2 decigrams/minute.

The properties of the three resulting monolayer blown film structures were as set forth below.

Example 2 Example 3 Example 4 Dart Impact1 (grams) 524 773 844 Gardner Clarity2 9.1 45.9 55.7 (% transparency) 15 20 Gloss3 804 29.4 46.9 40 Gloss3 24.7 45.9 50.5 Haze (~) 29.5 21.6 19.4 Elmendorf Tear5, Machine Direction32 70.4 60.8 (MD) (grams) Transverse Direction 64 76.8 70.4 (TD) (grams) Tensile Strength6 MD kg/cm2 (psi)1,031 909 1,009 ~5 (14,735) (12,990)(14,415) TD kg/cm2 ~psi)978 910 937 (13,970) (13,000)-(13,390) ~ensile Yield6 MD kg/cm2 (psi)420 463 476 (6,005) (6,615) (6,795) TD kg/cm2 (psi)363) 467 460 (5,1~5) ~6,670) (6,565) 30,661-F -14-.i ~2~
-15~

Exam~le 2 Example 3 Fxample 4 Elongation6, MD (%) 440 400 420 TD (%) 410 410 400 2% Secant Modulus 5MD kg/cm2 (psi) 7,994 (114,200) N.D.* N.D.*
TD kg/cm2 (psi) 8,043 : (114,900) N.D.* N.D.*
Toughness7, MD kg/cm379,829 68,840 74,127 10(lb/in3) (2,884) ~2,487) (2,678) TD kg/cm3 72,106 68,619 66,017 ~lb/in3) (2,605) (2,479) (2,385) Oxygen Transmission 3.00 ~.D.* N.D.*
(cc-mils/100 in2 24 hr atm) * N.D. = Not Determined 1 ASTM D1709-67;
2 ASTM D1746;
ASTM D2457;
4 ASTM D1003-52;
5 ASTM D1922;
ASTM D882, D638 While the subject mat-ter hereof has been described by reference to certain specific embodiments and examples such fact is not to be interpreted as in any way limiting the scope of the presently claimed invention.

30,661-F -15-

Claims (12)

1. A process for the preparation of a biaxially oriented monolayer polyamide film structure comprising the steps of intimately admixing from 1 to 50 parts by weight of a random ethylene/ethylenically unsaturated carboxylic acid copolymer with from 50 to 99 parts by weight of a polyamide resin, melt blending said admixture in an extruder, and extruding the blend through a die to form the blend into a monolayer blown film, wherein the blend in the extruder is maintained at a higher temperature than the temperature of the blend at the die.

2. The process of Claim 1 wherein the random ethylene/ethylenically unsaturated carboxylic acid copolymer is derived from the addition polymerization of a monomer mixture comprising from 65 to 99 weight percent of ethylene and from 1 to 35 weight percent of an ethylenically unsaturated carboxylic acid monomer.

3. The process of Claim 1 wherein the random ethylene/ethylenically unsaturated carboxylic acid copolymer has a melt index of from 0.5 to 10 decigrams/minute as determined pursuant to ASTM D 1238, Condition E.

4. The process of Claim 1, 2 or 3 wherein the polyamide resin is selected from nylon-6, nylon-66, nylon-610, nylon-11 and nylon-12.

5. The process of Claim 1 wherein the polyamide constitutes from 70 to 95 weight percent of the polyamide--ethylene/ethylenically unsaturated carboxylic acid copolymer blend and wherein the ethylene/ethylenically unsaturated carboxylic acid copolymer constitutes from 5 to 30 weight percent of said blend.

6. The process of Claim 1 wherein the polyamide resin and the ethylene/ethylenically unsaturated carboxylic acid copolymer are melt preblended in a separate extrusion operation conducted prior to the blown film extrusion operation.

7. The process of Claim 6 wherein the separate melt preblending extrusion operation includes the steps of solidification and pelletization of the polyamide--ethylene/ethylenically unsaturated carboxylic acid copolymer blend.

8. The process of Claim 1 wherein the extruder is operated with a temperature profile along the barrel length which gradually decreases from a relatively higher temperature at its feed end to a relatively lower temperature at the die end thereof.

9. The process of Claim 1 wherein the blown film manufacturing equipment employed is of a type which is conventionally employed for the manufacture of blown films from low density polyethylene resins and wherein the blown film manufacturing operation is conducted such that the frost line height of the polymer film bubble is less than 76.2 cm (30 inches) from the extruder die.

10. The process of Claim 9 wherein the frost line height is less than 38.1 cm (15 inches).

11. The process of Claim 1 wherein a chilled gaseous cooling medium is employed to cool the film bubble as it exits the extruder die.

12. The process of Claim 11 wherein the chilled gaseous cooling medium is air at a temperature of less than 25°C.