U.S. patent number 3,765,817 [Application Number 05/193,512] was granted by the patent office on 1973-10-16 for apparatus for the calendering of polymeric materials.
This patent grant is currently assigned to Union Carbide Corporation. Invention is credited to Fred H. Ancker.
United States Patent |
3,765,817 |
Ancker |
October 16, 1973 |
APPARATUS FOR THE CALENDERING OF POLYMERIC MATERIALS
Abstract
Apparatus for the calendering of polymeric material comprising
feeding said polymeric material thru the nip of a calender having a
pair of counter-rotating rolls while maintaining a volumetric
obstruction across the width and between the pair of calender
rolls, the most downstream projection of said obstruction being
positioned so as to at least penetrate the bank of material formed
between the pair of calender rolls upstream of the nip by the
selection of calendering conditions and while concurrently feeding
a stream of polymeric material to said nip opening on each side of
said volumetric obstruction.
Inventors: |
Ancker; Fred H. (Warren,
NJ) |
Assignee: |
Union Carbide Corporation (New
York, NY)
|
Family
ID: |
26889073 |
Appl.
No.: |
05/193,512 |
Filed: |
October 28, 1971 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
Issue Date |
|
|
839292 |
Jul 7, 1969 |
3658978 |
|
|
|
Current U.S.
Class: |
425/325;
425/335 |
Current CPC
Class: |
B29C
48/08 (20190201); B29C 48/35 (20190201); B05D
1/265 (20130101); B29C 43/24 (20130101); B05D
1/28 (20130101); B29C 44/30 (20130101); B29C
44/485 (20130101); B29L 2009/00 (20130101); B05D
2252/02 (20130101); B29C 43/46 (20130101); B05D
2252/10 (20130101) |
Current International
Class: |
B29C
44/48 (20060101); B29C 43/24 (20060101); B29C
44/30 (20060101); B29C 44/34 (20060101); B29C
44/00 (20060101); B29C 47/32 (20060101); B29C
47/12 (20060101); B05D 1/26 (20060101); B29C
43/44 (20060101); B29C 43/46 (20060101); B29c
015/00 () |
Field of
Search: |
;425/223,224,325,335,363
;164/277 ;18/2C |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Annear; R. Spencer
Parent Case Text
This application is a division of application Ser. No. 839,292,
filed July 7, 1969 and entitled CALENDERING OF POLYMERIC MATERIALS
and now having issued as U.S. Pat. No. 3,658,978.
Claims
What is claimed is:
1. Apparatus for the calendering of polymeric materials, comprising
a pair of cylindrical counter-rotating calender rolls positioned to
define therebetween a nip opening, volumetric obstruction means
positioned across the width and between said pair of calender rolls
for penetrating the bank of material formed between the pair of
calender rolls upstream of the nip by the selection of calendering
conditions and for removing a substantial portion of a stagnant
flow zone of the material, and means for feeding streams of
polymeric material to said nip on opposite sides of said
obstruction means.
2. Apparatus in accordance with claim 1, wherein said pair of
calender rolls is equal in radius and said volumetric obstruction
means is symmetrically shaped in cross-section and symmetrically
positioned with respect to the pair of calender rolls.
3. Apparatus in accordance with claim 1, wherein said volumetric
obstruction means is of decreasing cross-sectional thickness along
its width as it projects into the space between said pair of
calender rolls.
4. Apparatus for the direct extrusion-calendering of polymeric
materials comprising sheet extruder means for producing two sheets
of extruded polymeric material, a pair of cylindrical
counter-rotating calender rolls positioned to define therebetween a
nip opening, and volumetric obstruction means positioned across the
width and between said pair of calender rolls for penetrating the
bank of material formed between the pair of calender rolls upstream
of the nip by the selection of calendering conditions and for
removing a substantial portion of a stagnant flow zone of the
material, the clearances between said volume obstructing means and
each of said calender rolls being such as to permit the
unobstructed passage of each of said two sheets of extruded
polymeric material to freely pass therebetween and join before
passage thru said nip opening.
5. Apparatus in accordance with claim 4, wherein said pair of
calender rolls is equal in radius and said volumetric obstruction
means is symmetrically shaped in cross-section and symmetrically
positioned with respect to the pair of calender rolls.
6. Apparatus in accordance with claim 4, wherein said volumetric
obstruction means is of decreasing cross-sectional thickness along
its width as it projects into the space between said pair of
calender rolls.
Description
The present invention relates to the calendering of polymeric
materials and, more particularly, to apparatus for controlling the
flow of such materials between a pair of counter-rotating calender
rolls.
The calendering of polymeric materials is well known in the prior
art. For a detailed discussion of the calendering process,
reference is made to an article by F.H. Ancker entitled "Trends in
Calendering," Plastics Technology, 14 .music-sharp.12, 50, 1968 and
British Pat. No. 1,127,743 and the references quoted therein. The
conventional calendering process consists in shaping a molten or
heat-softened polymeric material into film or sheeting by passage
thru the nip opening of one or more pairs of counter-rotating
rolls. Usually, three-roll passes (four rolls) are required, i.e.,
the calendering process is repeated three times over in order to
obtain a sheet of satisfactory surface quality.
In recent years, there has been considerable interest in attempting
to accomplish the calendering operation in a single-roll pass by
feeding a two-roll calender directly from an extruder slot die.
Unfortunately, such attempts have had very limited success, except
in embossing or roll planishing where the rolls exert little or no
thickness reduction of the hot extruded sheet, i.e., where the
rolls actually do not shape or calender the material. In fact, even
minor flow irregularities in the molten polymer stream on the inlet
side of the roll nip generally lead to very pronounced surface
defects in the sheet emerging from the roll nip. Accordingly,
attemps to reduce the cost of current calendering equipment and
simplify the calendering process have been largely
unsuccessful.
However, even allowing for the very appreciable cost of standard
multi-roll plastic calenders, the conventional calendering process
still has several major limitations. First, the maximum thickness
of sheeting which can be calendered without porosity and/or surface
air streaks is usually about 25 mils, depending somewhat on the
rheological properties of the material. Second, the maximum
calendering rate is limited by the thermal stability and viscosity
of the polymeric compound; this is a very serious limitation in the
processing rates of many unplasticized polyvinyl chloride
compounds. Third, very few polymers other than polyvinyl chloride
have the roll release and rheological properties necessary for the
complicated film tracking required on a four-roll calender. These
and similar problems have to a large extent prevented the
calendering process from reaching its potential as a broadly useful
process for producing high-quality polymeric film and sheeting
having excellent thickness uniformity and superior surface
properties.
Reference is made to the accompanying drawings, wherein:
FIG. 1 shows schematically an idealized bank streamline flow
pattern for isothermal calendering of a Newtonian fluid;
FIG. 2 shows schematically the corresponding velocity vectors in
such fluid within the nip of the calender;
FIGS. 3 and 4 show typical fluid flow patterns drawn from
photographs of banks of polymeric materials during calendering;
FIG. 5 is a schematic elevational sectional view of apparatus
embodying the invention and capable of the calendering of polymeric
material directly fed from an extruder;
FIG. 6 is a partial schematic plan view of the apparatus of FIG.
5;
FIG. 7 is a partial schematic sectional view of modified apparatus;
and
FIGS. 8, 9 and 10 are schematic sectional views of further modified
calendering apparatus embodying the invention.
It has been found that it is possible to overcome the calendering
problems mentioned hereinabove by a radical change in the flow
pattern of the natural calendering or milling bank. However, in
order to appreciate the significance of this change, it is
necessary first to consider the nature of the flow pattern in a
conventional calendering bank and how the major problems
encountered in current calendering processes arise from this
pattern.
Referring specifically to FIG. 1, the streamline marked .chi. = 0
comprises the so-called stagnation line or surface. It separates
the progressive or active flow zone from a stagnant flow zone which
consists of two vortices with opposite directions of rotary flow.
The fluid within the stagnant zone undergoes vortex flow and has
extremely long residence times compared to fluid within the
progressive flow zone. A comparison with the diagrams of the fluid
velocity vectors of FIG. 2 shows that the stagnation line
represents the line or surface where the volume of back flow (due
to the hydrostatic pressure generated in the fluid) exactly equals
the volume of forward flow (due to viscous drag from the moving
roll surfaces). The apex of a stagnation line is commonly referred
to as a stagnation point, referred to as x = -x.sub.* in FIG. 1. It
can be shown that the stagnation point approaches the roll nip (x =
0) and the stagnation surface approaches the roll surfaces as the
roll nip opening is decreased. Also, if the peripheral roll speeds
are unequal, the stagnation surface will recede from the fast roll
and approach the slow roll. Furthermore, the hydrostatic pressure
in the bank, which is very appreciable when calendering highly
viscous polymers in thin gauges, has its maximum value at x =
-x.sub.e, i.e., within the progressive flow zone at a point
symmetrical to the film egress point (x = x.sub.e).
FIGS. 3 and 4 show two typical real flow patterns drawn from
photographs taken of actual calendering banks of rigid polyvinyl
chloride compounds. The similarity with the theoretical flow
pattern in FIG. 1 is apparent, but the two vortices are far from
symmetrical. The rotation of the outer bank surface is determined
by the particular vortex which happens to predominate. The flow
pattern shown in FIG. 3 is most typical for conventional
calendering operations, but the opposite bank rotation shown in
FIG. 4 is occasionally encountered in practice.
The basic problems of the conventional calendering process have
been traced experimentally to the flow pattern of the actual
calendering bank shown in FIGS. 3 and 4.
First, the maximum thickness limitation of about 25 mils for most
calendered sheeting is due to the peculiar air entrapment and
rejection behavior of a natural calendering bank. We have found
that air bubbles almost invariably are introduced into the
calendering bank where the hot sheet moves into the bank (points P
on FIGS. 3 and 4), no matter in which direction the bank is
rotating. If the bank surface is fluid and glossy, this tendency is
generally less than when the bank surface is dry and matte, but
some air is nearly always introduced. If the bank is cold and
"folding," additional air is often introduced due to air cavities
between the folds and due to formation of secondary vortices.
Nevertheless, as long as the nip opening is small, the stagnation
surface is very close to the roll surface, air becomes trapped
within the stagnant flow zone and has no opportunity to pass thru
the roll nip. Accordingly, it is often seen in calendering of thin
films that the calendering bank is filled with air bubbles, yet the
emerging film is completely free of air. However, as the nip
opening is increased in order to produce thicker sheeting, this
fortunate situation no longer exists. The stagnation surface will
recede from the roll surfaces and the roll nip, the air bubbles
introduced at point P now will be captured within the progressive
or active flow zone and the emerging sheet will become porous
and/or contain air streaks on the surface and be commercially
useless.
Second, the problem of polymer decomposition encountered in
attempting to calender thermally unstable, yet highly viscous,
materials is also intimately connected with the natural flow
pattern of a normal calendering bank. As the roll speeds increase,
the residence time of molten polymer in the progressive zone of the
bank decreases; however, the residence time of the polymer melt
within the stagnant zone remains very great. Actually, because of
the increase in viscous heat dissipation with increasing roll
speed, the polymer within this zone may degrade severly before any
visible degradation occurs in the emerging sheet. Thus, the
stagnant flow zone with its associated extreme residence times is
the major rate-limiting factor of the calendering process.
The third major problem of the conventional calendering process is
the difficulty with which many polymer melts comply with the
complicated film tracking and roll release required on a four-roll
calender. The fact that three-roll passes are required to produce a
calendered sheet of acceptable surface quality is, of course, the
underlying reason for this limitation since tracking on a two-roll
calender generally is quite simple. In studying the calender bank
flow of many polymeric materials, it has been consistently
surprising how seemingly minor flow disturbances on the inlet side
of a roll nip often cause very objectionable surface defects in the
sheet emerging from the roll nip. This phenomenon, which
undoubtedly stems from the elastic memory typical of high polymer
melts, is believed to be responsible for the redundancy required in
conventional calendering. In other words, the flow history, melt
temperature, etc. within a calendering bank is not sufficiently
uniform to obtain a high quality sheet unless the process is
repeated at least once, usually twice or sometimes even three times
over.
It is, accordingly, the prime object of the present invention to
provide apparatus for the calendering of polymeric materials in
which material thickness, degradation and surface defect
limitations are greatly minimized or eliminated.
Other objects and advantages of the present invention will be
apparent from the following description and appended claims.
In accordance with the present invention, apparatus is provided for
the calendering of polymeric materials wherein said materials are
fed thru the nip opening of a pair of counter-rotating calender
rolls while maintaining a volumetric obstruction across the width
and between said pair of calender rolls, with the most downstream
projection of said obstruction being positioned so as to at least
penetrate the bank of material formed between the pair of calender
rolls upstream of the nip by the selection of calendering
conditions, and while concurrently feeding a stream of polymeric
material to said nip opening on each side of said volumetric
obstruction.
The present invention provides a simple and effective solution to
the above-mentioned and other problems inherent in the calendering
process. The solution to this problem is effected by removing a
substantial part of the stagnant flow zone by placing within this
region of flow a volumetric obstruction, while at the same time
introducing the polymeric fluid in the form of separate streams
conforming to the active or progressive flow zone, i.e., one stream
on each side of the obstruction. The flow obstruction substantially
reduces the natural back flow in the calendering bank and thus
makes it possible to reduce or eliminate the usual bank rotation
with its associated problems of air entrapment, thermal
degradation, sensitivity to surface defects, etc. In fact, the
present invention makes it possible to calender film and sheeting
of excellent surface quality on a two-roll calender or mill by
direct feeding from an extruder using a suitably designed die.
Also, the invention makes it possible to calender much heavier
gauge sheeting of a variety of polymers on conventional calenders
or mills by the use of a suitably arranged obstruction.
The invention is more fully explained by reference to the apparatus
embodiment shown in FIGS. 5 and 6. As there shown, calender 10 is
provided comprising a pair of counter-rotating rolls 12 and 14 and
stripper roll 16. Calender 10 is directly fed two molten polymer
streams 18 and 20 from extrusion die 22, which comprises die
housing 24 and flow divider 26. A stream of molten polymeric
material 28 is forced from conventional extruder means (not shown)
and enters extrusion die 22 thru inlet means 30. The polymeric
material then passes thru passage 32 to internal die manifold 34,
having two manifold branches 34a and 34b.
Along the manifold edge, the molten polymeric material stream is
separated into two streams by flow divider 26 which, in its most
forward projection 36, also serves as solid volumetric obstruction.
Because the forward projection of the flow divider (volumetric
obstruction) preferably occupies a substantial portion of the
back-flow region (stagnant flow zone), smooth, gently curved bank
surfaces 18a and 20a are formed between the die lips and the roll
surfaces, as shown in FIG. 7 of the drawings.
It has been found that the forward projection of the flow divider
(volumetric obstruction) does not have to conform closely to the
particular stagnation surface resulting from a particular roll
diameter and nip opening. Actually, it is preferable that the front
end of the flow divider is considerably more blunt than the
theoretical stagnation surface and that it stops somewhat short of
the stagnation point. The reason for this is that the hydrostatic
pressure in the roll nip is low in the outer region of the bank,
whereas it increases steeply near the maximum pressure point (FIG.
1, x = -x.sub.e). Consequently, if the front end of the flow
divider (volumetric obstruction) protrudes only moderately into the
bank, some misalignment of the die can be tolerated.
Furthermore, a blunt front end is more tolerant of operation with
variable relative roll speeds which, as previously mentioned,
changes the shape of the stagnation surface and thus the optimum
position of the volumetric obstruction. On the other hand, if the
front end of the flow divider is sharp and protrudes far into the
roll nip, then the alignment of the die, i.e., volumetric
obstruction, must be very accurate in order to avoid undesirable
deflections and flow disturbances.
It should also be pointed out that the use of a blunt flow
obstruction which stops far short of the apex of the stagnation
surface does not eliminate vortex flow per se. It has been found,
experimentally, that, as is shown in FIG. 7 of the drawings, a flow
region containing two rotating vortices 40 sometimes exists in
front of a blunt volumetric obstruction. Nevertheless, in contrast
to the conventional calendering bank (FIGS. 3 and 4), these small
vortices are submerged well within the fluid stream and occupy a
volume which is only a small fraction of the stagnant flow volume
in a corresponding natural calendering bank. Accordingly, it has
been found that small internal vortices of this type do not cause
any of the problems previously related to the large stagnant flow
zone in a conventional calendering bank.
It is, of course, to be understood that volumetric obstruction 36
is maintained across the full width of and between calender rolls
12 and 14. It has been found that the most forward (downstream in
the direction of material passage) projection of the obstruction
should be positioned so as to at least penetrate the bank of
material formed between the pair of calender rolls upstream of the
nip by the selection of calendering conditions.
It has been found preferable that the most forward projection of
the volumetric obstruction be positioned well within the space
between the pair of calender rolls beyond the position of merely
slight penetration of the bank of material being calendered.
However, any positioning of the most forward projection of the
volumetric obstruction (within such penetration of the bank)
between the rolls will provide a significant reduction in back flow
and consequently improved calendering results.
It is most preferred that calendering operations be performed with
the obstruction maintained at a sufficiently close distance to the
nip to substantially reduce the calender back flow and thus
eliminate the natural bank rotation typical of conventional
calendering banks. This has been found capable of accomplishment by
substantially contouring and positioning the volumetric obstruction
with the stagnation zone or area as defined in FIGS. 1 and 2.
However, as pointed out hereinabove, this contouring and
positioning is by no means critical and the desired results are
progressively accomplished as a more substantial portion of the
back-flow zone becomes occupied by the volumetric obstruction.
An alternate embodiment of apparatus embodying the invention is
shown in FIG. 8. As there shown, two molten polymer streams 18 and
20 are introduced into a roll nip along the surfaces of two
counter-rotating rolls 12 and 14 and normal bank build-up and
rotation in the nip is prevented by volumetric obstruction 36 which
is maintained in the roll nip by hydraulic, pneumatic or mechanical
means 42. The volumetric obstruction 36 is hydrodynamically
balanced in a sidewards direction by the two fluid streams, and
deflections within the plane formed by the volumetric obstruction
means and the roll nip can be easily reduced to a desired level by
using obstruction means having sufficient stiffness in this plane
or by hydraulically, pneumatically or mechanically back-loading the
obstruction means. Accordingly, the obstruction means automatically
seeks its optimum position for the prevention of back flow by the
hydrodynamic forces acting in the roll nip.
The two polymer streams introduced on either side of the
obstruction means may originate from any suitable source, such as
sheet extruders, calenders or the like. FIG. 8 illustrates an
embodiment suitable for any such arrangement. Specifically, the
fluid streams may also be generated by calendering operations on
the same conventional calender, as illustrated in the inverted "L"
or "Z" calenders of FIGS. 9 and 10. The threading arrangements
illustrated in FIGS. 9 and 10 may seem rather cumbersome; however,
far more complicated approaches have heretofore been suggested in
order to achieve similar improvements in the calendering process,
i.e., tripple and quadruple mills. Actually, the main advantage of
threading systems, such as those illustrated in FIGS. 9 and 10, is
that they make it possible to practice the present invention by
merely modifying already existing equipment.
As specifically shown in the inverted "L" calender embodiment of
FIG. 9, the pair of calendering rolls 12 and 14 cooperate to
perform the calendering operation of the present invention. Rolls
44 and 46 are employed, as shown, to provide the two streams of
polymeric material 18 and 20. These streams are produced by feeding
molten polymeric material to the material banks 48 and 50, formed
between the two conventionally operating calender paired rolls
12-44 and 14-46, respectively.
As specifically shown in the "Z" calender embodiment of FIG. 10,
the pair of calendering rolls 12 and 14 similarly co-operate to
perform the calendering operation in accordance with the present
invention. Other elements of this embodiment perform functions of
similarly numbered elements of the embodiment of FIG. 9.
In order to avoid confusion and more fully understand the
significance of the direct extruder-fed calendering aspect of the
present invention, the differences between such a process and the
conventional roll planishing or embossing process should be set
forth.
Calendering is the process of forming a molten polymeric material
into film or sheet by passing it between one or more pairs of
counter-rotating rolls, i.e., in calendering, the fluid is greatly
compressed in the thickness direction by passing thru the roll nip.
In other words, the ratio of the bank "diameter" (shortest distance
between the points where the fluid touches both rolls on the
ingress side) to the sheet thickness (shortest distance between the
points where the fluid touches both rolls on the egress side) is
considerably larger than unity, in fact, usually ten to a thousand
fold.
In contrast, embossing or roll planishing is the process of
imparting a desired surface to an already-shaped sheet with
substantially no thickness reduction by passing it between one or
more pairs of counter-rotating rolls. Accordingly, the compression
in the roll nip is so slight that only a very slight bulging in the
sheet is allowed to form in front of the roll nip and the
ingress-to-egress thickness ratio is very close to unity. In
conventional sheet extrusion, the plastic is formed into final
thickness by extrusion thru a die and the hot sheet is then cooled
and roll planished or embossed by slight compression between
cooling rolls. Excellent illustrations and descriptions of the
conventional sheet extrusion process are given in chapter 4 of A.L.
Griff: "Plastics Extrusion Technology," New York (Reinhold Book
Corporation) 1968.
The advantages of forming the final film or sheet between rolls (as
in the present invention), rather than in a film or sheeting die
(as in extrusion-embossing are considerable:
First, the output of a single screw extruder increases markedly
with channel depth and screw speed. However, if the attached die
has considerable flow resistance, such as is the case if the
ultimate web thickness is achieved in the die, then the output of
the extruder is severely limited due to overheating caused by
excessive generation of viscous heat in the extruder. In contrast,
dies for feeding thick molten webs for subsequent calendering can
be designed with very low flow resistance resulting in vastly
greater overall production rates.
Second, due to elastic memory effects, the surface of a
thermoplastic sheet after reheating usually reverts to the
appearance it received at the highest temperature during its
forming operation. For example, an extruded/planished sheet may
have received an excellent surface in the planishing operation, yet
if reheated, say for subsequent vacuum forming, it may revert to
the original extruded surface having die streaks, non-uniformities,
etc. In contrast, the calender rolls impart the final surface at
the highest forming temperature encountered, thereby resulting in a
thermally superior surface.
Third, in case of subsequent in-line orientation of a plastic web,
it is usually desired to form the web at as low a temperature as
possible. This is especially important in cases of thick sheeting
where it is difficult to achieve a uniform temperature profile
across the thickness of the sheet by subsequent external cooling.
It has been found that it is possible to extrude and calender a
sheet with excellent surface properties at melt temperatures much
closer to the optimum orientation temperature than is possible by
the standard extrusion method employed in extrusion-embossing. This
has proven to be a significant advantage for in-line orientation of
sheeting, especially in thick gauges.
The following basic equipment units were used in various
combinations in the examples listed below:
Extruders
No. 1 No. 2 Barrel Diameter 31/2" 6" L/D Ratio 21 24 Screw Helix
square pitch square pitch Channel Depth A-screw 0.125" 0.300"
B-screw 0.200" Compression Ratio, A-screw 4.5 3.7 B-screw 2.8
CALENDERS
No. 1 No. 2 Type 2-roll vertical 4-roll inverted L Roll Drives
individual common, equal roll speeds Roll Heating individual
individual Roll Diameter 12" 8" Roll Face 24" 16"
The polymeric compounds used in the examples were characterized in
terms of the power law expression for the viscosity of
non-Newtonian fluids:
.mu. = .mu..sub.o (.gamma./.gamma..sub.o).sup.n =
c.sub.o.sup...gamma..sup.n
where:
.mu. = apparent melt viscosity (lbs.sup.. sec.sup..
in.sup..sup.-2)
.gamma. = shear rate (sec.sup..sup.-1)
c.sub.o = extrapolated viscosity at unit shear rate (.gamma. =
1)
n = power law exponent
EXAMPLE 1
This example illustrates the versatility of the split-stream
calendering method for producing sheeting in an extreme range of
thicknesses without surface defects or air entrapment. The
equipment arrangement was that of FIGS. 5-6, i.e., a two-roll
calender fed directly from an extruder using a split-stream die.
The polymeric material was rigid (unplasticized) polyvinyl
chloride.
A granulated PVC compound having a unit shear rate viscosity
(c.sub.o) equal to 2.5 and a power law exponent (n) equal to -0.42
at 180.degree. C. was fed to extruder -1 equipped with extruder
screw B. Attached to the discharge end of the extruder thru a
flexible adapter was a split-stream die as illustrated in FIGS.
5-6. The discharge orifice of the die was 1 .times. 18 in.
Protruding thru the die orifice was a 0.6 .times. 18 in. flow
divider leaving two net die orifices of 0.2 .times. 18 in.
symmetrically disposed on either side of the flow divider. The
front end of the flow divider had a semi-circular shape as shown in
FIG. 7 which protruded 11/4 in. beyond the die lips. The
extruder/die combination was operated at the following
conditions:
Extruder Barrel Zones, Rear-to-Front
160.degree.C./145.degree.C./150.degree.C. Melt Temperature at Die
180.degree.C. Melt Pressure at Die 1000 psi Die Temperature (Oil
Heat) 165.degree.C. Screw Speed 22 rpm Throughput Rate 210
lbs./hr.
After stable operating conditions had been achieved, the
extruder/die combination unit was moved into the roll nip of
calender -1 using a mechanical die linkage support (not shown) to
assure that the die orifice remained aligned with the roll nip
independently of the nip opening. Using an initial nip opening of
0.205 in. corresponding to a calendered sheet thickness of about
0.250 in., the calender rolls were adjusted to the following
conditions to accommodate the output of the extruder:
Temperature, Top Roll 155.degree.C. Temperature, Bottom Roll
165.degree.C. Roll Speed, Top Roll 1.15 fpm Roll Speed, Bottom Roll
1.25 fpm
The die equipped with the flow obstruction described above was now
forced into the roll nip by a mechanical screw-down attachment
between the die and the calender frame until a smooth flow pattern
as shown in FIG. 7 was achieved across the width of the die. The
hot sheeting emerging from the roll nip was completely free of air
entrapment, of high gloss and free of any surface
imperfections.
The roll nip opening was now gradually decreased and the calender
roll speeds commensurately increased to match the constant output
of the extruder. It was noted that the emerging sheet thickness
could be reduced at least to half of the original value without
disturbing the smooth flow pattern between the die lips and the
calender rolls.
As the sheet thickness decreased further, it became necessary to
force the die slightly closer to the roll nip in order to secure
the intended flow pattern. When this was done, however, excellent
flow uniformity and sheet quality was obtained continuously up
until the maximum roll speed of the calender of about 60 fpm
corresponding to a final film thickness of about 5 mils.
In similar experiments, the calender was supplied with a single
stream of the same compound from a conventional slot die without
any volumetric obstruction for control of back flow in the roll
nip. In these cases, conventional rotating bank flow occurred and
unavoidable flow irregularities in the bank resulted in severe
defects in the emerging sheet. Also, at sheet thicknesses above 30
mils, air entrapment occurred to increasing extents with increasing
thickness in agreement with the general experience with the
conventional calendering process.
These results show clearly the superiority of the dual-stream
calendering methods as compared to conventional calendering with
rotating banks. The split-stream method of feeding a calender
enables not only production of high-quality sheeting in a single
roll pass rather than three roll passes, but it even allows
production of air-free sheeting in much heavier gauges than is now
possible on conventional calenders.
EXAMPLE 2
This example illustrates the ability of split-stream calendering
for producing sheeting at high rates without surface defects or air
entrapment. The equipment arrangement was the same as that of
Example 1, except that a larger extruder was used. Also, the
polymeric material was high-density polyethylene.
A granulated compound of pigmented, high-density polyethylene
having a unit shear rate viscosity (c.sub.o) equal to 5.4 and a
power law exponent (n) equal to -0.66 at 185.degree. C. was fed to
extruder -2. The split-stream die described in Example 1 was
attached to the extruder thru a flexible, valved adapter and the
extruder/die combination was operated at the following
conditions:
Extruder Barrel Zones, Rear-to-front 150.degree.C./160.degree.C. 1
.degree.C. Melt Temperature at Die 191.degree.C. Melt Pressure at
Die 2.000 psi Die Temperature (Oil Heat) 185.degree.C. Screw Speed
30 rpm Valve Section slightly closed Throughput Rate 915
lbs./hr.
Using the same procedure as described in Example 1, the extruder
die w/volumetric flow obstruction was moved into the roll nip. A
nip opening of 0.040 in. corresponding to a calendered sheet
thickness of about 0.050 in. was used and the calender was adjusted
to the following conditions to accommodate the output of the
extruder:
Temperature, Top Roll 130.degree.C. Temperature, Bottom Roll
135.degree.C. Roll Speed, Top Roll 31 fpm Roll Speed, Bottom Roll
32 fpm
Keeping the extruder output constant, the roll nip opening was then
first doubled and later reduced to half of the original value
making commensurate changes in the roll speeds. Without changing
the die position relative to the calender, sheeting with excellent
surface quality and complete freedom from entrapped air was
produced.
This experiment illustrates what may be the greatest advantage of
the split-stream calendering system, namely, the ability to produce
calendered film and sheeting of excellent quality at high rate and
yet with very low extruder back pressure. If fluxed compound is fed
to the extruder rather than solid pellets, then no fluxing and
mixing is required of the extruder and an inexpensive,
short-barrel, deep-channel strainer-extruder can be used to feed a
low-pressure, split-stream die. In contrast, deep-channel extruders
are impractical in normal high-pressure extrusion because the
output of such extruders decreases sharply with the flow resistance
of the die, thus negating the advantage. However, in this system,
the major work connected with shaping the melt into sheeting is
done by the calender rolls and a split-stream die can, therefore,
be designed with very low flow resistance.
EXAMPLE 3
This example illustrates the capability of split-stream calendering
in forming film and sheeting at much lower melt temperatures than
those normally attainable by sheet extrusion. This is especially
important for in-line orientation of heavy sheeting because the
optimum melt temperature for orientation is considerably lower than
the optimum melt temperature for sheet extrusion. The polymeric
material used in this example was polystyrene.
A polystyrene homopolymer compound having a unit shear rate
viscosity (c.sub.o) equal to 5.8 and a power law exponent (n) equal
to -0.74 at 160.degree. C. was fed to extruder -1 equipped with
extruder screw A. The split-stream die was attached as described in
Example 1. The extruder/die combination was operated at the
following conditions:
Extruder Barrel Zones, Rear-to-Front
135.degree.C./145.degree.C./160.degree.C. Melt Temperature at Die
155.degree.C. Melt Pressure at Die 650 psi Die Temperature (Oil
Heat) 150.degree.C. Screw Speed 15 rpm Throughput Rate 120
lbs./hr.
The extruder/die combination unit was then moved into the roll nip
of calender -1 and the die w/volumetric flow obstruction positioned
as described earlier. The roll nip opening was adjusted to 0.160
in. corresponding to a sheet thickness of about 0.200 in. The
calender rolls were adjusted as follows:
Temperature, Top Roll 100.degree.C. Temperature, Bottom Roll
100.degree.C. Roll Speed, Top Roll 1 fpm Roll Speed, Bottom Roll 1
fpm
The sheet was completely air free and of excellent surface quality.
The temperature of the sheet immediately as it emerged from the
roll nip, i.e., without following either roll, was measured to be
135.degree. C. This is very closely the optimum orientation
temperature for polystyrene sheeting and much lower than the
minimum melt temperature attainable in conventional sheet extrusion
which is 175.degree.-180.degree. C. if a good surface is
required.
This example illustrates the ability of split-stream calendering to
produce sheeting of excellent surface quality at much lower
temperatures than those possible in ordinary sheet extrusion. As
mentioned above, this is of particular commercial importance for
in-line orientation of heavy sheeting.
EXAMPLE 4
This example illustrates the split-stream calendering system
applied on a conventional four-roll calender in order to produce
heavier gauge sheeting than normally possible by ordinary
calendering. The polymeric material in this example was low-density
polyethylene.
A low-density (0.918) polyethylene compound containing a red
pigment was fluxed in a banbury, transferred to a mill (roll
temperatures -- 115.degree.-125.degree. C.) and then fed to the top
roll nip (48) on calender -2 as shown in FIG. 9. Another batch,
containing a green pigment, was fed to the lower roll nip (50) and
a volumetric flow obstruction (36) as shown in FIG. 9 was then
hydraulically forced into the roll nip formed by rolls 12 and 14.
The calendering conditions were as follows:
"Red" Nip Opening 0.020" "Green" Nip Opening 0.020" Split-Stream
Nip Opening 0.040" Rolls 44 and 46 115.degree.C. Roll 14
120.degree.C. Roll 12 125.degree.C. Roll Speed (all rolls) 10
fpm
No bank rotation occurred in the dual-stream roll nip containing
the volumetric obstruction and the sheeting stripped off roll 12
was air free and of good surface quality. The top side of the sheet
was red and the bottom side green and very little pigment
intermixing had occurred.
The volumetric flow obstruction was now removed and natural bank
rotation allowed to occur. The sheet emerging on roll 12 now became
porous and contained notable air streaks and surface roughness.
Also, considerable pigment intermixing was evident due to the
uncontrolled rotational flow in the last roll bank.
This example illustrates the use of the split-stream calendering
principle for making heavier sheeting than normally possible on a
standard calender. Also, the experiment shows the utility of this
system for melt lamination of dissimilar polymers on a
calender.
All of the above examples illustrate the versatility of the
invention in calendering a wide range of polymers as compared to
the very limited range which can be handled in conventional
calendering.
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