CA2215204A1 - Process for preparing polyvinylbutyral sheet - Google Patents

Abstract

This invention discloses a process for preparing PVB sheeting having a desired uniform adhesivity for glass lamination interlayer applications. The process for preparing PVB sheeting comprises preparing a blend of polyvinylbutyral and a compatible quantity of at least one plasticizer and an adhesion control agent, and extruding the blend to form a sheet. The improvement comprises monitoring the acidity of the sheet and adding water in the sheet forming process as an agent for controlling the acidity and resultant adhesivity of the sheet.

Description

CA 0221~204 1997-09-11 WO 96/28504 PCT/US9.,~971 TITLE
PROCESS FOR PREPARING POLYVINYLBUI YRAL SHEET

~ACKGROUND OF THE INVENTION
This invention relates to a process of m~mlf~ct~lre of polyvinylbutyral (PVB) sheeting having a desired ullirO, . 1l adhesivity for use in l~min~ted safety glass. More particularly, it relates to a process for monitoring the properties and controlling the uniformity of PVB sheeting, in particular the acidity of the sheet and adding water to control the resultant adhesivity of the sheet to glass.
The most widely used vehicle windshield is a three-ply l~min~te comprising an energy absorbing plastic sheet sandwiched between two glass sheets. Such windshields are capable of absorbing a blow from the head of an occupant with resistance to penetration and shattering. In so doing, the windshields dissipate a substantial amount of impact energy as they undergo plastic deformation.
Polyvinylbutyral resins are capable of being cast or preferably extruded by processes analogous to those used to compound and extrude thermoplastics. Although it is possible to form a plastic sheet directly from polyvinylbutyral resins, the glass transition temperature of appr-xim~tely 70~C

2 o for PVB resin is too high for l~min~ted glass application. Plasticizer is mixed with PVB resin to lower the glass transition temperature to near 25~ C. In the process to form the sheeting film from its molten state, temperatures must be high enough to obtain processable film forming melt viscosities and intimate mixing of the PVB resin and plasticizer.
2 5 Plasticizer is typically a large fraction of the final sheet composition.
In PVB sheeting, for example, plasticizers contribute 15% to 50% of the film weight, typically 25% to 30%. Choice of plasticizer is limited to materials thatare low in volatility, chemically stable under processing conditions, and compatible with the particular acetal resin selected. Diester plasticizers having 3 o from 16 to 28 carbon atoms are preferred, and plasticizers based on difunctional acids as well as glycols are also used. Commercially available plasticizers and their compatibility with polyvinylbutyral resin are listed in Modern Plastics Encyclopedia 1994-95, Vol. 71, No. 12, pp. C-99 to C-109. Examples of suitable plasticizers include esters of aliphatic diols with aliphatic carboxylic acids, in 3 5 particular the esters of di-, tri- and tetraethylene glycol with aliphatic carboxylic acids having 6 to 10 carbon atoms, e.g., triethylene glycol di-(2-ethyl-butyrate), triethylene glycol di-n-heptanoate, or tetraethylene glycol di-n-heptanoate. Also suitable are esters or mixed esters of dicarboxylic acids, preferably adipic, sebasic or phthalic acid with aliphatic alcohols or mixed alcohols. For example, CA 0221~204 1997-09-11 di-n-hexyl adipate, 2-ethylhexyl cyclohexyl adipate, dibu~l phth~l~te7 butyl ben~yl phthz~l~te, or hexylphth~l~te- Also, polymeric propylene oxide oligimers,as disclosed in U.S. Pat. No. 4,335,036, can be used as polyvinylbutyral -plasticizers.
Plasticizers are hydrolyzable to various degrees during m~mlfacturing processes for PVB sheeting. Ester-based plasticizers react with water to break down into alcohols and acids. The adhesivity of PVB sheeting is directly proportional to its acidity. In order to be suitable for use in glazing applications, including automobile win~l~hielt1s and architectural glass, PVB sheeting requires 0 controlled, uniform adhesivity. Heretofore, the acidity has been controlled by the use of additives of the type described in U.S. Pat. No. 4,292,372.

SUMMARY OF THE INVENTION
This invention discloses a process for preparing PVB sheeting having a desired uniform adhesivity for glass l~min~tion interlayer applications. The process for preparing PVB sheeting comprises preparing a blend of polyvinylbutyral and a compatible quantity of at least one plasticizer and an adhesion control agent, and extruding the blend to form a sheet. The improvement comprises monitoring the acidity of the sheet and adding water in 2 o the sheet forming process as an agent for controlling the resultant adhesivity of the sheet. Water is added before any substantial blending of the polyvinylbutyral and plasticizer occurs. In a preferred embodiment the plasticized composition comprises PVB which has a hydroxyl content from about 15 to 30 ~o by weight, calculated as vinyl alcohol, and from about 20 to 55 ~o by weight of at least one compatible plasticizer.

BRIEF DESCRIPTION OF THE DR~WINGS
Figure 1 is a process flow diagram of the feed system to a main extrusion compounder. Figure 2 is the process flow diagram of Figure 1 3 o modified by the addition of recycle to the main extrusion compounder.

DETAILED DESCRIPTION OF THE INVENTION
The overall process for production of plasticized polyvinyl acetal sheeting consists of mechanical compounding and sheet production. As shown in 3 5 Figure 1, polyvinylbutyral resin, plasticizer, adhesion control agent additive, and importantly, water are fed to a main extrusion compounder to form a blend. The extrusion equipment selected and feed rates for the blend will establish the general process conditions used in the extrusion process. The extruded blend exits the main extrusion compounder and is fed to the sheet production process.

CA 022l~204 l997-09-ll WO 96/28504 PCT/~JS9S/02971 Acidity tests are performed on the sheet product and the acidity test results are used to set a water flow control regulator, which in turn regulates the flow of water into the main extrusion compounder.
An alternative embo-liment as shown in Figure 2, is the addition of ~ 5 recycle to the main extrusion compounder. PVB classified as recycle is fed to a satellite mechanical compounder, and subsequently fed to the main extrusion compounder.
The water addition and vapor extraction control system consists of both a means for injecting liquid water directly into the main extrusion 0 compounder at a locus close to the fresh PVB resin feed, and a steam vaporvacuum vent downstream in the main extrusion compounder. Liquid water, preferably purified, distilled, and demineralized, is injected into the main extrusion compounder upstream of the molten recycle addition point, preferably at a point of resin plasticization in the main compounder and as close as possible to the primary PVB resin inlet feed port into the main plasticizing extruder, but without interfering with solids feeding due to steam generation and backflow into the flake inlet port. By accurately measuring the acidity via chemiluminescent titration at a locus downstream of the discharge from the main plasticizing extruder, the concentration of water added is adjusted relative 2 o to the inlet feed streams. A concentration of water is m~int~ined within a range of 0.5 to 5 weight percent based on total plasticizer and polyvinylbutyral in order to control the acidity and resultant adhesivity.
Residual water is controlled by a vacuum vent operating at high vacuum below ambient pressure. Due to the increased load from the addition of 2 5 water, the vapor extraction system must be particularly reliable to ensure the desired water content, which, if too high may cause bubbling of the final sheet product. Preferrably, vent port devices for the main compounding extruder should be equipped with mechanically wiped surfaces to remove buildups of solids entrained in the extracted vapor.
3 o In principle, a variety of satellite extruder systems close coupled to a controlled speed gear pump can be used to inject molten PVB recycle resin into the main extrusion compounding device. The satellite recycle extruder can be of any suitable design including single or multiple screws. The recycle web feed stock can be chopped or gr~n~ ted. Any suitable control system can be 3 5 used to maintain substantially uniform pressure inlet to the recycle gear pump, which can be operated at any substantially constant speed, and thus output, to set the recycle ratio. Re-melting is accomplished at low temperatures and low screw speeds to prevent plasticizer, or polymer, degradation and assist adhesion chemistry control in the main extrusion compounder.

CA 0221~204 1997-09-11 WO 96/28~04 PCT/US95/02971 Preferably, a single screw extruder with pin-barrel, such as model GE-lSOKS mz~nllf~ctured by Berstorff, may be employed as a satellite feed extruder for full web re-l~m~tion of visco-elastic plasticized polyvinylbutyral sheet, film or trim. Adding recycle makes it possible to drop the main screw 5 speed significantly and l..i.~i...i,es acidity generation irl the main extrusion compounder.
The pin barrel extruder outlet is close-coupled to, and uses pressure control at, the recycle gear pump inlet which controls the speed of thepin barrel extruder screw to compensate for recycle width fluctuations while 0 filling its gear pump teeth completely. Speed of recycle gear pump, discharging directly into the main extrusion compounder, is preferrably m~in~ined constant to provide a timewise unirollll recycle concentration and melt temperature in the main extrusion compounder, while benefiting its rate of thermal energy input.
The satellite recycle system injects molten recycle directly into the extrusion 5 process at some optimal locus upstream of the film formation component, and preferably into a middle barrel locus of the main extrusion compounder and downstream of the main resin fresh feed inlet.
Flake granules of one or more PVB resins, preferably with moisture content in the range of 0.5 to 3 weight percent water, are fed into the2 o main extrusion compounder by a system of silos, process vessels and gravimetric feeders. The main extrusion compounder is preferably equipped with intermeshin~ twin screws and volatiles extraction capability.
A high throughput process yields the m~ximllm rate of heat energy input to barrel zones near the polyvinylbutyral resin feed. The main extrusion 2 5 compounder screws are preferrably configured to accomplish partial polyvinylbutyral fusion before plasticizer addition. Location of the plasticizerinjection in important; there is an o~Lilllulll position for its addition. Preferrably, plasticizer is injected at a distance of 5 to 13 screw diameters downstream fromthe upstream edge of the polyvinylbutyral feed throat. If the plasticizer is 3 o injected too far downstream, high yellowness and discharge melt temperature surging occurs. If the plasticizer is injected too close to the first screw working element or isolation stage, plasticizer can back up into the primary feed barrelinlet and cause pluggage.
Other additives may be fed in minor quantities to the main 35 extrusion compounder as a~llro~3liate to adjust glass adhesion, see U.S. Pat. No.
4,292,372, and color. Antioxidants, ultraviolet absorbers and stabilizers may beused to prevent deterioration of the plasticized PVB interlayer of a l~min~te, see U.S. Pat. No. 5,190,826. In providing a desired adhesivity, water and adhesion control agents such as alkali or alkaline earth metal formates, alkali or alkaline CA 022l~204 l997-09-ll earth metal acetates, or the metal carboxylates of m~gneSillm, calcium, or zinc are used. Addition of such additives to the main extrusion compounder as close as possible to the main resin feed inlet is preferred, consistent with vapor control. Adhesion control agents, antioxidants, ultraviolet absorbers and ~ 5 stabilizers, and other additives may be dissolved in aqueous or organic mediums, such as alcohol or preferably, into a liquid plasticizer.
pigment~ or colorants may be added to PVB interlayer for tinting or solar control use. Any suitable method for ~lepa,illg ul~irollllly colored interlayer tints may be used. A combination of colorants and/or pigments may 0 be dispersed as concentrates and added directly to the main extrusion compounder or mixed with the plasticizer prior to injecting the plasticizer intothe main extrusion compounder.
The extruded blend from the main extrusion compounder is formed into sheeting by processes known in the art for sheet production, e.g. pressure generation, melt filtration, film formation, sheet quenching, sheet conditioning, sheet cooling and roll or film pack~ging Pressure generation is preferrably provided by close-coupling the main extrusion compounder to a high capacity polymer melt gear pump. The gear pump has associated inlet pressure and speed controls. The gear pump 2 o inlet pressure is set at the minimllm level needed for filling the gear pump teeth uniformly, and avoiding high melt temperatures at the high-pressure gear pump outlet. Fluctuations in gear pump inlet pressure are further controlled, which minimi7es variations in the melt temperature rise across the gear pump. When the main extrusion compounder, its feed system, and its screw are properly 2 5 configured for mixing the blend, the gear pump inlet pressure is substantially free of surging and is controllable by small changes to the main extrusion compounder screw speed and to the melt gear pump speed.
Optionally, this process may be economically expanded by adding or combining in parallel one or more substantially similar extrusion plastization 3 o or recycle processes at any locus upstream of a common film forming or coextrusion die. Two or more similar melt streams may be combined in a die tool or flow layering device upstream of a die tool for preparing coextruded , multiple layer sheeting. Additionally, static melt mixers may be provided upstream of the die inlet duct to elimin~te differences between the sources of 3 5 molten plasticized resin or may be used in this invention to improve uniformity of film formation.
Penetration resistance of glass l~min~tçs is important for suitability as windscreens, and depends on the adhesivity of the PVB interlayer to glass for a particular interlayer thickness. Good windscreen impact - -CA 0221~204 1997-09-11 performance and penetration resistance is attained at co~ ressive shear strengths of 5,500 to 18,000 kPa (800 to 2600 psi) on l~min~ted windscreens fromcommercial l~min~ting operations using glass washed with process water, as described in U.S. Pat. No. 4,292,372. If adhesivity measured by compressive shear strength is too high, penetration resistance observed as mean break heightis reduced and not optimal. If adhesivity is too low, resi~t~nce to penetration is higher but del~min~tion can occur at very low ~lhe~ion. A controlled and uniform interlayer adhesivity to glass is needed for suitable use in l~min~ting windscreens and architectural gl~7ing lo Samples of windscreen l~min~tes from commercial l~min~ting operations using as-produced glass washed with process water can be tested as described in U.S. Pat. No. 4,292,372. For each test, typically five or more square or circular specimens with nominal area of 645 mm2 (1.0 sc~uare inch) are cut and tested for compressive shear strength. The area of each specimen is measured to the nearest 0.6 mm2 (0.001 square inch) from linear dimensions.
After conditioning, each specimen is held at a 45~ angle to a supporting table in a compression testing mzlchine and a compressive force is applied to shear the sample at the rate of 2.5 mm (0.1 inch) per minute. The force required to break the bond between the glass and the interlayer is recorded. The commercial 2 o "windscreen compressive shear strength" is calculated in units of pressure per unit area of l~min~te tested, as an average of results accoldillg to the formula:

Force required to break bond Windscreen compressive shear strength =
Windscreen area to O.lYo accuracy However for process and quality control, adhesivity of the PVB
interlayer to glass is measured under controlled laboratory conditions using standard glass washed with demineralized water. Adhesivity is measured in the 3 o "demin compressive shear strength" described herein below. The windscreen adhesion index typically has a value of about 0.6, depending on particular windscreen laminating and glass washing conditions, where this ratio is defined by the formula:

3 5 Windscreen compressive shear strength Windscreen adhesion index =
Demin compressive shear strength CA 022l~204 lss7-os-wo 96/28504 PCT/USg5l02971 In general, good impact performance in windscreen mz~mlfacture is attained at demin compressive shear strengths of 9,600 to 30,300 kPa (1400 psi to 4400 psi) using laboratory l~min~tes wherein glass is washed with demineralized water.
potzlc~ m concentration was determined by x-ray fluorescence spectroscopy of the sheet. In detelll~in~llg acidity, shear strength, and yellowness, the following tests and procedures were used:
Acidity Concentration Analysis: A 4.000 g sample ( + /-0.05 g) of PV~, sheeting is dissolved in 100 ml of benz,vl alcohol at 75~ C ( + /-5~ C) andcooled to ambient temperature. Lucigenin (the term of art for Bis-N-methylacridinium nitrate) indicator solution in methanol is added along with 30%aqueous hydrogen peroxide. A blue-green chemiluminescence is generated under titration to alkaline conditions. A photometric detector senses this chemiluminescence and determines an end point. An automated acid-base titration and calculation is performed using standardized 0.05 N sodium hydroxide or sodium methoxide titrant solution in anhydrous methanol. The apparatus used was a fully automated computerized titration system, m~nllf~ctnred by Sanda, 4005 Gypsy Lane, Philadelphia, PA 19144 USA. Acidity concentration is calculated in units of equivalents of acid per million parts of sheet (Equiv/lE6) as 2 o gram equivalents of the primary acid from plasticizer hydrolysis per million grams, by using appropriate values for molecular weight and valence. Multiple aliquots of preheated benzyl alcohol are titrated and averaged as the blank. Titrant normality is standardized using a known solution of benzoic acid in benzyl alcohol.
Demin Compressive Shear Strength: The adhesion of interlayer 2 5 samples to glass washed with demineralized water was measured by the following procedure. Samples of interlayer were conditioned by controlled humidity to a standard water content and l~min~ted into two sheets of standard glass washed with demineralized water. For each test, six square or circular l~minzlte specimens with nominal area of 645 mm2 (1.0 square inch) are cut from 3 o PVB/glass laminate with a water cooled glass cutoff saw or circular cutter having a diamond or carborundum blade. The area of each specimen is measured to the nearest 0.6 mm2 (0.001 square inch) from linear dimensions. After conditioning, each specimen is held at a 45~ angle to a supporting table in a compression testing machine and a compressive force is applied to shear the sample at the rate of 2.5 mm (0.1 inch) per minute. After conditioning l~min:~tes at ambient temperature and controlled humidity, the force required to break the bond between the laboratory washed glass and the interlayer is recorded and the "demin compressive shear strength" is calculated for specimens using "demin" or demineralized water--washed glass by reporting an average for individual results obtained according to the formula:

Force required to break bond Demin compressive shearstrength =
Lab sample area to 0.1~o accuracy Yellowness Index Test: Yellowness of PVB interlayer is measured on transparent molded disks of interlayer 1 cm thick, having smooth polymeric 0 surfaces which are essentially plane and parallel. The index is measured according to ASTM method D 1925, "Standard Test Method for Yellowness Index of Plastics" from spectrophotometric light transmittance in the visible spectrum.
Values are corrected to 1 cm thickness using measured specimen thickness.
The present invention is further illustrated by the following specific examples, in which parts and percentages are by weight unless otherwise indicated, and in which SI units are used (inch-pound units are converted to SI
units as so indicated):

2 o PVB interlayer sheeting was produced using an extrusion plasticization process of this invention by compounding a mixture consisting of 100 parts of dry polyvinylbutyral resin, having a moisture content of less than 2 Ycwater and a residual vinyl alcohol concentration of 235~ (ASTM D 1396), with 37.4 parts tetraethylene glycol di-n-heptanoate (4G7) plasticizer and 30% of total 2 5 rate as recycle sheet stock returning from a previous similar extrusion. The main extrusion compounder was a twin-screw Berstorff model ZE130/130A*28/lOD.
An aqueous solution of pot~c~ m formate was fed to the extruder at a rate of 12.5 liters per hour with an adhesion control agent additive concentration sufficient to give nominally 300 parts per million (ppm) potassium in the final sheeting 3 o product. A sheet having a nominal thickness of 0.76 mm (0.030 inch) was prepared by the process at a total extrusion rate of 1200 kg/hr (2646 pounds perhour). For purposes of comparison, the process was carried out both with and without injection of 19 liters per hour of demineralized water into Zone No. 3 of the main extrusion compounder. After steady operation with water injection, the 3 5 pure water addition was stopped and the effect on sheet acidity and resultant adhesivity was observed. The recycle extruder was a Berstorff model GE-150KS* 16D single screw extruder with pin barrel. The diameter of the screws in the twin-screw main extrusion compounder was 130 mm (5.1 inch), and the diameter of the single-screw recycle extruder with pin barrel was 150 mm (5.9 CA 0221~204 1997-09-11 inch). Screw speed was 137 RPM in the main extrusion compounder and 15 RPM
in the recycle extruder. The process portion of the extruder screw in the main extrusion compounder was about 38 diameters in length with working elements a~pl o~liate to the melting and vapor control functions. The main barrel 5 configuration consisted of one short primary PVB flake feed barrel, about 3 - diameters long, and seven process barrel sections, each 5 diameters long, to which the process feed streams were added as follows:

Barrel No. 1 PVB -- primary dry flake feed Barrel No. 2 Pot~ssillm formate additive aqueous solution Barrel No. 3 4G7 plasticizer and liquid water injection Barrel No. 4 Melt recycle from the pin barrel extruder Barrel No. S Enclosed process barrel Barrel No. 6 Enclosed process barrel Barrel No. 7 Vacuum vapor extraction with wiped adapters Barrel No. 8 Enclosed process barrel The interlayer obtained was analyzed for acidity concentration and yellowness index. Samples of the interlayer were conditioned to 0.47% water content and laminated into two sheets of standard glass washed with demineralized water.
2 o The following results were obtained:
Comparison Example 1 Demineralized water injected in Barrel 3 -zero- 19 l/h Recycle as percent of total plasticized PVB 30~ 30~o Acidity concentration test, Equiv/lE6 3.14 2.25 2 5 Demin compressive shear strength, kPa 37,020 23,880 Demin compressive shear strength, psi (5369) (3463) Potassium from adhesion control agent, ppm 300 298 Yellowness index, by ASTM D 1925 13.23 11.46 3 o Water injection into the process of this invention produced a 28~o reduction in sheeting acidity concentration. The adhesivity represented by the demin compressive shear strength was reduced to a value within the expected range for good impact performance in windscreen mzlmlf~ctllre. Yellowness was reduced.
J

The process described in Example 1 was operated without recycle at a total extrusion rate of 1529 kg/hr (3371 pounds per hour) to produce similar sheet having a nominal thickness of 0.76 mm (0.030 inch). Screw speed was 199 CA 0221~204 1997-09-11 RPM in the main extrusion compounder and integrated recycle processing was not operated. An aqueous solution of pot~ccillm formate was fed to the main extrusion compounder at a rate of 27.3 liters per hour with an adhesion control agent additive concentration sufficient to give nomin~lly 360 parts per million 5 (ppm) pot:~ccillm in the final sheeting product. Composition and flow rate of pure demineralized water addition was set to provide plasticized polyvinylbutyral melt with time-wise ullirollllity for sheet production, substantially similar to Example 1.
A sheeting specimen was analyzed for acidity and yellowness. Sheeting was conditioned and l~min~ted. The resnlt~nt adhesivity without recycle was within 0 the range suitable for windscreen m~mlf~ctllre. The following results were obtained:

Example 2 Demineralized water injected into Barrel 3 23.5 liter/hr Recycle as percent of total plasticized PVB -zero-Acidity concentration test, Equiv/lE6 4.17 Demin compressive shear strength, kPa 12,160 Demin compressive shear strength, psi (1764) Potassium from adhesion control agent, ppm 360 Yellowness index, by ASTM D 1925 10.11

Claims (12)

WHAT IS CLAIMED IS:
1. Claim 1. A process for preparing polyvinylbutyral sheet having a desired uniform adhesivity comprising preparing a blend of polyvinylbutyral and a compatible quantity of at least one plasticizer and an adhesion control agent,and extruding the blend to form a sheet, the improvement comprising monitoring the acidity of the sheet and adding water to the blend as an agent for controlling the adhesivity of said sheet.
2. Claim 2. The process of claim 1 wherein the water is added before any substantial blending of the polyvinylbutyral and plasticizer occurs.
3. Claim 3. The process of claim 1 wherein the plasticizer is selected from the group consisting of one or more diester organic compounds having from 16 to 28 carbon atoms.
4. Claim 4. The process of claim 3 wherein the adhesion control agent is selected from the group consisting of at least one alkali or alkaline earth metal formate, alkali or alkaline earth metal acetate, or the metal carboxylates of magnesium, calcium, or zinc.
5. Claim 5. The process of claim 1 wherein recycle polyvinylbutyral is added to the blend.
6. Claim 6. The process of claim 5 wherein the recycle polyvinylbutyral is chopped polyvinylbutyral sheet.
7. Claim 7. The process of claim 5 wherein the recycle polyvinylbutyral is molten recycle from a satellite extruder.
8. Claim 8. The process of claim 7 wherein rolls of polyvinylbutyral sheet are fed to said satellite extruder.
9. Claim 9. The process of claim 8 wherein said satellite extruder is a single screw extruder with static pins in the barrel.
10. Claim 10. In a process for preparing a sheet of plasticized polyvinylbutyral by extruding a blend comprised of polyvinylbutyral having a moisture content no more than 3 % by weight and a hydroxyl content of from 15 to 30% by weight, calculated as vinyl alcohol, from 20 to 55 % by weight of at least one plasticizer selected from the group consisting of triethyleneglycol di-n-heptanoate and tetraethyleneglycol di-n-heptanoate, from 50 to 1500 parts per million parts of the sheet of at least one alkali or alkaline earth metal formate, the improvement comprising controlling the acidity of the sheet by adding water to said polyvinylbutyral in a concentration from 0.5 to 5 weight percent of total plasticizer and polyvinylbutyral to control the acid concentration in the sheet to less than 10 equivalents of acid per million parts of sheet.
11. Claim 11. The process of claim 10 wherein the acidity of the extruded blend is monitored and molten recycle polyvinylbutyral is added.
12. Claim 12. The process of claim 10 wherein water is added prior to any substantial plasticization of the polyvinylbutyral.