CA2079686A1 - Method and installation for the production of plastic products with the aid of a hot mixture of pvc powder and additives, and a hot mixer suitable for use with this method - Google Patents
Method and installation for the production of plastic products with the aid of a hot mixture of pvc powder and additives, and a hot mixer suitable for use with this methodInfo
- Publication number
- CA2079686A1 CA2079686A1 CA002079686A CA2079686A CA2079686A1 CA 2079686 A1 CA2079686 A1 CA 2079686A1 CA 002079686 A CA002079686 A CA 002079686A CA 2079686 A CA2079686 A CA 2079686A CA 2079686 A1 CA2079686 A1 CA 2079686A1
- Authority
- CA
- Canada
- Prior art keywords
- hot
- pvc powder
- additives
- mixing
- mixer
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J3/00—Processes of treating or compounding macromolecular substances
- C08J3/20—Compounding polymers with additives, e.g. colouring
- C08J3/22—Compounding polymers with additives, e.g. colouring using masterbatch techniques
- C08J3/226—Compounding polymers with additives, e.g. colouring using masterbatch techniques using a polymer as a carrier
-
- 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
- B29B7/00—Mixing; Kneading
- B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
- B29B7/58—Component parts, details or accessories; Auxiliary operations
- B29B7/60—Component parts, details or accessories; Auxiliary operations for feeding, e.g. end guides for the incoming material
- B29B7/603—Component parts, details or accessories; Auxiliary operations for feeding, e.g. end guides for the incoming material in measured doses, e.g. proportioning of several materials
-
- 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
- B29B7/00—Mixing; Kneading
- B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
- B29B7/58—Component parts, details or accessories; Auxiliary operations
- B29B7/72—Measuring, controlling or regulating
- B29B7/728—Measuring data of the driving system, e.g. torque, speed, power, vibration
-
- 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
- B29C48/285—Feeding the extrusion material to the extruder
- B29C48/297—Feeding the extrusion material to the extruder at several locations, e.g. using several hoppers or using a separate additive feeding
-
- 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
- B29C48/36—Means for plasticising or homogenising the moulding material or forcing it through the nozzle or die
- B29C48/375—Plasticisers, homogenisers or feeders comprising two or more stages
- B29C48/39—Plasticisers, homogenisers or feeders comprising two or more stages a first extruder feeding the melt into an intermediate location of a second extruder
-
- 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
- B29B7/00—Mixing; Kneading
- B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
- B29B7/34—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices
- B29B7/38—Mixing; Kneading continuous, with mechanical mixing or kneading devices with movable mixing or kneading devices rotary
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J2327/00—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Derivatives of such polymers
- C08J2327/02—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Derivatives of such polymers not modified by chemical after-treatment
- C08J2327/04—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Derivatives of such polymers not modified by chemical after-treatment containing chlorine atoms
- C08J2327/06—Homopolymers or copolymers of vinyl chloride
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
- C08J2427/00—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen; Derivatives of such polymers
Abstract
A method is disclosed for the production of extruded plastic products by using an extruder (1) which has an extruder hopper (2) which is supplied with a hot mixture obtained by discontinuous mixing of PVC powder and additives in a hot mixing zone, with the supply of frictional heat, wherein a first amount of PVC powder is mixed with an excess of additives with the supply of frictional heat, after which the mixture thus obtained is homogenised in the same mixing zone with a supplementary amount of PVC powder, in such a way that the final mixture has the desired concentration of additives, after which the hot mixture obtained after homogenisation is fed directly to the extruder hopper (2). An installation for the production of plastic products by extrusion, comprising a discontinously operating hot mixer is also disclosed, as well as said hot mixer (3).
Description
~V09l~15347 2 ~ 7 9 & ~ g PCT/NLg1/00053 Method and installation for the production of plastic products with the aid of a hot mixture of PVC powder and additives, and a hot mixer suitable for use with this method.
The invention relates to a method for the production of extruded plastic products using an extruder which has an extruder hopper which is supplied with a hot mixture obtained by discontinuous mixing of PVC powder and additives in a hot mixing zone, with the supply of frictional heat.
A method of this type is known. In this method the additives become predominantly soft or fluid at the elevated temperatures, as a consequence of frictional heat, as a result of which the said additives adhere very well to the PVC powder.
Following the preparation of this mixture by discontinuous hot mixing, the mixture obtained is tr~ns-ferred into a horizontal rotating and homogenising heat-retaining silo, from which the extruder i9 fed con-tinuously or discontinuously. With this method the additives can be sUpplied to the mixer from a central weighing installation.
one drawback of this method is that a horizontal heat-retaining silo is needed in the extrusion line, while, moreover, a great deal of space is lost because a high vertical mixing installation i9 positioned above each extruder, as a result of which the building costs for a factory are appreciably increased.
The aim of the invention is, now, to provide a method of the type mentioned in the preamble, with which method a horizontal rotating and homogenising heat-retaining silo is no longer needed, since the hot mixture obtained is fed directly to an extruder hopper of an extruder without the use of special installations for keeping the mixture hot, while, moreover, less space is .
WO91/1~7 ~ ~ 7 ~ b 8 6 PCT/NL91/00053 _ required for installin~ a mixing zone above the extruder, so that the building costs for a factory are reduced.
This aim is achieved according to the invention in that a first amount of PVC powder is mixed with an S excess of additives with the supply of frictional heat, hfter which the mixture thus obtained is homogenised in the same mixing zone with a supplementary amount of PVC
powder, in such a way that the final mixture has the desired concentration of additives, after which the hot mixture obtained after homogeni~ation i8 fed directly to the extruder hopper. When a method of this type is used, the hot mixture obtained after homogenisation can be fed directly to an extruder hopper, even temperature fluc-tuations of, for example, lO-C having no influence on the processing of the plastic.
As a result of the lower temperature of this mixture, preferably between 70 and 90C, no agglomeration of the mixture occurs snd the mixture remains readily flowable, which is in contrast to mix-tures at higher temperature such as are obtained with asingle-step mixing method.
In addition, this method has the advantage that it makes possible a high flexibillty in the production, since an optimum formulation is now possible per ex-trusion line and per product.
Moreover, this method can be u~ed for all pos-sible extrusion applications. Even in the case of ex-trusion of corrugated drainage tubing, where, because of the thin wall of the tubing and the stretching of the plastic tubing to form the corrugations, malfunctions in extrusion immediately cause problems, malfunctions no longer occur when this method is used.
Finally, smoother products are obtained with an equal yield compared with processin~ with cold mixtures, as a result of which a higher yield per extruder is - possible. At the same time, an opti~um grade can be obtained per extrusion line since the material flows can now be accurately monitored and controlled from raw material to end product.
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~09]/15~7 PCT/NL91/00053 ; - 3 -Finally, a fully integrated automation of the process is possible. It is pointed out that it is known per se to mix PVC powder with additives at elevated temperatures and to feed the resulting product con-tinuously directly to an extruder without the use of ahorizontal rotating and homogenising heat-retaining silo.
A disadvantage is, however, that with this method the supply of raw material to the hot mixer must also be continuous, in which ca~e it has been found that a volumetric metering of the relatively small amount~ of additive is insufficiently accurate and, therefore, use must be made of a much more expensive weight metering.
Consequently, the total investment costs for an extrusion line are very high.
In addition, it is also known to mix PVC powder with an excess of additives in a hot mixer, after which the mixture obtained is transferred to a cool mixer, where it is mixed with a supplementary amount of poly-vinyl chloride powder in order to obtain the desired concentration of additives in the final mixture, and in which cool m~xer the mixture i~ cooled and homogenised, after which the powder mix is stored in hopper~, from which extruders are fed.
A drawback is thst with this method the energy consumption for the entire method is higher than in the ca~e of the method according to the invention, ~ince the homogenised mixture must be cooled and must then be fully heated up again for extrusion. In addition, the total ! investment in equipment and space is much higher.
~xpediently the temperature is r~ised to a temperature sbove 80-C, preferably of lO0 to 140-C, during mixing, with the supply of frictional heat.
$he ratio of first amount of PVC powder to supplementary amount of PVC powder is between approxi-mately 2:l and l:2, but preferably identical amounts of first amount of PVC powder and supplementary amount of PVC powder are used, 80 that the ratio i8 about l:l.
The mixing and homogenisation is expediently carried out in a horizontal mixer, a6 a result of which !
,:
The invention relates to a method for the production of extruded plastic products using an extruder which has an extruder hopper which is supplied with a hot mixture obtained by discontinuous mixing of PVC powder and additives in a hot mixing zone, with the supply of frictional heat.
A method of this type is known. In this method the additives become predominantly soft or fluid at the elevated temperatures, as a consequence of frictional heat, as a result of which the said additives adhere very well to the PVC powder.
Following the preparation of this mixture by discontinuous hot mixing, the mixture obtained is tr~ns-ferred into a horizontal rotating and homogenising heat-retaining silo, from which the extruder i9 fed con-tinuously or discontinuously. With this method the additives can be sUpplied to the mixer from a central weighing installation.
one drawback of this method is that a horizontal heat-retaining silo is needed in the extrusion line, while, moreover, a great deal of space is lost because a high vertical mixing installation i9 positioned above each extruder, as a result of which the building costs for a factory are appreciably increased.
The aim of the invention is, now, to provide a method of the type mentioned in the preamble, with which method a horizontal rotating and homogenising heat-retaining silo is no longer needed, since the hot mixture obtained is fed directly to an extruder hopper of an extruder without the use of special installations for keeping the mixture hot, while, moreover, less space is .
WO91/1~7 ~ ~ 7 ~ b 8 6 PCT/NL91/00053 _ required for installin~ a mixing zone above the extruder, so that the building costs for a factory are reduced.
This aim is achieved according to the invention in that a first amount of PVC powder is mixed with an S excess of additives with the supply of frictional heat, hfter which the mixture thus obtained is homogenised in the same mixing zone with a supplementary amount of PVC
powder, in such a way that the final mixture has the desired concentration of additives, after which the hot mixture obtained after homogeni~ation i8 fed directly to the extruder hopper. When a method of this type is used, the hot mixture obtained after homogenisation can be fed directly to an extruder hopper, even temperature fluc-tuations of, for example, lO-C having no influence on the processing of the plastic.
As a result of the lower temperature of this mixture, preferably between 70 and 90C, no agglomeration of the mixture occurs snd the mixture remains readily flowable, which is in contrast to mix-tures at higher temperature such as are obtained with asingle-step mixing method.
In addition, this method has the advantage that it makes possible a high flexibillty in the production, since an optimum formulation is now possible per ex-trusion line and per product.
Moreover, this method can be u~ed for all pos-sible extrusion applications. Even in the case of ex-trusion of corrugated drainage tubing, where, because of the thin wall of the tubing and the stretching of the plastic tubing to form the corrugations, malfunctions in extrusion immediately cause problems, malfunctions no longer occur when this method is used.
Finally, smoother products are obtained with an equal yield compared with processin~ with cold mixtures, as a result of which a higher yield per extruder is - possible. At the same time, an opti~um grade can be obtained per extrusion line since the material flows can now be accurately monitored and controlled from raw material to end product.
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~09]/15~7 PCT/NL91/00053 ; - 3 -Finally, a fully integrated automation of the process is possible. It is pointed out that it is known per se to mix PVC powder with additives at elevated temperatures and to feed the resulting product con-tinuously directly to an extruder without the use of ahorizontal rotating and homogenising heat-retaining silo.
A disadvantage is, however, that with this method the supply of raw material to the hot mixer must also be continuous, in which ca~e it has been found that a volumetric metering of the relatively small amount~ of additive is insufficiently accurate and, therefore, use must be made of a much more expensive weight metering.
Consequently, the total investment costs for an extrusion line are very high.
In addition, it is also known to mix PVC powder with an excess of additives in a hot mixer, after which the mixture obtained is transferred to a cool mixer, where it is mixed with a supplementary amount of poly-vinyl chloride powder in order to obtain the desired concentration of additives in the final mixture, and in which cool m~xer the mixture i~ cooled and homogenised, after which the powder mix is stored in hopper~, from which extruders are fed.
A drawback is thst with this method the energy consumption for the entire method is higher than in the ca~e of the method according to the invention, ~ince the homogenised mixture must be cooled and must then be fully heated up again for extrusion. In addition, the total ! investment in equipment and space is much higher.
~xpediently the temperature is r~ised to a temperature sbove 80-C, preferably of lO0 to 140-C, during mixing, with the supply of frictional heat.
$he ratio of first amount of PVC powder to supplementary amount of PVC powder is between approxi-mately 2:l and l:2, but preferably identical amounts of first amount of PVC powder and supplementary amount of PVC powder are used, 80 that the ratio i8 about l:l.
The mixing and homogenisation is expediently carried out in a horizontal mixer, a6 a result of which !
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WO91/15~7 PCT/NL91/00053^
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relatively little space is required above the extruder for the installation of a hot mixer of this type.
Although the hot mixture obtained after the homogenisation is usually fed to one extruder, it can be advisable for extruders with a low yield to fill the hot mixture into several extruder hoppers, with the aid of a distributing installation. In this case it is necessary that all these extruders use the same formulation.
However, the extruder hoppers can also be filled in turn; in this ca~e it is then possible to use dif-ferent formulations.
In addition, the invention relates to an instal-lation as de~cribed in Claim lO.
Finally, the invention relates to a hot mixer according to Claim 14.
The invention will now be illustrated with reference to an ~xemplary embodiment with the aid of the appended figure, in which an in~tallation for carrying out the method according to the $nvention is shown diagrammatically.
I The diagram show~ an extruder l with an extruder hopper 2 and a hot mixer 3, which is positioned above this extruder and operates discontinuou~ly, for mixing PVC powder and additive~ with the supply of frictional heat.
The hot mixer 3 is provided with drive means 6 for driving tho mixing elements 7 of the hot mixer.
The drive means 6 can be set to various speeds of revolution. At a high speed of revolution, the mixing element~ can consequently supply a large amount of frictional energy and therefore form a hot mixture of PVC
powder and additives. The mixing elements 7 can then serve as homogenising elements at a low speed of revolu-tion, after which the hot mixture containing an excess of ; 35 additives is homogenised with a supplementary amount of PVC powder in order to achieve the desired concentration of additives.
The outlet 9 of the hot mixer opens directly into an extruder hopper 2.
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`~091/15~7 PCT/NL91/00053 In order to fill extruder hoppers of several extruders which operate at low capacity, the hot mixer outlet 9 can expediently be provided with a distributing installation lO to feed several outlets 9', 9 and 9' .
5The hot mixer 3 is preferably a horizontal hot mixer, for example of a type which largely corresponds to a mixer as described in German Patent 27 30 283.
The hot mixer i8 provided with an additive feed 4, which can be ~hut off, and with a PVC powder feed 5, lOwhich can be shut off.
After feeding a specific amount of additives to a first amount of PVC powder fed through PVC powder feed 5, both the additive feed 4 and the PVC powder feed 5 are closed, after which, after mixing with the 8upply of 15frictional heat, the PVC powder feed 5 is opened again and the ~upplementary amount of PVC powder i8 fed in.
In~tead of using only original PVC powder, the in~tallation i~ also provided with a feed ll for broken or ground polyvinyl chloride, as a conseguence of which 20broken ox ground polyvinyl chloride to be reprocessed can be us~d.
The installation can al80 be provided with a colorant feed 14 for feeding colorant from colorant reservoir 13. This colorant i8 appropriately fed to the 25mixer. If desired, direct feeding to the extrudsr i8 z180 possible.
During mixing with the 8upply of frictional he~t, the mlxture is heated to a temperature of 110C when use is made of a mixture of PVC powder with twice the amount 30of additives. During this operation the mixing elements 7 of hot mixer 3 are driven to a high speed of revolution (llO0 rev~min) by the drive means 6, controlled by first control means 8.
The speed of revolution of the mixing elements 7 35of the hot mixer is then reduced to a low speed of revolution of 550 rev/min using second control means 8a.
A second amount of PVC powder at ambient temperature, which amount is identical to the first amount of PVC
powder already present in the mixer, is then fed to the .. ... . : . ,, ~ .:. :;: . . . .. . .
.,.. . . ~ .. ~ . . : . . . . .
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, . . . . . . :
WO91/15~7 ~ ~ 7 ~ PCT/NL91/00053 mixer 3 and the mixture is homogenised for l minute at the low speed of revolution of 550 rev/min.
During this operation the temperature of the hot mixture of PVC and the desired amount of additives falls to 80C.
The hot mixture is then fed directly, via hot mixer outlet 9, into extruder hopper 2 and from there directly into extruder 1 with extrusion head 18, which extrudes a tube 15, which is calibrated and cooled in calibrating bush 16 and cooler 16a and removed via draw-bench 17.
During extrusion, no "plate out~ deposition is observed, the energy consumption in the method according to the invention is very low and the mixing costs per extruder are low, while the hot mixture i8 outgtandingly suitable for all possible applications, in particular tubing, including corrugated drainage tubing.
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WO91/15~7 PCT/NL91/00053^
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relatively little space is required above the extruder for the installation of a hot mixer of this type.
Although the hot mixture obtained after the homogenisation is usually fed to one extruder, it can be advisable for extruders with a low yield to fill the hot mixture into several extruder hoppers, with the aid of a distributing installation. In this case it is necessary that all these extruders use the same formulation.
However, the extruder hoppers can also be filled in turn; in this ca~e it is then possible to use dif-ferent formulations.
In addition, the invention relates to an instal-lation as de~cribed in Claim lO.
Finally, the invention relates to a hot mixer according to Claim 14.
The invention will now be illustrated with reference to an ~xemplary embodiment with the aid of the appended figure, in which an in~tallation for carrying out the method according to the $nvention is shown diagrammatically.
I The diagram show~ an extruder l with an extruder hopper 2 and a hot mixer 3, which is positioned above this extruder and operates discontinuou~ly, for mixing PVC powder and additive~ with the supply of frictional heat.
The hot mixer 3 is provided with drive means 6 for driving tho mixing elements 7 of the hot mixer.
The drive means 6 can be set to various speeds of revolution. At a high speed of revolution, the mixing element~ can consequently supply a large amount of frictional energy and therefore form a hot mixture of PVC
powder and additives. The mixing elements 7 can then serve as homogenising elements at a low speed of revolu-tion, after which the hot mixture containing an excess of ; 35 additives is homogenised with a supplementary amount of PVC powder in order to achieve the desired concentration of additives.
The outlet 9 of the hot mixer opens directly into an extruder hopper 2.
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`~091/15~7 PCT/NL91/00053 In order to fill extruder hoppers of several extruders which operate at low capacity, the hot mixer outlet 9 can expediently be provided with a distributing installation lO to feed several outlets 9', 9 and 9' .
5The hot mixer 3 is preferably a horizontal hot mixer, for example of a type which largely corresponds to a mixer as described in German Patent 27 30 283.
The hot mixer i8 provided with an additive feed 4, which can be ~hut off, and with a PVC powder feed 5, lOwhich can be shut off.
After feeding a specific amount of additives to a first amount of PVC powder fed through PVC powder feed 5, both the additive feed 4 and the PVC powder feed 5 are closed, after which, after mixing with the 8upply of 15frictional heat, the PVC powder feed 5 is opened again and the ~upplementary amount of PVC powder i8 fed in.
In~tead of using only original PVC powder, the in~tallation i~ also provided with a feed ll for broken or ground polyvinyl chloride, as a conseguence of which 20broken ox ground polyvinyl chloride to be reprocessed can be us~d.
The installation can al80 be provided with a colorant feed 14 for feeding colorant from colorant reservoir 13. This colorant i8 appropriately fed to the 25mixer. If desired, direct feeding to the extrudsr i8 z180 possible.
During mixing with the 8upply of frictional he~t, the mlxture is heated to a temperature of 110C when use is made of a mixture of PVC powder with twice the amount 30of additives. During this operation the mixing elements 7 of hot mixer 3 are driven to a high speed of revolution (llO0 rev~min) by the drive means 6, controlled by first control means 8.
The speed of revolution of the mixing elements 7 35of the hot mixer is then reduced to a low speed of revolution of 550 rev/min using second control means 8a.
A second amount of PVC powder at ambient temperature, which amount is identical to the first amount of PVC
powder already present in the mixer, is then fed to the .. ... . : . ,, ~ .:. :;: . . . .. . .
.,.. . . ~ .. ~ . . : . . . . .
: . .- ~ , . . :
.. - .: . . . , : .
, . . . . . . :
WO91/15~7 ~ ~ 7 ~ PCT/NL91/00053 mixer 3 and the mixture is homogenised for l minute at the low speed of revolution of 550 rev/min.
During this operation the temperature of the hot mixture of PVC and the desired amount of additives falls to 80C.
The hot mixture is then fed directly, via hot mixer outlet 9, into extruder hopper 2 and from there directly into extruder 1 with extrusion head 18, which extrudes a tube 15, which is calibrated and cooled in calibrating bush 16 and cooler 16a and removed via draw-bench 17.
During extrusion, no "plate out~ deposition is observed, the energy consumption in the method according to the invention is very low and the mixing costs per extruder are low, while the hot mixture i8 outgtandingly suitable for all possible applications, in particular tubing, including corrugated drainage tubing.
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Claims (14)
1. Method for the production of extruded plastic products using an extruder which has an extruder hopper which is supplied with a hot mixture obtained by discon-tinuous mixing of PVC powder and additives in a hot mixing zone, with the supply of frictional heat, charac-terised in that a first amount of PVC powder is mixed with an excess of additives with the supply of frictional heat, after which the mixture thus obtained is homo-genised in the same mixing zone with a supplementary amount of PVC powder, in such a way that the final mixture has the desired concentration of additives, after which the hot mixture obtained after homogenisation is fed directly to the extruder hopper.
2. Method according to Claim 1, characterised in that the ratio of first amount of PVC powder to sup-plementary amount of PVC powder is between approximately 2:1 and 1:2 and is preferably approximately 1:1.
3. Method according to Claim 1 or 2, characterised in that the mixing with the supply of frictional heat is continued until the mixture has a temperature of above 80°C and preferably a temperature of 100 to 140°C.
4. Method according to one or more of Claims 1-3, charaçterised in that the supplementary amount of PVC
powder has a temperature of below 30°C and preferably ambient temperature.
powder has a temperature of below 30°C and preferably ambient temperature.
5. Method according to one or more of Claims 1-4, characterised in that the final mixture has a temperature of between 70°C and 90°C.
6. Method according to one or more of Claims 1-5, characterised in that one hot mixer is added to one extruder.
7. Method according to one or more of Claims 1-5, characterised in that the hot mixture obtained after homogenisation is fed from the mixer to several extruders with the aid of a distributing installation.
8. Method according to one or more of the preceding claims, characterised in that the mixing and homogenisa-tion is carried out in a horizontal mixer.
9. Method according to one or more of Claims 1-8, characterised in that the PVC powder is at least par-tially replaced by broken or ground PVC to be reproces-sed.
10. Installation for the production of plastic products by extrusion, at least comprising an extruder (1) with extruder hopper (2) and a hot mixer (3), which operates discontinuously and has an additive feed (4), which can be shut off, and a PVC powder feed (5), which can be shut off, for mixing PVC powder and additives with the supply of frictional heat, the hot mixer (3) being provided with drive means (6) for driving mixing elements (7) of the hot mixer to a high speed of revolution with mixing of PVC powder and additives, characterised in that the drive means (6) can interact either with first control means (8) for driving the mixing elements (7) of the hot mixer to a high speed of revolution with mixing of PVC powder and additives, or with second control means (8a) for driving the mixing elements (7) to a low speed of revolution for homogenising a hot mixture of PVC
powder and excess additives which is obtained following the action of the mixing elements (7) at a high speed of revolution, with a supplementary amount of PVC powder, in order to adjust the additives concentration in the final mixture to the desired value, and the outlet (9) of the hot mixer opens directly into an extruder hopper (2) of an extruder (1).
powder and excess additives which is obtained following the action of the mixing elements (7) at a high speed of revolution, with a supplementary amount of PVC powder, in order to adjust the additives concentration in the final mixture to the desired value, and the outlet (9) of the hot mixer opens directly into an extruder hopper (2) of an extruder (1).
11. Installation according to Claim 10, characterised in that the hot mixer outlet (9) is provided with a distributing installation (10) which is provided in order to feed several extruder hoppers (2, 2', 2") from one hot mixer.
12. Installation according to Claim 11 or 12, charac-terised in that the installation is provided with a feed (11) for broken PVC to be reprocessed.
13. Installation according to one or more of Claims 10-12, characterised in that the hot mixer (3) is a horizontal mixer.
14. Hot mixer (3) which has an additive feed (4), which can be shut off, and a PVC powder feed (5), which can be shut off, and is provided with drive means (6) for driving mixing elements (7) of the hot mixer to a high speed of revolution with mixing of PVC powder and addi-tives, characterised in that the hot mixer (3) is pro-vided with first control means (8), which can interact with the drive means (6) to drive the mixing elements (7) to a high speed of revolution with mixing of PVC powder and additives, and with second control elements (8a) for driving mixing elements (7) for homogenising a hot mixture of PVC powder with excess additives, obtained following the action of the mixing elements (7) at a high speed of revolution, with a supplementary amount of PVC
powder at a low speed of revolution, in order to adjust the additives concentration in the final mixture to the desired value.
powder at a low speed of revolution, in order to adjust the additives concentration in the final mixture to the desired value.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL9000840 | 1990-04-10 | ||
| NL9000840A NL9000840A (en) | 1990-04-10 | 1990-04-10 | METHOD AND INSTALLATION FOR MANUFACTURING PLASTIC PREPARATIONS USING A HOT PVC POWDER MIXTURE AND ADDITIVES, AND A WARM BLENDER SUITABLE FOR USE IN THIS METHOD |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2079686A1 true CA2079686A1 (en) | 1991-10-11 |
Family
ID=19856897
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002079686A Abandoned CA2079686A1 (en) | 1990-04-10 | 1991-03-28 | Method and installation for the production of plastic products with the aid of a hot mixture of pvc powder and additives, and a hot mixer suitable for use with this method |
Country Status (12)
| Country | Link |
|---|---|
| US (1) | US5286437A (en) |
| EP (1) | EP0527777B1 (en) |
| JP (1) | JPH05506621A (en) |
| AT (1) | ATE123684T1 (en) |
| AU (1) | AU646862B2 (en) |
| CA (1) | CA2079686A1 (en) |
| DE (1) | DE69110464T2 (en) |
| DK (1) | DK0527777T3 (en) |
| ES (1) | ES2075442T3 (en) |
| NL (1) | NL9000840A (en) |
| PT (1) | PT97302A (en) |
| WO (1) | WO1991015347A1 (en) |
Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IT1263149B (en) * | 1993-02-05 | 1996-08-01 | Giancarlo Colombo | EXTRUSION METHOD AND PLANT FOR IT |
| DE4313290A1 (en) * | 1993-04-23 | 1994-10-27 | Kempter Werner | Method and device for producing a cross-linked extruded polymer product |
| DE19723467A1 (en) * | 1997-06-04 | 1998-12-10 | Huels Troisdorf | Process for the production of soft PVC |
| US7261545B2 (en) * | 2003-11-18 | 2007-08-28 | Chip Investments, Llc | Powder preheating |
| EP2098353A1 (en) * | 2008-03-07 | 2009-09-09 | Emtelle UK Limited | Method and apparatus for producing PVC |
| US9594999B2 (en) | 2012-04-03 | 2017-03-14 | X-Card Holdings, Llc | Information carrying card comprising crosslinked polymer composition, and method of making the same |
| US9122968B2 (en) | 2012-04-03 | 2015-09-01 | X-Card Holdings, Llc | Information carrying card comprising a cross-linked polymer composition, and method of making the same |
| DE102012208717A1 (en) | 2012-05-24 | 2013-11-28 | Coperion Gmbh | Weighing/mixing-handling device for e.g. throughmixing of plastic granulates and additives into polymer mixture, has weighing device weighing bulk materials, and gas supply nozzles introducing mixed gas into interior for mixing materials |
| DE102012109502A1 (en) * | 2012-10-05 | 2014-06-12 | Zeppelin Reimelt Gmbh | Process for the preparation of an inorganic or organic pasty molten mass |
| WO2014149926A1 (en) | 2013-03-15 | 2014-09-25 | X-Card Holdings, Llc | Methods of making a core layer for an information carrying card, and resulting products |
| IL235828A (en) | 2014-11-20 | 2017-12-31 | Margalit Eli | Multi-channel gravimetric batch blender |
| WO2017003307A1 (en) * | 2015-06-29 | 2017-01-05 | Secura B.C. Sp. Z O.O. | Manifold for the heads of an extruder, and related method for producing plastic products using such an extruder |
| US11361204B2 (en) | 2018-03-07 | 2022-06-14 | X-Card Holdings, Llc | Metal card |
| CN111546530B (en) * | 2020-04-16 | 2022-06-14 | 张康伟 | Improved device and system for lower auxiliary engine of all-steel radial tire internal mixer |
Family Cites Families (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR640357A (en) * | 1927-09-01 | 1928-07-11 | Buhler Freres Soc | Safety device for roller mills |
| NL297041A (en) * | 1961-02-23 | 1900-01-01 | ||
| BE640357A (en) * | 1963-11-25 | 1964-03-16 | ||
| US3522934A (en) * | 1968-08-08 | 1970-08-04 | Ulrich Walter | Method and apparatus for producing a homogeneous mixture of granular and viscous substances |
| DE2149668C3 (en) * | 1971-10-05 | 1978-12-14 | Kabel- Und Metallwerke Gutehoffnungshuette Kabelwerk Berlin Gmbh, 1000 Berlin | Method and device for producing elongated material from an elastomer mixture |
| AT328170B (en) * | 1973-01-16 | 1976-03-10 | Kleinewefers Ind Company Gmbh | MULTI-SCREW EXTRUSION PRESS FOR PLASTICIZING AND MIXING PLASTICS |
| US4197381A (en) * | 1976-10-22 | 1980-04-08 | Alia Dominic A | Preparation of vulcanizable compositions by extruder mixing |
| DE2730283C3 (en) * | 1977-07-05 | 1982-03-11 | Thyssen Industrie Ag, 4300 Essen | Mixing device |
| GR64950B (en) * | 1978-03-29 | 1980-06-10 | Pwt Plastic World Tech | Method and apparatus for continuous modulation by pushing and blowing of fine membranes made of plastic from particularly rigid chlor polyvinyl |
| DE2837435B2 (en) * | 1978-08-28 | 1981-06-25 | Friedrich Horst 5840 Schwerte Papenmeier | Process and device for processing PVC powder |
| NL8201928A (en) * | 1981-10-30 | 1983-05-16 | Chemische Ind En Handelmaatsch | PROCESS FOR PREPARING A GRANULAR MIXTURE OF ADDITIVES FOR THE PLASTIC INDUSTRY BY MIXING SUCH ADDITIVES AND THEN PROCESSING TO A GRAIN FORM. |
| US4528155A (en) * | 1983-07-12 | 1985-07-09 | Alcan Aluminum Corporation | Production of cross-linked polymeric extruded articles |
| DE3710418A1 (en) * | 1987-02-26 | 1988-09-08 | F W Hundhausen Gmbh & Co Kg | Process for producing extruded plastic products, in particular plastic pipes |
| JPH0649288B2 (en) * | 1988-01-22 | 1994-06-29 | 豊田合成株式会社 | Method for producing polyvinyl chloride material for extrusion molding |
| DE3927777A1 (en) * | 1989-08-23 | 1991-02-28 | Solvay Werke Gmbh | SOFTENER-FREE MOLDING MATERIAL BASED ON POLYVINYL CHLORIDE, METHOD FOR THE PRODUCTION AND USE THEREOF |
| US5198170A (en) * | 1991-09-19 | 1993-03-30 | The B. F. Goodrich Company | Method for extrusion of powered PVC compounds |
-
1990
- 1990-04-10 NL NL9000840A patent/NL9000840A/en not_active Application Discontinuation
-
1991
- 1991-03-28 ES ES91907915T patent/ES2075442T3/en not_active Expired - Lifetime
- 1991-03-28 DE DE69110464T patent/DE69110464T2/en not_active Expired - Fee Related
- 1991-03-28 DK DK91907915.2T patent/DK0527777T3/en active
- 1991-03-28 CA CA002079686A patent/CA2079686A1/en not_active Abandoned
- 1991-03-28 JP JP91507721A patent/JPH05506621A/en active Pending
- 1991-03-28 WO PCT/NL1991/000053 patent/WO1991015347A1/en active IP Right Grant
- 1991-03-28 US US07/930,512 patent/US5286437A/en not_active Expired - Fee Related
- 1991-03-28 AU AU76854/91A patent/AU646862B2/en not_active Ceased
- 1991-03-28 AT AT91907915T patent/ATE123684T1/en not_active IP Right Cessation
- 1991-03-28 EP EP91907915A patent/EP0527777B1/en not_active Expired - Lifetime
- 1991-04-09 PT PT97302A patent/PT97302A/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| ES2075442T3 (en) | 1995-10-01 |
| AU7685491A (en) | 1991-10-30 |
| ATE123684T1 (en) | 1995-06-15 |
| EP0527777B1 (en) | 1995-06-14 |
| NL9000840A (en) | 1991-11-01 |
| AU646862B2 (en) | 1994-03-10 |
| JPH05506621A (en) | 1993-09-30 |
| PT97302A (en) | 1992-01-31 |
| DE69110464D1 (en) | 1995-07-20 |
| US5286437A (en) | 1994-02-15 |
| WO1991015347A1 (en) | 1991-10-17 |
| DK0527777T3 (en) | 1995-11-06 |
| DE69110464T2 (en) | 1995-12-14 |
| EP0527777A1 (en) | 1993-02-24 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FZDE | Discontinued |