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WO1999011379A1 - Procede et dispositif pour centrifuger des fluides visqueux - Google Patents

Procede et dispositif pour centrifuger des fluides visqueux Download PDF

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Publication number
WO1999011379A1
WO1999011379A1 PCT/EP1998/005541 EP9805541W WO9911379A1 WO 1999011379 A1 WO1999011379 A1 WO 1999011379A1 EP 9805541 W EP9805541 W EP 9805541W WO 9911379 A1 WO9911379 A1 WO 9911379A1
Authority
WO
WIPO (PCT)
Prior art keywords
shear
fluid
centrifuging
centrifuge
viscosity
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.)
Ceased
Application number
PCT/EP1998/005541
Other languages
German (de)
English (en)
Inventor
Rolf Schnause
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Individual
Original Assignee
Individual
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Priority to DE59800897T priority Critical patent/DE59800897D1/de
Priority to AU10228/99A priority patent/AU1022899A/en
Priority to EP98952584A priority patent/EP1011867B1/fr
Publication of WO1999011379A1 publication Critical patent/WO1999011379A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B11/00—Feeding, charging, or discharging bowls
    • B04B11/06—Arrangement of distributors or collectors in centrifuges
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B1/00—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles
    • B04B1/20—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles discharging solid particles from the bowl by a conveying screw coaxial with the bowl axis and rotating relatively to the bowl
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B15/00—Other accessories for centrifuges
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B1/00—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles
    • B04B1/20—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles discharging solid particles from the bowl by a conveying screw coaxial with the bowl axis and rotating relatively to the bowl
    • B04B2001/2033—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles discharging solid particles from the bowl by a conveying screw coaxial with the bowl axis and rotating relatively to the bowl with feed accelerator inside the conveying screw

Definitions

  • the invention relates to devices for centrifuging viscous fluids, in particular melting viscous plastic, or to a shearing device and a method for shearing viscous fluids, in particular viscous plastic melts.
  • Centrifugation processes are based on the principle that mixtures of different densities are separated by centrifugal forces.
  • heavier substances In solid bowl centrifuges, heavier substances have to pass through the lighter liquid substance under the influence of centrifugal forces. The higher the viscosity of the lighter substance, the slower the specifically heavier substance migrates to the outer wall of the centrifuge.
  • centrifuges have been developed for low-viscosity, low-viscosity masses mixed with another substance, such as contaminated water, polymers in monomers or suspensions, from which solid or polymeric particles are separated.
  • another substance such as contaminated water, polymers in monomers or suspensions, from which solid or polymeric particles are separated.
  • plasticized plastic melts which have a viscosity at normal processing temperatures that is approx. 10 6 to 10 9 times higher than that of water
  • centrifuges that have become known so far, such as continuously working solid bowl centrifuges , not particularly suitable in terms of economy.
  • the separation or cleaning performance depends on the sinking rate of the contamination in the thermoplastic melt according to the following formula.
  • the rate of descent thus increases in inverse proportion to the decrease in viscosity.
  • thermoplastic melt The greater the sinking or separating speed or the separation speed of the foreign matter particles from the thermoplastic melt, the greater the throughput of the cleaned thermoplastic melt through the centrifuge.
  • the level of viscosity of the melt in the centrifuge thus becomes a decisive factor for the economics of the process.
  • the cone jacket of the centrifuge is correspondingly larger, whereby on the one hand the cone jacket can be destroyed when the centrifuge is started while passing through the resonance frequency and on the other hand the forces occurring due to the guidance and storage of the shear element cannot be absorbed due to the design, so that they are damaged become. If the shear element is lengthened and the cone-shaped centrifuge jacket has to be lengthened, the resulting increase in size means that the centrifuge is no longer economical.
  • a cylindrical solid bowl centrifuge with a discharge screw for a continuous flow is known from the published patent application DE 44 14 750 AI by the same applicant.
  • the unpurified substance initially flows into a space of a hollow cylinder located in the central axis of the centrifuge, which carries an outside helical web as a discharge screw.
  • the plastic melt is fed through a feed pipe into the space inside the hollow cylinder, which has openings, so that the supplied material flows through the openings in the radial direction into the centrifuging stage due to the centrifugal force.
  • the discharge screw of the hollow cylinder has the task of removing the separated substance or impurities from the centrifuge, the hollow cylinder with the discharge screw rotating independently of the solid shell on which the separation of the substances takes place.
  • a shear force can be exerted on the plastic melt in the course of the feed in such a solid-bowl centrifuge, but it has been shown that no suitable device for shearing is known.
  • a solid-bowl screw centrifuging device for centrifuging viscous fluids, in particular viscous plastic melts or thermoplastic melts according to claim 1 has the advantage that a structurally separate shear device, which is operated independently of the centrifuging device, shears for such a reduction in viscosity of the fluid that the viscosity can of the fluid is reduced in an almost optimal manner.
  • This almost optimal reduction in viscosity enables economical centrifugation of highly viscous masses, since contamination of the viscous mass can be separated in a conventional centrifuging device without the melt being under a considerable the time required must be centrifuged.
  • centrifuges with lower performance can be used, which such highly viscous masses could not carry out without first reducing the viscosity.
  • the shear device Since the decrease in viscosity due to shear differs from thermoplastic to thermoplastic, it is also essential that the shear device is structurally separate from the centrifuging device in order to be able to take appropriate adaptation measures to the respective plastic.
  • the shearing process is advantageously independent of the general conditions of centrifuging, in particular the speed and the construction or size, which effectively reduces the viscosity of the fluid with regard to the entire centrifuging process. This makes economical centrifugation even for highly viscous masses effective
  • the device according to the invention makes it possible to increase the shear rate before the actual centrifuging process by a multiple and thus to considerably lower the viscosity of the melt.
  • the maximum shear force acting on the fluid can be freely selected in order to avoid destruction of the macromolecules of the plastic, which would disintegrate into several parts if the shear forces were too high. Due to the cylindrical shape of the shear surfaces ensures uniform shear over the entire area of these cylindrical shear surfaces.
  • the freely selectable speed of the rotating shear surface makes it possible to adjust the shear force depending on the height of the shear gap to a specific plastic melt in such a way that an almost optimal reduction in viscosity is achieved without the macromolecules of the plastic to destroy.
  • the viscosity of the plastic can decrease due to the almost optimally adjustable shear rate depending on the temperature up to 10% of the original viscosity value, which increases the performance of the centrifuge considerably.
  • the method according to claim 8 makes it possible to limit the shear force in such a defined way that the viscosity of the melt is considerably reduced without destroying the macromolecules of the plastic. Due to the prevailing pressure generated by an extruder, the fluid is transported spirally between the cylindrical shear surfaces, so that shearing can be carried out over the longest possible distance. With a development of the method according to claim 9, an almost optimal shear is possible due to the adjustable speed on a specific fluid or a specific thermoplastic melt.
  • a device has the advantages that the shearing process takes place immediately before centrifuging, so that an increase in viscosity after shearing does not take place, so that economical centrifuging of highly viscous masses is possible due to a reduction in viscosity before centrifuging.
  • This considerable reduction in viscosity enables economical centrifugation of highly viscous masses, since contamination of the viscous mass can be separated without the melt having to be centrifuged in a considerable amount of time.
  • centrifuges with lower performance can be used, which such highly viscous masses could not carry out without first reducing the viscosity.
  • the device according to claim 10 achieves an extremely economical centrifugation in that the plasticized viscous mass is sheared in a shearing device under pressure to reduce the viscosity before being fed to the centrifuging stage, the reduced viscosity of the fluid between the shearing device and the centrifuging stage being effected by the immediate Feed is essentially maintained. Due to the prevailing pressure, the fluid enters the centrifugation stage through the feed opening, in which an economical centrifugation of highly viscous fluids takes place due to the effective viscosity reduction.
  • the advantage is achieved that the plastic melt within the hollow cylinder of the solid bowl centrifuge is sheared as long as possible, so that the viscosity of the plastic melt is further reduced.
  • a further development according to claim 12 is also advantageous since a rotatably driven shear element enables the shear rate to be adjusted. An almost optimal viscosity reduction can thus be carried out, which can be adjusted to a specific plastic.
  • the shape of the shear element limits the shear force to a defined value as a function of the shear gap and the speed, so that a uniform, almost optimal reduction in viscosity is achieved without destroying the macromolecules due to excessive shear force.
  • Fig. 1 The dependence of the viscosity on the shear rate
  • thermoplastic 3 shows a solid bowl centrifuge, in section in the area of the shear of the thermoplastic
  • Fig. 4 is a partial view of the centrifuge of Fig. 3 in the shear area
  • 5 shows a conical head or a conical inner part 5b
  • Fig. 6 is a diagram showing the dependence of the viscosity of one
  • FIG. 8 is a sectional view of a shear device according to the present invention.
  • Fig. 9 is a top plan view of the shear device of Fig. 8; 10 shows a vertically arranged centrifuging device with a shearing device according to the present invention.
  • FIG. 11 shows a horizontal centrifuging device with a shearing device according to the present invention.
  • Fig. 1 shows the decrease in viscosity with increasing shear rate using the example of a polyethylene.
  • Fig. 2 shows the relationship between the pressure of the melt and the viscosity using the example of a polyethylene and a polystyrene.
  • the pressure dependence of thermoplastic melts is also used to reduce the viscosity. 2 shows, by way of example for thermoplastics in the thermoplastics polyethylene and polystyrene, how strongly the viscosity decreases as the pressure decreases. (Source: Westover, RF .: SPE Tech. Papers (ANTEC) 6 (1969) p. 80- 5).
  • the initial pressure of the polymeric material plasticized by the screw can be up to about 600 bar in a single-screw extruder and up to about 1000 bar in a twin-screw extruder. This pressure is released when the melt leaves the shear channel through the openings.
  • FIG. 3 shows a solid-bowl centrifuge in a vertical design with the material feed in the form of a flow channel or feed tube 1, an outer part 11 in the form of a hollow cylinder with a screw conveyor 10 and a centrifuge coat 15, partially cut open.
  • the centrifuge is mounted in a vertical design with a housing 21, the centrifuge jacket 15 and the hollow cylinder 11 in a centrifuging head 22.
  • the unpurified viscous mass enters the centrifuge.
  • the cleaned melt leaves the centrifuge at "B”.
  • the cone at the lower end of the centrifuge jacket causes the fluid to drop towards the material outlet at B, where the cleaned melt exits after centrifuging.
  • the separated impurities are removed from the centrifuge at "C”.
  • a plasticizing extruder presses the melt through the feed pipe 1 or the flow channel into the chamber space with an overpressure between 300 and 1,000 bar.
  • the head 5a or the inner part sits on the feed pipe 1.
  • the head 5a has the shape of a cylinder or a truncated cone with its base surface on the feed pipe 1.
  • the head 5a is drilled through in the extension of the feed pipe. With the head 5a in the form of a truncated cone, the shear rate in the direction of flow increases steadily up to the openings of the outer part 11.
  • the maximum possible shear rate is limited by the minimum distance between the head or inner part 5a and the hollow cylinder or outer part 11. This distance results from the dimensions of the solid particles to be separated and possibly from the amplitude of the resonance vibrations when passing through the critical speed during the Start phase.
  • the melt is sheared between the stationary head 5a and the rotating chamber wall, which is part of the hollow cylinder 11, which carries the screw conveyor on the outside and moves at 5,000 to 10,000 revolutions / min. turns.
  • the centrifuge jacket 15 is heated, preferably by induction.
  • the inductive heating of the cylindrical jacket 15 has considerable advantages over other possible methods.
  • electromagnetic heating By means of electromagnetic heating, the cylindrical jacket can be reached in a very short time to the maximum permissible temperature for each thermoplastic, taking into account the throughput time of the viscous masses.
  • An electric generator is connected to a coil for the inductive heating of the centrifuge jacket 15.
  • the generator supplies medium-frequency current, preferably between 1000 and 10,000 hearts.
  • Fig. 4 shows the material feed device within the solid bowl centrifuge in section, as well as a part of the induction coil.
  • the feed line 1 runs within a cylindrical head or inner part 5a.
  • the viscous mass flows from the plasticizing extruder (not shown) through the head 5a into the chamber 2 formed by the head 5a, the outer part 11 and an intermediate ceiling 3 and from there into a cylindrical space or shear channel 4.
  • the viscous mass is sheared between the stationary head 5a and the outer part 11 rotating at high speed.
  • the material which has become less viscous, exits through the openings 12 under the action of the centrifugal forces and flows against the centrifuge jacket 15.
  • the outer part 11 carries the webs 13 on the outside, through which the screw conveyor 10 is formed.
  • the screw conveyor 10 conveys the material centrifuged on the centrifuge jacket 15 in the direction of a cone opening 17 ("C" in Fig. 3).
  • the outer part 11 is drawn into a cone 14. Remnants of melt that have not emerged through the feed openings 12 in the outer part 11 are conveyed back to the feed openings 12 by the centrifugal force.
  • the conical part 14 of the outer part 11 thus has the effect of a seal.
  • the melt reaches the centrifuging stage 18 from the feed openings.
  • the lower part of the centrifuge jacket 15, which also rotates at high speeds, is also drawn into a cone 16 for the solids outlet.
  • the centrifuge jacket 15 is located in an outer jacket 21 made of a non-magnetizable material, such as light metal, non-ferrous metal or titanium.
  • Fig. 5 shows a conical or conical design of the inner part.
  • FIGS. 6 and 7 show three LDPE types which are used, inter alia, for packaging films, which represent the dependence of the viscosity or the kinematic viscosity of various polyethylenes on the shear rate D with respect to a temperature level. 7 shows a reduction in viscosity of up to 10% of the original value for alkatenes 46 with a temperature of 210 ° C. and a shear rate D of approx. 5 l / sec, which corresponds to a rate of 5 cm per second per cm of flow layer thickness . Due to this reduction in viscosity, a theoretical increase in performance of a downstream centrifuging device is calculated to ten times the original performance.
  • FIG. 8 shows a shear device 30 according to the present invention, which has a rotatably driven inner part 31 and a fixed outer part 32, which are geometrically similar to one another.
  • the fluid is introduced into the shear device 30 via an inflow pipe 34 through a tangentially arranged inflow opening 36, a shear gap 33 being formed between the rotating inner part 31 and the fixed outer part 32.
  • the fluid is evenly sheared between a cylindrical shear surface 39 of the rotating inner part 31 and a cylindrical shear surface 40 of the fixed outer part 32 due to a constant speed and thus a constant shear rate.
  • the fluid is supplied to the conically tapered region of the shear gap during a spiral circulation in the shear gap 33.
  • the fluid is accelerated due to the reduced diameter and fed to an outflow opening 37. Furthermore, due to the reduced diameter, there is only less shear than in the cylindrical section of the shear channel, so that the reduced viscosity is only maintained.
  • a feed tube 35 of the Huid directly adjoins the outflow opening 37, the inside diameter of the feed tube 35 corresponding to the diameter of the outflow opening 37.
  • the rotating inner part 31 is driven by a freely selectable drive shaft 38.
  • FIG. 9 shows the approximately tangential inflow of the fluid via the inflow pipe 34 into the shear channel 33.
  • the rotating inner part 31 and the outflow opening 37 are also shown.
  • the fluid is introduced into the shearing device 30 via the inflow pipe 34 and introduced into a hollow cylinder 51 of the centrifuging device 50 via a feed pipe 35 from the shearing device 30 in such a way that the fluid is sheared by the shearing device 30 through a immediate feeding into the centrifugation stage 54 of the full jacket-screw centrifuge 50 is introduced almost continuously under pressure such that the fluid after it emerges from the feed pipe 35 is deflected by means of a deflection device 52 directly into the area of feed openings 53 in the hollow cylinder 51, through which the fluid is retained of the reduced viscosity in the radial direction enters the centrifugation stage 54, so that the reduced viscosity of the fluid caused by the shear action is substantially maintained.
  • the deflection device 52 preferably has a tip aligned with the feed pipe 35, which is arranged in the region of the feed pipe 35, the fluid being distributed uniformly only in the circumferential direction by the deflection device 52 and via the feed openings 53, which are essentially in the middle of the centrifugation stage 54 are arranged, directly enters the centrifugation stage 54, the centrifugation stage 54 preferably being inductively heatable to maintain viscosity.
  • the feed openings 53 extend over the entire circumference of the
  • FIG. 11 shows a horizontal solid bowl centrifuge which is constructed similarly to the vertical solid bowl centrifuge shown in FIG. 10.
  • the vertically designed solid bowl centrifuge has a plurality of feed openings 53 in the hollow cylinder 51.
  • the rotating outer jacket 57 of the centrifuge is mounted only once, the lower end of the centrifuge jacket 57 being stabilized by the gyroscopic effect.
  • the centrifugal number Z of such centrifuges is in a range from approximately 1000 to 5000, preferably in a range from 2500 to 3500, which is calculated as follows:

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  • Centrifugal Separators (AREA)

Abstract

L'invention concerne des dispositifs pour centrifuger des fluides visqueux, notamment des matières plastiques fondues visqueuses, et un dispositif de cisaillement ainsi qu'un procédé pour cisailler des fluides visqueux, notamment des matières plastiques fondues visqueuses. La viscosité du fluide est nettement réduite par sollicitation mécanique avant l'étage de centrifugation, dans un dispositif de cisaillement (30), afin de permettre une centrifugation économique de fluides visqueux. Ce fluide est soumis, afin de réduire sa viscosité, à une contrainte de cisaillement entre une partie intérieure en rotation (31) et une partie extérieure fixe (32) dans un canal de cisaillement (33) à l'intérieur du dispositif du cisaillement (30), afin de permettre une élimination rentable des impuretés du fluide de viscosité élevée, dans l'étage de centrifugation (54). Les impuretés du fluides dans l'étage de centrifugation (54) sont évacuées du dispositif de centrifugation dans le sens opposé à l'écoulement du fluide épuré, le long de la gaine de centrifugeur (57).
PCT/EP1998/005541 1997-09-01 1998-09-01 Procede et dispositif pour centrifuger des fluides visqueux Ceased WO1999011379A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
DE59800897T DE59800897D1 (de) 1997-09-01 1998-09-01 Vorrichtung zum zentrifugieren von viskosen fluiden
AU10228/99A AU1022899A (en) 1997-09-01 1998-09-01 Method and device for centrifuging viscous fluids
EP98952584A EP1011867B1 (fr) 1997-09-01 1998-09-01 Dispositif pour centrifuger des fluides visqueux

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19738128.6 1997-09-01
DE19738128A DE19738128A1 (de) 1997-09-01 1997-09-01 Verfahren und Vorrichtung zum Zentrifugieren von viskosen Fluiden, insbesondere viskosen Kunststoffschmelzen

Publications (1)

Publication Number Publication Date
WO1999011379A1 true WO1999011379A1 (fr) 1999-03-11

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ID=7840834

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP1998/005541 Ceased WO1999011379A1 (fr) 1997-09-01 1998-09-01 Procede et dispositif pour centrifuger des fluides visqueux

Country Status (4)

Country Link
EP (1) EP1011867B1 (fr)
AU (1) AU1022899A (fr)
DE (2) DE19738128A1 (fr)
WO (1) WO1999011379A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111437783A (zh) * 2020-05-19 2020-07-24 福州大学 一种高粘流体形态尺寸精准控制的连续生成装置

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB449542A (en) * 1934-12-27 1936-06-29 John Philip Baxter Process for the treatment of solutions of chlorinated rubber
DE2814217A1 (de) * 1977-04-04 1978-10-12 Dyno Industrier As Verfahren und vorrichtung zum kontinuierlichen herstellen eines explosivstoffs
WO1987006496A1 (fr) * 1986-04-25 1987-11-05 Bernard Alzner Dispositif de melange
WO1991013686A1 (fr) * 1990-03-13 1991-09-19 Alfa-Laval Separation A/S Separateur centrifuge
DE4414750A1 (de) * 1993-04-29 1995-01-05 Rolf Schnause Verfahren und Vorrichtung zum Reinigen viskoser Kunststoffschmelzen
DE19527784A1 (de) * 1995-07-28 1997-01-30 Vit Robert Vorrichtung zum Eindicken und Fördern von Abwässerschlämmen

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB449542A (en) * 1934-12-27 1936-06-29 John Philip Baxter Process for the treatment of solutions of chlorinated rubber
DE2814217A1 (de) * 1977-04-04 1978-10-12 Dyno Industrier As Verfahren und vorrichtung zum kontinuierlichen herstellen eines explosivstoffs
WO1987006496A1 (fr) * 1986-04-25 1987-11-05 Bernard Alzner Dispositif de melange
WO1991013686A1 (fr) * 1990-03-13 1991-09-19 Alfa-Laval Separation A/S Separateur centrifuge
DE4414750A1 (de) * 1993-04-29 1995-01-05 Rolf Schnause Verfahren und Vorrichtung zum Reinigen viskoser Kunststoffschmelzen
DE19527784A1 (de) * 1995-07-28 1997-01-30 Vit Robert Vorrichtung zum Eindicken und Fördern von Abwässerschlämmen

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111437783A (zh) * 2020-05-19 2020-07-24 福州大学 一种高粘流体形态尺寸精准控制的连续生成装置

Also Published As

Publication number Publication date
AU1022899A (en) 1999-03-22
EP1011867B1 (fr) 2001-06-20
EP1011867A1 (fr) 2000-06-28
DE59800897D1 (de) 2001-07-26
DE19738128A1 (de) 1999-03-11

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