Patent Application
20070235907
The invention relates to a method and a system for gently manufacturing injection-molded parts out of thermoplastics at high throughputs. The invention further relates to a method and a system for gently manufacturing injection-molded parts out of thermoplastics while simultaneously incorporating additives or compounding plastic mixtures.
The invention relates further to a system that makes it possible to combine the continuous plasticization step in a multi-screw extruder with the intermittent injection molding process.
An injection molding process involving the use of single-screw extruders is known in prior art from multiple sources, e.g., from DE 1142229 and DE 4221423. Growing throughputs require increasingly large screw diameters, which results in very long extruders at a prescribed length-to-diameter ratio, and also no longer permits gentle melting above all for temperature-sensitive plastics, since the ever-diminishing surface-to-volume ratio must be offset by longer retention times and higher operating temperatures. Another disadvantage is that the compounding and degassing options are limited with a single-screw extruder, and that a given screw shank is optimally designed only for one input material.
The disadvantages described above are partially eliminated through the use of two-screw extruders, e.g., the dependence between throughput and speed enables an adjustment to several material specifications. Compounding options are also improved.
Such systems are disclosed in WO 86/06321, for example, in which a discontinuous extruder is used, or in WO 02/02293, in which a continuous two-screw extruder is used.
Despite this fact, the disadvantages described above persist in part, and it also remains necessary to use a plasticization extruder with further improved compounding and degassing options along with shorter retention times, and above all, a shorter overall length.
The object of the invention is to eliminate these disadvantages. In particular, the plasticization extruder is to be characterized by a high throughput capacity at a low overall length, good mixing and degassing characteristics, gentle treatment and short processing time.
This object is achieved via the method according to claim 1, as well as the system according to claim 9, wherein a continuously operating multi-screw extruder with screw shanks arranged on a rim line is used.
Additional embodiments are described in the specification below.
Possible thermoplastics include polycondensates, e.g., polyester, polyamide, polycarbonates and their copolymers and blends or polyolefins, e.g., polyethylene, polypropylene and their copolymers and blends. However, all thermoplastics can basically be used, as long as their rheological and thermal properties permit use in an injection molding process.
The polycondensates can include polyamides, polyester or polylactide obtained in a polycondensation reaction while separating out a low-molecular reaction product. Polycondensation can here take place directly between the monomers, or by way of an intermediate stage that is subsequently converted via transesterification, wherein transesterification can again take place while separating out a low-molecular reaction product or via ring opening polymerization.
The polyamide is here a polymer obtained via polycondensation from its monomers, either a diamine component or a dicarbonic acid component, or a bifunctional monomer with an amine and a carbonic acid end group.
The polyester here involves a polymer obtained via polycondensation from its monomers, a diol component and a dicarbonic acid component. Various, mostly linear or cyclic, diol components are used. Various, mostly aromatic dicarbonic acid components can also be used. The dicarbonic acid can be replaced by its corresponding dimethyl ester. Typical examples for polyester include polyethylene terephthalate (PET), polybutylene terephthalate (PBT) and polyethylene naphthalate (PEN), which are used either as a homopolymer or as copolymers.
The thermoplastics used can be either new or recycled.
Blends or plastic material mixtures can also be used as the thermoplastics.
The method according to the invention is also suitable for incorporating additives. The additives can be added prior to melting, either together with the polycondensate or via a separate metering and feeding device. The additives are here optimally mixed at the same time by the kneading elements during the melting process. The additives can also be added after melting in the extruder. The additives are added by means of a lateral feeding device, for example. Additional kneading or mixing elements can optionally be provided in the extruder to optimally mix the additives. In special cases, the additives can also be added only after the extruder.
Suitable additives include dyes and pigments, UV blockers, processing aids, stabilizers, impact modifiers, chemical and physical foaming agents, fillers like nucleating agents, particles that improve barrier or mechanical properties, reinforcing bodies, such as balls or fibers, along with reactive substances, for example oxygen absorbers, acetaldehyde absorbers or molecular weight-increasing substances, etc.
The additives can be added along or as part of an additive packet. Several additives are used to fabricate the additive packet. In addition, use can be made of a carrier material that allows incorporation of all additives. The additive packet can be present both as a homogenous powder or granulate, or as a simple additive mixture.
The thermoplastic is added to the process in a solid state, normally as a loose material like granulate, powder, agglomerate, flakes or chips. A granulate can here be cylindrical, globular or spherical, for example.
The thermoplastic can be dried prior to entry into the plasticization extruder. Drying can also take place at least in part outside the extruder.
A multi-screw extruder consists at least of a drive, a gearing and a processing section. The gearing is usually divided into a reduction gear and power divider, so that the individual screw shanks can be individually driven. The processing section is the part of the extruder in which the material to be processed is worked or conveyed by the screw shanks.
Filling takes place in an intake area of the processing section, e.g., via one or more intake funnels, through which one or more streams of material can be gravimetrically or volumetrically metered in. The addition of other components, e.g., additives or gases, for example for purposes of foaming, can also take place through openings in the melting area. Openings can also be used for degassing.
The processing section of the multi-screw extruder has numerous (at lest three, normally at least six, preferably at least eight) rotatable processing screws (screw shanks) that are arranged axially parallel to each other on a rim line in a casing, and exert a conveying action at least in partial areas, wherein the processing elements of adjacent screws intermesh tightly at least in part.
The casing has at least one material inlet, and at least one material outlet, as well as notches in the processing area interior walls on either side of the screw shanks that run parallel to each other and the screw shanks, in which the screw shanks are incorporated and guided, thereby defining a first partial processing area and a second partial processing area lying on one or the other side of the barrier formed by the screw shanks running parallel to each other.
In a special embodiment, the multi-screw extruder is a ring extruder in which at least six, in particular twelve, fully enclosed screw shanks are arranged in a rim or ring-like manner, wherein the interior of the screw rim incorporates a core. Such an extruder is described in DE 196 22 582, for example. Other embodiments can also be found in DE 102 11 673 and DE 10211673.
The invention enables high throughput levels:
In a generally valid correlation, throughput number Z can be expressed as a function of the processing section length L and throughput Q as follows:
Z=Q/Lˆ2.8, wherein Q is in [kg/h] and L in [m].
According to the invention, Z is greater than 800, in particular greater than 2750.
The process retention time must be kept as short as possible to gently handle the plastic. While the retention time in the buffer containers is determined by the cycle time, the retention time in the plasticization extruder and melt flow-ways can be optimized. The average retention time of the plasticized plastic in the process from the moment melting begins until the point of injection into the injection molding tool must not exceed 60 seconds plus the cycle time, in particular no more than 30 seconds plus the cycle time. The average retention time of the plasticized plastic in the processing section of the plasticization extruder from the moment melting begins until the point of exit from the processing section must not exceed 15 seconds, in particular 10 seconds.
The processing section can be followed by components for building up pressure, e.g., a melt pump, a melt filter, devices for measuring Theological properties, on-off valves and/or buffer containers.
The plasticized plastic is pressed into an injection molding tool via a melt flow-way. Injection molding tools are sufficiently known from prior art. The injected plastic melt is distributed to one or more cavities via distribution channels, and solidifies in the desired shape.
The plasticized plastic is most preferably first injected into at least one buffer container, and from there into the injection molding tool. The plasticized plastic can be prevented from flowing back into the extruder by means of an on-off valve.
The buffer container is designed in such a way that its volume increases for accommodating the plasticized plastic, and decreases again for ejecting the plasticized plastic, which can be achieved by a movable piston, for example. Ejection normally takes place more quickly than filling the buffer.
In order to ensure the continuous operation of the plasticization extruder while intermittently pressing the plasticized plastic into the injection molding tool, the screw shanks are mounted in an axially shiftable manner in a special embodiment, giving rise to a buffer area in the processing section during an axial shift toward the back. This is achieved either by:
Continuous operation can also be ensured by a second buffer container arranged between the plasticization extruder and the first buffer container.
Another possibility would be to use a downstream tandem extruder with an axially shiftable screw shank.
It is also conceivable to make the center screw described in DE 10211673 axially shiftable.
In another embodiment of the invention, the system has at least one on-off valve and at least two buffer containers, wherein the plasticized plastic is variably pressed into the buffer container via the on-off valve and either
If an injection molded part is to be fabricated out of several layers of material, several plasticization extruders can be used, wherein at least the one with the higher throughput must satisfy the requirement according to the invention. The several layers of material can here be generated simultaneously or consecutively.
One embodiment of the method provides for the manufacture of parisons for hollow items, in particular beverage bottles. In this case, for example, a polyethylene terephthalate or one of its copolymers is first preliminarily dried and then melted in a ring extruder, after which it is pressed into a plurality of cavities of at least one injection molding tool. Drying can also take place inside the extruder via degassing both before and after melting, making it possible to achieve tangible energy savings compared to conventional methods of today.
The method according to the invention can be executed by means of a co-rotating multi-screw extruder, whose processing area has a jacket surface Am and a free volume Vf, wherein the screw elements have an outer diameter Da at the screw thread, and an inner diameter Di at the screw base, and wherein at least part of the process zone has an Am3/Vf2 ratio≧1020 for two-start screw elements, and an Am3/Vf2≧2000 for three-start screw elements given a Da/Di ratio=1.3 to 1.7.
The method according to the invention can also be performed using a co-rotating multi-screw extruder, whose processing area has an intermeshing zone Az and a free volume Vf, wherein the screw elements have an outer diameter Da at the screw thread, and an inner diameter Da at the screw base, and wherein at least part of the process zone has an Az3/Vf2 ratio≧5×10−1 for two-start screw elements, and an Az3/Vf2 ratio≧2×10−2 for three-start screw elements given a Da/Di ratio=1.3 to 1.7.
In this case, a torque density (torque per screw/axial distance3) of at least 7 Nm/cm3, in particular of at least 9 Nm/cm3, is preferably introduced in the extruder.
It is particularly advantageous if the Da/Di ratio=1.5 to 1.63, and if the Az3/Vf2 ratio≧1500 for two-start screw elements and the Az3/Vf2 ratio≧3000 for three start screw elements.
Additional advantages, features and possible applications of the invention can be gleaned from the following description of embodiments according to the invention based on the drawing, wherein:
The processing section is followed by two on-off valves 19n1 to 19n2 and a buffer container 20, wherein the stream of plastic is controlled via the on-off valves as the buffer container is filled and evacuated. A melt line is used to press the plasticized plastic into an injection-molding tool 21, and distribute it to several cavities 22n1 to 22nx through distribution channels. Injection-molding tools are sufficiently known in prior art. The injected plastic melt is cooled, and solidifies in the desired shape.
With the on-off valve 19n1 closed, a buffer area must be generated inside the extruder by moving the screw shanks toward the back. To this end, the power divider is rigidly connected with the screw shanks, and moves relative to the reduction gear, which is rigidly secured to the frame 23.
The processing section is followed by an on-off valve 39n1, which can alternately route the plasticized plastic to one of the two buffer containers 4, 42. Shown as a constituent of each buffer container is a respective piston 41, 43, which can be used to increase and decrease the buffer container volume. The on-off valves 39n2, 39n3 can be used to regulate the flow of plastic while filling and evacuating the buffer container 40, 42. The plasticized plastic is pressed into the respective accompanying injection-molding tool 44, 46 via a melt line, and distributed to several cavities 45n1 to 45nx or 47n1 to 47nx via distribution channels.
| Number | Date | Country | Kind |
|---|---|---|---|
| 103-57-578.2 | Dec 2003 | DE | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/CH04/00644 | 10/28/2004 | WO | 6/6/2006 |
