Plastic article or earthenware shaping or treating: apparatus – Distinct means to feed – support or manipulate preform stock... – Extrusion shaping means
Reexamination Certificate
2001-11-30
2004-08-17
Davis, Robert (Department: 1722)
Plastic article or earthenware shaping or treating: apparatus
Distinct means to feed, support or manipulate preform stock...
Extrusion shaping means
C425S204000, C425S208000, C425S378100, C425S308000, C118S125000, C118S424000, C118S427000, C366S076100, C366S076500, C366S081000
Reexamination Certificate
active
06776596
ABSTRACT:
BACKGROUND OF THE INVENTION
1. Field of the Invention
The invention relates to a method for the manufacture of fiber-reinforced plastic compositions. It furthermore relates to an apparatus for the practice of the method.
2. Related Art
A method of this kind is disclosed in U.S. Pat. No. 6,238,733 (which claims priority from DE 198 36 787 A1), which is incorporated herein by reference in its entirety. The method and the plasticizing extruder described therein have worked well in practice. But for special applications, especially bulk material containing fibers, there is still room for improvement.
It is furthermore known that so-called rodlet granules, which at present are usually glass fiber reinforced plastic rodlets, are used for plasticate extrusion. The rodlet granules are generally 25 mm long and are melted in slow rotating single-screw extruders. Relatively large extruders are necessary for practical melting performance, because these fiber/plastic rodlets have to be fused with as little shear energy as possible, but insofar as possible by thermal conduction. This gentle melting is necessary in order to obtain the largest possible percentage of the initial fiber length. These rodlet granules are semi-manufactured products in which the fiber content is determined by the component to be manufactured. Since this semi-manufactured product is relatively expensive to produce, a method has been adopted in which so-called concentrate rodlets with the greatest possible fiber content are used. These concentrate rodlets are then mixed in the melting extruder with lower-cost plastic granules to the fiber content required in the component. This method has favorably influenced the material costs, but the extruders are not made smaller nor is the melting performance improved.
Since the melting performances required in practice involve ever larger extruders with greater material capacities, fiber damage also increases and performance decreases in brief cycling times with regard to plasticate weight tolerance and start-up.
It is furthermore known that, for the drawing of non-sticky materials of low bulk weight into the extruder, relatively great screw pitches and grooved barrels are commonly used in order to increase the thrust of material in the open feed area.
If bulk material, such as chopped fibers, for example, is to be combined with plastic melted in a separate extruder, then of course the melted plastic is fed to the bulk material downstream in the closed area by the extruder into which the fibers are fed. This has the disadvantage, however, that the fibers and the melted plastic do not mix uniformly when they meet, but form zones of fiber concentration and plastic concentration. These must then be blended downstream by mixing means in order to achieve uniform mixing and impregnation of the fibers. This signifies that a correspondingly long stay in the extruder with the mixing means is necessary, which of course signifies fiber damage and calls for large amounts of material.
In the attempt to feed melted plastic and bulk material simultaneously into the feed opening of an extruder and at the same time mix them, adhesion and therefore bridging very quickly take place, which interferes with or blocks the proportional feed.
SUMMARY OF THE INVENTION
The invention is addressed to the problem of providing a method whereby a mixing of bulk material containing fibers (fiber material) and plastic granules for the plasticate extrusion of long fiber reinforced thermoplastics (LFT) will be possible during the melting process with high production outputs and with minimized material content in the extruder system and minimized fiber damage, and to the problem of creating an apparatus with an extruder for the practice of the method, which will have an extruder housing of modified geometry as to the feed opening and the corresponding screw elements, so that the disadvantages described above are avoided.
The solution of this problem as to the method consists in melting the plastic granules at a preferably higher temperature than the necessary plasticate temperature, the molten plastic and the fiber material are combined together in the feed opening of a second extruder, the plasticizing extruder, and the fiber material is largely uniformly embedded in the molten plastic within the feed and impregnation section of the plasticizing extruder and is brought completely to the plasticate temperature in the discharge and conveyor section, the fiber material being preheated before it is combined, preferably to such an extent that it can be delivered without problems into the feed opening without any adhesion, and that the fiber material together with the molten plastic is drawn into a cylindrical bore in the feed screw from a ¼ to a ¾ wrap-around from the point of contact with the fiber material, with a diameter D enlarged by 2 to 20 mm, and preferably arranged off-center.
The solution as to the apparatus is that a simultaneously rotating dual screw extruder with preferably mop-up screw elements of great pitch is provided, which has a slot-like feed opening over a feed screw, while beginning from the feed opening and in the range of the feed screw the cylindrical bore of the feed screw is increased beginning from the infeed opening and at the feed screw the cylindrical bore increases over an arc u of ¼ to ¾ of the circumference by 2 to 20 mm, and at the end a stripping bar is disposed, and then the housing bore of the feed screw is reduced to the screw diameter d.
It is especially advantageous that a parallel double-screw extruder is used, in which a slot-shaped, relatively long feed opening is above the one screw. This screw is referred to hereinafter as the feed screw. In the area of the feed screw the diameter of the screw housing is increased so that the molten plastic ribbon lying on the screw land is spaced away from the screw housing. To prevent any material build-up on the screw land beyond the enlarged diameter of the housing, the screw bore in the housing is reduced to the screw diameter before the molten plastic ribbon comes onto it. This is achieved preferably by an inserted stripper bar. To assure that the mixing of bulk material and molten plastic ribbon or film will be as uniform as possible, the bulk material is laid out flat with no heaping approximately over the width of the plastic ribbon. In the feed area, mop-up screws of relatively great pitch are preferably used.
For the infeed of bulk material, as for example concentrate rodlets, staple fibers, sprinkle fibers, granules or other such material, the reach of the second screw in the housing bore is preferably not increased.
It is also advantageous to work with concentrate rodlets and the plastic required for the fiber concentration in the component is fused before it is combined with the concentrate rodlets or the fiber material. That is to say, the fusion heat for the admixed plastic is applied while the long fibers are not present. Therefore it is possible to use high rotary speeds and great dissipation in this range. It is also advantageous if the plastic is melted at a higher temperature than the temperature required in the plasticate and the fiber material is preheated up to the temperature at which it still does not tend to become tacky and can still be fed in without problems. Thus the heat is present in the material according to the fiber concentration in the bulk material and in the component fiber content, so that all that is needed in order to achieve fusion and equalization of temperature is the conduction of heat to the concentrate rodlets embedded in the fluid plastic.
This takes place over a relatively short distance in the extruder with a low material content. The parallel-running dual screw extruder has in this case proven advantageous. The diameter increase in the feed area is narrowed more or less far downstream into the closed area, according to the fiber structure and impregnation ratio. At the same time the enlargement of the cylinder diameter terminates preferably spirally in the sen
Davis Robert
Del Sole Joseph S
Maschinenfabrik J. Dieffenbacher GmbH & Co.
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