EP1768770B1 - Method for mixing, device for the same and use thereof - Google Patents

Method for mixing, device for the same and use thereof Download PDF

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Publication number
EP1768770B1
EP1768770B1 EP05752464A EP05752464A EP1768770B1 EP 1768770 B1 EP1768770 B1 EP 1768770B1 EP 05752464 A EP05752464 A EP 05752464A EP 05752464 A EP05752464 A EP 05752464A EP 1768770 B1 EP1768770 B1 EP 1768770B1
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EP
European Patent Office
Prior art keywords
suspension
stator
pulp
rotor
rotary mixer
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EP05752464A
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German (de)
French (fr)
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EP1768770A1 (en
Inventor
Berndt Cupak
Anton Ortner
Johann GRÖSTLINGER
Andreas Krotscheck
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Lenzing Technik GmbH
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Lenzing Technik GmbH
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Priority to AT05752464T priority Critical patent/ATE409076T1/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/50—Pipe mixers, i.e. mixers wherein the materials to be mixed flow continuously through pipes, e.g. column mixers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/50—Mixing liquids with solids
    • B01F23/53—Mixing liquids with solids using driven stirrers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/27—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices
    • B01F27/272—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices with means for moving the materials to be mixed axially between the surfaces of the rotor and the stator, e.g. the stator rotor system formed by conical or cylindrical surfaces
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/05—Stirrers
    • B01F27/07—Stirrers characterised by their mounting on the shaft
    • B01F27/072—Stirrers characterised by their mounting on the shaft characterised by the disposition of the stirrers with respect to the rotating axis
    • B01F27/0721—Stirrers characterised by their mounting on the shaft characterised by the disposition of the stirrers with respect to the rotating axis parallel with respect to the rotating axis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/05—Stirrers
    • B01F27/07—Stirrers characterised by their mounting on the shaft
    • B01F27/072—Stirrers characterised by their mounting on the shaft characterised by the disposition of the stirrers with respect to the rotating axis
    • B01F27/0724—Stirrers characterised by their mounting on the shaft characterised by the disposition of the stirrers with respect to the rotating axis directly mounted on the rotating axis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/27—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices
    • B01F27/271—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices with means for moving the materials to be mixed radially between the surfaces of the rotor and the stator
    • B01F27/2712—Mixers with stator-rotor systems, e.g. with intermeshing teeth or cylinders or having orifices with means for moving the materials to be mixed radially between the surfaces of the rotor and the stator provided with ribs, ridges or grooves on one surface

Definitions

  • the object of the invention is to obviate these disadvantages and difficulties, and has set itself the task of a method of the type described above and a device for optimum continuous mixing and / or fluidization of a suspension or pulp and / or for mixing in gaseous and / or liquid media To create a suspension or a pulp, with which it is possible to accomplish the mixing process or the mixing efficiently and possibly over a longer period of time with little effort.
  • this oversized dimensions of the device serving for this purpose or inadmissibly high peripheral speeds should be avoided.
  • a further preferred variant is characterized in that the width of the flow breaker is in the range between 1/100 to 10/1 whose height.
  • At least some flow breakers and / or drivers extend only over partial regions of the length of the rotary mixer and are preferably arranged offset to one another in the circumferential direction.
  • Fig. 1 shows a view of a rotary mixer.
  • Fig. 2 represents one according to line II-II of the Fig. 1 guided section dar.
  • a rotatably mounted about its longitudinal axis 3 rotor 4 is provided, the bearing 5 are arranged on the drum 1 frontally closing walls 6.
  • a drive shaft 7 of the rotor 4 extends beyond a bearing 5 and is driven by a motor 8.
  • the rotor 4 can also be designed as a single-sided, cantilevered unit.
  • the inlet and outlet openings 11 ', 12' for the suspension or pulp and chemicals 4 are arranged either radially on the stator 2 or parallel to the longitudinal axis 3 of the rotor 4.
  • flow baffles 15 extending essentially transversely to the circumferential direction of the drum 1 are arranged.
  • the rotor 4 has drivers 16 extending substantially transversely to the circumferential direction.
  • the axis 3 of the rotor 4 is arranged eccentrically with respect to the axis 9 of the stator 2 by the dimension e.
  • a gap is thereby formed between the circle of the driver 16 and the flow breakers 15, the thickness at its narrowest point 17 from 0.02 to 80 and at its widest point 18 a thickness of 1 to 90, each in Percent of the inner diameter D of the stator.
  • Another characteristic is the very efficient interference, i. especially in the mixing of gases, a very homogeneous, fine-pored dispersion is achieved, which finely distributes the gaseous chemicals directly to the fibers of the suspension and there enables the reaction with the pulp.
  • a special application of the rotary mixer is primarily for fiber suspensions, e.g. Pulp having a consistency of 4 to 20% with other fluids (bleaching chemicals), e.g. H2O2, ClO2, NaOH, O3, O2, Cl, N, etc., as well as further for transport-limited reactions for the production of viscose or mash by mixing solvents or Aushärtesubstanzen.
  • fiber suspensions e.g. Pulp having a consistency of 4 to 20% with other fluids (bleaching chemicals), e.g. H2O2, ClO2, NaOH, O3, O2, Cl, N, etc.
  • Pulp is conveyed through a medium-consistency pump under a pressure of 1 to 20 barü to the rotary mixer.
  • the ozone gas is also added to the rotary mixer.
  • the pulp is fluidized very quickly and at the same time the ozone gas is mixed into the pulp suspension in a very homogeneous and fine-pored manner.
  • the main reaction takes place in the fluidized state, wherein the ozone gas comes in the form of small bubbles directly to the fiber and there takes place the bleaching reaction.
  • a much better reaction is already achieved in the rotary mixer.
  • the chemical reaction after the rotary mixer is more efficient than with conventional mixing principles. That At lower ozone inputs, a higher ozone conversion is achieved. Finally, the largely reacted ozone gas is separated from the pulp suspension via a degassing vessel.
  • Pulp is fed to the rotary mixer at a pressure of 3 to 20 bar.
  • the oxygen gas is also added to the rotary mixer.
  • the pulp is fluidized very quickly and at the same time the oxygen gas is mixed very homogeneously and with fine pores into the pulp suspension.
  • the main reaction takes place in the subsequent reactor with a relatively long residence time of up to two hours. Due to the more efficient mixing of the oxygen gas and the generation of a very homogeneous and fine-pored dispersion, a higher delignification rate is achieved with the same residence time in the reactor than in previous mixing principles.
  • the mixing principle is also excellent for incorporation of liquid chemicals, e.g. Chloride oxide or hydrogen peroxide in a medium-consistency pulp suspension.
  • liquid chemicals e.g. Chloride oxide or hydrogen peroxide
  • a shorter mixer length can be selected, since in the first instance the efficient mixing and not the increased residence time in the fluidized state comes into play.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Dispersion Chemistry (AREA)
  • Paper (AREA)
  • Mixers Of The Rotary Stirring Type (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)

Abstract

In a process for continuous blending and/or fluidization of a suspension or a pulp and/or for incorporation of gaseous and/or liquid media into a suspension or pulp, respectively, in particular into a suspension of a fibrous material with fluids, the suspension or pulp, respectively, is subjected to shear forces in a rotary mixer. So as to be able to effect blending or incorporation, respectively, of media into the suspension or pulp, respectively, in an efficient manner and, optionally, over an extended period of time, the suspension or pulp, respectively, is subjected to shear forces of varying sizes across the circumference of the rotary mixer (FIG. 2 ).

Description

Die Erfindung betrifft ein Verfahren zum kontinuierlichen Durchmischen und/oder Fluidisieren einer Suspension oder einer Pulpe und/oder zum Einmischen von gasförmigen und/oder flüssigen Medien in eine Suspension bzw. eine Pulpe, insbesondere in eine Suspension aus einem faserartigen Stoff mit Fluiden, wobei die Suspension bzw. Pulpe in einem Rotationsmischer über den Umfang des Rotationsmischers unterschiedlich großen Scherkräften ausgesetzt wird, sowie eine Vorrichtung zur Durchführung des Verfahrens und weiters eine Verwendung der Vorrichtung.The invention relates to a method for continuously mixing and / or fluidizing a suspension or a pulp and / or for mixing gaseous and / or liquid media in a suspension or a pulp, in particular in a suspension of a fibrous material with fluids, wherein the Suspension or pulp is exposed in a rotary mixer over the circumference of the rotary mixer of different sizes shear forces, and a device for carrying out the method and further use of the device.

Um Suspensionen aus einem zähflüssigen Zustand in einen leicht fließfähigen sozusagen dünnflüssigen Zustand zu bringen, ist ein Durchmischen erforderlich, insbesondere für Suspensionen aus Zellstoff und Wasser. Erst wenn dieser leicht fließfähige Zustand - auch fluidisierter Zustand genannt - der Suspension erzielt ist, kann die Suspension gut durchmischt werden und weiters mit Medien versetzt werden, die beispielsweise Chemikalien sind, die mit der Suspension eine Reaktion eingehen bzw. die sich gegenüber der Suspension inert verhalten, wie beispielsweise ein Farbstoff etc.In order to bring suspensions from a viscous state into an easily flowable, so to speak, low-viscosity state, thorough mixing is necessary, in particular for pulp and water suspensions. Only when this easily flowable state - also called fluidized state - the suspension is achieved, the suspension can be well mixed and further mixed with media, which are, for example, chemicals that react with the suspension or which are inert to the suspension behave, such as a dye, etc.

Zu diesem Zweck ist es bekannt, Zellstoff zwischen einer sich drehenden Rotorscheibe mit strahlenartig angeordneten Radialrippen und einer stillstehenden Statorscheibe mit Rippen zu fluidisieren. Die Fluidisierung erfolgt ausschließlich in der sich einstellenden radialen Strömung von Innen nach Außen und ist nach Erreichen des Außenumfangs der Rotorscheibe beendet. Hierdurch lässt sich nur eine kurzzeitige Fluidisierung erzielen, zumal für länger auftretende Fluidsierungen die Rotor- und Statorscheibe extrem große Durchmesser annehmen müssten. Dies würde wiederum extrem hohe Umfangsgeschwindigkeiten und aufwendige Konstruktionen ergeben.For this purpose, it is known to fluidize pulp between a rotating rotor disk with radially arranged radial ribs and a stationary stator with ribs. The fluidization takes place exclusively in the self-adjusting radial flow from inside to outside and is completed after reaching the outer periphery of the rotor disk. As a result, only a short-term fluidization can be achieved, especially for longer occurring fluidizations, the rotor and stator would have to accept extremely large diameter. This in turn would result in extremely high peripheral speeds and complex designs.

Beispielsweise ist aus der US 2,448,042 ein Verfahren zum kontinuierlichen Durchmischen und/oder Fluidisieren einer Suspension oder einer Pulpe und/oder zum Einmischen von gasförmigen und/oder flüssigen Medien mittels eines Roatationsmischers in eines Suspension bzw. eine Pulpe, insbesondere in eine Suspension aus einem faserartigen Stoff mit Fluiden, wobei die Suspension bzw. die Pulpe vom Eintritt bis zum Austritt des Rotationsmischers zusätzlich entlang seiner Länge bzw. Längsachse bewegt wird, wobei die Suspension bzw. Pulpe in dem Rotationsmischer über den Umfang des Rotationsmischers unterschiedlich großen Scherkräften ausgesetzt wird. Eine Vorrichtung zur Durchführung des Verfahrens zum kontinuierlichen Durchmischen und/oder Fluidisieren einer Suspension oder einer Pulpe und/oder zum Einmischen von gasförmigen und/oder flüssigen Medien mittels eines Roatationsmischers in eines Suspension bzw. eine Pulpe, insbesondere in eine Suspension aus einem faserartigen Stoff mit Fluiden, umfasst einen Stator, und einen an dem Stator um seine Achse drehbar gelagerten Rotor, wobei die Achse des rotors zur Achse des Stators versetzt angeordnet ist, sowie mit einer Ein- und Austrittsöffnung für die Suspension bzw. Pulpe, wobei die Eintrittsöffnung zur Austrittsöffnung in Richtung der als Längsachse ausgebildeten Stators distanziert angeordnet ist.For example, is from the US 2,448,042 a method for continuously mixing and / or fluidizing a suspension or a pulp and / or for mixing gaseous and / or liquid media by means of a roasting mixer in a suspension or a pulp, in particular in a suspension of a fibrous material with fluids, wherein the Suspension or the pulp from the inlet to the outlet of the rotary mixer is additionally moved along its length or longitudinal axis, wherein the suspension or pulp is exposed in the rotary mixer over the circumference of the rotary mixer of different sizes shear forces. A device for carrying out the method for continuously mixing and / or fluidizing a suspension or a pulp and / or mixing of gaseous and / or liquid media by means of a roasting mixer in a suspension or a pulp, in particular in a suspension of a fibrous material with Fluids, comprising a stator, and a rotor rotatably mounted on the stator about its axis, wherein the axis of the rotor is arranged offset to the axis of the stator, and with an inlet and outlet opening for the suspension or pulp, wherein the inlet opening to the outlet opening is arranged distanced in the direction of the stator formed as a longitudinal axis.

Aus der US 2,402,905 ist ebenfalls ein Verfahren und eine Vorrichtung zum Durchmischen einer Suspension oder Pulpe bekannt. Auch hier ist ein Rührwerk exzentrisch gelagert in einer äußeren Kammer vorgesehen, wobei das Rührwerk Öffnungen aufweist, welche die äußere Kammer mit einer inneren Kammer des Rührwerks verbinden. Das Rührwerk weist Schaufeln auf, die sich in die innere und äußere Kammer erstrecken.From the US 2,402,905 Also, a method and apparatus for mixing a suspension or pulp is known. Again, an agitator is eccentrically mounted in an outer chamber, wherein the agitator has openings which connect the outer chamber with an inner chamber of the agitator. The agitator has blades which extend into the inner and outer chambers.

Das Dokument US 4,205,919 zeigt ein Verfahren zur Erzeugung eines kontinuierlichen Materialstroms, in dem wenigstens ein Bestandteil aus einem kleinkörnigen Material besteht. Die kleinkörnigen Materialbestandteile werden in ein rohrförmiges Gehäuse eingespeist, das einen skelettförmigen Rotor enthält der relativ zum Gehäuse umläuft und dabei ein Umwälzen sowie eine Transportbewegung des Materials längs des rohrförmigen Gehäuses bewirkt, wodurch ein kontinuierlicher Materialstrom erzeugt wird.The document US 4,205,919 shows a method for producing a continuous stream of material in which at least one component consists of a small-grained material. The small-grained material components are fed into a tubular housing containing a skeletal rotor which rotates relative to the housing, thereby causing a circulation and a transport movement of the material along the tubular housing, whereby a continuous flow of material is generated.

Die US 2003 072216 A1 zeigt ein zylindrisches Mischgefäß, in welchem eine rotierende Welle mit daran ausgebildeten Schaufeln angeordnet ist. An einer Innenwandung des Mischgefäßes sind ebenfalls Schaufeln ausgebildet, wobei die Schaufeln an der Welle und diejenigen an der Innenwandung eine bestimmte, feste Länge aufweisen und nicht miteinander in Kontakt kommen.The US 2003 072216 A1 shows a cylindrical mixing vessel in which a rotating shaft is arranged with blades formed thereon. On an inner wall of the mixing vessel also blades are formed, wherein the blades on the shaft and those on the inner wall have a certain, fixed length and do not come into contact.

Verfahren und Einrichtungen zum Fluidisieren sind weiters aus der EP 0 664 150 A1 und der US 5,813,758 A bekannt. Beide Dokumente weisen Einrichtungen auf, bei denen in einem Stator zentrisch ein Rotor angeordnet ist, der mit Mitnehmern ausgestattet ist, die eine Fluidisierung einer Suspension bzw. ein Einmischen eines Gases in eine Pulpe ermöglichen. Die Suspension bzw. die Pulpe durchströmt hierbei sehr enge Spalte zwischen Stator und Rotor, wobei die Spalte parallel zur Rotorachse oder geneigt hierzu bzw. radial gerichtet sind. Auch gemäß diesen Dokumenten gelingt es nicht, eine Suspension bzw. Pulpe über einen längeren Zeitraum dünnflüssig zwecks Einmischen von Gasen oder flüssigen Medien zu halten. Gemäß der US 5,813,758 A ergeben sich durch die größtenteils radiale Verbringung der Suspension vom zentrischen Zulauf bis zum Auslauf ebenfalls extrem große Vorrichtungen mit den daraus resultierenden Nachteilen hoher Umfangsgeschwindigkeiten.Methods and apparatus for fluidizing are further from the EP 0 664 150 A1 and the US 5,813,758 A known. Both documents have facilities in which a rotor is arranged centrally in a stator, which is equipped with drivers that enable a fluidization of a suspension or a mixing of a gas into a pulp. The suspension or the pulp flows through very narrow gaps between stator and rotor, the gaps being directed parallel to the rotor axis or inclined thereto or radially. Even according to these documents, it is not possible to keep a suspension or pulp thin over a longer period of time for the purpose of mixing in gases or liquid media. According to the US 5,813,758 A resulting from the largely radial movement of the suspension from the centric inlet to the outlet also extremely large devices with the resulting disadvantages of high peripheral speeds.

Ein Verfahren der eingangs beschriebenen Art ist aus der US 5,575,559 A bekannt, bei dem der Durchfluss einer Suspension bzw. Pulpe senkrecht zur Achse des Rotationsmischers erfolgt. Dies bedingt - soll ein Durchmischen über einen längeren Zeitraum stattfinden - einen großen Durchmesser des Rotationsmischers, was aus Gründen des Platzbedarfes und hoher Umfangsgeschwindigkeiten nachteilig ist.A method of the type described above is known from US 5,575,559 A known, in which the flow of a suspension or pulp is perpendicular to the axis of the rotary mixer. This requires - should take place a mixing over a longer period - a large diameter of the rotary mixer, which is disadvantageous for reasons of space requirements and high peripheral speeds.

Aus der AT 372 992 B ist ein Rotationsmischer für Suspensionen bzw. Pulpen bekannt, bei dem ein Rotor in einem Stator zentrisch angeordnet ist, wobei in einem Spalt zwischen einem im Querschnitt mehreckigen Rotor und Stator rippenartige Vorsprünge vorgesehen sind. Hierdurch wird ein Pulsieren einer auf die Suspension wirkende Scherkraft erreicht, wobei diese pulsierende Scherkraft jedoch über den Umfang gleichmäßig verteilt auftritt.From the AT 372 992 B a rotary mixer for suspensions or pulp is known in which a rotor is arranged centrally in a stator, wherein rib-like projections are provided in a gap between a cross-sectionally polygonal rotor and stator. As a result, a pulsation of a shearing force acting on the suspension is achieved, but this pulsating shear force occurs evenly distributed over the circumference.

Die Erfindung bezweckt die Vermeidung dieser Nachteile und Schwierigkeiten und stellt sich die Aufgabe, ein Verfahren der eingangs beschriebenen Art und eine Vorrichtung zum optimalen kontinuierlichen Durchmischen und/oder Fluidisieren einer Suspension oder einer Pulpe und/oder zum Einmischen von gasförmigen und/oder flüssigen Medien in eine Suspension bzw. eine Pulpe zu schaffen, mit welcher es möglich ist, mit geringem Aufwand, den Einmischvorgang bzw. das Durchmischen effizient und ggf. über einen längeren Zeitraum zu bewerkstelligen. Insbesondere sollen hierbei übergroße Abmessungen der hierzu dienenden Vorrichtung bzw. unzulässig hohe Umfangsgeschwindigkeiten vermieden werden.The object of the invention is to obviate these disadvantages and difficulties, and has set itself the task of a method of the type described above and a device for optimum continuous mixing and / or fluidization of a suspension or pulp and / or for mixing in gaseous and / or liquid media To create a suspension or a pulp, with which it is possible to accomplish the mixing process or the mixing efficiently and possibly over a longer period of time with little effort. In particular, this oversized dimensions of the device serving for this purpose or inadmissibly high peripheral speeds should be avoided.

Diese Aufgabe der Erfindung wird bei einem Verfahren der eingangs beschriebenen Art dadurch gelöst, dass die Suspension bzw. die Pulpe vom Eintritt bis zum Austritt des Rotationsmischers zusätzlich entlang seiner Länge bzw. Längsachse bewegt wird.This object of the invention is achieved in a method of the type described above in that the suspension or the pulp is additionally moved from the inlet to the outlet of the rotary mixer along its length or longitudinal axis.

Für den Fall, dass die Hauptreaktion mit einer zugemischten Chemikalie innerhalb des Rotationsmischers stattfindet, erfolgt die Bemessung der Verweilzeit der Suspension und damit die Reaktionszeit dadurch, dass das Volumen des Rotationsmischers, insbesondere dessen Länge, dementsprechend gestaltet wird.In the event that the main reaction takes place with an admixed chemical within the rotary mixer, the design of the residence time of the suspension and thus the reaction time takes place in that the volume of the rotary mixer, in particular its length, is designed accordingly.

Selbstverständlich ist es auch möglich in die Suspension ein gasförmiges oder flüssiges Medium einzubringen, wie beispielsweise Sauerstoff, mit dem eine Hauptreaktion erst außerhalb des Rotationsmischers stattfindet, wobei durch Bemessung des Volumens des Rotationsmischers, insbesondere dessen Länge, die Verweilzeit der Suspension so bestimmt wird, dass eine Hauptreaktion außerhalb des Rotationsmischers stattfindet.Of course, it is also possible to introduce into the suspension a gaseous or liquid medium, such as oxygen, with which a main reaction takes place only outside the rotary mixer, wherein by dimensioning the volume of the Rotary mixer, in particular its length, the residence time of the suspension is determined so that a main reaction takes place outside the rotary mixer.

Weiters ist es möglich in die Suspension ein inertes gasförmiges oder flüssiges Medium einzuleiten, wie beispielsweise einen Farbstoff mit dem keine chemische Reaktion erfolgt.Furthermore, it is possible to introduce into the suspension an inert gaseous or liquid medium, such as a dye with which no chemical reaction takes place.

Das erfindungsgemäße Verfahren lässt eine breite Anwendung zu, insbesondere für Zellstoffsuspensionen mit einer Stoffdichte zwischen 4 und 20%, insbesondere zwischen 8 und 15%.The process according to the invention allows a broad application, in particular for pulp suspensions with a consistency between 4 and 20%, in particular between 8 and 15%.

Eine Vorrichtung zum Durchmischen einer Suspension oder Pulpe und/oder zum Einmischen von gasförmigen und/oder flüssigen Medien in eine Suspension oder Pulpe, insbesondere in eine Suspension aus einem faserartigen Stoff mit Fluiden, mit einem Stator und einem am Stator um seine Achse drehbar gelagerten Rotor, wobei die Achse des Rotors zur Achse des Stators versetzt angeordnet ist, sowie mit einer Ein- und Austrittsöffnung für die Suspension bzw. die Pulpe, ist dadurch gekennzeichnet, dass die Eintrittsöffnung zur Austrittsöffnung in Richtung der als Längsachse ausgebildeten Achse des Stators distanziert angeordnet ist.A device for mixing a suspension or pulp and / or mixing of gaseous and / or liquid media in a suspension or pulp, in particular in a suspension of a fibrous material with fluids, with a stator and a rotatably mounted on the stator about its axis rotor , wherein the axis of the rotor is arranged offset to the axis of the stator, and with an inlet and outlet opening for the suspension or the pulp, characterized in that the inlet opening to the outlet opening in the direction of the axis formed as a longitudinal axis of the stator is arranged at a distance ,

Vorzugsweise ist die Längsachse des Rotors parallel zur Längsachse des Stators angeordnet.Preferably, the longitudinal axis of the rotor is arranged parallel to the longitudinal axis of the stator.

Eine bevorzugte Ausführungsform ist dadurch gekennzeichnet, dass eine Exzentrizität zwischen der Längsachse des Stators und der Längsachse des Rotors im Bereich von 1/200 bis 1/2 des Innendurchmessers der Trommel des Stators liegt.A preferred embodiment is characterized in that an eccentricity between the longitudinal axis of the stator and the longitudinal axis of the rotor in the range of 1/200 to 1/2 of the inner diameter of the drum of the stator.

Weiters ist es vorteilhaft, wenn das Verhältnis des Außendurchmessers des Rotors zum Innendurchmesser der Trommel des Stators im Bereich von 1:1,1 bis 1:5 liegt, wobei zweckmäßig die Höhe der Strömungsbrecher im Bereich zwischen 1/50 bis 1/1,4 des Außendurchmessers des Rotors liegt.Furthermore, it is advantageous if the ratio of the outer diameter of the rotor to the inner diameter of the drum of the stator in the range of 1: 1.1 to 1: 5, expediently the height of the flow breaker in the range between 1/50 to 1 / 1.4 the outer diameter of the rotor is located.

Eine weitere bevorzugte Variante ist dadurch gekennzeichnet, dass die Breite der Strömungsbrecher im Bereich zwischen 1/100 bis 10/1 deren Höhe liegt.A further preferred variant is characterized in that the width of the flow breaker is in the range between 1/100 to 10/1 whose height.

Vorzugsweise sind am Stator sich im Wesentlichen quer zur Umfangsrichtung erstreckende Strömungsbrecher und am Rotor sich im Wesentlichen quer zur Umfangsrichtung erstreckende Mitnehmer vorgesehen, wobei vorteilhaft sich die Strömungsbrecher und/oder die Mitnehmer durchgehend über die Länge des Rotationsmischers von der Eintrittsöffnung bis zur Austrittsöffnung erstrecken.Preferably, on the stator are substantially transversely to the circumferential direction extending flow breaker and the rotor is provided substantially transversely to the circumferential direction extending driver, wherein advantageously the flow breaker and / or the drivers extend continuously over the length of the rotary mixer from the inlet to the outlet.

Gemäß einer bevorzugten Ausführungsform erstrecken sich zumindest einige Strömungsbrecher und/oder Mitnehmer nur über Teilbereiche der Länge des Rotationsmischers und sind vorzugsweise in Umfangsrichtung versetzt zueinander angeordnet.According to a preferred embodiment, at least some flow breakers and / or drivers extend only over partial regions of the length of the rotary mixer and are preferably arranged offset to one another in the circumferential direction.

Der Eintrittsstutzen und/oder der Austrittsstutzen kann (können) radial zur Längsachse des Stators oder auch in Richtung der Längsachse des Stators ausgerichtet sein. Erfolgt eine Zumischung eines Mediums, so mündet eine Zuleitung für das Medium in den Stator im Bereich des Eintrittsstutzens bzw. werden mehrere Medieneintrittsstutzen über die Länge des Mischers verteilt angeordnet.The inlet nozzle and / or the outlet nozzle can (can) be aligned radially to the longitudinal axis of the stator or in the direction of the longitudinal axis of the stator. If an admixture of a medium, so opens a supply line for the medium in the stator in the region of the inlet nozzle or multiple media inlet nozzle distributed over the length of the mixer.

Gemäß einer bevorzugten Variante ist zwischen den Strömungsbrechern des Stators und den Mitnehmern des Rotors ein Spalt in radialer Richtung vorgesehen, der an seiner engsten Stelle im Bereich von 0,02 bis 80 und an seiner weitesten Stelle von 1 bis 90 jeweils in Prozent des Innendurchmessers des Stators liegt.According to a preferred variant, a gap in the radial direction is provided between the flow breakers of the stator and the drivers of the rotor, which at its narrowest point in the range of 0.02 to 80 and at its widest point from 1 to 90, each in percent of the inner diameter of Stators is.

Eine Verwendung der erfindungsgemäßen Vorrichtung ist insbesondere für die Zellstoffindustrie von Vorteil, wie zum Herstellen von Mehrphasengemischen hauptsächlich bestehend aus einer Suspension von Zellstoff, Wasser und Chemikalien (in flüssigem, gasförmigem oder festem Aggregatzustand oder zum Herstellen eines Mehrphasengemisches aus Altpapier und Wasser.Use of the device according to the invention is particularly advantageous for the pulp industry, such as for producing multiphase mixtures mainly consisting of a suspension of pulp, water and chemicals (in liquid, gaseous or solid state or for producing a multiphase mixture of waste paper and water.

Die Erfindung ist nachstehend anhand eines in der Zeichnung dargestellten Ausführungsbeispiels näher erläutert, worin Fig. 1 eine Ansicht eines Rotationsmischers zeigt. Fig. 2 stellt einen gemäß der Linie II-II der Fig. 1 geführten Schnitt dar.The invention is explained below with reference to an embodiment shown in the drawing, wherein Fig. 1 shows a view of a rotary mixer. Fig. 2 represents one according to line II-II of the Fig. 1 guided section dar.

In einer im wesentlichen zylindrisch gestalteten Trommel 1, die als Stator 2 eines Rotationsmischers dient, ist ein um seine Längsachse 3 drehbar gelagerter Rotor 4 vorgesehen, dessen Lager 5 an die Trommel 1 stirnseitig verschließenden Wänden 6 angeordnet sind. Eine Antriebswelle 7 des Rotors 4 erstreckt sich über ein Lager 5 hinaus und ist mittels eines Motors 8 antreibbar. Der Rotor 4 kann auch als einseitig, fliegend gelagerte Einheit ausgeführt werden.In a substantially cylindrical shaped drum 1, which serves as a stator 2 of a rotary mixer, a rotatably mounted about its longitudinal axis 3 rotor 4 is provided, the bearing 5 are arranged on the drum 1 frontally closing walls 6. A drive shaft 7 of the rotor 4 extends beyond a bearing 5 and is driven by a motor 8. The rotor 4 can also be designed as a single-sided, cantilevered unit.

An der zylindrischen Trommel 1 des Stators 2 sind in Richtung der Längsachse 9 des Stators 2 im Abstand 10 voneinander ein Eintrittsstutzen 11 für eine Suspension bzw. Pulpe und ein Austrittstutzen 12 für diese vorgesehen. Im Bereich des Eintrittsstutzens 11 mündet in das Innere des Stators 2, falls gewünscht, eine Zuleitung 13 für ein zuzumischendes Medium, beispielsweise ein Gas oder eine Flüssigkeit.On the cylindrical drum 1 of the stator 2, an inlet connection 11 for a suspension or pulp and an outlet connection 12 are provided for the latter in the direction of the longitudinal axis 9 of the stator 2 at a distance of 10 from each other. In the region of the inlet nozzle 11, if desired, a supply line 13 for a medium to be admixed, for example a gas or a liquid, opens into the interior of the stator 2.

Die Ein- bzw. Austrittsöffnungen 11', 12' für die Suspension bzw. Pulpe und Chemikalien 4 sind entweder radial am Stator 2 oder parallel zur Längsachse 3 des Rotors 4 angeordnet.The inlet and outlet openings 11 ', 12' for the suspension or pulp and chemicals 4 are arranged either radially on the stator 2 or parallel to the longitudinal axis 3 of the rotor 4.

An der Innenseite 14 der Trommel 1 des Stators 2 sind sich im Wesentlichen quer zur Umfangsrichtung der Trommel 1 erstreckende Strömungsbrecher 15 angeordnet. Der Rotor 4 weist wiederum sich im Wesentlichen quer zur Umfangsrichtung erstreckende Mitnehmer 16 auf.On the inner side 14 of the drum 1 of the stator 2, flow baffles 15 extending essentially transversely to the circumferential direction of the drum 1 are arranged. The rotor 4, in turn, has drivers 16 extending substantially transversely to the circumferential direction.

Die Achse 3 des Rotors 4 ist gegenüber der Achse 9 des Stators 2 um das Maß e exzentrisch angeordnet. Bei Drehung des Rotors 4 wird hierdurch zwischen dem Flugkreis der Mitnehmer 16 und den Strömungsbrechern 15 ein Spalt gebildet, der an seiner engsten Stelle 17 eine Dicke von 0,02 bis 80 und an seiner weitesten Stelle 18 eine Dicke von 1 bis 90, jeweils in Prozent des Innendurchmessers D des Stators aufweist.The axis 3 of the rotor 4 is arranged eccentrically with respect to the axis 9 of the stator 2 by the dimension e. Upon rotation of the rotor 4, a gap is thereby formed between the circle of the driver 16 and the flow breakers 15, the thickness at its narrowest point 17 from 0.02 to 80 and at its widest point 18 a thickness of 1 to 90, each in Percent of the inner diameter D of the stator.

Sowohl die Strömungsbrecher 15 als auch die Mitnehmer 16 müssen sich nicht über die gesamte Länge 19 des Rotationsmischers, d.h. dessen Trommel 1, in einem Stück durchgehend erstrecken; sie können aus mehreren hintereinander liegenden Teilen gebildet sein, die ggf. auch in Umfangsrichtung des Rotors 4 bzw. in Umfangsrichtung des Stators 2 zueinander versetzt angeordnet sind.Both the flow breakers 15 and the drivers 16 need not span the entire length 19 of the rotary mixer, i. the drum 1, extend continuously in one piece; they may be formed of several parts lying one behind the other, which are possibly also arranged offset in the circumferential direction of the rotor 4 and in the circumferential direction of the stator 2 to each other.

Die Breite B der Strömungsbrecher 15 liegt vorteilhaft im Bereich zwischen 1/100 bis 10/1 deren Höhe H.The width B of the flow breaker 15 is advantageously in the range between 1/100 to 10/1 whose height H.

Die Anzahl und Geometrie der Strömungsbrecher bzw. Mitnehmer am Rotor bzw. Stator ist frei wählbar.The number and geometry of the flow breaker or driver on the rotor or stator is freely selectable.

Für eine gute Einmischung, insbesondere eines Gases in eine Suspension von Zellstoff und Wasser, hat es sich als zweckmäßig erwiesen, wenn das Verhältnis des Außendurchmessers d des Rotors 4 zum Innendurchmesser D der Trommel 1 des Stators 2 im Bereich von 1:1,1 bis 1:5 liegt, wobei vorteilhaft die Höhe H der Strömungsbrecher 15 im Bereich zwischen 1/50 bis 1/1,4 des Außendurchmessers d des Rotors 4 liegt.For a good interference, in particular a gas in a suspension of pulp and water, it has proved to be expedient if the ratio of the outer diameter d of the rotor 4 to the inner diameter D of the drum 1 of the stator 2 in the range of 1: 1.1 to 1: 5, wherein advantageously the height H of the flow breaker 15 in the range between 1/50 to 1 / 1.4 of the outer diameter d of the rotor 4 is located.

Die Mitnehmer 16 und Strömungsbrecher 15 können in frei wählbarer Anzahl unterschiedlicher Ausführung vorgesehen sein. Die Funktion des Rotationsmischers ist weitgehend unabhängig von der in der Fig. 2 dargestellten Lage und Anzahl an Mitnehmern 16 und Strömungsbrechern 15, der Geometrieverhältnisse von Rotor 4 und Stator 2, Anordnung und Anzahl an Ein- und Austritts stutzen 11, 12 für Medien, der Mischerlänge 19 sowie der Größe der Exzentrizität zwischen Rotorachse und Statorachse gegeben.The driver 16 and flow breaker 15 may be provided in a freely selectable number of different design. The function of the rotary mixer is largely independent of that in the Fig. 2 shown location and number of drivers 16 and flow breakers 15, the geometry ratios of rotor 4 and stator 2, arrangement and number of inlet and outlet ports 11, 12 for media, given the mixer length 19 and the size of the eccentricity between the rotor axis and stator.

Charakteristisch für die Erfindung ist die exzentrische Anordnung des Rotors 4 und die axiale Strömung der Suspension bzw. der Pulpe.Characteristic of the invention is the eccentric arrangement of the rotor 4 and the axial flow of the suspension or the pulp.

Hierdurch wird die Suspension bzw. Pulpe zwischen den Mitnehmern 16 am Rotor 4 und den Strömungsbrechern 15 am Stator 2 aufgrund der hohen Umfangsgeschwindigkeit und der sich infolge der Rotation ergebenden, unterschiedlich engen Querschnitte variierend hohen Scherkräften ausgesetzt, wodurch die Suspension bzw. Pulpe sehr rasch in einen Zustand übergeht, in welchem sie sich strömungstechnisch wie Wasser verhält und somit pumpbar wird bzw. das effiziente Einmischen von Fluiden, insbesondere von Gasen, ermöglicht wird.As a result, the suspension or pulp between the drivers 16 on the rotor 4 and the flow breakers 15 on the stator 2 due to the high peripheral speed and resulting as a result of rotation, different narrow cross-sections varying high shear forces, whereby the suspension or pulp very quickly in a state in which it behaves fluidly as water and thus becomes pumpable and the efficient mixing of fluids, in particular of gases, is made possible.

Vorteilhaft ist beim erfindungsgemäßen Mischprinzip nicht nur das rasche Erreichen dieses oben beschriebenen Zustandes, sondern weiters das Aufrechterhalten dieses fluidisierten Zustandes über eine mittels des Mischervolumens bzw. der Mischerlänge beliebig wählbare Zeitdauer. Herkömmliche Mischer erreichen Verweilzeiten im fluidisierten Zustand von nur wenigen Zehntelsekunden.It is advantageous in the mixing principle according to the invention not only the rapid achievement of this state described above, but also the maintenance of this fluidized state over an arbitrarily selectable by means of the mixer volume or the mixer length period. Conventional mixers achieve residence times in the fluidized state of only a few tenths of a second.

Eine weitere Charakteristik ist die sehr effiziente Einmischung, d.h. speziell bei der Einmischung von Gasen wird eine sehr homogene, feinporige Dispersion erzielt, welche die gasförmigen Chemikalien fein verteilt direkt an die Fasern der Suspension bringt und dort die Reaktion mit dem Faserstoff ermöglicht.Another characteristic is the very efficient interference, i. especially in the mixing of gases, a very homogeneous, fine-pored dispersion is achieved, which finely distributes the gaseous chemicals directly to the fibers of the suspension and there enables the reaction with the pulp.

Eine spezielle Anwendung des Rotationsmischers ist primär für Fasersuspensionen gegeben, z.B. Zellstoff mit einer Stoffdichte von 4 bis 20% mit anderen Fluiden (Bleichchemikalien), z.B. H2O2, ClO2, NaOH, O3, O2, Cl, N etc, sowie weiters für stofftransportlimitierte Reaktionen zur Erzeugung von Viskosen bzw. Maischen durch Einmischen von Lösungsmitteln bzw. Aushärtesubstanzen.A special application of the rotary mixer is primarily for fiber suspensions, e.g. Pulp having a consistency of 4 to 20% with other fluids (bleaching chemicals), e.g. H2O2, ClO2, NaOH, O3, O2, Cl, N, etc., as well as further for transport-limited reactions for the production of viscose or mash by mixing solvents or Aushärtesubstanzen.

Nachfolgend sind spezielle Anwendungen beschrieben:The following describes special applications:

Ozonbleichstufe:Ozone bleaching stage:

Zellstoff wird über eine Mittelkonsistenzpumpe unter einem Druck von 1 bis 20 barü zum Rotationsmischer gefördert. Im Bereich des Stoffeintritts wird auch das Ozongas in den Rotationsmischer zudosiert. Im Rotationsmischer wird der Zellstoff sehr rasch fluidisiert und gleichzeitig das Ozongas sehr homogen und feinporig in die Zellstoffsuspension eingemischt. Die Hauptreaktion findet im fluidisierten Zustand statt, wobei das Ozongas in Form von kleinen Bläschen direkt an die Faser gelangt und dort die Bleichreaktion erfolgt. Infolge der deutlich längeren Verweilzeiten wird bereits im Rotationsmischer eine wesentlich bessere Reaktion erreicht. Aufgrund der effizienteren Einmischung des Ozongases und der Erzeugung einer sehr homogenen und feinporigen Dispersion ist auch die chemische Reaktion nach dem Rotationsmischer effizienter als bei herkömmlichen Mischprinzipien. D.h. bei geringeren Ozoneinsätzen wird ein höherer Ozonumsatz erreicht. Abschließend wird das großteils abreagierte Ozongas über einen Entgasungsbehälter von der Zellstoffsuspension separiert.Pulp is conveyed through a medium-consistency pump under a pressure of 1 to 20 barü to the rotary mixer. In the area of the substance inlet, the ozone gas is also added to the rotary mixer. In the rotary mixer, the pulp is fluidized very quickly and at the same time the ozone gas is mixed into the pulp suspension in a very homogeneous and fine-pored manner. The main reaction takes place in the fluidized state, wherein the ozone gas comes in the form of small bubbles directly to the fiber and there takes place the bleaching reaction. As a result of the significantly longer residence times, a much better reaction is already achieved in the rotary mixer. Due to the more efficient mixing of the ozone gas and the generation of a very homogeneous and fine-pored dispersion, the chemical reaction after the rotary mixer is more efficient than with conventional mixing principles. That At lower ozone inputs, a higher ozone conversion is achieved. Finally, the largely reacted ozone gas is separated from the pulp suspension via a degassing vessel.

Sauerstoffbleiche:Oxygen bleach:

Zellstoff wird mit einem Druck von 3 bis 20 barü zum Rotationsmischer gefördert. Im Bereich des Stoffeintritts wird auch das Sauerstoffgas in den Rotationsmischer zudosiert. Im Rotationsmischer wird der Zellstoff sehr rasch fluidisiert und gleichzeitig das Sauerstoffgas sehr homogen und feinporig in die Zellstoffsuspension eingemischt. Die Hauptreaktion findet im anschließenden Reaktor mit einer relativ langen Verweildauer von bis zu zwei Stunden statt. Aufgrund der effizienteren Einmischung des Sauerstoffgases und der Erzeugung einer sehr homogenen und feinporigen Dispersion wird bei gleichbleibender Verweilzeit im Reaktor eine höhere Delignifizierungsrate als bei bisherigen Mischprinzipien erzielt.Pulp is fed to the rotary mixer at a pressure of 3 to 20 bar. In the area of the substance inlet, the oxygen gas is also added to the rotary mixer. In the rotary mixer, the pulp is fluidized very quickly and at the same time the oxygen gas is mixed very homogeneously and with fine pores into the pulp suspension. The main reaction takes place in the subsequent reactor with a relatively long residence time of up to two hours. Due to the more efficient mixing of the oxygen gas and the generation of a very homogeneous and fine-pored dispersion, a higher delignification rate is achieved with the same residence time in the reactor than in previous mixing principles.

Einmischen von flüssigen Bleichkomponenten:Mixing in liquid bleach components:

Das Mischprinzip eignet sich auch hervorragend zur Einmischung von flüssigen Chemikalien, wie z.B. Chloridoxid oder Wasserstoffperoxid in eine mittelkonsistente Zellstoffsuspension. Bei diesen Anwendungen kann zur Reduktion des Stromverbrauchs eine kürzere Mischerlänge gewählt werden, da hierbei in erster Linie die effiziente Einmischung und nicht die erhöhte Verweilzeit im fluidisierten Zustand zum Tragen kommt.The mixing principle is also excellent for incorporation of liquid chemicals, e.g. Chloride oxide or hydrogen peroxide in a medium-consistency pulp suspension. In these applications, to reduce the power consumption, a shorter mixer length can be selected, since in the first instance the efficient mixing and not the increased residence time in the fluidized state comes into play.

Claims (19)

  1. A process for continuous blending and/or fluidization of a suspension or a pulp
    and/or for incorporation of gaseous and/or liquid media into a suspension or pulp, respectively, in particular into a suspension of a fibrous material with fluids, using a rotary mixer, wherein the suspension or pulp, respectively, is moved, in addition, from the inlet to the outlet of the rotary mixer along the length (19) or longitudinal axis thereof, wherein the suspension or pulp, respectively, is subjected to shear forces of varying sizes in the rotary mixer across the circumference of said rotary mixer, characterized in that the flow of the suspension or pulp, respectively, is broken on the stator (2) in the peripheral direction by flow breakers (15) extending essentially transversely to the peripheral direction, as a result of gaps (17, 18) between drivers (16) arranged on the rotor (4) and extending essentially transversely to the peripheral direction and the flow breakers (15), which gaps have varying sizes across the circumference.
  2. A process according to claim 1, characterized in that a gaseous or liquid chemical such as, for example, ozone gas is admixed into a suspension of a fibrous material with fluids and that, by appropriately dimensioning the volume of the rotary mixer, in particular the length (19) thereof, the residence time of the suspension and hence the reaction time are determined such that a main reaction with the chemical will take place inside the rotary mixer.
  3. A process according to claim 1 or 2, characterized in that a gaseous or liquid medium such as, for example, oxygen is admixed into a suspension of a fibrous material with fluids, wherein, by appropriately dimensioning the volume of the rotary mixer, in particular the length (19) thereof, the residence time of the suspension is determined such that a main reaction will take place outside of the rotary mixer.
  4. A process according to claim 1, 2 or 3, characterized in that a gaseous or liquid medium such as, for example, a dye is admixed into a suspension of a fibrous material with fluids, with the medium being inert relative to the suspension.
  5. A process according to claims 1 to 4, characterized in that a pulp suspension with a stock consistency of from 4 to 20%, in particular from 8 to 15%, is mixed with gaseous and/or liquid chemicals.
  6. A device for blending a suspension or a pulp and/or for incorporation of gaseous and/or liquid media into a suspension or a pulp, in particular into a suspension of a fibrous material with fluids, designed as a rotary mixer comprising a stator (2) and a rotor (4) arranged on the stator so as to be rotatable around its axis (3), with the axis (3) of the rotor (4) being arranged so as to be offset relative to the axis (9) of the stator (2), as well as comprising an inlet and an outlet opening (11', 12') for the suspension or pulp, respectively, and with the inlet opening (11') being arranged at a distance from the outlet opening (12') in the direction of the axis of the stator (2) which is configured as a longitudinal axis (9), characterized in that flow breakers (15) extending essentially transversely to the peripheral direction are provided on the stator (2) and drivers (16) extending essentially transversely to the peripheral direction are provided on the rotor (4).
  7. A device according to claim 6, characterized in that the longitudinal axis (3) of the rotor (4) is arranged in parallel to the longitudinal axis (9) of the stator (2).
  8. A device according to claim 7, characterized in that an eccentricity (e) between the longitudinal axis (9) of the stator (2) and the longitudinal axis (3) of the rotor (4) lies in the range of from 1/200 to 1/2 of the inside diameter (D) of the drum (1) of the stator (2).
  9. A device according to one or several of claims 6 to 8, characterized in that the ratio of the outside diameter (d) of the rotor (4) to the inside diameter (D) of the drum (1) of the stator (2) lies in the range of from 1:1.1 to 1:5.
  10. A device according to one or several of claims 6 to 9, characterized in that the height (H) of the flow breakers (15) lies in the range of between 1/50 and 1/1.4 of the outside diameter (d) of the rotor (4).
  11. A device according to one or several of claims 6 to 10, characterized in that the width (B) of the flow breakers (15) lies in the range of between 1/100 and 10/1 of their height (H).
  12. A device according to one or several of claims 6 to 11, characterized in that the flow breakers (15) and/or the drivers (16) extend continuously across the length (19) of the rotary mixer from the inlet opening (14) to the outlet opening (15).
  13. A device according to one or several of claims 6 to 12, characterized in that at least some flow breakers (15) and/or drivers (16) extend only over partial sections of the length (19) of the rotary mixer and are preferably arranged so as to be offset to each other in the peripheral direction.
  14. A device according to one or several of claims 6 to 13, characterized in that the inlet opening (14) and/or the outlet opening is/are oriented radially to the longitudinal axis (9) of the stator (2).
  15. A device according to one or several of claims 6 to 14, characterized in that the inlet opening (14) and/or the outlet opening is/are oriented in the direction of the longitudinal axis (9) of the stator (2).
  16. A device according to one or several of claims 6 to 15, characterized in that, in the area of the inlet opening (14), a feeding pipe (13) for a gas or a liquid runs into the stator (2).
  17. A device according to one or several of claims 6 to 16, characterized in that a gap is provided in a radial direction between the flow breakers (15) of the stator (2) and the drivers (16) of the rotor (4), which gap lies, at its narrowest spot (17), in the range of from 0.02 to 80 and, at its widest spot (18), in the range of from 1 to 90, indicated, in each case, in percent of the inside diameter (D) of the stator (2).
  18. The use of a device according to one or several of claims 6 to 17 in the pulp industry, in particular for the production of multiphase mixtures primarily consisting of a suspension of pulp, water and chemicals in a liquid, gaseous or solid state of matter.
  19. The use according to claim 18, in the paper industry, in particular for the production of a multiphase mixture of waste paper and water.
EP05752464A 2004-07-21 2005-06-24 Method for mixing, device for the same and use thereof Revoked EP1768770B1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT05752464T ATE409076T1 (en) 2004-07-21 2005-06-24 METHOD FOR MIXING, DEVICE THEREOF AND USE THEREOF

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AT0124504A AT413656B (en) 2004-07-21 2004-07-21 METHOD OF MIXING, DEVICE THEREFOR AND THEIR USE
PCT/AT2005/000229 WO2006007609A1 (en) 2004-07-21 2005-06-24 Method for mixing device for the same and use thereof

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EP1768770A1 EP1768770A1 (en) 2007-04-04
EP1768770B1 true EP1768770B1 (en) 2008-09-24

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US (1) US20070175604A1 (en)
EP (1) EP1768770B1 (en)
AT (2) AT413656B (en)
CA (1) CA2574368C (en)
DE (1) DE502005005481D1 (en)
WO (1) WO2006007609A1 (en)

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Publication number Publication date
WO2006007609A1 (en) 2006-01-26
EP1768770A1 (en) 2007-04-04
ATA12452004A (en) 2005-09-15
CA2574368A1 (en) 2006-01-26
DE502005005481D1 (en) 2008-11-06
AT413656B (en) 2006-04-15
CA2574368C (en) 2013-02-12
US20070175604A1 (en) 2007-08-02
ATE409076T1 (en) 2008-10-15

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