Screw extruder with improved dispersive mixing elements
A screw extruder (10) having a barrel (18) which has a bore (26) defining an inner surface (44) and one or more extruder screws (28), positioned within the bore (26). The extruder screw or screws (28) include a central shaft (34) and one or more screw flights (30). The extruder screw or screws (28) farther including one or more dispersive mixing elements (204), (234), (308), (406), (508), (558), which interact with the inner surface of the barrel (44) to form one or more progressively narrowing passages (46) through which material is forced into multiple regions of high elongational and shear stress (480, (120), (214), (310), (410), (510), (564). A second preferred embodiment is a screw extruder (10) having a barrel (18) having a bore (26) defining an inner surface (44) and one or more extruder screws (600), (701), positioned within the bore (26). The extruder screw or screws (600), (701) include a central shaft (602), (706) and a number of dispersive mixing elements (604), (608), (714), which are configured and positioned to form a number of progressively narrowing passages (606), (716) through which material is forced into multiple regions of high elongational and shear stress (608), (718).
| Inventors: | Rauwendaal; Chris J. (Los Altos Hills, CA), Gramann; Paul J. (Madison, WI), Davis; Bruce A. (Oregon, WI), Osswald; Tim A. (Madison, WI) |
| Assignee: | Rauwendaal Extrusion Engineering (Los Altos Hills, CA) |
| Appl. No.: | 09/241,822 |
| Filed: | February 1, 1999 |
| Application Number | Filing Date | Patent Number | Issue Date | ||
| 966272 | Nov., 1997 | 5932159 | |||
| Current U.S. Class: | 264/211.21 ; 264/211.23; 264/349; 366/300; 366/301; 366/318; 366/319; 366/322; 366/323; 366/324; 366/79; 366/81; 366/84; 366/85; 366/89; 425/200; 425/204; 425/208; 425/209 |
| Current International Class: | B29C 47/58 (20060101); B29C 47/38 (20060101); B29C 47/60 (20060101); B29C 47/40 (20060101); B29C 47/62 (20060101); B29C 47/66 (20060101); B29C 47/64 (20060101); B29C 047/60 (); B29C 047/62 (); B29C 047/66 () |
| Field of Search: | 264/211.21,211.23,349 425/200,204,208,209 366/79,81,84,85,89,300,301,318,319,322,323,324 |
| 3593843 | July 1971 | Hill |
| 3901482 | August 1975 | Kieffaber |
| 3989941 | November 1976 | Gasior et al. |
| 4092015 | May 1978 | Koch |
| 4173417 | November 1979 | Kruder |
| 4215978 | August 1980 | Takayama et al. |
| 4227870 | October 1980 | Kim |
| 4277182 | July 1981 | Kruder |
| 4363768 | December 1982 | Kruder |
| 4834543 | May 1989 | Nortey |
| 5035509 | July 1991 | Kruder |
| 5071256 | December 1991 | Smith et al. |
| 5332309 | July 1994 | Ramazzotti et al. |
| 5356208 | October 1994 | Tadmor |
| 5551777 | September 1996 | Tjahjadi et al. |
Cheremisinoff, Nicholas P.; "Polymer Mixing and Extrusion Technology" (1987, Marcel Dekker, Inc.), pp. 372-375. . Levy, Sidney; "Plastics Extrusion Technology Handbook, second edition" (1989, Industrial Press Inc.), pp. 14-15 and 82-93. . Rauwendaal, Chris J.; "Polymer Extrusion, 3rd rev. ed." (1994, Carl Hanser Verlag), pp. 322-323, 332-333, 416-417, and 432-433.. |
Primary Examiner: Tentoni; Leo B. Attorney, Agent or Firm: Guernsey; Larry B. Hickman Stephens Coleman & Hughes, LLP
The following is a continuation-in-part of application 08/966,272 which was filed on Nov. 7, 1997, now U.S. Pat. No. 5,932,159.
What is claimed is:
1. A screw extruder comprising:
a barrel, said barrel having a bore defining an inner surface; and
at least one extruder screw, positioned within said bore, said at least one extruder screw including a central shaft and at least one screw flight, said at least one extruder screw further including at least one dispersive mixing element which interacts with said inner surface of said barrel to form at least one progressively narrowing passage through which material is forced into at least one region of high elongational and shear stress.
2. The screw extruder of claim 1 wherein:
said at least one dispersive mixing element includes at least one tapered slot formed in said at least one screw flight, said at least one tapered slot forming at least one progressively narrowing passage through which material is forced into at least one region of high elongational and shear stress.
3. The screw extruder of claim 2 wherein:
said at least one tapered slot has a taper angle which is in the range of 20 to 60 degrees.
4. The screw extruder of claim 1 wherein:
said at least one flight includes a mixing portion and a wiping portion.
5. The screw extruder of claim 1 wherein:
said at least one flight includes discrete mixing segments and wiping segments.
6. The screw extruder of claim 1 wherein:
said at least one flight has only wiping segments.
7. The screw extruder of claim 2 wherein:
said at least one flight includes at least one non-zero slot pushing flank angle.
8. The screw extruder of claim 2 wherein:
said at least one flight includes at least one non-zero slot trailing flank angle.
9. The screw extruder of claim 1 wherein:
said at least one flight is a fully wiping flight.
10. The screw extruder of claim 2 wherein:
said extruder screw has a Diameter dimension;
said flight has a helix angle, a slot trailing flank angle, a slot pushing flank angle, a slot width and a flight width;
said helix angle is in the range of 20-90 degrees;
said slot pushing flank angle is in the range of 0-90 degrees;
said slot trailing flank angle is the range of 0-50 degrees;
said slot width is in the range 0.02-0.25 Diameters; and
said flight width is in the range of 0.0-0.5 Diameters.
11. The screw extruder of claim 5 wherein:
said screw extruder has four flights which are arranged in a flight segment configuration, which is a variable to be selected from a group consisting of every flight 1/4 wiped, every other flight 1/2 wiped, one flight is completely wiped, and two flights 1/6 wiped and two flights 1/3 wiped and every flight 1/3 wiped except for the fourth flight.
12. The screw extruder of claim 1 wherein:
said at least one dispersive mixing element include at least one fluted mixing section;
each said fluted mixing section having a plurality of adjacent dispersive regions;
each of said adjacent dispersive regions including at least one inlet portion and at least one outlet portion, and at least one region of high elongational and shear stress; and
said adjacent dispersive regions being configured so that an outlet portion of one adjacent dispersive region directs material into an inlet portion of another adjacent dispersive region so that material is forced through multiple regions of high elongational and shear stress.
13. A screw extruder as in claim 12 wherein:
said adjacent dispersive regions of said fluted mixing section include a plurality of barrier flights which create multiple regions of high elongational and shear stress.
14. A screw extruder as in claim 13 wherein:
said barrier flights include ramps which are formed on said central shaft of said extruder screw.
15. A screw extruder as in claim 14 wherein:
each of said ramps has a crest and a trough, said ramps being arranged crest to crest and trough to trough.
16. A screw extruder as in claim 14 wherein:
each of said ramps has a crest and a trough, said ramps being arranged crest to trough.
17. The screw extruder of claim 13 wherein:
said barrier flights are bounded by main flight sections and mixing flight sections.
18. The screw extruder of claim 17 wherein:
said mixing flight sections are formed with wedge-shaped profiles to further create regions of high elongational and shear stress.
19. The screw extruder of claim 17 wherein:
said mixing flights include distributive mixing elements.
20. The screw extruder of claim 13 wherein:
said barrier flights of said fluted mixing section include a plurality of triangular wedge shapes which are formed on said central shaft.
21. The screw extruder of claim 13 wherein:
said barrier flights include distributive mixing elements.
22. The screw extruder of claim 12 wherein:
said fluted mixing section includes a plurality of semi-circular channels.
23. The screw extruder of claim 1 wherein:
said at least one extruder screw is a pair of twin extruder screws.
24. The screw extruder of claim 23 wherein:
said twin extruder screws rotate in counter directions.
25. The screw extruder of claim 23 wherein:
said twin extruder screws rotate in the same direction.
26. The screw extruder of claim 1 wherein:
said at least one extruder screw includes modular sections which are arranged on a central shaft to provide variable mixing characteristics.
27. The screw extruder of claim 1 wherein:
said at least one screw right is a plurality of screw fights which are symmetrically arranged about a central shaft to balance deflection forces.
28. The screw extruder of claim 27 wherein:
the number of screw flights is a variable selected from the group consisting of two, three, four, five, and six.
29. A screw extruder comprising:
a barrel, said barrel having a bore defining an inner surface; and
at least one extruder screw, positioned within said bore, said at least one extruder screw including a central shaft and a plurality of dispersive elements, said dispersive elements being configured and positioned on said at least one extruder screw to form a plurality of progressively narrowing passages through which material is forced into a plurality of regions of high elongational and shear stress.
30. The screw extruder of claim 29 wherein:
said dispersive elements are positioned in a helical configuration.
31. The screw extruder of claim 29 wherein:
said screw extruder includes a slip ring and at least one stationary ring.
32. The screw extruder of claim 29 wherein:
said screw extruder includes a non-return valve.
33. The screw extruder of claim 31 wherein:
said slip ring includes a plurality of dispersive elements.
34. The screw extruder of claim 31 wherein:
said stationary ring includes a plurality of dispersive elements.
35. A method of extruding material from a screw extruder comprising the steps of:
providing a screw extruder including a barrel having input and output ends, a bore defining an inner surface, and an extrusion die at said output end;
providing at least one extruder screw positioned within said bore, each screw including a central shaft, said at least one extruder screw further including a plurality of dispersive mixing elements which interact with said inner surface of said barrel to form progressively narrowing passages through which material is forced into multiple regions of high elongational and shear stress;
introducing extrusion material into said input end of said barrel;
rotating said at least one screw to force said material through said dispersive mixing elements where said material passes through multiple regions of high elongational and shear stress; and
conveying said material towards said extrusion die at said output end to be shaped.
36. The method for extruding material from a screw extruder of claim 35 wherein:
said dispersive mixing elements are selected from a group consisting of tapered slots formed in said flights, fluted sections with ramped barrier flights formed on the central shaft, fluted sections with barrier flights formed on said central shaft which are triangular wedge shapes, barrier flights with triangular profile, diamond shaped protrusions, triangular pins, and protrusions which are positioned on a stationary ring and protrusions which are positioned on the interior of a slide ring.
TECHNICAL FIELD
The present invention relates generally to machines for extrusion of materials and more particularly to screw extruders adapted for use with plastics and plastic-like materials. The inventor anticipates that primary application of the present invention will be for the manufacture of color concentrates, polymer blends, and polymer alloys.
BACKGROUND ART
A screw extruder is a machine in which material, usually some form of plastic, is forced under pressure to flow through a contoured orifice in order to shape the material. Screw extruders are generally composed of a housing, which is usually a cylindrical barrel section, surrounding a central motor-driven screw. At a first end of the barrel is a feed housing containing a feed opening through which new material, usually plastic particles, is introduced into the barrel. The screw contains raised portions called flights having a larger radial diameter than the screw's central shaft and which are usually wrapped in a helical manner about the central shaft. The material is then conveyed by these screw flights toward the second end of the barrel through a melting zone, where the material is heated under carefully controlled conditions to melt the material, and then passes through a melt-conveying zone, also called a pumping zone. The melted plastic is finally pressed through a shaped opening or die to form the extrudate.
Besides conveying material toward the die for extrusion, the screw is depended upon to perform mixing of the feed material. Very generally, mixing can be defined as a process to reduce the non-uniformity of a composition. The basic mechanism involved is to induce relative physical motion in the ingredients. The two types of mixing that are important in screw extruder operation are distribution and dispersion. Distributive mixing is used for the purpose of increasing the randomness of the spatial distribution of the particles without reducing the size of these particles. Dispersive mixing refers to processes that reduce the size of cohesive particles as well as randomizing their positions. In dispersive mixing, solid components, such as agglomerates, or high viscosity droplets are exposed to sufficiently high stresses to cause them to exceed their yield stress, and they are thus broken down into smaller particles. The size and shape of the agglomerates and the nature of the bonds holding the agglomerate together will determine the amount of stress required to break up the agglomerates. The applied stress can either be shear stress or elongational stress and generally, elongational stress is more efficient in achieving dispersion than is shear stress. An example of dispersive mixing is the manufacture of a color concentrate where the breakdown of pigment agglomerates below a certain critical size is crucial. An example of distributive mixing is the manufacture of miscible polymer blends, where the viscosities of the components are reasonably close together. Thus, in dispersive mixing, there will always be distributive mixing, but distributive mixing will not always produce dispersive mixing.
In extrusion processes, the need for good dispersive mixing is often more important than for distributive mixing. This is particularly true in the extrusion of compounds which contain pigments which must be uniformly mixed or small gage extrusion such as spinning of fibers or extrusion of thin films.
In screw extruders, significant mixing occurs only after the polymer has melted. Thus, the mixing zone is thought of as extending from the start of the melting zone to the end of the extrusion die. Within this area there will be considerable non-uniformities in the intensity of the mixing action and the duration of the mixing action, both in the barrel section and in the extrusion die. In molten polymer, the stress is determined by the product of the polymer melt viscosity and rate of deformation. Therefore, in general, dispersive mixing should be done at as low a temperature as possible to increase the viscosity of the fluid, and with it, the stresses in the polymer melt.
Fluid elements are spoken of as having a "mixing history", which refers to the amount of elongational and shear stress to which it has been exposed, and the duration of that exposure. A polymer element that melts early in the mixing zone process will have a more significant mixing history than one that melts near the end of the melting zone.
Generally, in an extruder with a simple conveying screw the level of stress or the fraction of the fluid exposed to it is not high enough to achieve good dispersive mixing. Distributive mixing is easier to achieve than dispersive mixing, but unmodified screws have also been found to produce inadequate distributive mixing for many applications. Therefore, numerous variations in screw design have been attempted in prior inventions to increase the amount of distributive or dispersive mixing in screw extruders. These devices usually contain a standard screw section near the material input hopper, and one or more specially designed sections to enhance mixing. These mixing sections naturally fall into the categories of distributive and dispersive mixing elements.
Varieties of distributive mixing elements are shown in FIGS. 2A-F. Practically any disruption of the velocity profiles in the screw channel will cause distributive mixing. Thus even simple devices, such as the placement of pins (see FIG. 2A) between the screw flights can enhance distributive mixing. FIG. 2B shows the well-known Dulmage mixing section, in which the polymer flow is divided into many narrow channels, which are combined and divided again several times. The Saxton mixing section (FIG. 2C) and the "pineapple" mixing section (FIG. 2D) are used to produce similar results. FIG. 2E shows a screw which has slots cut into the flights. A variation called the Cavity Transfer Mixer is shown in FIG. 2F. There are cavities both in the rotor and the barrel. This type of device reportedly performs both dispersive and distributive mixing.
In addition to these devices, static mixers are often used to divide and recombine the melt stream to intermingle the material and eliminate variations in temperature, composition and mixing history. These generally do not provide regions of high stress, and are thus mostly used for distributive mixing.
The devices shown in FIGS. 2A-F have been primarily classified as distributive mixers because their action is mainly to spatially redistribute material without subjecting it to regions of high shear stress. The variations shown in FIGS. 2G-J are designed to include high shear stress regions and thus perform dispersive mixing.
The most common dispersive mixing section is the fluted or splined mixing section in which one or more barrier flights are placed along the screw so that material has to flow over them. In passing through the barrier clearance, the material is subjected to a high shear rate which acts to break up agglomerates. One such device is the Maddock mixing section, which is shown in FIG. 2G. The Maddock has longitudinal splines that form a set of semicircular grooves. Alternate grooves are open on the upstream and downstream ends. Material that enters the inlet grooves is forced to pass over the mixing flights, which are shown as cross hatched areas, before reaching the outlet grooves. While passing over the mixing flights, the material is subjected to high shear stress. The disadvantage of this type of mixing element is that it reduces the pressure at the output side of the mixing section and thus reduces the output of the extruder. Also there may be regions in which material may stagnate since the grooves have constant depth in a longitudinal direction. This makes it less suitable for materials of limited thermal stability.
FIG. 2H shows the Egan mixing section, which has splines that run in a helical direction to form channels separated by mixing barriers. These channels can have a gradually reducing depth, tapering to zero depth at the end of the mixing section, which reduces the chance of stagnation points. This helical design consumes less pressure than the Maddock style, thus producing less reduction in extruder output.
A blister ring, shown in FIG. 2J, is simply a cylindrical section on the screw that has a small radial clearance, through which all material must pass. This can cause a large pressure drop on the output side of the blister ring, resulting in a significant reduction in overall extruder output.
FIG. 2K reproduces in part FIG. 2 from U.S. Pat. No. 5,356,208 to Tadmor. A portion of the screw surface 33 gradually increases in a radial distance, making a smooth transition to radial maximum at the tip 50. This tip 50 is also rounded and the screw surface 33 then gradually and smoothly decreases in radius to a minimum near the leading wall 58 of a scraping flight 75. The entire cycle from radial minimum through maximum and back to minimum takes place in nearly 180 degree of angular rotation. This increase in the radial distance of the screw surface portion has the necessary effect of decreasing the depth of the screw channel. The volumetric capacity of the screw extruder is decreased when the channels are decreased in depth, thus efficiency of output is reduced. Also, although the Tadmor invention may produce some shearing action at the tips, there is no strong elongational flow due to the very gradual reduction in channel depth. As discussed above, elongational stress is much more efficient than shear stress in breaking down agglomerates of material. The Tadmor invention also uses a conventional helix angle of 17-18 degrees. As will be discussed later, the present invention preferably uses a much larger helix angle, which produces much more effective dispersive mixing and much higher output.
Screw extruders can have more than one central screw. Twin-screw extruders may operate with two screws that may either rotate in the same direction, or they may be counter-rotating. There are some machines that use more than two screws.
In counter-rotating twin-screw extruders, dispersive mixing primarily occurs in the intermeshing region between the screws. This action is similar to that in a two-roll mill. This configuration has the disadvantage that the mixing action creates substantial separating forces on the screws. These forces can push the screws against the barrel, if these forces grow too great. This can cause wear on the screws and the barrel, thus the screw speed has to be kept low, with resulting decrease in the throughput of the extruder.
In intermeshing co-rotating twin-screw extruders, the screw surfaces in the intermeshing region move in opposite directions. As a result, most of the material bypasses the intermeshing region and moves from one screw to the other repeatedly.
Some twin screw machines have kneading blocks included to increase dispersive mixing. These kneading blocks are most commonly flat paddles of roughly elliptical shape which are stacked on a central shaft, but offset at varying angles. Each paddle on the shaft is paired with a corresponding paddle on the second shaft. The shafts usually both rotate in the same direction but with the angular orientation of the paddles staggered at a certain angle. We can consider the elliptical paddle shapes to have a major and a minor axis with a "tip" on each end of the major axis and a "mid-point" at each end of the minor axis. At one point in the rotation cycle, a tip of a paddle on the first shaft, when horizontally oriented, will nearly contact the midpoint of a paddle on the second shaft, whose tip will then be vertical. As this second, vertical tip rotates towards horizontal, the first tip traces along the elliptical outline of the second paddle, thus "wiping" it. At a further point in the rotation cycle, the second paddle wipes the outline of the first. This wiping action keeps material from stagnating or collecting on the paddle edges. It also imposes constraints on the shapes of the paddles, as the travel of the tip of the neighboring paddle defines the outline of the paddle itself. Although this configuration of paddles can produce fairly good elongational stress in material, the above constraint on the shape of the paddles prevents variations in design, which may produce even better elongational stress regions.
In general, twin-screw extruders are considered to be better at dispersive mixing than single-screw extruders. However for a given capacity, multi-screw machines are usually considerably more costly than single-screw extruders.
For improved mixing to occur, there are several important aspects to be considered. In dispersive mixing, it is the passage of material through a region of high stress that produces the desired breakdown of agglomerates. A single pass through a high stress region will likely achieve only a single rupture of the agglomerate. To achieve a fine scale of dispersion, multiple passes and ruptures ay be necessary. Also, for efficient dispersive mixing, stresses in the high stress region should have a strong elongational component, as well as a shear component. For efficient operation of the extruder as a whole, a low pressure drop across the mixing section is desirable. It is also important to combine dispersive and distributive mixing to achieve a more uniform overall mixture. Some distributive mixing occurs whenever dispersive mixing is done, but by deliberately combining distributive elements with the dispersive elements, chances are improved that all fluid elements will pass through the high stress region, preferably many times, for proper dispersion.
To make sure that all agglomerates and droplets pass through high stress regions at least once, the flow rate through the high stress regions must be large enough compared to the overall forward flow rate. This can be done by designing the number of high stress regions, their length and the size of the gap through which material will pass. It is also preferable that there be more than one high stress region, and that these regions are symmetrically arranged around the circumference of any section along the length of the screw, so that forces will be balanced and the possibility of deflection of the screw will be minimized. To reduce pressure drop in the mixing section, it is desirable to have the high stress regions in a forward helical orientation, which can be done by a continuous forward helix or in a stepped forward helix with kneading disks.
Another consideration which makes improved dispersive mixing desirable, is that as the size of unmelted particles is reduced by better dispersive mixing, these particles are more easily melted. Thus if more efficient dispersive mixing can be generated in the melting zone of the extruder, it can speed up the melting process and the required length of the melting zone can be decreased. This would allow more compact and efficient extruders to be designed.
For the foregoing reasons, there is a great need for a screw extruder which provides better dispersive mixing than in presently available extruders.
DISCLOSURE OF INVENTION
Accordingly, it is an object of the present invention to provide a screw extruder which provides improved dispersive and distributive mixing.
Another object of the present invention is to provide a screw extruder in which material is repeatedly passed through regions of high stress for better break-down of agglomerates into smaller particles.
And, another object of the invention is to provide a screw extruder having a number of high stress regions which produce high elongational stress as well as shear stress.
Yet another object of the invention is to provide a single screw extruder which is less costly to manufacture for its capacity than a multi-screw extruder, but which provides dispersive mixing comparable or better than conventional multi-screw extruders.
A further object of the present invention is to provide a screw extruder in which the high stress regions do not produce a large pressure drop which may impede overall throughput.
A still further object of the present invention is to provide a screw extruder that has symmetrically balanced high stress regions which avoid possible deflection of the central screw.
A yet further object of the present invention is to provide a multi-screw extruder that provides improved dispersive mixing over present multi-screw extruders.
An additional object is to provide a screw extruder with modular, exchangeable mixing sections.
A further additional object is to provide a screw extruder with dispersive mixing elements which can be used in injection and blow molding operations and which provides improved dispersive and distributive mixing.
Briefly, one preferred embodiment of the present invention is a screw extruder having a barrel which has a bore defining an inner surface and one or more extruder screws, positioned within the bore. The extruder screw or screws include a central shaft and one or more screw flights. The extruder screw or screws further including one or more dispersive mixing elements which interact with the inner surface of the barrel to form one or more progressively narrowing passages through which material is forced into multiple regions of high elongational and shear stress.
A second preferred embodiment of the present invention is a screw extruder having a barrel, the barrel having a bore defining an inner surface; and one or more extruder screws, positioned within the bore. The extruder screw or screws include a central shaft and a number of dispersive mixing elements which are configured and positioned on the extruder screw or screws to form a number of progressively narrowing passages through which material is forced into multiple regions of high elongational and shear stress.
Also presented is a method of extruding material using a screw extruder having pushing face profiles that form progressively narrowing passages in conjunction with barrel inner surfaces to provide improved dispersive mixing.
The described versions of the present invention have many advantages which address the above-mentioned objects. One such advantage of the present invention is that it provides both good dispersive and good distributive mixing.
Another advantage of the invention is that it provides regions of both high elongational and shear stress.
A further advantage of the present invention is that material is repeatedly passed through regions of high stress for improved breakdown of material agglomerates.
Yet another advantage of the invention is that it may be used in a single-screw extruder, which is less costly for its capacity than a comparable twin screw extruder, yet may provide comparable or better dispersive mixing.
A still further advantage of the present invention is that the high stress regions may be in a forward helical orientation, thus reducing pressure drop in the mixing section, and therefore enhancing overall efficiency and throughput.
A yet further advantage of the present invention is that the high stress regions are symmetrically arranged around the central screw, so that deflection is minimized.
An additional advantage of the present invention is that the improved dispersive mixing process can enhance melting, so that if dispersive mixing elements are located in the melting zone of an extruder, it can speed up the melting process and reduce the length required for melting the plastic.
A yet further advantage of the present invention is that the dispersive mixing elements can be used in a screw extruder used for injection molding, compression molding and blow molding operations to provide improved dispersive and distributive mixing.
These and other objects and advantages of the present invention will become clear to those skilled in the art in view of the description of the best presently known mode of carrying out the invention and the industrial applicability of the preferred embodiment as described herein and as illustrated in the several figures of the drawings.
BRIEF DESCRIPTION OF THE DRAWINGS
The purposes and advantages of the present invention will be apparent from the following detailed description in conjunction with the appended drawings in which:
FIG. 1 is an overhead view of a simplified screw extruder, in which a portion of the barrel has been cut-away;
FIGS. 2A-K illustrate a variety of prior art mixing sections for distributive and dispersive mixing;
FIG. 3 shows an isometric view of an extruder screw according to one embodiment of the present invention;
FIG. 4 illustrates a cross-sectional view taken through the screw extruder along line A--A in FIG. 1;
FIGS. 5A-F shows a variety of flight face profiles which embody the present invention;
FIG. 6 illustrates a plan view of a prior art mixing section corresponding to a detailed view of the prior art mixing section seen above in FIG. 2G;
FIG. 7 shows a plan view of an improved mixing section according to an embodiment of the present invention;
FIG. 8 is a side view of a screw extruder with a portion of the barrel removed to expose an extruder screw which has been formed according to the present invention;
FIG. 9 is a cross-sectional view taken through the screw extruder along line B--B in FIG. 8;
FIG. 10 shows a perspective view of prior art kneading paddles;
FIG. 11 illustrates a perspective view of dispersion disks, which are a preferred embodiment of the present invention;
FIG. 12 shows a perspective view of a screw extruder of which a portion of the barrel has been cut away, including dispersion disks of the present invention;
FIG. 13 illustrates a side view of prior art kneading paddles including approach angle .alpha.;
FIG. 14 shows a side view of the dispersion disks of the present invention, including approach angle .alpha.;
FIGS. 15A & B show front and side plan views of a dispersion disk of the present invention;
FIGS. 16A & B show front and side plan views of a further embodiment of a dispersion disk of the present invention;
FIGS. 17A & B illustrate front and side plan views of a prior art kneading paddle;
FIGS. 18A & B show front and side plan views of a modified kneading paddle according to the present invention;
FIG. 19 shows a side plan view of a stack of dispersion disks and interleaved transitional elements according to the present invention;
FIG. 20 shows a side plan view of an extruder screw having tapered slots formed in the screw flights according to the present invention;
FIG. 21 illustrates a side view of the mixing section of a screw extruder showing both wiping flights and mixing flights according to the present invention;
FIG. 22 shows a close-up detail view of the tapered slot between two flights according to the present invention;
FIG. 23 illustrates a view of an extruder screw, where the cylindrical surface has been "unrolled" into a flat surface, the view showing a fluted dispersive mixing section according to the present invention;
FIGS. 24A-D shows a variety of arrangements of wiping and mixing segments which insure complete wiping as according to the present invention, where the cylindrical surface has again been "unrolled" into a flat surface;
FIG. 25 illustrates a perspective view of an extruder screw where the cylindrical surface has been "unrolled" into a flat surface, the view showing a fluted dispersive mixing section according to the present invention;
FIG. 26 shows a perspective view of another embodiment of a extruder screw where the cylindrical surface has been "unrolled" into a flat surface, the view showing a fluted dispersive mixing section according to the present invention;
FIG. 27 illustrates a perspective view of another embodiment of a extruder screw where the cylindrical surface has been "unrolled" into a flat surface, the view showing a fluted dispersive mixing section according to the present invention;
FIG. 28 shows a perspective view of another embodiment of a extruder screw where the cylindrical surface has been "unrolled" into a flat surface, the view showing a fluted dispersive mixing section according to the present invention;
FIG. 29 illustrates a side view of a mixing section of an extruder screw having semi-circular channels, according to the present invention;
FIG. 30 shows an unrolled view of a mixing section of an extruder screw having semi-circular channels, according to the present invention;
FIG. 31 illustrates a side view of a mixing section of an extruder screw including a number of dispersive mixing elements, according to the present invention;
FIG. 32 shows a side view of a mixing section of an extruder screw including a number of another variation in dispersive mixing elements, according to the present invention;
FIG. 33 illustrates a side cut away view of an extruder screw which is used in an injection molding operation, showing a non-return valve in open valve position, according to the present invention;
FIG. 34 shows a cross-sectional view of the extruder screw taken through line 34--34 in FIG. 33;
FIG. 35 illustrates a side cut away view of an extruder screw which is used in an injection molding operation, showing a non-return valve in closed valve position, according to the present invention;
FIG. 36 shows a detail cut-away view of a slide ring used with an extruder screw in an injection molding operation; and
FIG. 37 illustrates a front view of the slide ring seen in side view in FIG. 36.
BEST MODE FOR CARRYING OUT THE INVENTION
A preferred embodiment of the present invention is a screw extruder having improved dispersive mixing. As illustrated in the various drawings herein, and particularly in the view of FIG. 1, a form of this preferred embodiment of the inventive device is depicted by the general reference character 10.
FIG. 1 illustrates the major portions of a screw extruder 10, having a central longitudinal axis 11, and which also has an input end 12 and an output end 14. Generally, for convenience of reference, the terms "downstream" shall refer to those ends closest to the output portion of the screw extruder and the term "upstream" shall refer to those ends farthest away from the output. The downstream direction is indicated by a large arrow, which shows the direction of material flow. The screw extruder 10 has a barrel 18. The input end 12 includes an input hopper 20 for feeding in material, and an extrusion die 22 on the output end 14. A portion of the barrel 18 has been cut away to show the barrel wall 24, and an inner bore 26. Positioned within the bore 26 is an extrusion screw 28 having screw flights 30. Although this version of the preferred embodiment has a single screw, it is to be understood that the screw extruder could contain two or more screws.
FIG. 2 illustrates a variety of prior art mixing sections of extruder screws, as discussed above in the Background Art section.
FIG. 3 illustrates an isometric cross-sectional view of one version of a mixing section of an extruder screw 28 used in the present invention. The general reference character 31 designates the mixing section of the extruder screw 28. This mixing section can be an integral portion of the overall screw 28, or it may be a modular section which is combined with other modular sections upon a central shaft to provide varying characteristics which can be customized for different materials and applications. In FIG. 3, an optional central bore 32 is shown in phantom line for the case where mixing section 31 is a modular section which can be stacked upon an independent central shaft. This mixing section is defined as having a length (L) 33. The mixing section 32 includes a central shaft 34 and screw flights 30, which are used to mix the material as well as convey it forward. A screw diameter (D) 35 is defined as the tip to tip distance between flights 30 when positioned on opposite sides of the central shaft 34. An arrow is included to indicate the direction of rotation. The flights 30 include the forward pushing face 36, and the rear face 38. Reference character 40 will be used to refer to the cross-sectional profile of the flight 30. As will be seen below, it is the shape of this profile 40 that produces the multiple regions of high elongational and shear stress, which are crucial in producing increased dispersive mixing. In this version of the preferred embodiment, slots 42 have been provided to increase distributive mixing. These slots 42 are optional, and their size and placement are subject to considerable variation, as will be apparent to one skilled in the art. Additionally many other distributive mixing devices may be used, including, but not limited to, pins or protrusions which could be round, square, diamond shape or irregular, secondary flights with interruptions, and changes in channel depth or width (defined below).
FIG. 4 shows a cross-sectional view through the screw extruder 10 along line A--A in FIG. 1. Barrel 18 includes the barrel wall 24 surrounding a central bore 26 which is defined by the barrel inner surface 44. In this version of the preferred embodiment, the central bore 26 is cylindrical and accommodates a single extruder screw 28, but it should be understood that the present invention can be used with two or more extruder screws, in which case, the bore 26 cross-section may resemble multiple overlapping circles or ellipses.
The flights 30 of the screw 28 are shown, and in this version of the preferred embodiment there are four flights which are positioned at 90 degree intervals around the circumference of the central shaft 34. It is to be understood that other numbers of flights such as two, three, five, six, etc. may be used, and their positions around the circumference of the shaft 34 is likewise variable. It is desirable, however, that the flights 30 be symmetrically arranged around the shaft 34 circumference in order that the forces on the shaft 34 are balanced and deflection is minimized. The front pushing faces 36 and the rear faces 38 of the flights 30 are shown, as well as the flight profile 40. The front pushing faces 36 and the inner surface of the barrel 44 define a progressively narrowing passage 46 into which the material in the bore 26 moves. The rotational movement of the screw 28 causes the material to enter the large end of the passage 46 and to be squeezed as the passage 46 narrows into high stress
regions 48, which are created between the flight tips 50 and the barrel inner surface 44. The reducing cross sectional area of the progressively narrowing passage 46 causes an increase in the average flow velocity. Thus the high stress regions 48 develop both elongational and shear stresses which are important in providing increased dispersive mixing. The action of the screw 28 rotation ensures that material agglomerates passes through many of these high stress regions 48, and thus very high quality dispersive mixing may be obtained.
The distance between the barrel inner bore 44 and the central shaft 34 will define the channel height (H) 52. The distance between the flight tip 50 and the barrel inner bore 44 is defined as the radial flight clearance (.delta.) 54. The ratio of the flight clearance 54 to the channel height 52 is defined as .delta./H. The distance between the forward pushing face 36 of one flight 30 and the rear face 38 of the next flight 30 on the extruder screw measured circumferentially will be referred to as the channel width 56. Additionally, the width of the tip of the flight (w.sub.f) will be designated as 58, although it is quite possible that this w.sub.f 58 may be zero, depending on the flight face profile 40. Indeed, the profile shown in FIG. 4 is a smooth curve at the tip 50 and thus the flight tip width 58 is zero in this case.
FIG. 5 shows a variety of pushing face profiles 40 of the screw flights 30 which can be used in conjunction with the barrel wall 24 to produce progressively narrowing passages 46 to force material into high stress regions 48. It should be understood that many other variations in profile are possible, and the present invention is not limited to the profiles shown.
The versions of the preferred embodiment discussed so far have had a "positive helix angle" or forward flighted configuration. In a forward flighted screw, the pushing flight face moves the material forward toward the output end of the extruder. Returning to FIG. 1, a positive helix angle (.phi.) 60 can be seen as measured between the face of a screw flight 30 and a vertical reference line 63. It is also possible to have a rearward flighted configuration. In this case, the pushing flight face moves the material backward toward the feed opening of the extruder. It is also possible to have a neutral flight configuration. In this case, the flight angle is ninety degrees, and the pushing flight face moves the material only in the circumferential direction.
In a screw extruder 10, it is possible to have a mixing section that contains a negative helix angle. The sections of the screw which are upstream from the mixing section may still have a positive helix angle in order to make sure that the material is conveyed toward the output end 14 effectively. Thus it should be understood that the present invention 10 may be practiced with variations which include negative helix angles. It is anticipated that the extruder screw 28 may be made to be "modular", having a central shaft upon which mixing sections of varying geometry may be stacked to be adaptable to various materials and operations.
One type of modular mixing section which may be employed is the Maddock mixing section, which was discussed in the background art section and shown in FIG. 2G. FIG. 6 PRIOR ART shows a Maddock mixing section in more detail. The Maddock has longitudinal splines that form a set of semicircular grooves. Alternate grooves are open on the upstream and downstream ends. Material that enters the inlet grooves 70 is forced to pass over the mixing barrier flights 72, which are shown as cross hatched areas, before reaching the outlet grooves 74. While passing over the mixing flights 72, the material is subjected to high shear stress. This can produce some dispersive mixing, but this prior art mixing section only subjects material to a single pass through the high stress region.
In contrast, FIG. 7 shows another preferred embodiment of the present invention in which a multi-flight mixing section 80 can be incorporated in a modular fashion to a screw extruder. Material is introduced through the inlet grooves 70 as before, but must pass over a series of mixing barrier flights 82 before reaching the outlet grooves 74. In passing over this series of flights 82, the material must repeatedly pass through high stress regions. Additionally, the barrier flights 82 can include a number of progressively narrowing passages 46 to produce regions of high elongational stress 48, thus achieving much better dispersive mixing.
It should be understood that the use of multiple mixing barriers can be used in many different configurations to improve dispersive mixing from that achieved by the prior art. A further example would be to improve the blister ring mixer seen in FIG. 2J of the prior art by using a series of small rings with wedge-shaped leading edges to create multiple high stress regions. Additionally, similar modifications can be made to all fluted mixers such as the Egan, (FIG. 2H), the Zorro, the Troester, etc.
In designing extruder screw mixing sections for good dispersive mixing, there are several variables which can be adjusted to optimize results. According to Tadmor and Manas-Zloczower, (Z. Tadmor and I. Manas-Zloczower, Advances in Polymer Technology, V.3, No.3, 213-221 (1983)), the passage distribution function can be written as: ##EQU1## where k is the number of passes through the clearance, the dimensionless time .lambda.t.sub.r /t is the ratio of the residence time t.sub.r and the mean residence time of the control volume t. The residence time for a Newtonian fluid can be approximated as follows: ##EQU2## where z is the helical length of the screw section considered, V.sub.bz the down-channel barrel velocity, and r the throttle ratio (pressure flow rate divided by drag flow rate). The mean residence time can be determined from: ##EQU3## where W is the channel width, H the channel depth, .delta. the radial flight clearance, and w.sub.f the flight width. The dimensionless time can be written as: ##EQU4## where L is the axial length corresponding to down-channel distance z. The fraction of the fluid experiencing zero passes through the clearance is:
The G.sub.0 fraction should be low to make sure that most of the fluid experiences at least one or more passes through the clearance. In a simple conveying screw the G.sub.0 fraction is usually around 0.9, which means that most of the fluid passes through the extruder without ever passing through the clearance. The expressions above can be used to determine the minimum value that will yield a G.sub.0 less than 0.01, meaning that less than one percent of the fluid will not pass through the clearance at all. This is achieved when the dimensionless time .lambda.>4.6. For certain values of L, H. W, r, .phi., w.sub.f we can then determine how large the flight clearance .delta. has to be to make .lambda.>4.6 or G.sub.0 <0.01.
When L=3W, r=0, and .phi.=17.67.degree., the ratio of .delta./H has to be about 0.8 to achieve a G.sub.0 <0.01. Clearly, with such a high ratio of .delta./H it will be almost impossible to create large stresses in the clearance and to accomplish effective dispersive mixing. From equation 4 it is clear what geometrical variables we have to change to achieve a low G.sub.0 fraction at a small clearance. We can do this by 1) increasing L, the length of the mixing section, 2) increasing .phi., the helix angle, 3) reducing w.sub.f, the width of the flight, and 4) increasing the number of flights.
If the helix angle is increased from 17.67 to 60 degrees with the other values being the same, the .delta./H ratio has to be about 0.35 or greater for the G.sub.0 fraction to be less than 0.01. This value is still rather larger, but substantially better than 0.8. The .delta./H ratio can be further reduced by increasing the length of the mixing section or reducing the flight width or by increasing the helix angle even more. This procedure allows a first order determination of the design variables. Further refinement of the initial values can be obtained from computer simulation.
It is estimated that in prior art screw extruders with a simple conveying screw, G.sub.0, the fraction of material that does not pass through the clearance, is typically 0.9. This means that a great deal of material never passes through high stress regions, and thus dispersive mixing is poor.
In the present invention, it is desired that G.sub.0 is less than 0.01, and therefore greater than 99% of the material will pass through a region of high stress. It is anticipated from the above formulas that for this value of G.sub.0, in order to achieve a .delta./H ratio in a reasonable range of 0.05 to 0.3, the helix angle (.phi.) will lie in the range of -90.degree. to -30.degree. and +30.degree. to +90.degree., the length of the mixing section (L) will lie in the range of 1 to 20 times the bore diameter, and the width of the screw flight at the tip (w.sub.f) will lie in the range of 0 to 0.5 times the diameter, D.
It should be understood that although the preferred range of helix angles is -90.degree. to -30.degree. and +30.degree. to +90.degree., values in the range from +30.degree. to -30.degree. will work as well.
Multiple passes through a high stress region are necessary to break down agglomerates. Thus even in mixing sections with very low values for G.sub.0, there is no assurance that good dispersive mixing will be achieved. For example, in the Maddock prior art mixer, all the material has to pass through the high stress region, but it only passes through this region once, which is insufficient.
Another parameter of interest is the ratio of flight clearance to the screw diameter or .delta./D. This gives an indicator of how much material flows through the high stress regions, and thus is proportional to how well the material is dispersively mixed. The higher this number is, the better the dispersion can be expected. For prior art single screw extruders, this .delta./D figure is typically 0.001, and for prior art twin screw extruders, this .delta./D figure improves to 0.005. In contrast, the .delta./D value for the various preferred embodiments of the present invention is 0.005 to 0.250. When the .delta./D number becomes too high the stresses that will be generated may be too low to accomplish dispersive mixing. The clearance should be small enough to be able to generate high enough stresses but large enough to allow sufficient material to flow through it.
The flights of a screw extruder can convey material in the downstream direction and can also serve to prevent material from building up on the walls of the extruder barrel. This latter function is known as "wiping" and it is possible to have elements that perform this wiping separately from the function of conveying material, although typically the functions are combined. It is also possible that wiping and conveying can be performed by one set of screw flights, while mixing is done by a second set of flights. This second set of flights may be in a separate modular section, or in the same section by incorporating this second set of flights between the conveying/wiping flights. The mixing flights do not have to have the same helix angle as the conveying/wiping flights, and indeed it may be beneficial that they be different. The helix angle of the conveying flights can be chosen to give the best pumping action, while the helix angle for the mixing flights can be chosen to give the best dispersive mixing action. A functional separation of the two types of flights can thus be achieved, allowing optimization of the overall performance.
FIG. 8 show a screw extruder 90 with a modified central screw 92 in which the mixing flights 94 are included between the conveying/wiping flights 96.
FIG. 9 is a cross-sectional view of FIG. 8 taken through line B--B. The profile 40 of the mixing flights 94 can be seen to produce a progressively narrowing passage 46 in the barrel 18 which again forces material into regions of high stress 48. This configuration causes enhanced material dispersion while the wiping/conveying flight 96 has been designed for optimal pumping characteristics.
As mentioned above, it is also possible to have a variation in which the helix angle is ninety degrees. This is accomplished by using straight disks which are offset from each other at varying rotational angles. For a single screw extruder, this version of the preferred embodiment is similar to kneading paddles used in twin screw extruders, but with the important difference and advantage that the geometry of the disks can be optimized for production of effective elongational and shear stress, rather than being constrained by the need to trace the outline of a second screw.
FIG. 10 Prior Art shows the configuration of the kneading paddles in one screw of a twin screw extruder as in the prior art. In contrast, FIG. 11 illustrates a second preferred embodiment 100 of the present invention for use in a single screw extruder having dispersion disks 102 aligned upon a central longitudinal axis 104. The pushing flight faces 106 have a pronounced wedge shape, and the trailing flight face 108 is flat. Stagger angle .beta. 109 is shows the rotational offset of the successive disks. In a similar manner to that discussed above in regard to the profile of the pushing flight faces 30 in the positive helix angle embodiment, the profiles of the pushing faces 106 of the dispersion disks 102 are capable of much variation, such as elliptical sections, triangles, circular sections, etc. Additionally, these dispersion disks 102 may also be modular, and may be stacked upon a central shaft to provide various mixing characteristics.
FIG. 12 shows such a version of the preferred embodiment 100 in which dispersion disks 102 having a ninety degree helix angle have been fixedly stacked upon a central shaft 110. A portion of the barrel 118 has been cut away to show the orientation of the disks 102. A central longitudinal axis 104 has again been included for easy reference. Elongational and shear stress necessary for good dispersive mixing are produced in the high str
