EP2865806A1 - Verfharen und Vorrichtung zum Rühren einer Flüssigkeit in einem Gefäss - Google Patents

Verfharen und Vorrichtung zum Rühren einer Flüssigkeit in einem Gefäss Download PDF

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Publication number
EP2865806A1
EP2865806A1 EP20130189963 EP13189963A EP2865806A1 EP 2865806 A1 EP2865806 A1 EP 2865806A1 EP 20130189963 EP20130189963 EP 20130189963 EP 13189963 A EP13189963 A EP 13189963A EP 2865806 A1 EP2865806 A1 EP 2865806A1
Authority
EP
European Patent Office
Prior art keywords
fillet
agitators
vessel
edges
fluid
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.)
Withdrawn
Application number
EP20130189963
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English (en)
French (fr)
Inventor
Janne Tamminen
Vesa Vikman
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sulzer Pumpen AG
Original Assignee
Sulzer Pumpen AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Sulzer Pumpen AG filed Critical Sulzer Pumpen AG
Priority to EP20130189963 priority Critical patent/EP2865806A1/de
Publication of EP2865806A1 publication Critical patent/EP2865806A1/de
Withdrawn legal-status Critical Current

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Classifications

    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21D—TREATMENT OF THE MATERIALS BEFORE PASSING TO THE PAPER-MAKING MACHINE
    • D21D5/00—Purification of the pulp suspension by mechanical means; Apparatus therefor
    • D21D5/28—Tanks for storing or agitating pulp
    • 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
    • B01F27/23—Mixers with rotary stirring devices in fixed receptacles; Kneaders characterised by the orientation or disposition of the rotor axis
    • B01F27/232—Mixers with rotary stirring devices in fixed receptacles; Kneaders characterised by the orientation or disposition of the rotor axis with two or more rotation axes
    • B01F27/2322—Mixers with rotary stirring devices in fixed receptacles; Kneaders characterised by the orientation or disposition of the rotor axis with two or more rotation axes with parallel axes
    • 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
    • B01F27/23—Mixers with rotary stirring devices in fixed receptacles; Kneaders characterised by the orientation or disposition of the rotor axis
    • B01F27/232—Mixers with rotary stirring devices in fixed receptacles; Kneaders characterised by the orientation or disposition of the rotor axis with two or more rotation axes
    • B01F27/2323—Mixers with rotary stirring devices in fixed receptacles; Kneaders characterised by the orientation or disposition of the rotor axis with two or more rotation axes with perpendicular axes
    • 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
    • B01F27/71—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis with propellers
    • B01F27/711—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis with propellers co-operating with stationary guiding means, e.g. baffles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/50—Mixing receptacles
    • B01F35/53—Mixing receptacles characterised by the configuration of the interior, e.g. baffles for facilitating the mixing of components
    • B01F35/531—Mixing receptacles characterised by the configuration of the interior, e.g. baffles for facilitating the mixing of components with baffles, plates or bars on the wall or the bottom

Definitions

  • the present invention relates to a method of and an arrangement for agitating fluid in a vessel in the manner described in the preambles of claims 1 and 5.
  • the method and the arrangement of the present invention are, for instance, especially suitable for treating fiber suspensions of pulp and paper making industry, i.e. both for diluting the suspensions and for agitating such for some other purpose, for instance for mixing a chemical with the suspension.
  • the present invention is, naturally, applicable in other branches of industry, too, where agitation of fluid in a large sized vessel is desired.
  • Agitating of fluid in a vessel is a well-known basic process in various branches of industry. Such agitation may be performed in smaller or larger vessels depending on the branch of industry.
  • Chemical, especially petro-chemical industry as well as pulp and paper making industry represent processes where the size of the mixing vessels or storage towers is relatively large, i.e. the diameter of the vessel may exceed 10 meters, and the height 30 meters. All mixing vessels, reactors, storage towers etc. require, in the least, that the fluid that is to be discharged from the vessel is homogenous, i.e. its concentration or composition remains substantially constant over time.
  • the vessel is used for mixing a chemical or some other substance with the fluid, it is of utmost importance that the concentration of the chemical or other substance is, practically seen, constant in the fluid to be discharged from the vessel. Naturally, the larger the vessel is the more difficult it is to ensure the homogeneity of the fluid to be discharged.
  • US-A-5711600 discusses a vessel used in pulp and paper industry, i.e. pulp tower to which fiber suspension is introduced in a consistency of 0 - 40%, typically the consistency is 10 - 30% and from which the suspension is discharged in a consistency of 0 - 5%, typically 4 - 5%.
  • the vessel is used, for instance, for treating fillers of paper making industry the dry matter content may be up to 80%.
  • the fiber suspension or pulp is diluted at the bottom part of the vessel by feeding and mixing the required amount of dilution liquid in the pulp.
  • the bottom of the vessel is provided with a central rotationally symmetrical fillet.
  • the fillet may be mainly cylindrical provided with a cone shaped top or it may have a cylindrical bottom part and a top part formed of a truncated cone inserted on the cylindrical part such that its smaller diameter cross section is against the top of the cylinder and of a cone positioned on the top of the larger diameter cross section of the truncated cone, whereby the fillet may be considered mushroom-shaped.
  • the wall of the vessel round the bottom fillet is provided with a number of agitators positioned or directed such that the flow the agitators create is directed past the bottom fillet, i.e. the agitators make the fluid rotate at the bottom part of the vessel round the fillet.
  • the rotating fluid is to agitate the pulp and to mix the dilution liquid efficiently with the pulp.
  • a problem with the above discussed construction is that the larger the vessel is the greater is the number of agitators needed in ensuring the efficient rotation of the fluid round the bottom fillet.
  • Another problem is the orientation of the agitator shaft, as, for ensuring the rotation of fluid, the shaft has to be inclined with respect to the radius of the vessel, i.e. the direction of the shaft is not radially towards the bottom fillet, but inclined to the side thereof.
  • This brings two types of problems. Firstly, the diameter of the propeller of the agitator is limited due to the inclination of the agitator shaft. And secondly, the fastening of the agitators to the wall of the vessel in inclined direction subjects the fastening elements to significant bending forces.
  • the mechanical components of the agitator are subjected to stresses due to non-symmetrical orientation of the agitator. And further due to the circulation of the fluid in an annular cavity, the turbulence within the fluid is relatively weak. Only the agitators and the circular surfaces of both the fillet and the vessel subject the fluid to turbulence. And only when the velocity of the circulating annulus of fluid is high enough the surface friction between the fluid and both the vessel and the fillet is able to create high enough turbulence for mixing the layers close to the surfaces with the rest of the circulating fluid. The sufficient velocity of the circulating annulus of fluid may be ensured only by forcing the agitators to rotate at a high speed, which results in both high energy consumption and strong forces subjected to the support structures or elements of the agitator and of the wall of the vessel.
  • US-A-5746890 discusses mixing devices for mixing a processing agent with a pulp suspension.
  • the mixing devices include a mixing vessel, an agitator mounted on the upright side wall of the mixing vessel to create a flow of the pulp suspension across the mixing vessel, a processing agent supply for supplying processing agent to the flow of pulp suspension, and a flow divider mounted on the inner wall surface of the mixing vessel opposite the agitator.
  • the flow divider includes a substantially vertical front distribution edge and a pair of arcuate or concave front side surfaces extending from the distribution edge to the inner wall surface of the mixing vessel on opposite sides of the vertical distribution edge.
  • a problem with the vessel provided with such a flow divider is that the larger the vessel is the larger the agitator has to be in order to be able to keep the fluid within the entire bottom area of the tower in movement.
  • the power demand of a large-sized agitator is huge and also the construction of the agitator is so rugged that it may be necessary to provide the vessel wall with additional reinforcement for absorbing the forces subjected thereto, on the one hand, from the weight of the agitator, and on the other hand, from the working of the agitator while it is forcing the fluid to circulate within the bottom part of the vessel.
  • an object of the present invention is to raise the state of the art in the area of agitated vessels by introducing a method and an arrangement for agitating fluid in a vessel capable of minimizing at least some problems and drawbacks of prior art.
  • Another more detailed object of the present invention is to design the bottom part of a vessel such that an efficient turbulence for agitating the fluid in the zone of agitation is created with smaller agitators, with lower energy consumption and with lower stress to the vessel wall and the support elements of the agitator.
  • Prior art Figure 1 illustrates schematically a vessel 2 discussed in more detail in US-A-5,711,600 , the vessel 2 being used in pulp and paper industry.
  • a vessel 2 may be called a pulp tower to which fiber suspension is introduced in a consistency of 0 - 40%, typically the consistency is 10 - 30%, and from which the suspension is discharged in a consistency of 0 - 10%, typically 4 - 5%.
  • the vessel is used, for instance, for treating fillers of paper making industry the dry matter content may be up to 80%.
  • the fiber suspension or pulp is diluted at the bottom part of the vessel 2 by feeding and mixing required amount of dilution liquid in the pulp.
  • the bottom 4 of the vessel 2 is provided with a central rotationally symmetrical upright fillet 6.
  • the fillet 6 may be mainly cylindrical provided with a conically tapering top or it may have, as shown in Figure 1 , a cylindrical bottom part 61 and a top part formed of a truncated cone 62 inserted on the cylindrical part 61 such that its smaller diameter cross section is against the top of the cylindrical part 61 and of a cone 63 positioned on the top of the larger diameter cross section of the truncated cone 62 whereby the fillet 6 may be considered having a mushroom shape.
  • the wall 8 of the vessel 2 round the bottom fillet 6 is provided with a number of agitators 10 positioned or directed such that the agitators 10 direct the fluid flow past the bottom fillet 6 and the agitators 10, thus, make the fluid or pulp circulate at the bottom part of the vessel 2 round the fillet 6.
  • the circulating fluid is to agitate the pulp and to mix the dilution liquid efficiently with the pulp.
  • Prior art Figure 2 illustrates schematically a vessel 12 discussed in more detail in US-A-5746890 .
  • the US- patent discusses mixing devices for mixing a processing agent with a pulp suspension.
  • the mixing devices include a mixing vessel 12, an agitator 20 mounted on the side wall 18 of the mixing vessel 12 to create a flow of the pulp suspension across the mixing vessel 12, a processing agent supply for supplying processing agent to the flow of pulp suspension, and a flow divider 16 mounted on the inner surface of the wall 18 of the mixing vessel 12 opposite to the agitator 20.
  • the flow divider 16 includes a substantially vertical front distribution edge 161 and a pair of arcuate or concave front side surfaces 162 and 163 extending from the distribution edge 161 to the inner surface of the wall 18 of the mixing vessel 12 on opposite sides of the distribution edge 161.
  • Figure 3 illustrates schematically a novel construction of a fillet 26 and a novel way of treating fluid in the vessel 22 in accordance with a first preferred embodiment of the present invention.
  • the bottom 24 of the vessel 22 is provided with a substantially central upright fillet 26 and at least two agitators 30 supported radially to the upright side wall 28 of the vessel 22 on opposite sides of the fillet 26.
  • the upright side wall is understood as a wall surrounding the zone of agitation of the vessel and having an inclination (either inwards or outwards) of less than 45 degrees, preferably less than 30 degrees from the vertical direction. Most preferably the side wall is vertical.
  • the agitators 30 are fastened or supported to the side wall 28 such that the direction of the flow they create is inwardly in the vessel 22, i.e. towards the fillet 26.
  • the agitators are normally arranged such that their drive motor and gearbox are outside the vessel and only the shaft with possible support structures extends into the vessel, the shaft carrying at its end the agitator propeller. In some specific cases other parts of the agitators may be installed within the vessel wall, too.
  • the agitators 30 are supported to the vessel side wall 28 such that the shaft of the agitator points towards the fillet, which direction is here considered to be within the term "radial".
  • the shaft is arranged in a radial plane, i.e.
  • the axis of the shaft runs in a plane in which also the axis of the vessel runs.
  • the shaft of the agitator need not necessarily be horizontal, but it may be inclined in either direction by at most 30 degrees, which direction is also considered to be encompassed by the definition "radial”.
  • the fillet 26 has, in this embodiment, a square, in broader terms quadrangular, cross section such that two opposite edges (261 and 264) of the cross section face the agitators 30 and act as the flow receiving edges.
  • the fillet 26, thus, has four side faces 262, 263, 265 and 266 such that in operation, firstly, the receiving edges 261, 264 facing the agitators 30 divide the flow coming from the agitators 30 to the sides of the edges and the side faces 262, 263 and 265, 266 guide the flow to the sides of the fillet 26 as shown by arrows in the upper projection such that four separate vortices are formed at the zone of agitation.
  • the internal angle ⁇ between the side faces 262 and 263, and 265 and 266 at the receiving edges 261 and 264 is preferably 90 degrees whereby also the other internal angles at the flow departing or trailing edges of the square cross section are 90 degrees.
  • the internal angle ⁇ at the receiving edges 261 and 264 may vary between 60 and 120 degrees whereby the other two internal angles at the trailing edges are varying between 120 and 60 degrees.
  • the top of the fillet 26 may be designed freely whereby, for instance, the way the fluid is introduced into the vessel may have an influence on the top design.
  • Figure 3 shows a top design where the top is in fact a kind of a roof formed of two side planes 267 and 268 or slopes facing the agitators 30.
  • the roof may also be arranged in another direction i.e. the ridge being arranged on the same diametral plane with the agitators 30.
  • the top of the fillet may be formed of four side planes or slopes, whereby the top is pyramid-shaped. Or, if desired, cone-shaped.
  • This kind of a top design is preferable if the vessel is filled from the top, whereby the fluid flow hits the fillet from above.
  • the top may also be horizontal if there is no need to protect the top of the fillet from fluid hitting it from above.
  • the fillet may be open from inside if the fluid is introduced into the vessel via the fillet.
  • Figure 4 illustrates schematically a novel construction of a fillet 36 and a novel way of treating fluid in the vessel 32 in accordance with a second preferred embodiment of the present invention.
  • the bottom 34 of the vessel 32 is provided with a central upright fillet 36 and at least two agitators 30 (here four agitators are shown) supported radially to the side wall 38 of the vessel 32 on opposite sides of the fillet 36.
  • the upright side wall 38 is understood as a wall surrounding the zone of agitation of the vessel and having an inclination of less than 45 degrees, preferably less than 30 degrees from the vertical direction. Most preferably the side wall is vertical.
  • the agitators 30 are fastened to the wall 38 such that the direction of the flow they create is radially inwardly in the vessel 32, i.e. towards the fillet 36.
  • the agitators are normally arranged such that their drive motor and gearbox are outside the vessel and only the shaft with possible support structures extends into the vessel, the shaft carrying at its end the agitator propeller. In some specific cases other parts of the agitators may be installed within the vessel wall, too.
  • the agitators are supported to the vessel side wall such that the shaft of the agitator points towards the fillet, preferably towards the edge of the fillet, which direction is here considered to be within the term "radial".
  • the shaft is arranged in a radial plane, i.e.
  • the axis of the shaft runs in a plane in which also the axis of the vessel runs.
  • the shaft of the agitator need not necessarily be horizontal, but it may be inclined in either direction by at most 30 degrees, which direction is also considered to be encompassed by the definition "radial”.
  • This kind of an agitator arrangement may be applied either with the quadrangular fillet of Figure 3 or with a star-shaped fillet 36 of Figure 4 .
  • the fillet 36 has, in this embodiment of the present invention, a somewhat star-shaped cross section such that two opposite receiving tips or edges 361 and 364 of the cross section face the agitators 30.
  • the fillet 36 thus, has four arcuate or concave side faces 362, 363, 365 and 366 such that in operation, firstly, the receiving edges 361 and 364 of the fillet 36 facing the agitators 30 divide the flow coming from the agitators 30 to the sides of the receiving edges and the side faces 362, 363 and 365, 366 guide the flow to the sides of the fillet 36 as shown by arrows in the upper projection in Figure 4 such that four separate vortices are formed at the zone of agitation.
  • the side faces 362 and 363, and 365 and 366 are arranged to adjoin at the receiving edges 361 and 364 such that the tangents (in a radial plane) of the side faces at the receiving edges form an internal angle of less than 90 degrees, preferably less than 60 degrees, and more preferably less than 45 degrees.
  • the side faces 362 and 365, and side faces 363 and 366 adjoin at the flow departing or trailing edges of the fillet 36 such that their tangents (in a radial plane) form an internal angle of less than 90 degrees, preferably less than 45 degrees, i.e. all internal angles are sharp.
  • the top of the fillet of Figure 4 may be of any appropriate design.
  • the discussion in connection with the fillet of Figure 3 concerning the shape of the top is here referred to as an example of the variations in the top design.
  • the receiving and the trailing edges of the fillet may be vertical (as shown in the Figures) or slightly inclined. The same applies to the side faces, too.
  • the entire fillet may be pyramid shaped.
  • the fillet extends at least to the operative height of the agitators, i.e. to the height or level of the shaft of the uppermost agitator plus the length of the agitator blade.
  • the arrangement in accordance with the above embodiments of the present invention functions such that, when the agitators are arranged within the fluid in the vessel, a fluid flow is created by rotating each agitator, each fluid flow being directed towards the receiving edge of the fillet, in broader terms, towards the fillet.
  • the receiving edges divide each flow into two partial flows and the side faces of the receiving edges guide the partial flows to circulate in smaller volumes, i.e. in four smaller vortices ensuring efficient agitation in the entire area of the zone of agitation, i.e. the bottom area of the vessel round the fillet.
  • This kind of agitation may be maintained such that the agitators and their fastening elements or support structures are subjected to significantly lighter or lower stress than those in prior art vessels of the same size. Also, the efficiency of the agitation or mixing is better due to smaller size of each individual vortex or turbulence field.
  • the number of agitators in a certain level is a half of the number of edges in the fillet, or equal with the number of receiving edges in the fillet.
  • the number of agitators is a half of the number of edges in the fillet or multiple thereof, or equal with the number of receiving edges or a multiple thereof.
  • FIG 5 illustrates schematically a further agitator arrangement in a vessel 42 provided with a fillet 46 in accordance with Figure 3 , though also the fillet of Figure 4 could as well be applied.
  • the vessel wall is provided with an agitator 30, or a plurality of agitators one above the other, for each edge of the fillet 46.
  • each edge of the fillet operates as the receiving edge.
  • the agitators 30 make the fluid flow against each edge of the fillet 46 for creating partial flows whereafter the partial flows advance along the side faces of the fillet 46 until two partial flows originating from the operation of two neighboring agitators 30 and two adjacent receiving edges collide on the side face.
  • the collision of the partial flows forces the flows to turn towards the wall of the vessel 42, whereby, in a cross section of the vessel 42 at the level of the agitators eight vortices, more generally speaking, twice the amount of agitators, may be seen. It also a possible option that there may not be seen any vortices but the collision of the flows result in a chaos- type efficient turbulence field.
  • the agitators 30 of the arrangement of Figure 5 are preferably arranged on substantially the same horizontal level.
  • the agitators of Figure 5 on two horizontal levels either such that there are four agitators on both levels, whereby the agitators of the different levels are one above the other, or such that in total of four agitators are arranged such that a pair of opposite agitators are located on a lower horizontal level and another opposite pair on an upper horizontal level.
  • the number of agitators in a certain level is the number of edges in the fillet.
  • the number of agitators is the number of edges in the fillet or a multiple thereof.
  • FIG 6 illustrates schematically a yet further agitator arrangement in a vessel 52 provided with a fillet 56 in accordance with Figure 3 , though also the fillet of Figure 4 could as well be applied.
  • each single agitator on the vessel wall i.e. as shown in Figure 5
  • the agitators 50 of each pair of agitators are standard agitators, whereby they rotate in the same direction.
  • the agitators may be arranged, if desired, to rotate in opposite directions. In both cases, the two agitators create a powerful flow towards an edge or the side faces of the fillet 56 depending on the orientation of the agitators. Now all edges of the fillet 56 operate as flow receiving edges.
  • the agitator pairs make the fluid flow against the receiving edges or the side faces of the fillet 56 for creating partial flows whereafter the partial flows advance along the side faces of the fillet 56 until two partial flows originating from the operation of two neighboring agitators 50 of different pairs of agitators collide.
  • the collision of the partial flows force the flows to turn towards the wall of the vessel 52, whereby, in a cross section of the vessel 52 either eight vortices, more generally speaking, the same number with the agitators, or only a chaotic turbulent zone, may be seen.
  • the agitators 50 of the arrangement of Figure 6 are preferably arranged on substantially the same horizontal level.
  • the agitators of Figure 6 on two horizontal levels either such that there are eight agitators on both levels, whereby the agitators of the different levels are one above the other, or such that in total of eight agitators are arranged such that a pair of opposite pairs agitators are located on a lower horizontal level and another pair of opposite pairs on an upper horizontal level.
  • the number of agitators in a certain level is may start from the number of edges of the fillet, whereby there are flow receiving edges and trailing edges, i.e. not all edges of the fillet receives the flow.
  • a preferred number of agitators in a certain level is twice the number of edges in the fillet.
  • the number of agitators is twice the number of edges in the fillet or a multiple thereof.
  • the single agitators of the embodiment of Figures 3 or 4 with pairs of agitators, whereby the operation of the vessel - fillet - agitator combination is substantially the same as discussed in connection with Figures 3 and 4 .
  • the agitators of a pair of agitators need not necessarily have their shafts parallel with each other, but the shafts may be arranged slightly inclined such that the centerlines of the shafts of each pair of agitators cross in the centerline plane of the agitator pair, the centerline plane running via the axis of the fillet somewhere within the vessel or behind the fillet.
  • Figure 7 illustrates schematically a novel fillet construction and a novel way of treating fluid in the vessel in accordance with a third preferred embodiment of the present invention.
  • the fillet 66 of Figure 7 is formed of two substantially equal parts, i.e. a lower part 66' and an upper part 66" having either a square (shown in Figure 7 ) or a star-shaped cross section, or one having a square cross section and the other a star-shaped cross section.
  • the upper part 66" of the fillet 66 is arranged co-axially with the lower one 66', but, however, such that the angular position of the upper part 66" of the fillet 55 is turned 45 degrees round its axis compared to the lower one 66'.
  • the number of agitators in a certain level is the number of edges in the fillet.
  • the number of agitators is the number of edges in the fillet or a multiple thereof.
  • the fillet may have more than four edges. Also the number of edges may be an odd number, whereby the agitators may either direct the flow towards each edge of the fillet, or towards each side face between the edges.
  • the flows along the side faces of the fillet collide and are either directed to form vortices or form a chaotic turbulence field.
  • the flows follow the side faces to the end thereof and then turn to form vortices.
  • the side faces of the fillet are arcuate and divert the flow in an appropriate manner to counter rotating vortices the number of which is the same as that of the edges of the fillet.
  • the size of agitators may be maintained relatively small or at least reasonable, as there is no need for a single agitator to be able to keep the entire bottom area of the vessel in movement but the vessel bottom volume is divided between at least two agitators. Also, when the number of agitators increase, there is a point where taking one agitator out of use, for instance for service, does not result in a considerable weakening of the agitation in the vessel. This means in practice that the agitators may be serviced without interrupting the process the vessel is arranged in.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Mixers Of The Rotary Stirring Type (AREA)
EP20130189963 2013-10-23 2013-10-23 Verfharen und Vorrichtung zum Rühren einer Flüssigkeit in einem Gefäss Withdrawn EP2865806A1 (de)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105126689A (zh) * 2015-08-25 2015-12-09 芜湖集拓橡胶技术有限公司 全方位橡胶搅拌桶
CN107596942A (zh) * 2017-08-01 2018-01-19 曾凡友 一种喷涂用喷涂液配制设备
CN109197098A (zh) * 2018-11-01 2019-01-15 沈阳城市公用集团农业发展有限公司 一种带有肥料混合功能的农业灌溉设备

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5711600A (en) 1994-06-09 1998-01-27 Ahlstrom Machinery Corporation High consistency pulp tower with a parting member and the introduction of dilution liquid
US5746890A (en) 1993-12-21 1998-05-05 Sunds Defibrator Industries Ab Device for admixing a processing agent into a pulp suspension

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5746890A (en) 1993-12-21 1998-05-05 Sunds Defibrator Industries Ab Device for admixing a processing agent into a pulp suspension
US5711600A (en) 1994-06-09 1998-01-27 Ahlstrom Machinery Corporation High consistency pulp tower with a parting member and the introduction of dilution liquid

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105126689A (zh) * 2015-08-25 2015-12-09 芜湖集拓橡胶技术有限公司 全方位橡胶搅拌桶
CN107596942A (zh) * 2017-08-01 2018-01-19 曾凡友 一种喷涂用喷涂液配制设备
CN109197098A (zh) * 2018-11-01 2019-01-15 沈阳城市公用集团农业发展有限公司 一种带有肥料混合功能的农业灌溉设备

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