CA2340358A1 - Method and device for feeding and treating plastic strands - Google Patents
Method and device for feeding and treating plastic strands Download PDFInfo
- Publication number
- CA2340358A1 CA2340358A1 CA002340358A CA2340358A CA2340358A1 CA 2340358 A1 CA2340358 A1 CA 2340358A1 CA 002340358 A CA002340358 A CA 002340358A CA 2340358 A CA2340358 A CA 2340358A CA 2340358 A1 CA2340358 A1 CA 2340358A1
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- Prior art keywords
- temperature
- plastic
- extrudates
- liquid medium
- controlled
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- Abandoned
Links
- 239000004033 plastic Substances 0.000 title claims abstract description 100
- 229920003023 plastic Polymers 0.000 title claims abstract description 100
- 238000000034 method Methods 0.000 title claims abstract description 40
- 239000007788 liquid Substances 0.000 claims abstract description 67
- 238000002425 crystallisation Methods 0.000 claims abstract description 58
- 230000008025 crystallization Effects 0.000 claims abstract description 58
- 230000009477 glass transition Effects 0.000 claims abstract description 24
- 238000001816 cooling Methods 0.000 claims abstract description 17
- 238000010438 heat treatment Methods 0.000 claims abstract description 9
- 238000005453 pelletization Methods 0.000 claims description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 239000004952 Polyamide Substances 0.000 claims description 4
- 229920002647 polyamide Polymers 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 2
- 229920000098 polyolefin Polymers 0.000 claims description 2
- 239000008187 granular material Substances 0.000 abstract 1
- 238000005469 granulation Methods 0.000 abstract 1
- 230000003179 granulation Effects 0.000 abstract 1
- 238000002844 melting Methods 0.000 abstract 1
- 230000008018 melting Effects 0.000 abstract 1
- 239000008188 pellet Substances 0.000 description 12
- 239000002826 coolant Substances 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- 238000010791 quenching Methods 0.000 description 6
- 230000000171 quenching effect Effects 0.000 description 6
- 239000007921 spray Substances 0.000 description 6
- 238000001035 drying Methods 0.000 description 5
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 3
- 239000000110 cooling liquid Substances 0.000 description 3
- 150000003951 lactams Chemical class 0.000 description 3
- 238000005507 spraying Methods 0.000 description 3
- 241000195493 Cryptophyta Species 0.000 description 2
- 229920002292 Nylon 6 Polymers 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- OFOBLEOULBTSOW-UHFFFAOYSA-N Malonic acid Chemical compound OC(=O)CC(O)=O OFOBLEOULBTSOW-UHFFFAOYSA-N 0.000 description 1
- 229920000426 Microplastic Polymers 0.000 description 1
- 125000003277 amino group Chemical group 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 150000004985 diamines Chemical class 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 229910001092 metal group alloy Inorganic materials 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000006068 polycondensation reaction Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 229910021642 ultra pure water Inorganic materials 0.000 description 1
- 239000012498 ultrapure water Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
- B29B9/00—Making granules
- B29B9/02—Making granules by dividing preformed material
- B29B9/06—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/03—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the shape of the extruded material at extrusion
- B29C48/04—Particle-shaped
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/03—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the shape of the extruded material at extrusion
- B29C48/05—Filamentary, e.g. strands
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/88—Thermal treatment of the stream of extruded material, e.g. cooling
- B29C48/911—Cooling
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C35/00—Heating, cooling or curing, e.g. crosslinking or vulcanising; Apparatus therefor
- B29C35/16—Cooling
- B29C2035/1616—Cooling using liquids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
- B29K2077/00—Use of PA, i.e. polyamides, e.g. polyesteramides or derivatives thereof, as moulding material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
- B29K2995/00—Properties of moulding materials, reinforcements, fillers, preformed parts or moulds
- B29K2995/0037—Other properties
- B29K2995/0041—Crystalline
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
- Extrusion Moulding Of Plastics Or The Like (AREA)
Abstract
The invention relates to a method for feeding and treating plastic strands that are discharged from nozzles in a molten state by means of a cooling section in order to granulate the plastic strands. According to the invention, the plastic strands are partially crystallized in a temperature-adjusted liquid medium in a crystallization section once they are discharged from the nozzles, the liquid medium being maintained at a temperature above the glass transition temperature of the plastic strands. The invention further relates to a device for carrying out said method. The inventive device comprises a plastic melting device, a device for extruding the strands from nozzles, a crystallization section that is located directly downstream of the nozzles, and a granulation device that is located downstream of the crystallization section. The temperature of the crystallization section is adjusted by means of heating and/or cooling devices and is provided with temperature adjusting elements with which the temperature of the temperature-adjusted liquid medium can be adjusted to a temperature above the glass transition temperature of the plastic strands.
Description
Rieter Automatik GmbH Munich, 16 July 1999 R 28438 BD/Gt/pl/ti Method and apparatus for feeding and treating plastic extrudates The invent=ion relates to a method and an apparatus for feeding and treating plastic extrudates which emerge from dies in the form of a molten liquid, having a cooling zone for pelletizing the plastic extrudates, in accordance with the preambles of Claims 1 and 11.
A method of this type is known from document DE 43 14 162. In this method, which is known from the prior art, the plastic extrudates are only pelletized once the plastic e:~trudates have been quenched in cold water and then drained, dried and crystallized, for which purpose a device which generates a flow of cooling liquid is integrated in an outlet channel for quenching the plas~~ic extrudates emerging from a die.
Following a quenching zone of this nature, there comes a draining zone in which the cooling liquid is allowed to run freely out of the outlet channel, followed by a drying zone, in which blow nozzles blow the residual adhering cooling liquid off the plastic extrudates, the dried plastic extrudates crystallizing fully in an adjoining elongate drying zone, before subsequently being pelletized by means of a pelletizer. To carry out the method according to the prior art, an elongate running channel which is several meters long is required, in order to ensure that the different residence times in the quenching zone, the draining zone and the drying zone for crystallization of the plastic extrudates are achieved.
A known apparatus of this type has the drawback that to carry out the method a high outlay on apparatus is required, in particular because of the relatively long outlet channel in which the different phases from quenching through drying to crystallization of the
A method of this type is known from document DE 43 14 162. In this method, which is known from the prior art, the plastic extrudates are only pelletized once the plastic e:~trudates have been quenched in cold water and then drained, dried and crystallized, for which purpose a device which generates a flow of cooling liquid is integrated in an outlet channel for quenching the plas~~ic extrudates emerging from a die.
Following a quenching zone of this nature, there comes a draining zone in which the cooling liquid is allowed to run freely out of the outlet channel, followed by a drying zone, in which blow nozzles blow the residual adhering cooling liquid off the plastic extrudates, the dried plastic extrudates crystallizing fully in an adjoining elongate drying zone, before subsequently being pelletized by means of a pelletizer. To carry out the method according to the prior art, an elongate running channel which is several meters long is required, in order to ensure that the different residence times in the quenching zone, the draining zone and the drying zone for crystallization of the plastic extrudates are achieved.
A known apparatus of this type has the drawback that to carry out the method a high outlay on apparatus is required, in particular because of the relatively long outlet channel in which the different phases from quenching through drying to crystallization of the
- 2 -dried plastic extrudates have to take place before pelletizing can bE~ carried out. Other known methods pelletize the e:xtrudates in the non-crystalline amorphous state, which is reached by firstly cooling the plastic extrudates in a coolant to below the glass transition temperature, so that then they can be processed into pellets after the amorphous state has been reached under the influence of the coolant and in the presence of the coolant. For this "underwater pelletizing method", the cooling zone is considerably longer than a quenching zone in the outlet channel, in order to pelletiz.e the plastic extrudate using a cooling medium, which is usually cold water, in order to maintain the amorphous state as is also present in the molten plastic.
To carry out both methods which are known from the prior art, complex, elongate outlet channels are required which, although they do ensure exact and reproducible produca:ion of the pellets in crystalline or amorphous form, take up large amounts of space due to their length and the fact that their components have to be adapted to one another.
The object of the invention is to specify a method for feeding and treating plastic extrudates which emerge from dies in the form of a molten liquid, having a cooling zone for pelletizing the plastic extrudates, which method can make do with significantly shorter extrudate lengths prior to.pelletization and is therefore suitable for apparatus which take up little space.
This object is achieved by means of the subject matter of Claims 1 and 11. Features of preferred embodiment of the invention are disclosed in the associated sub-clairns .
To shorten the residence time in an outlet channel, the plastic extrudates are partially crystallized directly after they emerge from the dies, by means of a liquid temperature-controlled medium, for which purpose the liquid temperature-controlled medium
To carry out both methods which are known from the prior art, complex, elongate outlet channels are required which, although they do ensure exact and reproducible produca:ion of the pellets in crystalline or amorphous form, take up large amounts of space due to their length and the fact that their components have to be adapted to one another.
The object of the invention is to specify a method for feeding and treating plastic extrudates which emerge from dies in the form of a molten liquid, having a cooling zone for pelletizing the plastic extrudates, which method can make do with significantly shorter extrudate lengths prior to.pelletization and is therefore suitable for apparatus which take up little space.
This object is achieved by means of the subject matter of Claims 1 and 11. Features of preferred embodiment of the invention are disclosed in the associated sub-clairns .
To shorten the residence time in an outlet channel, the plastic extrudates are partially crystallized directly after they emerge from the dies, by means of a liquid temperature-controlled medium, for which purpose the liquid temperature-controlled medium
- 3 -is held at a temperature which is above the glass transition temperature of the plastic extrudates.
This method has the advantage that the plastic extrudates which emerge from the dies in the form of a molten liquid are not quenched with cold water, in order then to be dried, crystallized and pelletized, but rather the pl;sstic extrudates enter a relatively hot, liquid medium, the temperature of which is well controlled, thus ensuring that the temperature of the plastic extrudates does not fall below the glass transition temperature throughout an outlet channel for the plastic extrudates. As a result, partial crystallization at :Least in the surface region of the plastic extrudates occurs, so that the plastic extrudates become sufficiently strong to then be broken down into pellets in the pelletizing installation without prior drying of the plastic extrudates.
Immediately downstream of the pelletizing device there is a mixture of pellets and liquid cooling medium, from which the pellets can be separated using known means.
Since the partial crystallization at least of the surface of the plastic extrudates begins immediately after the molten plastic has emerged from the dies, the plastic extrudates can be pelletized after they have passed through a relatively short temperature-control zone.
Preferably, the length of the zone in which the plastic extrudates are held under temperature-controlled liquid medium is designed for residence times of longer than 0.5 second and shorter than 5 seconds. For this purpose, the temperature of the liquid medium is preferably controlled in such a way that a constant temperature which is above the glass transition temperature is maintained in the liquid medium. This holding of the temperature preferably takes place in a circuit for the liquid medium, in which appropriately controlled heating elements are used in the heating circuit. In this way, the temperature of the liquid medium is controlled in such
This method has the advantage that the plastic extrudates which emerge from the dies in the form of a molten liquid are not quenched with cold water, in order then to be dried, crystallized and pelletized, but rather the pl;sstic extrudates enter a relatively hot, liquid medium, the temperature of which is well controlled, thus ensuring that the temperature of the plastic extrudates does not fall below the glass transition temperature throughout an outlet channel for the plastic extrudates. As a result, partial crystallization at :Least in the surface region of the plastic extrudates occurs, so that the plastic extrudates become sufficiently strong to then be broken down into pellets in the pelletizing installation without prior drying of the plastic extrudates.
Immediately downstream of the pelletizing device there is a mixture of pellets and liquid cooling medium, from which the pellets can be separated using known means.
Since the partial crystallization at least of the surface of the plastic extrudates begins immediately after the molten plastic has emerged from the dies, the plastic extrudates can be pelletized after they have passed through a relatively short temperature-control zone.
Preferably, the length of the zone in which the plastic extrudates are held under temperature-controlled liquid medium is designed for residence times of longer than 0.5 second and shorter than 5 seconds. For this purpose, the temperature of the liquid medium is preferably controlled in such a way that a constant temperature which is above the glass transition temperature is maintained in the liquid medium. This holding of the temperature preferably takes place in a circuit for the liquid medium, in which appropriately controlled heating elements are used in the heating circuit. In this way, the temperature of the liquid medium is controlled in such
- 4 -a manner that the temperature of the medium is below 1500 of the glass transition temperature in °C and above 1000 of the glass transition temperature in °C
for the plastic e.xtrudate. In a preferred configuration of the method, the liquid medium used is hot water.
This has the advantage over methods which use cold-water quenching or cold-water cooling that there can be no problems with algae formation in the hot-water circuit, since these algae do not survive in the hot water. Furthermore, water has the advantage over other liquids that it can be prepared as ultrapure water relatively inexpensively, so that the costs of the overall method can. be kept relatively low.
In a further preferred configuration of the method, the plastic has a glass transition temperature of below 100°C. Plastics with such a low glass transition temperature have the advantage that hot water can be used as the temperature-controlled liquid medium. At temperatures above 100°C, it is preferably possible to use glycerol/water mixtures or oils as the temperature-controlled liquid media.
In a further preferred embodiment, the molten plastic contains polyamides. With polyamides of this type, which contain an NH group as the amino group, there are two plastics with entirely different glass transition temperatures. One of these plastics is polymerized by the addition of lactam to form polyamide-6 and has a glass transition temperature of between 40 and 60°C. For a plastic of this type, hot water is advantageous as the temperature-controlled liquid medium, since the deposits of lactam are lower in hot water than in cold water circuits, due to the higher solubility of lactam, and therefore there is less risk of contamination to the circuit. Furthermore, the present method yields significantly hotter partially crystal_7_ized pellets compared to the amorphous pellets produced hitherto under cold water.
These hotter pellets require shorter heating times during subsequent processing in the extraction phase
for the plastic e.xtrudate. In a preferred configuration of the method, the liquid medium used is hot water.
This has the advantage over methods which use cold-water quenching or cold-water cooling that there can be no problems with algae formation in the hot-water circuit, since these algae do not survive in the hot water. Furthermore, water has the advantage over other liquids that it can be prepared as ultrapure water relatively inexpensively, so that the costs of the overall method can. be kept relatively low.
In a further preferred configuration of the method, the plastic has a glass transition temperature of below 100°C. Plastics with such a low glass transition temperature have the advantage that hot water can be used as the temperature-controlled liquid medium. At temperatures above 100°C, it is preferably possible to use glycerol/water mixtures or oils as the temperature-controlled liquid media.
In a further preferred embodiment, the molten plastic contains polyamides. With polyamides of this type, which contain an NH group as the amino group, there are two plastics with entirely different glass transition temperatures. One of these plastics is polymerized by the addition of lactam to form polyamide-6 and has a glass transition temperature of between 40 and 60°C. For a plastic of this type, hot water is advantageous as the temperature-controlled liquid medium, since the deposits of lactam are lower in hot water than in cold water circuits, due to the higher solubility of lactam, and therefore there is less risk of contamination to the circuit. Furthermore, the present method yields significantly hotter partially crystal_7_ized pellets compared to the amorphous pellets produced hitherto under cold water.
These hotter pellets require shorter heating times during subsequent processing in the extraction phase
- 5 -and therefore reduce the energy consumption of the overall method.
A second group of polyamides is formed by polycondensation of two different monomers, such as the diamine and the dicarboxylic acid, which under condensation conditions form a polyamide-6.6 which has a glass transition temperature which is about 10°C
higher, lying between 50°C and 80°C.
In another preferred embodiment of the method, a plastic is processed wherein the molten plastic contains polyolefins. Molten plastics of this nature can likewise be processed into plastic extrudates by emerging from dies and can therefore be partially crystallized immediately after they leave the dies, according to the invention, in a heat-controlled liquid medium over a crystallization zone.
In a furl=her preferred embodiment of the method, the plastic extrudates pass through a substantially vertical crystallization zone. A
substantially vertical crystallization zone of this nature has the advantage that there is no need to take any special measures for guiding the crystallization extrudates towards the pelletizer, particularly if the plastic extrudates are guided over the crystallization zone by dropping freely.
An apparatus for feeding and treating plastic extrudates which emerge from dies in the form of a molten liquid has a crystallization zone part which is arranged immediately downstream of the dies, heating and cooling devices. preferably being provided for the crystallization zone, and a temperature-control unit, by means of which the temperature of a temperature-controlled liquid medium can be set to a temperature which is above the glass transition temperature of the plastic, is provided. For this purpose, the crysta:Llization zone part is preferably arranged substantially vertically.
Preferably, the temperature-controlled liquid medium is set to a constant initial temperature by
A second group of polyamides is formed by polycondensation of two different monomers, such as the diamine and the dicarboxylic acid, which under condensation conditions form a polyamide-6.6 which has a glass transition temperature which is about 10°C
higher, lying between 50°C and 80°C.
In another preferred embodiment of the method, a plastic is processed wherein the molten plastic contains polyolefins. Molten plastics of this nature can likewise be processed into plastic extrudates by emerging from dies and can therefore be partially crystallized immediately after they leave the dies, according to the invention, in a heat-controlled liquid medium over a crystallization zone.
In a furl=her preferred embodiment of the method, the plastic extrudates pass through a substantially vertical crystallization zone. A
substantially vertical crystallization zone of this nature has the advantage that there is no need to take any special measures for guiding the crystallization extrudates towards the pelletizer, particularly if the plastic extrudates are guided over the crystallization zone by dropping freely.
An apparatus for feeding and treating plastic extrudates which emerge from dies in the form of a molten liquid has a crystallization zone part which is arranged immediately downstream of the dies, heating and cooling devices. preferably being provided for the crystallization zone, and a temperature-control unit, by means of which the temperature of a temperature-controlled liquid medium can be set to a temperature which is above the glass transition temperature of the plastic, is provided. For this purpose, the crysta:Llization zone part is preferably arranged substantially vertically.
Preferably, the temperature-controlled liquid medium is set to a constant initial temperature by
- 6 -means of through-:flow thermostats as the heating and cooling device, which hold the temperature-controlled liquid medium at a constant initial temperature which is above the glass transition temperature and is up to 1500 of the glass transition temperature.
In a preferred embodiment of the apparatus, the pelletizing apparatus 7 is arranged immediately after the crystallizatic>n zone part 35, downstream of the crystallization zone 5 as seen in the direction of flow of the material. E'or this purpose, the crystallization zone part may be an integral component of the pelletizing device. In order to be able to start up a contact device of this nature, comprising crystallization zone and pelletizing device, a device of this nature ca.n be separated in such a way that initially, for stabilization purposes, the plastic extrudates emerging from the dies can drop freely downwards. After an automatic extrudate-cutting device has come into action, the separate parts of the device are moved together, so that stabilized plastic extrudates can at least partially crystallize immediately in th~~ area of the crystallization zone part and can be processed into a mixture of pellets and medium in the connected pelletizing device.
To control the temperature of the underside of the plastic extrudates emerging from the dies, a feedpipe is preferably arranged downstream of the dies.
This feedpipe carries the temperature-controlled liquid medium in its interior and guides the plastic extrudates on its outer surface. To supply the crystallization zone part with temperature-controlled medium, the feedpipe has a longitudinal slot which is positioned in such a way that it supplies the underside of the plastic extrudates with temperature-controlled liquid medium, by forming a film of temperature-contro7_led liquid medium on the crystallization zone part. The temperature of the top side of the plastic extrudates is controlled in the area of the crysta:Llization zone, preferably by spray nozzles which are supplied with temperature-controlled liquid medium from. a further feed pipe.
In a further preferred embodiment of the apparatus, the :Eeedpipe which guides the plastic extrudates may, instead of having a longitudinal slot at each position :For guiding a plastic extrudate, have a hole for controlling the temperature of the underside of the plastic extrudate by means of a temperature-controlled medium.
In a preferred alternative embodiment of the apparatus, the crystallization zone part can pivot between an at-rest position and a working position, the at-rest position allowing the molten plastic to emerge from the dies in the vertical direction, and the working position Feeding the plastic extrudates to a pelletizing device in partially crystallized form. This embodiment has the advantage that, despite a space-saving arrangement, the pelletizing device as an individual component may adopt a fixed position, while only the crystalli:~ation zone part is designed moveably or pivotably. The transition from the crystallization zone part to the palletizing device can be ensured by means of a short feed channel which preferably projects out of the pelletiz:ing unit.
Further advantages, features and possible applications of the invention will now be explained in more detail on the basis of an exemplary embodiment and with reference to the appended drawings, in which:
Fig. 1 shows an outline sketch of an apparatus for carrying out the method according to one embodiment of the present invention, Fig. 2 shows an outline sketch of an apparatus including a circuit for heat-controlled liquid medium according to a further embodiment of the present invention, Figs. 3 and 3B show cross-sectional views, in the longitudinal direction and perpendicular thereto, of a feedpipe leading to the crystallization zone, which on the inside -conveys a temperature-controlled and liquid medium and on the outside guides plastic extrudates, and Figs. 4A and 4B show cross-sectional views, in the longitudinal direction and perpendicular thereto, of a feedpipe leading to the crystallization zone, which on the inside carries a temperature-controlled liquid medium and on the outside guides plastic extrudates.
Figure 1 shows an outline sketch of an apparatus for carrying out the method for feeding and treating plastic extrudates 2 which emerge from dies 1 in the form of a molten liquid, having a cooling zone, for pelletizing the plastic extrudates 2, having a crystallization zone 5, for pelletizing the plastic extrudates 2, according to one embodiment of the present invention. Immediately after they emerge from the dies 1, the plastic extrudates 2 are partially crystallized in a temperature-controlled liquid medium 4 over a crystallization zone 5. For this purpose, the liquid medium 4 is held at a temperature which is above the glass tran~;ition temperature of the plastic extrudates 2 and is not quenched to below the glass transition temperature, let alone cooled 2 and held below the glass transition temperature in a long guide channel under cooling water, as is conventional in the prior art, in order to feed the plastic extrudates 2 to a pelletizing device in an amorphous state. Since in the method according to the invention partial crystallization is achieved by means of a temperature-controlled liquid medium 4 immediately after the extrudates emerge from the dies 1, the crystallization zone is extremely short, and therefore the distance between the pelletizing device and the die exit 15 is extremely short.
In a pre:Eerred apparatus for carrying out the method, as shown :in Figure 1, the crystallization zone 5 is therefore an integral component of the immediately adjoining pelletizing device. By means of a drive roller 16 and a pressure-exerting roller 17, which may be driven synchronously with the drive roller 16, the pelletizing device picks up the partially crystallized plastic extrudates 18 and feeds them to the cutting rotor 19, so that a mixture of temperature-controlled liquid medium and plastic pellets is formed in the pelletizing devices 7, and this mixture can be fed for further processing.
To control the temperature of the plastic extrudates which are to be crystallized by means of a temperature-controlled liquid medium 4, the apparatus as shown in Figure 1 has a feedpipe 13, which is explained in more detail below in conjunction with Figures 3A, 3B or 4A and 4B.
This feedpipe 13 leading to the crystallization zone 5 has an elongate slot 20, which makes it possible for the temperature-controlling liquid medium 4 to form a temperature-controlling film of liquid in the area of the crystallization zone 5. The longitudinal slot 20 may also be replaced by a series of holes, so that the temperature-contro:Lling liquid medium 4 emerges from the feedpipe 13 directly at those positions at which a plastic extrudate 2 is in each case introduced. To guide the plastic extrudates 2, the feedpipe has a structured shell on its outer circumference, in the longitudinal direction, which has circumferential channels 22, as shown in Figure 3A, or circumferential grooves 21, as shown in Figure 4A. These circumferential grooves 21 or circumferential channels 22 on the feedpipe 13 serve to guide the plastic extrudates towards the crystallization zone 5.
While the feedpipe 13 supplies the temperature-control:Ling liquid medium from one side of the plastic extrudates, referred to below as the underside, via i.ts longitudinal slot 20 or its corresponding holes, the temperature of the other side of the plastic ext:rudates, referred to below as the top side, is in this embodiment of a device for carrying out the method according to the invention controlled using temperature-controlled liquid medium coming out of spray nozzles 24. The spray nozzles 24 are supplied with temperature-controlling liquid medium 4 via a further feedline 23. The spray angle of the spray nozzles 24 can be adjusted by pivoting the feedpipe 23 about its axis 25. The angle at which the plastic extrudates 2 slide over the crystallization zone can be adjusted by pivoting the feedpipe 13 about its axis 26, since in this preferred apparatus a crystallization zone part 35 and th.e feedpipe 13 are fixedly connected to one another. In other embodiments, the angle of inclination of the crystallization zone 5 may also be adjusted independently of the position of the feedpipe 13.
In the integral embodiment shown in Figure 1, with the pelletizing device 7 and crystallization zone part 35 in a compact assembly, the feedpipe 13, the drive roller 16 and the cutting roller 19 with the cutting-edge support 27 are arranged on a frame, and the entire frame 28 can be displaced in the direction of arrow B, while a second frame 29, on which the feedline 23 and the pressure-exerting roller 17 are arranged, can be displaced in the direction of the arrow C. As a result of the frame being divided into two parts in this way, it is easier to start up the apparatus, in that the frames 28 and 29 are only moved together when the formation of plastic extrudates at the die exit 15 has stabilized. On the other hand, during the start-up phase the feedpipe 13 may be displaced in direction D with respect to the frame 28, in order to align the feedpipe 13 towards the die head 6.
Figure 2 shows an outline sketch of an apparatus for carrying out the method, including a circuit for a temperature-controlled liquid medium, according to a further embodiment of the present invention. This embodiment shown in Figure 2 differs from the embodiment shown in Figure 1 through the fact that the temperature of the top side of the pellet extrudates 2 is controlled by means of a large-area spraying device 30 with a multiplicity of spray nozzles 24. Furthermore, .in this embodiment the pelletizing device 7 is not displaceable, but rather is fixedly connected to a bottom crystallization zone part 47. A
top crystallization zone part 46 can pivot, together with the feedpipe 13, about the point 45, in direction F, in order to make it easier to start up the installation.
After a stable state has been reached at the die exit, the plastic extrudates 2 can be cut to length by means of an automated extrudate-cutting device (not shown), and the top crystallization zone part 46 can be pivoted in, and with the aid of the crystallization zone 5 partial crystallization of the extrudates can be achieved prior to pelletizing. For this purpose, the temperature of the undersides of the crystallization extrudates 2 is controlled using temperature-controlled liquid medium 4 from the feedline 13, via the longitudinal slot 2G or corresponding holes 40, and the top side of the extrudates is supplied with temperature-controlled liquid medium 4 by the large-area spraying device 30.
The partial:Ly crystallized extrudates are fed to the pelletizing device 7 via the feed channel 31, pelletizing taking place under a liquid medium. The mixture of liquid medium 4 and pellets 12 is fed to a separator 12, which feeds pellets 12 which have been separated from the liquid medium for further processing in the direction of arrow G and feeds the liquid medium to a temperature-control unit 9. In this temperature-control unit, the temperature of the liquid medium is controlled by means of heating and/or cooling devices 8 and this medium is fed to the large-area spraying device 30, the feedpipe 13 and the pelletizing device. In this embodiment, which is intended to process PA6 plastic extrudates, the coolant is a hot water, the temperature of which has been set to 80°C.
Figure 3A and Figure 3B show cross-sectional views in the longitudinal direction (Figure 3A) and perpendicular thereto (Figure 3B) through a feedpipe 13 leading to the crystallization zone, which pipe, on the inside, carries a temperature-controlled cooling medium 4 and, on the outside, guides plastic extrudates in circumferential rings 33. For this purpose, the feedpipe 13 is coated with an outer layer 32 of good thermal conductivity, for example a layer of a metal alloy, in which circumferential channels 22 are formed.
In this embodiment, the feedpipe 13 has a longitudinal slot 20 through which temperature-controlled liquid medium 4 can emerge in the direction of arrow L, and can cover a crystallization zone 5 on a crystallization zone part 35 with a film of temperature-controlled liquid.
Figures 4A and 4B show cross-sectional views in the longitudinal direction and perpendicular thereto of a feedpipe 13 leading to the crystallization zone, which on the inside carries temperature-controlled liquid medium 4 and on the outside guides plastic extrudates in c:ircumferential grooves 21. The circumferential grooves 21 differ from the circumferential channels 22 shown in Figure 3A in that they are formed in sawtooth form in an outer layer 32.
Furthermore, at the position of each extrudate, holes 40 are provided in order to allow liquid medium 4 to emerge from the :Eeedpipe 13 in the direction of arrow M, so that the temperature of the plastic extrudates 2 can b~e controlled on their underside by means of the medium 4.
In a preferred embodiment of the apparatus, the pelletizing apparatus 7 is arranged immediately after the crystallizatic>n zone part 35, downstream of the crystallization zone 5 as seen in the direction of flow of the material. E'or this purpose, the crystallization zone part may be an integral component of the pelletizing device. In order to be able to start up a contact device of this nature, comprising crystallization zone and pelletizing device, a device of this nature ca.n be separated in such a way that initially, for stabilization purposes, the plastic extrudates emerging from the dies can drop freely downwards. After an automatic extrudate-cutting device has come into action, the separate parts of the device are moved together, so that stabilized plastic extrudates can at least partially crystallize immediately in th~~ area of the crystallization zone part and can be processed into a mixture of pellets and medium in the connected pelletizing device.
To control the temperature of the underside of the plastic extrudates emerging from the dies, a feedpipe is preferably arranged downstream of the dies.
This feedpipe carries the temperature-controlled liquid medium in its interior and guides the plastic extrudates on its outer surface. To supply the crystallization zone part with temperature-controlled medium, the feedpipe has a longitudinal slot which is positioned in such a way that it supplies the underside of the plastic extrudates with temperature-controlled liquid medium, by forming a film of temperature-contro7_led liquid medium on the crystallization zone part. The temperature of the top side of the plastic extrudates is controlled in the area of the crysta:Llization zone, preferably by spray nozzles which are supplied with temperature-controlled liquid medium from. a further feed pipe.
In a further preferred embodiment of the apparatus, the :Eeedpipe which guides the plastic extrudates may, instead of having a longitudinal slot at each position :For guiding a plastic extrudate, have a hole for controlling the temperature of the underside of the plastic extrudate by means of a temperature-controlled medium.
In a preferred alternative embodiment of the apparatus, the crystallization zone part can pivot between an at-rest position and a working position, the at-rest position allowing the molten plastic to emerge from the dies in the vertical direction, and the working position Feeding the plastic extrudates to a pelletizing device in partially crystallized form. This embodiment has the advantage that, despite a space-saving arrangement, the pelletizing device as an individual component may adopt a fixed position, while only the crystalli:~ation zone part is designed moveably or pivotably. The transition from the crystallization zone part to the palletizing device can be ensured by means of a short feed channel which preferably projects out of the pelletiz:ing unit.
Further advantages, features and possible applications of the invention will now be explained in more detail on the basis of an exemplary embodiment and with reference to the appended drawings, in which:
Fig. 1 shows an outline sketch of an apparatus for carrying out the method according to one embodiment of the present invention, Fig. 2 shows an outline sketch of an apparatus including a circuit for heat-controlled liquid medium according to a further embodiment of the present invention, Figs. 3 and 3B show cross-sectional views, in the longitudinal direction and perpendicular thereto, of a feedpipe leading to the crystallization zone, which on the inside -conveys a temperature-controlled and liquid medium and on the outside guides plastic extrudates, and Figs. 4A and 4B show cross-sectional views, in the longitudinal direction and perpendicular thereto, of a feedpipe leading to the crystallization zone, which on the inside carries a temperature-controlled liquid medium and on the outside guides plastic extrudates.
Figure 1 shows an outline sketch of an apparatus for carrying out the method for feeding and treating plastic extrudates 2 which emerge from dies 1 in the form of a molten liquid, having a cooling zone, for pelletizing the plastic extrudates 2, having a crystallization zone 5, for pelletizing the plastic extrudates 2, according to one embodiment of the present invention. Immediately after they emerge from the dies 1, the plastic extrudates 2 are partially crystallized in a temperature-controlled liquid medium 4 over a crystallization zone 5. For this purpose, the liquid medium 4 is held at a temperature which is above the glass tran~;ition temperature of the plastic extrudates 2 and is not quenched to below the glass transition temperature, let alone cooled 2 and held below the glass transition temperature in a long guide channel under cooling water, as is conventional in the prior art, in order to feed the plastic extrudates 2 to a pelletizing device in an amorphous state. Since in the method according to the invention partial crystallization is achieved by means of a temperature-controlled liquid medium 4 immediately after the extrudates emerge from the dies 1, the crystallization zone is extremely short, and therefore the distance between the pelletizing device and the die exit 15 is extremely short.
In a pre:Eerred apparatus for carrying out the method, as shown :in Figure 1, the crystallization zone 5 is therefore an integral component of the immediately adjoining pelletizing device. By means of a drive roller 16 and a pressure-exerting roller 17, which may be driven synchronously with the drive roller 16, the pelletizing device picks up the partially crystallized plastic extrudates 18 and feeds them to the cutting rotor 19, so that a mixture of temperature-controlled liquid medium and plastic pellets is formed in the pelletizing devices 7, and this mixture can be fed for further processing.
To control the temperature of the plastic extrudates which are to be crystallized by means of a temperature-controlled liquid medium 4, the apparatus as shown in Figure 1 has a feedpipe 13, which is explained in more detail below in conjunction with Figures 3A, 3B or 4A and 4B.
This feedpipe 13 leading to the crystallization zone 5 has an elongate slot 20, which makes it possible for the temperature-controlling liquid medium 4 to form a temperature-controlling film of liquid in the area of the crystallization zone 5. The longitudinal slot 20 may also be replaced by a series of holes, so that the temperature-contro:Lling liquid medium 4 emerges from the feedpipe 13 directly at those positions at which a plastic extrudate 2 is in each case introduced. To guide the plastic extrudates 2, the feedpipe has a structured shell on its outer circumference, in the longitudinal direction, which has circumferential channels 22, as shown in Figure 3A, or circumferential grooves 21, as shown in Figure 4A. These circumferential grooves 21 or circumferential channels 22 on the feedpipe 13 serve to guide the plastic extrudates towards the crystallization zone 5.
While the feedpipe 13 supplies the temperature-control:Ling liquid medium from one side of the plastic extrudates, referred to below as the underside, via i.ts longitudinal slot 20 or its corresponding holes, the temperature of the other side of the plastic ext:rudates, referred to below as the top side, is in this embodiment of a device for carrying out the method according to the invention controlled using temperature-controlled liquid medium coming out of spray nozzles 24. The spray nozzles 24 are supplied with temperature-controlling liquid medium 4 via a further feedline 23. The spray angle of the spray nozzles 24 can be adjusted by pivoting the feedpipe 23 about its axis 25. The angle at which the plastic extrudates 2 slide over the crystallization zone can be adjusted by pivoting the feedpipe 13 about its axis 26, since in this preferred apparatus a crystallization zone part 35 and th.e feedpipe 13 are fixedly connected to one another. In other embodiments, the angle of inclination of the crystallization zone 5 may also be adjusted independently of the position of the feedpipe 13.
In the integral embodiment shown in Figure 1, with the pelletizing device 7 and crystallization zone part 35 in a compact assembly, the feedpipe 13, the drive roller 16 and the cutting roller 19 with the cutting-edge support 27 are arranged on a frame, and the entire frame 28 can be displaced in the direction of arrow B, while a second frame 29, on which the feedline 23 and the pressure-exerting roller 17 are arranged, can be displaced in the direction of the arrow C. As a result of the frame being divided into two parts in this way, it is easier to start up the apparatus, in that the frames 28 and 29 are only moved together when the formation of plastic extrudates at the die exit 15 has stabilized. On the other hand, during the start-up phase the feedpipe 13 may be displaced in direction D with respect to the frame 28, in order to align the feedpipe 13 towards the die head 6.
Figure 2 shows an outline sketch of an apparatus for carrying out the method, including a circuit for a temperature-controlled liquid medium, according to a further embodiment of the present invention. This embodiment shown in Figure 2 differs from the embodiment shown in Figure 1 through the fact that the temperature of the top side of the pellet extrudates 2 is controlled by means of a large-area spraying device 30 with a multiplicity of spray nozzles 24. Furthermore, .in this embodiment the pelletizing device 7 is not displaceable, but rather is fixedly connected to a bottom crystallization zone part 47. A
top crystallization zone part 46 can pivot, together with the feedpipe 13, about the point 45, in direction F, in order to make it easier to start up the installation.
After a stable state has been reached at the die exit, the plastic extrudates 2 can be cut to length by means of an automated extrudate-cutting device (not shown), and the top crystallization zone part 46 can be pivoted in, and with the aid of the crystallization zone 5 partial crystallization of the extrudates can be achieved prior to pelletizing. For this purpose, the temperature of the undersides of the crystallization extrudates 2 is controlled using temperature-controlled liquid medium 4 from the feedline 13, via the longitudinal slot 2G or corresponding holes 40, and the top side of the extrudates is supplied with temperature-controlled liquid medium 4 by the large-area spraying device 30.
The partial:Ly crystallized extrudates are fed to the pelletizing device 7 via the feed channel 31, pelletizing taking place under a liquid medium. The mixture of liquid medium 4 and pellets 12 is fed to a separator 12, which feeds pellets 12 which have been separated from the liquid medium for further processing in the direction of arrow G and feeds the liquid medium to a temperature-control unit 9. In this temperature-control unit, the temperature of the liquid medium is controlled by means of heating and/or cooling devices 8 and this medium is fed to the large-area spraying device 30, the feedpipe 13 and the pelletizing device. In this embodiment, which is intended to process PA6 plastic extrudates, the coolant is a hot water, the temperature of which has been set to 80°C.
Figure 3A and Figure 3B show cross-sectional views in the longitudinal direction (Figure 3A) and perpendicular thereto (Figure 3B) through a feedpipe 13 leading to the crystallization zone, which pipe, on the inside, carries a temperature-controlled cooling medium 4 and, on the outside, guides plastic extrudates in circumferential rings 33. For this purpose, the feedpipe 13 is coated with an outer layer 32 of good thermal conductivity, for example a layer of a metal alloy, in which circumferential channels 22 are formed.
In this embodiment, the feedpipe 13 has a longitudinal slot 20 through which temperature-controlled liquid medium 4 can emerge in the direction of arrow L, and can cover a crystallization zone 5 on a crystallization zone part 35 with a film of temperature-controlled liquid.
Figures 4A and 4B show cross-sectional views in the longitudinal direction and perpendicular thereto of a feedpipe 13 leading to the crystallization zone, which on the inside carries temperature-controlled liquid medium 4 and on the outside guides plastic extrudates in c:ircumferential grooves 21. The circumferential grooves 21 differ from the circumferential channels 22 shown in Figure 3A in that they are formed in sawtooth form in an outer layer 32.
Furthermore, at the position of each extrudate, holes 40 are provided in order to allow liquid medium 4 to emerge from the :Eeedpipe 13 in the direction of arrow M, so that the temperature of the plastic extrudates 2 can b~e controlled on their underside by means of the medium 4.
Claims (18)
1. Method for feeding and treating plastic extrudates (2) which emerge from dies (1) in the form of a molten liquid, having a cooling zone for pelletizing the plastic extrudates (2), characterized in that the plastic extrudates (2), immediately after they leave the dies (1), are partially crystallized in a temperature-controlled liquid medium (4) over a crystallization zone (5), the liquid medium (4) being held at a temperature which is above the glass transition temperature of the plastic extrudates (2) until the subsequent pelletization stage.
2. Method according to Claim 1, characterized in that the temperature of the liquid medium (4) is controlled in such a manner that a constant temperature which is above the glass transition temperature is maintained in the liquid medium (4).
3. Method according to Claim 1 or 2, characterized in that the temperature of the liquid medium (4) is controlled in such a manner that the temperature of the medium is below 150% of the glass transition temperature in °C and above 100% of the glass transition temperature in °C.
9. Method according to one of the preceding claims, characterized in that the liquid medium (4) used is hot water.
5. Method according to one of the preceding claims, characterized in that the plastic extrudates (2) have a glass transition temperature of below 100°C.
6. Method according to one of the preceding claims, characterized. in that the molten plastic (6) contains polyamides.
7. Method according to one of the preceding claims, characterized in that the molten plastic (6) contains polyolefins.
8. Method according to one of the preceding claims, characterized in that the temperature of the plastic extrudates (2) is controlled as they pass through a substantially vertical crystallization zone (5).
9. Method according to one of the preceding claims, characterized in that the plastic extrudates (2) are guided in the crystallization zone (5) by dropping freely.
10. Method according to one of the preceding claims, characterized in that the plastic extrudates (2) are fed to a pelletizing device (7) for further treatment.
11. Apparatus for feeding and treating plastic extrudates, having dies (1), from which the plastic extrudates emerge in the form of a molten liquid, having a cooling zone part, which is arranged immediately downstream of the dies (1), and having a pelletizing apparatus (7) which is arranged downstream of the cooling zone part, characterized in that the cooling zone part is designed as a crystallization zone part (35) and, to control the temperature of the crystallization zone (5) of the crystallization zone part (35), heating and/or cooling devices (8) and temperature-control units (9) are provided, by means of which the temperature of a temperature-controlled liquid medium (4) can be set to a temperature which is above the glass transition temperature of the plastic extrudates (2).
12. Apparatus according to Claim 11, characterized in that the crystallization zone part (35) is arranged substantially vertically.
13. Apparatus according to Claim 11 or 12, characterized in that the heating and cooling devices (8) are through-flow thermostats which set the temperature-controlled liquid medium (4) to a constant initial temperature.
14. Apparatus according to one of Claims 11 to 13, characterized in that the pelletizing device (7) is arranged immediately after the crystallization zone part (35), downstream of the crystallization zone (5) as seen in the direction of flow of the material.
15. Apparatus according to one of Claims 11 to 14, characterized in that a feedpipe (13), in order to control the temperature of the underside of the plastic extrudates (2), conveys the temperature-controlled liquid medium (4) in its interior and guides the plastic extrudates (2) on its outer surface.
16. Apparatus according to Claim 15, characterized in that the feedpipe (13) has a longitudinal slot (20) for supplying the crystallization zone part with temperature-controlled medium.
17. Apparatus according to Claim 15 or 16, characterized in that the feedpipe (13), at each position for guiding a plastic extrudate (2), has a hole for controlling the temperature of the underside of the plastic extrudate by means of a temperature-controlled medium (4).
18. Apparatus according to one of the preceding claims, characterized in that a crystallization zone part (35) can pivot between an at-rest position and a working position, the at-rest position allowing the molten plastic (6) to emerge from the dies (1) in the vertical direction, and the working position feeding the plastic extrudates to the pelletizing device in partially crystallized form.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19933476A DE19933476B4 (en) | 1999-07-16 | 1999-07-16 | Method and device for the supply and treatment of plastic strands |
| DE19933476.5 | 1999-07-16 | ||
| PCT/EP2000/006691 WO2001005566A1 (en) | 1999-07-16 | 2000-07-13 | Method and device for feeding and treating plastic strands |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2340358A1 true CA2340358A1 (en) | 2001-01-25 |
Family
ID=7915075
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002340358A Abandoned CA2340358A1 (en) | 1999-07-16 | 2000-07-13 | Method and device for feeding and treating plastic strands |
Country Status (11)
| Country | Link |
|---|---|
| EP (1) | EP1113913B2 (en) |
| JP (1) | JP4085419B2 (en) |
| KR (1) | KR100783805B1 (en) |
| CN (1) | CN1315628C (en) |
| AT (1) | ATE304435T1 (en) |
| CA (1) | CA2340358A1 (en) |
| DE (2) | DE19933476B4 (en) |
| ES (1) | ES2244458T5 (en) |
| MX (1) | MXPA01001618A (en) |
| TW (1) | TW487624B (en) |
| WO (1) | WO2001005566A1 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7329723B2 (en) | 2003-09-18 | 2008-02-12 | Eastman Chemical Company | Thermal crystallization of polyester pellets in liquid |
| US7790840B2 (en) | 2006-05-24 | 2010-09-07 | Eastman Chemical Company | Crystallizing conveyor |
| US7875184B2 (en) | 2005-09-22 | 2011-01-25 | Eastman Chemical Company | Crystallized pellet/liquid separator |
| US7879969B2 (en) | 2006-05-24 | 2011-02-01 | Eastman Chemical Company | Crystallizer temperature control via fluid control |
| US8022168B2 (en) | 2004-09-02 | 2011-09-20 | Grupo Petrotexmex, S.A. de C.V. | Spheroidal polyester polymer particles |
| US8039581B2 (en) | 2003-10-10 | 2011-10-18 | Grupo Petrotemex, S.A. De C.V. | Thermal crystallization of a molten polyester polymer in a fluid |
| US8079158B2 (en) | 2004-09-02 | 2011-12-20 | Grupo Petrotemex, S.A. De C.V. | Process for separating and drying thermoplastic particles under high pressure |
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| DE102004010680A1 (en) | 2004-03-04 | 2005-10-06 | Zimmer Ag | Process for the preparation of highly condensed polyesters in the solid phase |
| DE102005029501A1 (en) * | 2005-05-09 | 2006-11-16 | Bki Grundbesitz Gmbh & Co. Kg | Method for thermally treating polyester pellets used as packaging material comprises feeding and granulating a polyester melt to a cold granulating device, feeding the granules to a water-solid separating device and further processing |
| DE102006027176B4 (en) | 2005-08-26 | 2015-08-06 | Lurgi Zimmer Gmbh | Process and apparatus for reducing the acetaldehyde content of polyester granules and polyester granules |
| DE102006012587B4 (en) | 2006-03-16 | 2015-10-29 | Lurgi Zimmer Gmbh | Process and apparatus for the crystallization of polyester material |
| LT5394B (en) | 2006-06-14 | 2007-01-25 | Zimmer Aktiengesellschaft | Method for the production of highly condensed polyester |
| DE102007027543A1 (en) | 2006-11-27 | 2008-05-29 | Bühler AG | Strand granulation method and apparatus and granules made therefrom |
| DE102008058173A1 (en) * | 2008-11-20 | 2010-05-27 | Automatik Plastics Machinery Gmbh | Apparatus and method for continuous casting and granulation of strands of thermoplastic material |
| DE102009009957A1 (en) | 2009-02-23 | 2010-08-26 | Bühler AG | Process for the production of polyester particles at high throughput in one line |
| DE102009059306A1 (en) * | 2009-12-23 | 2011-06-30 | Automatik Plastics Machinery GmbH, 63762 | Apparatus for continuous casting of strands of thermoplastic material |
| MY178343A (en) * | 2015-09-30 | 2020-10-08 | Shinetsu Chemical Co | Apparatus for continuously cutoff machining sintered magnet blocks |
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| DE2559541C3 (en) * | 1975-01-28 | 1980-03-20 | Automatik Apparate-Maschinenbau H. Hench Gmbh, 8754 Grossostheim | Device for pelletizing strands made from thermoplastics |
| DE3205052C2 (en) * | 1982-02-12 | 1984-10-31 | Automatik Apparate-Maschinenbau H. Hench Gmbh, 8754 Grossostheim | Device for feeding molten plastic strands emerging from nozzles to a granulating device |
| DE3421647A1 (en) * | 1984-06-09 | 1985-12-12 | Bayer Ag, 5090 Leverkusen | METHOD FOR PRODUCING POLYCARBONATE INJECTION MOLDED BODIES |
| US5206339A (en) * | 1989-04-05 | 1993-04-27 | Mitsui Toatsu Chemicals, Inc. | Extrusion process of polyimide and polyimide pellet used for the process |
| DE4133329C2 (en) * | 1991-10-08 | 1994-09-15 | Hench Automatik App Masch | Process for cooling and granulating strands which melt out of nozzles |
| DE4207944C2 (en) * | 1992-03-12 | 1994-08-25 | Hench Automatik App Masch | Device for cooling and granulating strands of thermoplastic plastics emerging from the nozzle in molten form |
| US5267845A (en) * | 1992-05-13 | 1993-12-07 | Polysource, Inc. | Apparatus for manufacturing expandable polystyrene (EPS) pellets |
| JPH061547A (en) * | 1992-06-19 | 1994-01-11 | Mitsubishi Denki Bill Techno Service Kk | Elevator operation device |
| US5242289A (en) * | 1992-10-20 | 1993-09-07 | The Conair Group, Inc. | Apparatus for providing controlled cooling of thermoplastic strands |
| DE4314162C1 (en) * | 1993-04-29 | 1994-04-28 | Rieter Automatik Gmbh | Simultaneous drying and crystallisation process for thermoplastics, e.g. PET - has cooling, dewatering and drying sections with max. extrudate passage time in each section |
| DE4419579A1 (en) * | 1994-06-03 | 1995-12-07 | Basf Ag | Plastic material and process for its manufacture |
| JPH091547A (en) * | 1995-06-21 | 1997-01-07 | Sumitomo Chem Co Ltd | Manufacture of methacrylate resin pellet |
| DE19739747A1 (en) * | 1997-09-10 | 1999-03-11 | Rieter Automatik Gmbh | Thermoplastic extrusion head nozzle array for granulator |
-
1999
- 1999-07-16 DE DE19933476A patent/DE19933476B4/en not_active Expired - Fee Related
-
2000
- 2000-07-13 WO PCT/EP2000/006691 patent/WO2001005566A1/en active IP Right Grant
- 2000-07-13 KR KR1020017002562A patent/KR100783805B1/en not_active IP Right Cessation
- 2000-07-13 AT AT00949332T patent/ATE304435T1/en active
- 2000-07-13 MX MXPA01001618A patent/MXPA01001618A/en active IP Right Grant
- 2000-07-13 DE DE50011159T patent/DE50011159D1/en not_active Expired - Lifetime
- 2000-07-13 CN CNB008012962A patent/CN1315628C/en not_active Expired - Fee Related
- 2000-07-13 ES ES00949332T patent/ES2244458T5/en not_active Expired - Lifetime
- 2000-07-13 JP JP2001510636A patent/JP4085419B2/en not_active Expired - Fee Related
- 2000-07-13 CA CA002340358A patent/CA2340358A1/en not_active Abandoned
- 2000-07-13 EP EP00949332A patent/EP1113913B2/en not_active Expired - Lifetime
- 2000-09-08 TW TW089114190A patent/TW487624B/en not_active IP Right Cessation
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7329723B2 (en) | 2003-09-18 | 2008-02-12 | Eastman Chemical Company | Thermal crystallization of polyester pellets in liquid |
| US7674877B2 (en) | 2003-09-18 | 2010-03-09 | Eastman Chemical Company | Thermal crystallization of polyester pellets in liquid |
| US8039581B2 (en) | 2003-10-10 | 2011-10-18 | Grupo Petrotemex, S.A. De C.V. | Thermal crystallization of a molten polyester polymer in a fluid |
| US8309683B2 (en) | 2003-10-10 | 2012-11-13 | Grupo Petrotemex, S.A. De C.V. | Thermal crystallization of a molten polyester polymer in a fluid |
| US8022168B2 (en) | 2004-09-02 | 2011-09-20 | Grupo Petrotexmex, S.A. de C.V. | Spheroidal polyester polymer particles |
| US8079158B2 (en) | 2004-09-02 | 2011-12-20 | Grupo Petrotemex, S.A. De C.V. | Process for separating and drying thermoplastic particles under high pressure |
| US7875184B2 (en) | 2005-09-22 | 2011-01-25 | Eastman Chemical Company | Crystallized pellet/liquid separator |
| US7790840B2 (en) | 2006-05-24 | 2010-09-07 | Eastman Chemical Company | Crystallizing conveyor |
| US7879969B2 (en) | 2006-05-24 | 2011-02-01 | Eastman Chemical Company | Crystallizer temperature control via fluid control |
Also Published As
| Publication number | Publication date |
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| DE19933476B4 (en) | 2006-09-28 |
| ES2244458T5 (en) | 2009-04-01 |
| EP1113913B2 (en) | 2008-11-26 |
| JP2003504246A (en) | 2003-02-04 |
| WO2001005566A1 (en) | 2001-01-25 |
| DE50011159D1 (en) | 2005-10-20 |
| ATE304435T1 (en) | 2005-09-15 |
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| EP1113913B1 (en) | 2005-09-14 |
| CN1315628C (en) | 2007-05-16 |
| MXPA01001618A (en) | 2004-06-07 |
| CN1315900A (en) | 2001-10-03 |
| DE19933476A1 (en) | 2001-01-25 |
| EP1113913A1 (en) | 2001-07-11 |
| KR100783805B1 (en) | 2007-12-07 |
| ES2244458T3 (en) | 2005-12-16 |
| TW487624B (en) | 2002-05-21 |
| KR20010074857A (en) | 2001-08-09 |
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