EP1027141B1 - Zusammenstellung aus reaktor und mischer und verfahren - Google Patents

Zusammenstellung aus reaktor und mischer und verfahren Download PDF

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Publication number
EP1027141B1
EP1027141B1 EP98924882A EP98924882A EP1027141B1 EP 1027141 B1 EP1027141 B1 EP 1027141B1 EP 98924882 A EP98924882 A EP 98924882A EP 98924882 A EP98924882 A EP 98924882A EP 1027141 B1 EP1027141 B1 EP 1027141B1
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EP
European Patent Office
Prior art keywords
mixing chamber
baffles
mixing
fluid
blade
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.)
Expired - Lifetime
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EP98924882A
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English (en)
French (fr)
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EP1027141A4 (de
EP1027141A1 (de
Inventor
Robert Yant
Piotr Piechuta
Kevin Butler
Mark Piechuta
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Quantum Technologies Inc
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Quantum Technologies Inc
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Publication date
Priority claimed from US08/942,575 external-priority patent/US6036355A/en
Application filed by Quantum Technologies Inc filed Critical Quantum Technologies Inc
Publication of EP1027141A1 publication Critical patent/EP1027141A1/de
Publication of EP1027141A4 publication Critical patent/EP1027141A4/de
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    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/0057—Oxidation of liquors, e.g. in order to reduce the losses of sulfur compounds, followed by evaporation or combustion if the liquor in question is a black liquor
    • 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
    • B01F27/60—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis
    • B01F27/72—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis with helices or sections of helices
    • B01F27/724—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis with helices or sections of helices with a single helix closely surrounded by a casing

Definitions

  • the present invention relates to a continuous dynamic mixing assembly for mixing first and second fluid materials together and, in particular, to a reactor mixer for oxidizing liquors for use in the paper pulping industry.
  • Oxidized white liquor is typically made by oxidizing reducing compounds found in white liquor such as sodium sulfide, sodium polysulfide and sodium thiosulfate to form an oxidized white liquor having non-reducing compounds such as sodium sulfate therein.
  • a stirred tank of white liquor and either air or oxygen or a combination thereof and an external heat source is a common method of commercially producing white liquor as disclosed in U.S. Patent Nos. 5,500,085 and 5,382,322.
  • the oxidation reaction of sodium sulfide is exothermic and generates a significant amount of heat.
  • a typical stirred tank process used to oxidize sodium sulfide requires additional heat input from an external source and a long residence time in the tank for the oxidation reaction to progress to a beneficial extent.
  • Large equipment is required to hold volumes of white liquor being oxidized.
  • two stirred tanks each about 3.0 meters (10 feet) in diameter and 7.9 meters (26 feet) high are used. Such large tanks require a long residence time, making them inefficient and costly.
  • US Patent No. 2,914,385 discloses a vertically operating elongated contacting apparatus vessel designed to effect countercurrent mixing between descending denser liquids and ascending less dense liquids.
  • the present invention is directed to a continuous dynamic reactor mixing assembly which disperses and dissolves a second fluid, e.g., gas, into a first fluid, e.g., liquid material.
  • the reactor mixer of the invention employs first axially extending baffles and second circumferential baffles along with a unique agitator design to enable very efficient mixing of the first and second fluids.
  • the invention is particularly well suited to conducting chemical reactions in the mixing assembly.
  • the mixing assembly of the present invention may be applied in mixing a wide variety of fluids and one, two, or three-phase mixtures.
  • Some examples include the injection of a gas as a secondary fluid into the mixing chamber which already contains a liquid or liquid/solid material as a primary fluid or injecting a liquid as a secondary fluid into the mixing chamber for dissolution in and reaction with some primary fluid or slurried material within the mixing chamber.
  • the secondary fluid may be introduced into the mixing chamber through insert assemblies which influence its flow rate. Virtually any combination of flowable materials may be introduced through both the insert assemblies and the mixing assembly as a whole.
  • the mixing assembly of the present invention is particularly well suited for conducting chemical reactions which involve the injection of a gas into a material for subsequent dilution and chemical reaction.
  • Solutions which contain oxidizable compounds, such as paper pulp mill white liquor, black liquor, green liquor, and similar solutions are particularly suitable for oxidation reactions within the reactor mixer of the present invention.
  • the patent application entitled “Method of oxidizing White Liquor,” filed July 14, 1997, describes materials that may be oxidized in accordance with the present invention and an overall system for producing a solution of oxidized liquor in which the present reactor mixer may be used.
  • the present invention is directed to a dynamic mixing assembly in accordance with the features of claim 1, comprising a preferably cylindrical mixing chamber having an inner wall which is generally symmetrical about a central (longitudinal) axis.
  • At least one first fluid inlet introduces first fluid material into the mixing chamber.
  • At least one second fluid inlet introduces second fluid material into the mixing chamber.
  • At least one outlet enables fluid to leave the mixing chamber.
  • First or axial baffles extend along the inner wall generally parallel to the axis for disrupting fluid flow generally circumferentially in the mixing chamber.
  • Second or circumferential baffles extend generally transverse to the axis for disrupting fluid flow in a generally axial direction in the mixing chamber.
  • the second baffles are constructed and arranged to segment the mixing chamber axially.
  • a rotatable agitator comprises a cylindrical central portion extending in the mixing chamber along the axis and at least one blade having a twisted orientation on the central portion.
  • the circumferential baffles partition the mixing chamber into at least two axial segments.
  • the axial baffles in one of the segments are offset from the axial baffles in an adjacent one of the segments as viewed in a direction of the axis.
  • a generally annular space is located radially between each blade and the axial baffles.
  • a size of the space is selected to produce the particular residence time of liquid material in the mixing chamber. The space ranges from about .01 to about 0.1 times an inside diameter of the mixing chamber and, in particular, from about .03 to about 0.11 times an inside diameter of the mixing chamber.
  • a ratio of a height of each of the axial baffles to an inside diameter of the mixing chamber ranges from about 0.001 to about 0.40 and, in particular, from about 0.01 to about 0.20.
  • Each blade has a pitch such that there is a generally constant gap between an edge of the blade and edges of the axial baffles, along an entire length of the blade.
  • insert assemblies may each be disposed at a location of a second fluid inlet adjacent the mixing chamber wall for admitting the second fluid into the reactor at a selected flow rate.
  • a variable speed drive may be used that can rotate the agitator in both a clockwise and counterclockwise direction.
  • a preferred embodiment of the mixing assembly of the invention comprises the generally cylindrical mixing chamber having the inner wall which is generally symmetrical about the central axis, the first and second fluid inlets, and outlet. Also included are the axial and circumferential baffles. The circumferential baffles are constructed and arranged to segment the mixing chamber axially. The insert assemblies are each disposed at a location of a second fluid inlet adjacent the mixing chamber wall.
  • the rotatable agitator comprises a central cylindrical hub portion extending in the mixing chamber along the axis and at least one blade having a twisted orientation on the hub portion.
  • Another preferred embodiment of the mixing assembly of the present invention comprises the generally cylindrical mixing chamber having the inner wall which is generally symmetrical about the central axis, the first and second fluid inlets, and outlet. Also included are the axial and circumferential baffles. The circumferential baffles are constructed and arranged to segment the mixing chamber axially. The insert assemblies are each disposed at a location of a second fluid inlet adjacent the mixing chamber wall.
  • the rotatable agitator comprises a central cylindrical hub portion extending in the mixing chamber along the axis and at least one blade having a twisted orientation on the hub portion. Each blade has a pitch such that a generally constant gap is maintained between an edge of the blade and edges of the axial baffles along an entire length of the blade.
  • the generally annular space is located radially between each blade and the axial baffles.
  • a size of the space is selected to produce a particular residence time of liquid material in the mixing chamber.
  • the variable speed drive mechanism capable of both clockwise and counterclockwise rotation of the agitator.
  • the assembly may include a device for pressurizing the liquid.
  • the agitator can produce substantially superatmospheric pressure in the mixing chamber.
  • the reactor mixer of the present invention enables the efficient dispersion and dissolution of different materials into one another.
  • the reactor mixer enables secondary gas to be inlet into the insert assemblies for oxidizing primary liquid material.
  • the present invention enables the oxidation of white liquor solution to occur at least about 16 times faster than in the tank reactor system.
  • the design of the agitator blades and axial and circumferential baffles offer numerous advantages and serve a plurality of purposes.
  • the baffle systems disrupt axial and circumferential fluid flow and enable efficient mixing.
  • a constant gap between the blades and the baffles is maintained upon passing of the blades. Only a small section of any blade is opposite any axial baffle at any one time, which lessens mixing power consumption.
  • the twisted blade design on the central cylindrical portion of the agitator enables the blades to utilize a sweeping action past the inward edges of the axial baffles. Since the blades are twisted, only a small portion of a blade is advantageously opposite an axial baffle at one time by the predetermined space.
  • the sweeping of the blades past the baffles causes a unique mixing action and further lessens mixing power consumption.
  • at least one point on at least one blade edge is separated from at least one point on at least one axial baffle edge by the predetermined gap, which maximizes mixing efficiency.
  • the flow in the mixing chamber can be increased or retarded based upon the speed and rotational direction of the agitator, in view of its unique twisted blade orientation.
  • the circumferential baffles advantageously partition the mixing chamber into one or more axial segments.
  • liquid contacts the circumferential baffles it is directed inwardly toward the agitator, forming a liquid seal in each of the axial segments.
  • the liquid seal prevents gas from traveling unobstructed along the shaft of the mixing device.
  • the present mixer is well suited for conducting chemical reactions, such as oxidation of liquids, in view of its thorough liquid/gas mixing.
  • the reactor is believed to enable the formation of three discrete fluid zones, an inner primarily gas zone around the agitator, a primarily liquid zone radially outward from the gas zone, and a reaction zone between the liquid and gas zone having a combination of liquid and gas.
  • An interaction among the axial baffles, circumferential baffles and agitator enable residence time of fluid (e.g., liquid) in the mixing chamber to be selectively adjusted.
  • fluid e.g., liquid
  • a generally radial spacing between the agitator and axial baffles enables the reaction zone size, and thus the residence time of the liquid, to be selectively adjusted.
  • a method of mixing first and second fluid materials comprises directing the first and second fluid materials into the mixing chamber.
  • the agitator having at least one blade with the twisted orientation on the cylindrical central portion is rotated. Fluid flow is disrupted generally circumferentially in the mixing chamber with the axial baffles. Fluid flow is disrupted in a general direction of the axis with the circumferential baffles.
  • the residence time of liquid material in the mixing chamber may be selectively adjusted based upon the relative construction and arrangement among the agitator, the axial baffles and the circumferential baffles. This may be accomplished by selecting a size of the annular space located radially between the blades and the axial baffles. Alternatively, the residence time of liquid material in the chamber may be increased or decreased as desired by rotating the agitator in a particular direction and at a particular speed.
  • a reactor mixer assembly of the present invention which is for dispersion and dissolution of a secondary fluid material, preferably gas, into a primary fluid material, preferably liquid, is designated generally at 10.
  • the mixing assembly comprises a generally cylindrical mixing vessel shell 12 having a wall 14 with an inner surface which forms a mixing chamber 16 that is generally symmetrical about a central axis X ( Figure 1).
  • At least one first fluid inlet 18 is connected to the shell for introducing the first fluid material into the mixing chamber and at least one outlet 20 is connected to the shell for discharging mixed fluid from the mixing chamber.
  • Second fluid inlets 22 are disposed at a plurality of locations around the mixing chamber for introducing the second fluid material into the first fluid material.
  • First baffles 24 extend axially along the inner wall generally parallel to the axis X.
  • Second circumferential baffles 26 extend generally transverse to the axis X and are constructed and arranged to partition the mixing chamber axially into at least two segments ( e.g ., S 1 and S 2 ).
  • Insert assemblies 28 are disposed at each of the second fluid inlets 22 adjacent the mixing chamber wall.
  • a rotatable agitator 30 comprises a cylindrical central portion 32 extending in the mixing chamber along the axis X and blades 34 that each have a twisted orientation on the central portion of the agitator.
  • the entry pipe 18 communicates with the mixing vessel shell in such a way that primary fluid from the entry pipe enters the mixing chamber 16. Entry pipe 18 is of sufficient size to admit the desired flow rate of primary fluid.
  • the primary fluid may be pumped under pressure at a particular flow rate into the mixing chamber by a pump 35. After the mixing of the primary and secondary fluids, the mixed fluid leaves the mixing chamber via the exit pipe 20.
  • the agitator is driven by an external drive mechanism shown schematically at M and includes a shaft 36 that is coupled to a drive shaft 38 in a manner known to those skilled in the art.
  • the agitator preferably includes a cylindrical hub portion 40 located concentrically around the shaft.
  • the shaft 36 is supported by an appropriate bearing assembly 42 and pillow blocks 44.
  • the mixing vessel shell is supported by suitable supports 46.
  • the rotating shaft is sealed in the mixing vessel by suitable sealing devices 48.
  • the sealing devices 48 are preferably dual-face rotating mechanical seals, although any suitable sealing mechanism may be used.
  • included in the assembly is a removable cover 50, over a maintenance access hole, which is used for shaft removal and other tasks.
  • Secondary fluid enters secondary fluid entry headers 52, only one of which is shown in Figure 1. From headers 52 the secondary fluid enters ports 54, which communicate with the insert assemblies 28. The headers 52 and the ports 54 may have other configurations. The secondary fluid flows into the mixing chamber through the insert assemblies 28. The insert assemblies 28 may be positioned at various locations around the mixing vessel shell 12.
  • the circumferential baffles 26 have an annular shape.
  • the circumferential baffles 26 communicate with the inside wall of the mixing vessel shell 12 and partition the reactor into two or more axial segments. This disrupts the bulk flow of fluid material in the axial direction, causing definite axial segmentation in the mixing chamber and substantially lessening the possibility of fluid flowing axially through the chamber undermixed.
  • the circumferential baffles 26 temporarily force the bulk flow of fluid generally radially into the agitator blades to ensure complete mixing, and to form a unique liquid barrier through which gases cannot pass unobstructed.
  • the axial baffles 24 extend generally radially inwardly from the inner wall of the mixing vessel shell and provide for circumferential mixing within an individual axial segment. As best shown in Fig. 4, the axial baffles in one of the segments S 1 are offset by an angle ⁇ from the axial baffles in an adjacent one of the segments S 2 as viewed in a direction of the axis X. The angle ⁇ ranges from about 0° to about 180° and, in particular, not greater than about 90°.
  • the axial baffles 24 extend substantially the entire length of each axial segment and preferably have a length less than an axial segment.
  • the axial baffles may be circumferentially spaced apart from each other by a central angle ranging from about 0° to about 180°.
  • a ratio of a height H of each of the axial baffles 24 to an inside diameter of the mixing chamber ranges from about 0.001 to about 0.40 and, in particular, from about 0.01 to about 0.20.
  • the mixing chamber is about 51cm (20 inches) in diameter and about 2 metres (6 feet) long, for example.
  • the hub portion of the multibladed agitator extends into the interior of the mixing chamber along the axis X.
  • the shaft 36 extends through the vessel shell 12, the hub portion 40, the bearings 42 and the seals 48.
  • the hub portion may be formed integrally with the shaft, formed separately from the shaft or otherwise omitted.
  • the blades may extend directly from a cylindrical shaft with no hub portion.
  • the shaft 36 is preferably machined so that its outside diameter is less at the bearings 42 than along substantially the balance of the shaft.
  • the blades 34 are advantageously twisted as shown, although other degrees of twist are within the scope of the current invention. It is preferred that the blades extend perpendicular to a tangent to the cylindrical portion as the blades twist, throughout the length of the blades. As shown in Figures 3 and 4, the blades have a pitch such that there is a generally constant gap G between each blade edge B and edges E of the axial baffles along the twist T for the entire length L of the blade.
  • the blade twist T is important in that it lessens momentary power peaks that a blade parallel to the axis X would be prone to, and in that it creates a means to either propel the fluid from the mixing chamber or to retard the flow of fluid from the chamber.
  • the axial length L of each agitator blade ( Figure 3) is preferably approximately equal to that of each axial baffle.
  • FIG. 5 a preferred insert assembly 28 is shown, although other configurations may be used.
  • U.S. Patent No. 5,607,233 describes specific features and effects of insert assemblies that may be suitable in the present invention.
  • An insert sleeve 56 is connected to the vessel shell 12 such as by welding.
  • a shoulder 58 extends from the insert sleeve 56 to allow an end cap 60 of the insert assembly 28 to engage the sleeve 56.
  • An insert 62 communicates with an insert wall 64 which in turn communicates with the end cap 60.
  • the inserts 62 are generally coplanar with the inner surface of the wall 14 but may extend further into the mixing chamber.
  • the inserts 62 can admit different fluids and may be formed from materials so as to adjust their porosity as desired or to have drilled openings of a particular size and number, enabling a wide variety of flow rates of the secondary fluid into the mixing chamber.
  • the inserts 62 are preferably removable.
  • a gasket 66 may be used in conjunction with fasteners 68 to seal the end cap against the insert sleeve 56. Secondary fluid is injected into the insert via the feed pipe 54 which has exterior threads 69 for engaging an interiorly threaded opening 70 in the end cap.
  • the secondary fluid may be a gas, for example, an oxygen-containing gas.
  • the primary fluid may be, for example, liquid material, for example, a liquor solution to be oxidized.
  • Primearily gas is located in an innermost zone B located in an annulus that extends radially outwardly from the hub portion to the outer edges B of the blades.
  • a discrete annular reaction zone C is located radially between the outer liquid material zone A and the inner gas zone B and contains a mixture of liquid and gas.
  • the reaction zone C is located in the generally annular space G radially between the outermost edges of the blades and the edges of the axial baffles.
  • the size of the reaction zone C is selected to produce a particular residence time of liquid material in the mixing chamber. When the size of the reaction zone C is increased, the liquid material will have a longer residence time in the mixing chamber. When the size of the reaction zone C is decreased, the liquid material will have a shorter residence time in the mixing chamber.
  • the relative sizes of the zones A, B and C may be adjusted mechanically or operationally.
  • the size of the space G may be determined when the reactor mixer is designed, by adjusting the size or height of the blades and the height of the axial baffles as well as the inside diameter of the mixing chamber.
  • the space G preferably ranges from about .01 to about 0.1 times the inside diameter of the mixing chamber and, in particular, from about .03 to about 0.11 times the inside diameter of the mixing chamber.
  • the drive M is capable of variable speeds and can rotate the agitator clockwise or counterclockwise. While not wanting to be bound by theory, it is believed that the sizes of the zones are relatively constant or they may vary somewhat.
  • Rotating the agitator assembly 40 clockwise in view of the particular blade pitch and the view of Figures 3 and 4, propels the material out of the reactor, and is the most effective in reasonably gentle oxidation reactions. Clockwise rotation is also desirable when a rapid rate of mixing is required.
  • the size of the reaction zone C may be affected by the directional rotation of the agitator. It is believed that clockwise rotation results in a relatively small reaction zone C. With clockwise rotation, the reaction zone C is believed to decrease in size radially outwardly, compared to counterclockwise rotation, that is, the size of the gas zone B increases.
  • the agitator 40 is rotated counterclockwise, in view of the particular blade pitch and the view of Figures 3 and 4, in such a manner as to retard the bulk flow of liquid through the mixing chamber. It is believed that counterclockwise rotation results in a larger reaction zone C, which is very effective in harsh mixing or harsh oxidation reactions. With counterclockwise rotation, the reaction zone C is believed to increase radially inwardly, that is, the size of the gas zone B decreases.
  • the drive is preferably a variable speed drive that can be operated to rotate the agitator slowly or quickly.
  • Slow rotation of the agitator is believed to increase the size of the reaction zone C and increases the residence time of the liquid material in the mixing chamber.
  • Fast rotation of the agitator is believed to result in a smaller reaction zone C and decreases the residence time of the liquid material in the mixing chamber.
  • first fluid material for example a white liquor solution to be oxidized
  • Second fluid material for example, oxygen-containing gas
  • the agitator 30 rotates at a particular speed and direction depending upon the desired residence time of fluid material in the reactor mixer.
  • the residence time is also adjusted by selecting the size of the annular space G in view of the inside diameter of the mixing chamber and heights of each of the blades and axial baffles. Fluid flow is disrupted generally circumferentially in the mixing chamber by the axial baffles 24. Fluid flow is disrupted in a general direction of the axis by the circumferential baffles 26.
  • the mixed fluid e.g., oxidized white liquor
  • the mixing system can process from 0.4 to 1892 liters per minute (0.1 to 500 gallons per minute) of a pulp mill liquor converting the liquor to an oxidized liquor useful within pulp mill operations.
  • the mixing chamber is capable of containing pressures up to 27.2 atmospheres (400 pounds per square inch gauge). The blade speed depends upon the geometry of the agitator and the degree of mixing required.

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  • Chemical Kinetics & Catalysis (AREA)
  • Mixers Of The Rotary Stirring Type (AREA)

Claims (39)

  1. Mischanordnung (10) zum kontinuierlichen dynamischen Mischen, aufweisend:
    eine allgemein horizontal verlaufende Mischkammer (12) mit einer Innenwand (14), die allgemein symmetrisch um eine zentrale Achse (X) ist, wobei die Mischkammer allgemein zylindrisch ist und einen Innendurchmesser hat;
    mindestens einen ersten Fluideinlass (18), der zum Einleiten von erstem Fluidmaterial in die Mischkammer ausgebildet und angeordnet ist;
    mindestens einen zweiten Fluideinlass (22), der zum Einleiten von zweitem Fluidmaterial in die Mischkammer ausgebildet und angeordnet ist;
    mindestens einen Auslass (20) zum Ausleiten einer Mischung aus dem ersten Fluidmaterial und dem zweiten Fluidmaterial aus der Mischkammer;
    erste Prallplatten (24), die sich entlang der Innenwand allgemein parallel zu der Achse erstrecken, um eine allgemein umfangsmäßige Fluidströmung in der Mischkammer aufzubrechen;
    zweite Prallplatten (26), die sich von der Innenwand allgemein quer zu der Achse weg erstrecken, um eine allgemein axiale Fluidströmung in der Mischkammer aufzubrechen; und
    eine drehbare Rühreinrichtung (30) mit einem zentralen Bereich, der sich in der Mischkammer entlang der Achse erstreckt, und mit mindestens einer Schaufel (34), die sich von dem zentralen Bereich weg erstreckt, wobei der zentrale Bereich und die mindestens eine Schaufel undurchlässig für die Fluidströmung sind.
  2. Mischanordnung nach Anspruch 1,
    wobei der zentrale Bereich zylindrisch ist.
  3. Mischanordnung nach Anspruch 1,
    wobei die Kammer (12) allgemein zylindrisch ist.
  4. Mischanordnung nach Anspruch 1,
    wobei der mindestens eine erste Fluideinlass (18) zum Einleiten von flüssigem Material in die Mischkammer (12) ausgebildet und angeordnet ist.
  5. Mischanordnung nach Anspruch 1,
    mit Plattenanordnungen (28), die jeweils an einer Stelle des mindestens einen Fluideinlasses (22) in der Nähe der Mischkammerwand (14) angeordnet sind und die Öffnungen mit einer bestimmten Porosität und/oder Größe aufweisen, die zum Einlassen des zweiten Fluidmaterials in die Mischkammer (12) mit einer ausgewählten Strömungsrate wirksam sind,
  6. Mischanordnung nach Anspruch 1,
    wobei die mindestens eine Schaufel (34) eine derartige Steigung hat, dass ein allgemein konstanter Spalt zwischen einem Rand der mindestens einen Schaufel sowie Rändern der ersten Prallplatten (24) entlang der gesamten Länge der mindestens einen Schaufel vorhanden ist.
  7. Mischanordnung nach Anspruch 1,
    wobei die zweiten Prallplatten (26) die Mischkammer (12) in mindestens zwei axiale Segmente (S1, S2) unterteilen.
  8. Mischanordnung nach Anspruch 1,
    wobei ein allgemein ringförmiger Raum (G) radial zwischen der mindestens einen Schaufel (34) und den ersten Prallplatten (24) vorhanden Ist.
  9. Mischanordnung nach Anspruch 8,
    wobei die Größe des Raums (G) das ca. 0,01-fache bis ca. 0,1-fache des Innendurchmessers der Mischkammer (12) beträgt.
  10. Mischanordnung nach Anspruch 8,
    wobei die Größe des Raums (G) das ca. 0,03-fache bis ca. 0,11-fache des Innendurchmessers der Mischkammer (12) beträgt.
  11. Mischanordnung nach Anspruch 1,
    wobei ein Verhältnis einer Höhe jeder der ersten Prallplatten (24) zu dem Innendurchmesser der Mischkammer (12) in einem Bereich von ca. 0,001 bis ca. 0,40 liegt.
  12. Mischanordnung nach Anspruch 1,
    wobei ein Verhältnis einer Höhe jeder der ersten Prallplatten (24) zu dem Innendurchmesser der Mischkammer (12) in einem Bereich von ca. 0,01 bis ca. 0,20 liegt.
  13. Mischanordnung nach Anspruch 1,
    mit einem Antrieb (M) mit variabler Drehzahl, der mit der Rühreinrichtung (30) verbunden ist und die Rühreinrichtung (30) im Uhrzeigersinn sowie im Gegenuhrzeigersinn drehen kann.
  14. Mischanordnung nach Anspruch 8,
    wobei der Raum (G) derart gewählt ist, dass seine Größe in einem Bereich von ca. dem 0,01- bis ca. 0,1-fachen des Innendurchmessers der Mischkammer (12) liegt und ein Verhältnis einer Höhe jeder der ersten Prallplatten (24) zu dem Innendurchmesser der Mischkammer in einem Bereich von ca. 0.020 bis ca. 0,40 liegt.
  15. Mischanordnung nach Anspruch 7,
    wobei der zentrale Bereich der drehbaren Rühreinrichtung (30) zylindrisch ist und sich die mindestens eine Schaufel (34) entlang eines Kreisbogens des zentralen Bereiches erstreckt; und
    wobei die ersten Prallplatten (24) in dem einen der Segmente (S1) bei Betrachtung in Richtung der Achse von den ersten Prallplatten in einem benachbarten der Segmente (S2) in Umfangsrichtung versetzt sind.
  16. Mischanordnung nach Anspruch 1,
    wobei die zweiten Fluideinlässe (22) an mehreren Stellen um die Mischkammer (12) herum angeordnet sind;
    wobei die zweiten Prallplatten (26) zum axialen Segmentieren der Mischkammer ausgebildet und angeordnet sind:
    wobei Plattenanordnungen (28) vorhanden sind, die jeweils an einer Stelle der zweiten Fluideinlässe (22) in der Nähe der Mischkammerwand (14) angeordnet sind und Öffnungen mit einer bestimmten Porosität und/oder Größe aufweisen, die zum Einlassen des zweiten Fluidmaterials in die Mischkammer (12) mit einer ausgewählten Strömungsrate wirksam sind:
    und wobei die mindestens eine Schaufel (34) der drehbaren Rühreinrichtung (30) sich entlang eines Kreisbogens des Nabenbereiches erstreckt.
  17. Mischanordnung nach Anspruch 16,
    wobei ein allgemein ringförmiger Raum (G) radial zwischen der mindestens einen Schaufel (34) und den ersten Prallplatten (24) vorhanden ist.
  18. Mischanordnung nach Anspruch 1,
    wobei es sich bei dem ersten Fluideinlass (18) um einen Flüssigkeitseinlass zum Einleiten von flüssigem Material in die Mischkammer (12) handelt;
    wobei Strömungseinrichtungen (28) in der Nähe der Mischkammerwand (14) angeordnet sind, um eine gasförmige Substanz als zweites Fluidmaterial mit einer ausgewählten Strömungsrate in die Mischkammer (12) einzuleiten:
    wobei der mindestens eine zweite Fluideinlass (22) mindestens eine Gasöffnung (54) zum Einleiten der gasförmigen Substanz durch jede der Strömungseinrichtungen in die Mischkammer aufweist;
    wobei die zweiten Prallplatten (26) die Mischkammer (12) in mindestens zwei separate axiale Segmente (S1, S2) unterteilen;
    wobei der zentrale Bereich der drehbaren Rühreinrichtung (30) einen zylindrischen Nabenbereich aufweist, der sich in der Mischkammer entlang der Achse erstreckt, wobei sich die Rühreinrichtungsschaufeln (34) entlang von Kreisbogenbereichen des Nabenbereiches erstrecken, wobei jede der Schaufeln (34) eine derartige Steigung hat, dass ein allgemein konstanter Spalt zwischen einem Rand jeder Schaufel (34) sowie Rändern der ersten Prallplatten (24) entlang der gesamten Länge der Schaufel (34) verbleibt,
    wobei ein ahgemein ringförmiger Raum (G) radial zwischen den Schaufeln (34) und den ersten Prallplatten (24) vorhanden ist; und
    wobei ein Antriebsmechanismus (M) mit variabler Drehzahl vorhanden ist, der mit der Rühreinrichtung (30) verbunden ist und die Rühreinrichtung Im Uhr zeigersinn und im Gegenuhrzeigersinn drehen kann.
  19. Mischvorrichtung nach Anspruch 18,
    mit einer Einrichtung (33') für die Druckbeaufschlagung des flüssigen Materials.
  20. Mischvorrichtung nach Anspruch 18,
    wobei die Rühreinrichtung (30) einen im Wesentlichen über dem Atmosphärendruck liegenden Druck in der Mischkammer erzeugen kann.
  21. Verfahren zum Mischen eines ersten Fluidmaterials und eines zweiten Fluidmaterials unter Verwendung der Vorrichtung nach einem der Ansprüche 1 bis 20, mit folgenden Schritten:
    Einleiten des ersten Fluidmaterials in die allgemein horizontal verlaufende Mischkammer (12);
    Einleiten des zweiten Fluidmaterials in die Mischkammer (12);
    Drehen der Rühreinrichtung (30), die den zylindrischen zentralen Bereich, der sich in der Mischkammer (12) entlang der Achse erstreckt, sowie die mindestens eine Schaufel (34) aufweist, die sich von dem zentralen Bereich weg erstreckt, wobei der zentrale Bereich und die mindestens eine Schaufel undurchlässig für die Fluidströmung sind;
    Aufbrechen der allgemein umfangsmäßigen Fluidströmung in der Mischkammer mittels der ersten Prallplatten (24), die sich von der Innenwand (14) allgemein entlang der Achse weg erstrecken: und
    Aufbrechen der allgemein axialen Fluidströmung mittels der zweiten Prallplatten (26), die sich von der Innenwand allgemein quer zu der Achse weg erstrecken.
  22. Verfahren nach Anspruch 21,
    wobei die Verweilzeit von flüssigem Material In der Mischkammer eingestellt wird durch Auswählen einer Größe eines ringförmigen Raums (G), der sich radial zwischen der mindestens einen Schaufel (34) und den ersten Prallplatten (24) befindet, in einem Bereich, die das ca. 0,01-fache bis ca, 0,1-fache des Innendurchmessers der Mischkammer (12) beträgt.
  23. Verfahren nach Anspruch 21,
    wobei die Mischkammer (12) flüssiges Material aus mindestens einem Material des ersten Fluidmaterials und des zweiten Fluidmaterials beinhaltet,
    wobei eine Verweilzeit des flüssigen Materials in der Mischkammer (12) durch Drehen der Rühreinrichtung (30) in einer Richtung zum Verzögern der Strömung des flüssigen Materials erhöht wird.
  24. Verfahren nach Anspruch 21,
    wobei das erste Fluidmaterial eine beim Aufschließen von Holz zur Herstellung von Papier verwendete Lauge aufweist.
  25. Verfahren nach Anspruch 24,
    wobei als erstes Fluidmaterial Frischtauge verwendet wird.
  26. Verfahren nach Anspruch 21,
    wobei das zweite Fluidmaterial ein sauerstoffhaltiges Gas aufweist.
  27. Verfahren nach Anspruch 21,
    wobei der Energieverbrauch beim Mischen auf der Basis einer relativen Konstruktion und Anordnung hinsichtlich der ersten Prallplatte, der zweiten Prallplatten und der Rühreinrichtung verringert wird.
  28. Verfahren nach Anspruch 21,
    wobei als erstes Fluidmaterial Schwarzlauge verwendet wird.
  29. Verfahren nach Anspruch 21,
    wobei als erstes Fluidmaterial Grünlauge verwendet wird.
  30. Verfahren nach Anspruch 21,
    wobei das erste Fluidmaterial oxidierbare Verbindungen aufweist.
  31. Verfahren nach Anspruch 21,
    bei dem das erste Fluidmaterial kontinuierlich in die Mischkammer (12) befördert wird.
  32. Mischanordnung nach Anspruch 1,
    bei der sich die zweiten Prallplatten (26) zwischen den ersten Prällplatten (24) erstrecken; und
    bei der die mindestens eine Schaufel (34) der drehbaren Rühreinrichtung (30) mehrere Schaufeln aufweist, die sich von dem zentralen Bereich nach außen erstrecken, wobei jede der Schaufeln in Bezug auf eine benachbarte Schaufel entlang eines anderen axialen Bereichs des zentralen Bereiches verläuft;
    wobei die zweiten Prallplatten (26) derart angeordnet sind, dass ein Bereich von mindestens einer der zweiten Prallplatten quer zu der Achse mit einer längs der Achse verlaufenden Region ausgerichtet ist, die ein axial abschließendes Ende einer ersten der Schaufeln enthält, und wobei die zweiten Prallplatten (26) die Mischkammer (12) in mindestens zwei axiale Segmente (S1, S2) unterteilen;
    wobei die erste Schaufel (34) derart verläuft, dass sie entlang der Achse von der einen zweiten Prallplatte (26) in einem ersten der Segmente (S1) begrenzt ist und eine zweite der Schaufeln, die der ersten Schaufel benachbart ist, derart verläuft, dass sie von der einen zweiten Prallplatte (26) in einem zweiten der Segmente (S2) axial begrenzt ist, das dem ersten Segment (S1) benachbart ist.
  33. Mischanordnung nach Anspruch 32,
    wobei der zentrale Bereich zylindrisch ist und sich die Schaufeln (34) entlang von Kreisbögen des zentralen Bereiches erstrecken.
  34. Mischanordnung nach Anspruch 32,
    wobei die Mischkammer (12) allgemein zylindrisch ist und ein allgemein ringförmiger Raum (G) radial zwischen den Schaufeln (34) und den ersten Prallplatten (24) vorhanden ist, wobei der Raum (G) derart gewählt ist, dass seine Größe in einem Bereich von ca. dem 0,01- bis ca. 0,1-fachen eines Innendurchmessers der Mischkammer (12) liegt und ein Verhältnis einer Höhe einer jeden der ersten Prallplatten (24) zu einem Innendurchmesser der Mischkammer (12) in einem Bereich von ca. 0,02 bis ca, 0,40 liegt.
  35. Mischanordnung nach Anspruch 32,
    mit einer Mehrzahl poröser Plattenanordnungen (28), die jeweils an einer Stelle des mindestens einen zweiten Fluideinlasses (22) in der Nähe der Mischkammerwand (14) angeordnet sind, wobei die porösen Plattenanordnungen (28) Öffnungen mit einer bestimmten Porosität und/oder Größe aufweisen, die zum Einlassen des zweiten Fluids in die Mischkammer (12) mit einer ausgewählten Strömungsrate wirksam sind.
  36. Mischanordnung nach Anspruch 32,
    wobei die ersten Prallplatten (24) in einem der Segmente (S1) bei Betrachtung in Richtung der Achse von den ersten Prallplatten (24) in einem benachbarten der Segmente (S2) in Umfangsrichtung versetzt sind.
  37. Mischanordnung nach Anspruch 32,
    wobei sich die ersten Prallplatten (24) und die zweiten Prallplatten. (26) von der Innenwand (14) der Mischkammer (12) quer zu der Achse nach innen er strecken, wobei sich die ersten Prallplatten (24) über eine größere Distanz nach innen erstrecken als die zweiten Prallplatten (26).
  38. Mischanordnung nach Anspruch 37,
    wobei die zweiten Prallplatten (26) einen ringförmigen Raum aufweisen und sich entlang der Innenwand (14) der Mischkammer (12) über den gesamten Umfang der Mischkamrrier erstrecken.
  39. Mischanordnung nach Anspruch 32,
    wobei sich die Region an ein axial abschließendes Ende der zweiten Schaufel (34) anschließt
EP98924882A 1997-10-01 1998-05-26 Zusammenstellung aus reaktor und mischer und verfahren Expired - Lifetime EP1027141B1 (de)

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