CA2015153C

Double bubble process for making strong, thin films

Abstract

Polymeric, thin oriented films can be made by use of a combination of a hot blown process and a blown bubble process, i.e. a double bubble process. The resulting film has use in replacing PVC for in store stretch wrap applications. Very low density polyethylene, VLDPE, is an especially preferred material for this process. It may be used as a monolayer, or as one layer of a multilayer structure. In practicing the invention, the polymer is extruded and hot blown, and heated to a temperature above its orientation temperature. This heating can be accomplished by the use of a heated liquid reservoir or sock disposed at the lower end of the primary bubble, inside the bubble. The hot blown heated film is then passed through a first set of pinch rolls, re-inflated into a blown bubble, and collapsed at a second set of pinch rolls. Thin, tough and elastic packaging materials are obtained by this process.

CA2015153C, drawing sheet 1 — Sheet 1 of 103

Term

No projected expiry on record.

6 claims: 2 independent, 4 dependent

1
THE EMBODIMENTS OF THE INVENTION IN WHICH AN EXCLUSIVE PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:I. A method of making a thin oriented polymeric film comprising: a) extruding the polymer as a melt stream through a tubular die;b) hot blowing the extruded film downward to a first set of pinch rolls, the film forming a primary bubble;c) passing the hot blown film in contact with a heated liquid medium located in a reservoir disposed at a lower end of the primary bubble;d) heating the hot blown film to a temperature above its orientation temperature;e) directing the heated film downward through a first set of pinch rolls;f) reinflating the hot blown film below said first set of pinch rolls by a blown bubble process;and g) collapsing the reinflated film through a second set of pinch rolls.
2
The method of claim 1 wherein the extruded film is hot blown at a blow-up ratio of between about 1.5:1 and 3:1.

Independent claims2

742 paragraphs in 86 sections, as filed

Double Bubble Process for Making Strong, Thin Films

Background of the Invention

The present invention pertains to packaging film, and more particularly to a thin polymeric film suitable for replacing polyvinyl chloride film especially in packaging applications.

Polyvinyl chloride (PVC) has long been used in many applications in the packaging art. One particularly widespread application for PVC is the use of such material as an overwrap material for trayed retail cuts of meat and other food products in a retail environment.

PVC has several desirable properties for this use. For example, it has excellent optics and good elasticity and stretch properties at use temperatures.

Unfortunately, PVC also has several disadvantages, including the production of hydrogen chloride gas during heat sealing and the generally corrosive effects of such gases in the packaging room.

It would be of great benefit to the packaging industry, and particular to applications requiring an instore film for overwrapping trayed food products, to provide a film with many of the advantages of PVC but without the disadvantages described above.

4/900406.4/SPECFLDR/10:51:49 AM/04/06/90

Applicant has discovered that a relatively thin polymeric film, preferably a polyolefin, and more preferably very low density polyethylene (VLDPE), produced by hot blowing and then stretch orienting the extruded film, exhibits excellent elasticity, toughness, stretch and optical properties.

The U.S. Patent No. 3,456,044 (Pahlke) mentions thin films of thicknesses less than 1 mil such as 0.5 mils, and discloses a double bubble method for biaxially orienting thermoplastic films including the steps of producing a primary 10 tubing which is inflated by introducing air into the interior thereof, and a cooling ring 22, as well as squeeze rolls 34 and 28, with rolls 34 having a greater speed than rolls 28. Between the two pairs of squeeze rolls is a reinflated secondary bubble. If annealing is desired, the tubing can be reinflated to form a bubble 70.

U.S. Patent No. 3,555,604 (Pahlke) is a patent based on a divisional application which was derived from the same priority application as the '044 patent described above, and discloses the same information described above for the '044 20 patent.

Summary of the Invention

According to one aspect of the present invention there is provided a method of making a thin oriented polymeric film comprising: a)extruding the polymer as a melt stream through a tubular die; b) hot blowing the extruded film downward to a first set of pinch rolls, the film forming a primary bubble;

c) passing the hot blown film in contact with a heated liquid medium located in a reservoir disposed at a lower end of the primary bubble; d) heating the hot blown film to a temperature above its orientation temperature; e) directing the heated film downward through a first set of pinch rolls; f) reinflating the hot blown film below said first set of pinch rolls by a blown bubble process; and g) collapsing the reinflated film through a 10 second set of pinch rolls.

Definitions

The term polyolefin is used herein in its stricter sense to mean a thermoplastic polymer derived from simple olefins. Among these are polyethylene, polypropylene and copolymers thereof with olefinic comonomers. For example, very low density polyethylene may be considered a linear ethylene copolymer with a comonomer comprising such materials as butene, hexene or octene. The term polyolefin is also used herein in a broader sense to include copolymers of ethylene with comonomers that are not themselves olefins,

such as vinyl acetate (e.g. ethylene vinyl acetate copolymer or EVA).

The term ’’very low density polyethylene” r or VLDPE is used herein to describe linear ethylene alphaolefin. copolymer having densities of generally between about 0.890 and 0.915 grams/cubic centimeterr and produced by a catalytic, low pressure process.

The term ethylene vinyl acetate copolymer (EVA) as used herein refers to a copolymer formed from ethylene and vinyl acetate monomers wherein the ethylene derived units are present in major amounts and the vinyl acetate derived units are present in minor amounts, generally one to 30 percent by weight.

Brief Description of the Drawings

The invention may be further understood by reference to the drawings herein, where:

FIG. 1 is a schematic diagram indicating the apparatus and process by which the film of the present invention is made; and

FIG. 2 is a graph showing the relationship between tensile force applied to a film, and elongation, for different types of films including the double bubble film of the present invention.

Description of the Preferred Embodiments

Figure 1 shows schematically a device 10 for making the thin films of the present invention.

4/900406.4/SPECFLDR/10:51:49 AM/04/06/90

A melt stream of a polymeric material, preferably a material such as VLDPE is extruded through an extruder (not shown) and exits through a die 12 in a conventional manner. The extruded film is hot blown by conventional techniques to form a blown bubble 14.

Air cooling ring 16 positioned circumferentially around the blown bubble at the position shown cools the thermoplastic melt as it exits die 12.

An optional auxiliary chilling ring 17 may also be positioned circumferentially around the blown bubble down stream from air cooling ring 16 to further chill the hot blown film.

The primary bubble 14 is melt oriented in both the machine and transverse directions. Various blow up ratios may be used, but preferably the primary bubble 14 is hot blown to a blow up ratio of between 1.5 and 3.0.

The primary bubble 14 is collapsed at pinch rolls 16.

To assist in this process, guide plates 18 are positioned at the extremities of the blown bubble 14.

The collapsed bubble is then reinflated in a blown bubble process to stretch orient the blown and collapsed film. This is done in a conventional manner by trapping air or other hot gas within the secondary bubble 20 so that the material stretches at its orientation temperature transversely to impart further orientation of the material in the transverse direction. The secondary bubble 20 is collapsed at a second set of pinch rolls 22. A second set of guide plates 24 may be employed to assist in the collapsing process.

The second set of pinch rolls 22 is rotated at a speed faster than the first set of pinch rolls 16 to impart

4/900406.4/SPECFLDR/10:51:49 ΆΜ/04/06/90 stretch orientation in the machine or longitudinal· direction to the thermoplastic material.

<td> The</td><td> recollapsed</td><td> bubble 20</td><td> then</td><td> passes from</td><td> the</td>

<td> second set of</td><td colspan="2"> pinch rolls 22 to take up</td><td> roll</td><td> 26.</td><td></td>

<td> The</td><td> take up roll</td><td> 26 may be a</td><td> mill</td><td> log which can</td><td> be</td>

immediately stored or shipped to a distributor or customer, or may be stored for further processing such as slitting into single wound film, machine or natural center fold film. Thus, as used herein the take up roll 26 represents any further processing, storage, or further modification of the double wound, collapsed film once it exits the second set of pinch rolls 22, and is used herein to denote any of these possible further processing steps.

When using very low density polyethylene, it was noticed that some thickened edges of the film resulted from this process. To correct this deficiency, it is preferred that a reservoir 28 of heated fluid be disposed at the lower end of primary bubble 14 in such a way that the collapsing material drawn through the primary set of pinch rolls 16 will pass in communication with the heated fluid. In this manner, the film is more uniformly heated and temperature control can be achieved. Thickened tape edges can be substantially avoided by such means.

Although the heated fluid of reservoir 28 is preferably hot water, other media may be used if temperatures above the 212°F limit of hot water are desired. For example propylene glycol ( a food approved material), hot oil or hot emulsions may be used. One skilled in the art will understand that the exact nature of the heated fluid is not as critical as its effectiveness in helping to uniformly heat the collapsing bubble 14 as it is drawn through pinch rolls 16, and to uniformly heat the collapsing bubble 14 to a temperature above its orientation temperature.

4/900406.4/SPECFLDR/10:51:49 ΆΜ/04/06/90

The heated fluid may also be an active substance which not only reheats the surrounding film, but also actually coats the interior of the bubble as it passes over the reservoir. An example is a hot wax or other functional coating.

The heated fluid may be recirculated from the reservoir through a heating means 30 by means of conduits 32 or other suitable transfer means. Using the reservoir 28 of heated fluid, the types of materials which may be effectively used in the present process and device are increased. These materials fall generally into three classes.

The first class consists of crystalline polymers which can be quenched to the amorphous state by either air or an external cooling mandrel of the types depicted schematically at 16 and 17 of Figure 1. Examples of such materials are polyethylene terephthalate, saran, and polypropylene. In the case of polyethylene terephthalate and saran, hot water is a suitable liquid medium for use in reservoir 28. In the case of polypropylene, a higher temperature liquid medium is preferred.

A second class of materials suitable for the present process are amorphous polymers such as polyethylene terephthalate glycol (PETG), polystyrene, and polycarbonate. In the case of PETG, hot water is a suitable liquid medium for reservoir 28. Higher temperature liquid media are preferred for polystyrene and polycarbonate.

A third class of materials which can be used with the present process are crystalline polymers which are not quenched amorphous by using air or external mandrel means. An example is high density polyethylene. In this case, a temperature of at least about 240°F for the medium of reservoir 28 is required to melt out most of the crystalline structure of HOPE material.

4/900406.4/SPECFLDR/10:51:49 AM/04/06/90

A major advantage of this process and device of the present invention is that a variety of polyolefinic materials may be made into relatively thin, oriented, tough materials suitable for packaging applications such as in store tray overwrap. Film gauges of less than 1 mil, and preferably less than .6 mils, even more preferctbly less than .5 mils and as low as .2 mils or less are obtainable. Even films with thicknesses as low as . 1 mils or lower can be made by the practice of the present invention.

Although monolayer films are preferred, and particularly materials such as very low density polyethylene, multilayer films may also be produced. This is both technically possible and also sometimes desirable depending on the nature of the monolayer film. For example, a VLDPE available from Union Carbide and sold under the designation DFDA 1138 is a desirable material from a performance point of view. However, where materials have not yet attained food contact status, outer layers of a food approved material such as EVA may be used to sandwich the VLDPE or other core material. When more than one layer is to be used, coextrusion techniques commonly available in the art may be employed.

The invention may be further understood by reference to the following examples.

Example 1

A central melt stream of very low density polyethylene (DFDA 1138 available from Union Carbide) and outside melt streams of an EVA (Elvax 3130 available from du Pont) were coextruded through a coextrusion die and hot blown to a blow up ratio of 1.78. The hot blown film had a thickness of 2 mils. The hot blown film was collapsed at a first set of pinch rolls and then inflated between the first set of pinch rolls and a second set of pinch rolls. The secondary bubble 4/900406.4/SPECFLDR/10: 51: 49 AM/04/06/90 did not impart any substantial· transverse orientation to the film material. The machine direction orientation was increased by speeding up the second set of pinch rolls relative to the first set of pinch rolls. The speed of the first set of pinch rolls was 36 feet per minute. The speed of the second set of pinch rolls was 180 feet per minute. The result was a stable bubble with no transverse expansion and 5:1 machine direction expansion to produce a final film with a thickness of .4 mils.

Example 2

A film was produced substantially like that of Example 1, with the same conditions for the primary bubble (hot blown film). The secondary bubble was inflated from 28 inch lay flat width to 46 inch lay flat width with transverse expansion of 1.64:1.

The speed of the second set of pinch rolls was 108 feet per minute to effect a machine direction expansion of the secondary bubble of 3:1. The film collected had cold thick edges because of lack of temperature control, but the center had a gauge thickness of .20 mils.

Example 3

The .20 mil film of Example 2 was used to package cut beef in a foam tray. The film exhibited strength and stretch characteristics approaching the characteristics of .60 mil stretch PVC. Hot wire cutting was similar to the

PVC, but sealing required a heat-cool cycle to prevent the tabs from shrinking.

4/900406.4/SPECFLDR/10:51: 49 AM/04/06/90

Packages made with the film of Example 2 exhibited more elastic recovery than PVC when poked with the finger.

It should be noted that when the heated hot blown film is collapsed through nip roll 16 and expanded into secondary bubble 20, the film can be either monoaxially or biaxially stretched. Stretching in the machine direction can be from ratios of 1:1 to 9:1. In the transverse direction, stretching ratios may range from 1:1 to 5:1. Any combination of ranges within those just described is possible. For example, the film may be essentially unstretched in the machine direction (1:1) and biaxially stretched at a 3:1 ratio in the transverse direction. The reverse is also true.

Additionally, the degree of transverse direction or machine direction stretching in secondary bubble 20 is substantially independent of the blow ratio in primary bubble 14, so that many combinations of blow up ratios in the primary and secondary bubble are achievable. However, more stress (higher bubble pressure) occurs in the secondary bubble if the blow ratio in the primary bubble is reduced. Therefore, higher blow up ratios in the primary bubble will make it easier to orient a given material in the secondary bubble.

Several additional films were also produced by substantially the same process as described in Examples 1 and

A liquid reservoir or sock containing heated water, located at the lower interior portion of the hot blown primary bubble (see reference numeral 28 of Figure 1) was used to control the temperature of the hot blown film prior to re-inflation into the second bubble. More specifically, the heated water was maintained at temperatures between 183°F and 204°F to raise the temperature of the hot blown film to above its orientation temperature.

4/900406.4/SPECFLDR/10: 51: 49 AM/04/06/90

It has been found that the liquid reservoir not only brings the temperature of the hot blown film up to its orientation temperature, but also equilibrates the temperature of the film around the circumference of the bubble. This in turn provides for better control of the final film gauge, and in particular reduces the incidence of thickened edges in the final film.

In Table 2, a list of the film structures produced, and the blow up ratios in the primary and secondary bubble are listed. The thickness of the final film, and temperature of the heated water inside the reservoir are also listed.

Table 1 describes materials utilized in Examples

3-17:

4/900406.4/SPECFLDR/10: 51: 49 AM/04/06/90

TABLE 1

RESIN

EVAX

EVA2 eva3

COMMERCIAL NAME

ELVAX 3130

32.89

9653

DESCRIPTION

EVA12% VA

MELT INDEX =

2.5 grams/ min.

EVA4%VA

MELT INDEX = grams/ min.

EVA12%VA ( including antifog additive)

COMPANY

DU PONT

EXXON

DU PONT

VLDPEx vldpe2

VLDPE3 vldpe4 vldpe5

<td> DFDA 1138</td><td> .900 grams/cc MELT INDEX = 0.4 grams/ 10 min.</td><td> UNION CARBIDE</td>

<td> 1121</td><td> DENSITY = .900 grams/cc MELT INDEX = 0.4 grams/ 10 min. (ANTIFOG VERSION OF DFDA 1138)</td><td> UNION CARBIDE</td>

<td> 4003</td><td> DENSITY = .905 grams/cc MELT INDEX = .8 grams/10 min.</td><td> DOW</td>

<td> XUR 1567 41225-18K</td><td> DENSITY = .900 grams/cc MELT INDEX = .8 grams/10 min.</td><td> DOW</td>

<td> DEFD 1491</td><td> DENSITY = .900 grams/cc MELT INDEX = 1.0 grams/10 min.</td><td> UNION CARBIDE</td>

4/900406

4/SPECFLDR/10: 51:49 AM/04/06/90

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All extruders were reduced to one half the rate jjf the extruders of Example 4, i.e. 41 rpm for Example 5.

2fill extruders were reduced to 60¾ of the rate of the extruders of Example 4, i.e. 50 rpm for Example 11.

3The take-off speed of the film was 59% faster than that of Example 4, i.e. 200 feet/min. for Example 14.

In Table 4, a list of other film structures produced, and the blow up ratios in the primary and secondary bubble are listed. The thickness of the final film, and temperature of the heated water inside the reservoir are also listed.

Table 3 describes materials utilized in Examples 18-50. Other materials used in Examples 18-50 are listed and described in Table 1.

4/900406.4/SPECFLDR/12:29:15 PM/04/06/90

Table 3

RESIN eva4

EVAS

EVAe

EVA7

EAAX

VLDPEe

VLDPEy

VLDPES

VLDPE9

COMMERCIAL NAME

ELVAX 3165

ELVAX 3170

DESCRIPTION

EVA18% VA

MELT INDEX = .7 grams/ min.

EVA18%VA

MELT INDEX =

2.5 grams/ min.

COMPANY

DU PONT

DUPONT

4/900406

ELVAX 3182

ELVAX 3508

EVA28%VA MELT INDEX = 3.0 grams/ 10 min.

EVA12% VA MELT INDEX = .3 grams/ 10 min.

DU PONT

DUPONT

PRIMACORE 1410

FW 1990

30S

OR

30Q

EAA9.5% AA

DENSITY = .900 grams/cc MELT INDEX = .8 grams/ 10 min.

DENSITY = .901 grams/cc

MELT INDEX = .8 GRAMS/ 10 min.

DENSITY = .902 grams/cc

MELT INDEX = .6 grams/ min.

DENSITY = .895 grams/cc

MELT INDEX = .42 grams/ 10 min.

DOW

NORSOLOR

DOW

4/SPECFLDR/12: 25: 30 PM/04/06/90

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Notes to Table 4

Die slough problem (new air ring) die gap .110.

5Reduced die slough. Couldn’t maintain bubble.

®No die slough, bubble life 15 min.

’Mottled coex. Secondary bubble life short.

aL. 0. film.

’Reduced die gap from .110 to .075 2 hr. bubble.

Couldn’t make .25 mil.

loChanged die gap to .040. Primary bubble terap. from die to sock 300, 173, 160, 186 - Still unstable orientation. Changed to Johnson air ring.

xlDie gap = .075. Primary bubble terap. from die to sock 279, 188, 138, 191. Secondary bubble gauge = ,2 - .6.

’^Adjusted Gauge: Secondary: .35-.5

Primary: .16-.27

Primary bubble gauge off-balanced to achieve better gauge. Probably due to skin layer thickness variations orienting differently.

13Turned off chiller causing primary bubble to widen.

i4Chilled air - Johnson air ring.

15Some incompatibility haze but ran well fewer gels causing bubble breaks.

n6Serious incompatability.

lvHard to process.

ieMade for low cost forming web.

^’Transverse orientation.

^Transverse maximum (obstruction limited).

2*Could not maintain bubble because of apparent excess primary orientation, hot blown instead.

22Amorphous clear primary bubble.

Primary bubble pulsed. Switched core to (LW2550).

Primary melt was too weak to make film.

z*Primary bubble too weak.

25Stable bubble.

3SMore stable than 41.

27Very stable (gels might have been due to EVA) 2BStable orientation, hazy film.

4/900406.4/SPECFLDR/12:37:18 PM/04/06/90 ^Progressed to hazy weak film. Melt became cheesy.

Suspected X-Hnteing in die or extruder.

3O.1% Irganox 1010 added to skins.

31Increased L. 0.

32Lower transverse & L. 0. ratio.

33Increased die from 350 to 375° F. Conclusion: Irganox

1010 reduced X-linking of skin layers.

In Table 6, a list of additional film structures produced, and a blow up ratio in the primary and secondary bubble are listed. The thickness of the final film, and temperature of the heated water inside the reservoir are also listed.

Table 5 describes materials utilized in Examples 51 through 76. Other materials used in Examples 51 through 76 are listed and described in Tables 1 and 3.

4/900406.4/SPECFLDR/12:37:18 PM/04/06/90

TABLE 5

<td> RESIN</td><td> COMMERCIAL NAME</td>

<td> VLDPExo</td><td> TAFMER 0680</td>

<td> VLDPEix</td><td> DEFD 1064 NT 7</td>

<td> vldpe12</td><td> 1210</td>

<td> vldpeX3</td><td> 61509.32</td>

<td> DESCRIPTION</td><td> COMPANY</td>

<td> DENSITY = .88 grams/cc MELT INDEX = .4 grams/ 10 min.</td><td> MITSUI</td>

<td> DENSITY = .912 grams/cc MELT INDEX = 1.0 grams/ 10 min.</td><td> UNION CARBIDE</td>

<td colspan="2"> DENSITY = .89 UNION grams/cc CARBIDE Narrow Molecular Weight Distribution MELT INDEX = 1 gram/ 10 min.</td>

DENSITY = .911 DOW grams/cc

MELT INDEX = .55 grams/ min.

STYRENE BUT ADI ENE PHI LLIP S COPOLYMER

DENSITY =1.01 grams/cc

MELT INDEX = grams/ min.

4/900406.4/SPECFLDR/12:37:18 PM/04/06/90

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201515¾

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Notes For Table 6 34Primary bubble too weak.

35Better primary bubble strength but secondary was unstable.

3eCould not maintain secondary bubble.

37Better primary stability but secondary still unstable.

3aSligbtly hazy film with 20 min. bubble life.

^Primary lost some stability secondary bubble life 20 min. better clarity.

4OUp to 2 hr. bubble (blend approach promising).

412000 ft. run when pumps failed.

42Hazy film, hard to blow secondary hut stable when blown.

43L. 0. material.

44Easiar to blow than Sample 5. Stable secondary but hazy film.

4^L. 0. material.

46Stable but hazy bubble.

47Lost feed on skin layers after a short time.

4e18% VS skin layers contributed to best stability yet.

^Best and most stable process yet. No cold stretch line as in 13 & 14. Very tough primary.

5°Could only maintain 10 min. bubbles plus primary was not as tough.

51Became hazy due to EVA blend.

S2Clear monax for label trials.

The inventor has found that materials with high molecular weight and wide molecular weight distribution are preferred for the core layer of multilayer film structures in accordance with the invention. These materials, particularly VLDPE, are also characterized by low crystallinity at processing temperatures.

4/900406.4/SPECFLDR/12:57:07 PM/04/06/90

It has also been found that high vinyl acetate EVA resins i.e. 18% and higher, are preferred for use in the outer layers of multilayer films of the present invention. These higher vinyl acetate EVA resins provide a wider sealing range for the final film when used in in-store overwrap applications on conventional manual and automatic equipment.

Although the invention has been described with respect to specific embodiments, those skilled in the art will understand that suitable modifications and changes may be made without departing from the spirit and scope of the invention as defined below.

For example, the oriented film produced by the process of the present invention has a relatively high free shrink and shrink force. At 185°F, a typical free shrink value for the film of the present invention is 50%. In end-use applications where it is desirable to reduce the amount of free shrink or shrink force or shrink tension in the film, the material exiting the secondary bubble may be annealed or heat set by means of a tertiary bubble. This bubble may be characterized as one of intermediate pressure, compared with the relatively high pressure secondary bubble, and the relatively low pressure primary bubble.

Films produced by the present double bubble process can be graphically characterized as shown in Fig.2. Because of the nature of the process, a thin film is produced that has excellent memory combined with good elongation. This combination of properties compares favorably with conventionally oriented film,which has good memory but poor elongation properties. The present film also compares favorably with conventional hot blown films which exhibit good elongation but poor memory.

4/900406.4/SPECFLDR/12: 49 :11 PM/04/06/90

Contents86

37 members in 20 offices

This recordMember, by publication datePriority claim10 more offices are in the list below

Priority claims10

Priority claims
Document	Office	Kind	Date
387056	United States of America	–	1989-07-28
38705689	United States of America	A	1989-07-28
38705689	United States of America	A	1989-07-28
494699	United States of America	–	1990-03-16
49469990	United States of America	A	1990-03-16
49469990	United States of America	A	1990-03-16
387056	–	–	–
494699	–	–	–
US19890387056	–	–	–
US19900494699	–	–	–

Members37

Family members, oldest first
Document	Office	Kind
CA2015153A1	Canada	A1	1991-01-28
EP0410792A2	European Patent Office (EPO)	A2	1991-01-30
AU5980690A	Australia	A	1991-01-31
CN1049311A	China	A	1991-02-20
KR910002582A	Republic of Korea	A	1991-02-25
JPH0369337A	Japan	A	1991-03-25
ZA905441B	South Africa	B	1991-04-24
IL95016A0	Israel	A0	1991-06-10
IL95016D0	Israel	D0	1991-06-10
BR9003666A	Brazil	A	1991-08-27
EP0410792A3	European Patent Office (EPO)	A3	1992-03-11
AU643691B2	Australia	B2	1993-11-25
AU4752693A	Australia	A	1993-12-09
AU4752793A	Australia	A	1993-12-09
US5298202A	United States of America	A	1994-03-29
NZ234429A	New Zealand	A	1994-05-26
AU652519B2	Australia	B2	1994-08-25
AU658330B2	Australia	B2	1995-04-06
EP0410792B1	European Patent Office (EPO)	B1	1995-04-12
AT121008T	Austria	T	1995-04-15
ATE121008T1	Austria	T1	1995-04-15
DE69018537D1	Germany	D1	1995-05-18
ES2071027T3	Spain	T3	1995-06-16
DK0410792T3	Denmark	T3	1995-07-03
AR248235A1	Argentina	A1	1995-07-12
DE69018537T2	Germany	T2	1995-08-17
MY107124A	Malaysia	A	1995-09-30
US5456979A	United States of America	A	1995-10-10
IL95016A	Israel	A	1995-12-31
HK1996A	Hong Kong, China	A	1996-01-12
US5674607A	United States of America	A	1997-10-07
US5674608A	United States of America	A	1997-10-07
PH31570A	Philippines	A	1998-11-03
JP2862648B2	Japan	B2	1999-03-03
KR0180533B1	Republic of Korea	B1	1999-05-15
CA2015153CThis record	Canada	C	2000-07-18
MXPA95005376A	Mexico	A	2004-08-18

2 legal events, as the office reported them to INPADOC

Over the term

Point at a mark for the event

Events

Legal events, newest first
	Event	Code
2004-04-23	LapsedLapsedMKLA	MKLA
1997-01-23	Examination requestEEER	EEER