DEVICE AND METHOD FOR DILUTION OF CELLULOSE PULP

Description

[0001] The present invention relates to an improved device for dilution of cellulose pulp in the form of flocs and to a related method. The dilution is intended to be performed in order to dilute HC-cellulose pulp of an original consistency of about 20 to 45% (HC =High Consistency), the dilution being withheld until the formation of a MC-pulp, i.e. until the pulp reaches a consistency in the range of 6-18% (MC=Medium consistency).

Background

[0002] In connection to the dilution of decomposed cellulose pulp of a high dryness, topically a consistency of above 20%, it is normal procedure to add dilution liquid whilst agitating by means of a dilution screw. This has also been the starting point in the Swedish patent SE 526292, which represents the prior art. Within this prior art dilution to the desired consistency is achieved by the addition of dilution liquid via a ring shaped supply chamber around a pulp chute.

[0003] A ring shaped supply chamber for the addition of dilution liquid has been used in the business for a long time and has for instance been utilized for the dilution of cellulose pulp after HC-Ozon reactors, i.e. bleaching reactors in which cellulose pulp of high consistency, i.e. above approximately 20%, is bleached with Ozon. A HC-Ozon reactor is conventionally a horizontal reactor with an interior transport and mixing screw, which normally is arranged directly after a shredding screw from a wash press, and in which the pulp falls down into a pulp chute after having been treated in the HC-Ozon reactor. In e.g. US 5 174 861, the fundamentals of a horizontal Ozon reactor is disclosed, in which the HC-pulp falls freely down into a dilution tank after the reactor.

[0004] It has been noticed that the use of a ring shaped supply chamber around a pulp chute that periferally injects dilution liquid towards the falling floes of pulp, only achieves a certain degree of penetration into the flow and that the maximum quantity of dilution liquid that may be added is limited.

[0005] In a plant with a capacity of 3000 ADT (Absolutely Dry Tons) of pulp a day, a pulp chute of a diameter in the range of 1,5 metre is utilized and conventionally no pulp chute for MC-pulp (Medium Consistency) with a diameter of less than 0,80 metres has been utilized. This means that a verv good agitation of the pulp is required in order to achieve a satisfactory dilution by means of a ring shaped supply chamber.

Short description of the invention

[0006] the present invention relates to an improvement of the dilution with respect to a ring shaped supply chamber. An object of the invention is to overcome the problems of the prior art and to evenly distribute the dilution such that substantially the whole pulp volume will have the same consistency. This is achieved by means of a device, according to claim 1.

[0007] According to a first aspect, the invention relates to a device for dilution of cellulose pulp of a consistency of between 20 and 45%, which device comprises a pulp chute through which cellulose pulp is arranged to fall down under the addition of dilution liquid, wherein the dilution is performed to a consistency in the range of 6-18%, and wherein the addition of dilution liquid is performed on the falling pulp above a level of established diluted pulp in the bottom of the pulp chute. Further, a central distribution device with a nozzle arranged in the centre of the pulp chute for the addition of dilution liquid to the falling pulp in the centre of the pulp chute and above the level of established diluted pulp in the bottom of the pulp chute, wherein the nozzle is fed with dilution liquid via a pipe that is arranged at least partly through the pulp chute.

[0008] According to a second aspect, the invention relates to a method of dilution of cellulose pulp with a consistency of between 20 and 45 °%v= where dilution liquids is added to the cellulose pulp in a pulp chute, which dilution is performed to a consistency in the range of 6-18% as the cellulose pulp is in free fall above an established level of diluted cellulose pulp at the bottom of the pulp chute. The dilution liquid is added in the centre of the pulp chute.

[0009] In the device and the method according to the invention flocs of pulp are wetted throughout essentially the whole cross section of the pulp chute before the flocs hit the established pulp level in the chute. Thus, not only the floes of pulp falling along the walls of the pulp chute will be wet, in which case the degree of wetting decreases with increasing distance from the walls of the pulp chute and is close to zero in the centre of the pulp chute. Instead, an even dilution, which is especially important with increasing capacity of the plants, and with the invention it is possible to reach a capacity of 4-5000 ADT pulp per day and plant.

[0010] With the invention it is possible to obtain a higher degree ofhomogen dilution of cellulose pulp in free fall, since more dilution liquid may be added, which furthermore may be more evenly distributed in the pulp. Also, it is possible to obtain a high degree of homogeneously diluted cellulose pulp already in the free fall, i.e. without agitating the liquid. Another advantage is that it is possible to divide the dilution liquids such that a less aggressive dilution liquid may be added in the periphery as a complement to treat the walls of the pulp chute leniently, wherein a less costly material may be used for these, while more aggressive pH adjusting chemicals, such as acids or bleaching chemicals, are added in the centre of the chute and surrounded by a protecting curtain of less aggressive cellulose pulp, closer to the inner walls of the chute.

Short description of the drawings

[0011] Below, an embodiment of the invention will be described in detail with reference to the accompanying figures, of which:

Fig. 1

schematically shows a comprehensive view of an embodiment of a dilution device according to the invention;

Fig. 2

shows a view from below of an embodiment of the invention;

Fig. 3

shows a cross sectional side view of an embodiment of the invention.

Detailed description of the invention

[0012] Figure 1 shows a position in the pulp line where decomposed cellulose pulp in the form of flocs is transported in a screw feeder 1 in which a feed screw 2 feeds flocs of cellulose pulp to a pulp chute 3. The screw feeder 1 may constitute the final part of a pulp shredder or transport screw in a bleaching reactor in which the cellulose pulp is beached at a high consistency, above at least 20%.

[0013] In the upper part of the pulp chute 3 a dilution device 10 is arranged, which adds dilution liquid to the flow of flocs that falls freely down towards an established level of pulp 6 in the pulp chute 3. The dilution device 1 comprises a line 15 that is drawn to a central distribution device with nozzles 11 arranged in the centre of the pulp chute 3 in order to distribute dilution liquid to the cellulose pulp, as it falls freely in the centre of the pulp chute. Additionally, in the shown embodiment there is also a supply chamber 16, which is arranged for adding dilution liquid concentrically around the pulp chute, and which is provided with a plurality of nozzles 14 on the inner wall 3A of the chute 3 (see fig. 2) for distributing dilution liquid to the Hocs that falls freely.

[0014] The diluted pulp, which by the addition of dilution liquid has obtained a relatively homogenous concentration, forms an established level 6 of diluted pulp in the bottom of the chute 3. In connection to the bottom of the chute a MC-pump 4 is arranged, which in a conventional manner is provided with a fluidizer 5 in front of the pump wheel of the pump. The fluidizer 5 is at least partly arranged inside the chute 3 and provides a hefty agitation of the cellulose pulp in the bottom of the pulp chute, which is indicated with rotational arrows, and accomplishes the homogenisation of the concentration of the cellulose pulp. Normally, the fluidizer is integrated with the pump wheel of the pump, but it may also be separated from the pump wheel and be provided with an own driving means, and placed in immediate connection of the inlet to the pump wheel.

[0015] I figure 2, an embodiment of the dilution device 10 is shown in a view from below. Dilution liquid is added via the line 12, wherein the dilution liquid reaches a certain pressure inside a supply chamber 16 defined by an outer wall 10A and the inner wall 3A the pulp chute 3. A number of outlets 14 are arranged in the periphery of the pulp chute from the supply chamber 16 and directed inwards, towards the centre of the pulp chute. The pressure in the supply chamber 16 is such that the dilution liquid is sprayed into the pulp chute towards the falling pulp. The pressure control, the shape of the outlet and the quantity of outlets may vary in a number of different way, which are evident to the skilled person. The object is however to yield maximal penetration into the flow of fulling pulp Flocks.

[0016] As is apparent from the figures, the central distribution device comprises at least one pipe 15 5 extending from the wall 3A of the pulp chute 3 inwards, towards the centre of the pulp chute. At the end of this pipe 5, at least one nozzle 11 is arranged, for the addition oaf at least a part of the dilution liquid. The nozzles 11 may have several outlets and may distribute the dilution liquid in form of a downwardly directed shower stream 11A with a substantially conical jet (see figure 3). However, the dilution liquid may also be added in a direction obliquely upwards or completely horizontally outwards towards the walls 3A in the pulp chute. An advantage of adding the dilution liquid obliquely upwards is that it thus is given more time for mixing with the falling pulp, whereby it of course mixes better. Another advantage is that the energy of impact from the dilution liquid hitting the pulp contributes in mixing the pulp, which leads to that the pulp mixing gets a more homogenous consistency. In order to further improve the distribution of dilution liquid to the falling cellulose pulp it is feasible to arrange several central nozzles 11, which are distributed over substantially the whole with of the pulp chute.

[0017] An alternative or complement to such a distribution of the nozzles 11 in the centre of the pulp chute 3 is to, as in the shown embodiment, also arrange peripheral outlets 14. In figures 1 and 3, the nozzle 11 of the central distribution device is arranged below the peripheral outlets 14 of the supply chamber 16 in the wall 3A of the pulp chute. In this way the addition of dilution liquid is directed towards the upper side of the pipe 11 of the central distribution device, partly in order to keep this free from flocs that otherwise easily may gather thereon. Therefore, as is shown in figure 3, one of the jets 14B from the peripheral outlets 14 may directed in parallel with the upper side of the pipe 11. The pipe may also be drawn into the pulp chute in the way that is shown in figure 3, i.e. obliquely downwards such that the flocs tailing from above towards the pipe shall fall of more easily. To a skilled person it is obvious that the pipe 15 also may be drawn in several other fashions. It is of course important that the pipe does not hinder the falling the pulp too much, a certain contact may however be positive since it may function as an agitation of the pulp, which may contribute to better mixing and homogenisation of it.

[0018] In one embodiment of the invention the feeding pipe 15 is provided with a separate feeding, wherein the outlets or nozzles 11 of the central distribution devices may be fed with a different dilution liquid from another source than the one that is being fed to the peripheral nozzles le. Thus, it is possible to add a pH-regulating agent, bleaching chemicals or other additives centrally in the pulp chute, whereby the falling flocs of pulp that has been totally or partly diluted with a less aggressive dilution liquid shields off the centrally added dilution liquid such that it does not reach the inner wall a of the pulp chute. The design of the supply chamber 16 and the upper parts of the pulp chute 3 may hence be designed in a simpler and cheaper material, where only the pipe 15 and nozzle 11 of the central distribution device requires materials that are resistant to a concentrated dilution liquid.

[0019] Large quantities of dilution liquid are added to the flow of freely falling pulp flocs and may be followed by air or gas in the flow, wherein an active deaeration may be needed in order to vent redundant volumes accompanying the flow. The pulp chute may therefore be designed with a deaeration canal 13 that is connected to the pulp chute above the supply chamber 10.

[0020] The deaerated gases may either he released to the surrounding atmosphere or to a decomposition system depending on whether the gases are environmental harmful or not.

Claims

1. Device (1) for dilution of cellulose pulp of a consistency of between 20 and 45%, which device comprises a pulp chute (3) through which cellulose pulp is arranged to fall down under the addition of dilution liquid, wherein the dilution is performed to a consistency in the range of 6-18%, and wherein the addition of dilution liquid is performed on the falling pulp above a level (6) of established diluted pulp in the bottom of the pulp chute (3), characterised in a central distribution device with a nozzle (11) arranged in the centre of the pulp chute (3) for the addition of dilution liquid to the falling pulp in the centre of the pulp chute (3) and above the level (6) of established diluted pulp in the bottom of the pulp chute, wherein the nozzle (11) is fed with dilution liquid via a pipe (15) that is arranged at least partly through the pulp chute.

2. Device according to claim 1, characterised in that the central distribution device comprises several nozzles (11) that are evenly distributed over the width of the pulp chute.

3. Device according to claim 1 or 2 characterised in that a peripheral distribution device with perifepheral nozzles (14) is arranged for adding dilution liquid from the inner wall (3A) of the pulp chute.

4. Device according to claim 3, characterised in that the central distribution device is arranged under the nozzles (14) of the peripheral distribution device.

5. Device according to claim 3 or 4, characterised in that the feeding to the nozzles (11) of the central distribution device is separated from the feeding to the nozzles (14) of the peripheral distribution device, wherein dilution liquid from different sources may be fed to the different nozzles (11 and 14, respectively).

6. Device according to claim 5 characterised in that a deaeration canal (13) is arranged in connection to the pulp chute (3) above the nozzles (11, 14).

7. Method for dilution of cellulose pulp with a consistency of between 20 and 45%, where dilution liquid is added to the cellulose pulp in a pulp chute, which dilution is performed to a consistency in the range of 6~18% as the cellulose pulp is in free fall above an established level of diluted cellulose pulp at the bottom of the pulp chute, characterised in that dilution liquid is added in the centre of the pulp chute.

8. Method according to claim 7, characterised in that the dilution liquid is added from several nozzles that are substantially evenly distributed over the width of the pulp chute.

9. Method according to claim 7 or 8, characterised in that dilution liquid also is added from the inner wall (3A) of the pulp chute.

10. Method according to claim 9, characterised in that different dilution liquids are added in the centre and the periphery of the pulp chute, wherein the dilution liquid added in the centre of the pulp chute preferably is more concentrated than the dilution liquid added in the periphery of the pulp chute.

11. Method according to any of the claims 7-10, characterised in that at least 25% of the dilution liquid is added in the centre of the pulp chute.

Ansprüche

1. Vorrichtung (1) zum Verdünnen celluloser Pülpe mit einer Konsistenz von zwischen 20 und 45 %, wobei die Vorrichtung eine Schütte (3) für die Pülpe aufweist durch die die Pülpe unter der Zugabe von Verdünnungsflüssigkeit hinunterfällt, wobei die Verdünnung auf eine Konsistenz im Bereich von 6-18 % erfolgt und wobei die Zugabe der Verdünnungsflüssigkeit auf die fallende Pülpe über einem Niveau (6) erfolgt, das der angekommenen, verdünnten Pülpe am Boden der Pülpeschütte entspricht, dadurch gekennzeichnet, dass eine zentrale Verteilungsvorrichtung mit einer Düse (11) im Zentrum der Pülpeschütte (3) für die Zugabe vom Verdünnungsflüssigkeit für die fallende Pülpe im Zentrum der Pülpeschütte (3) und oberhalb des Niveaus (6) der verdünnten, angekommenen Pülpe am Boden der Pülpeschütte angeordnet ist, wobei die Düse (11) mit Verdünnungsflüssigkeit über ein Rohr (15) versorgt wird, das zumindest teilweise durch die Pülpeschütte hindurch angeordnet ist.

2. Vorrichtung nach Anspruch 1, dadurch gekennzeichnet, dass die zentrale Verteilungsvorrichtung einige Düsen (11) umfasst, die gleichmäßig über die Breite der Pülpeschütte verteilt sind.

3. Vorrichtung nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass eine periphere Verteilungsvorrichtung mit peripheren Düsen (14) vorgesehen ist, um Verdünnungsflüssigkeit von der inneren Wand (3A) der Pülpeschütte her zuzuführen.

4. Vorrichtung nach Anspruch 3, dadurch gekennzeichnet, dass die zentrale Verteilungsvorrichtung unter den Düsen (14) der peripheren Verteilungsvorrichtung vorgesehen ist.

5. Vorrichtung nach Anspruch 3 oder 4, dadurch gekennzeichnet, dass die Zufuhr zu den Düsen (11) der zentralen Verteilungsvorrichtung von der Zufuhr zu den Düsen (14) der peripheren Verdünnungsvorrichtung getrennt ist, wodurch Verdünnungsflüssigkeit von unterschiedlichen Quellen zu den Düsen (11 bzw. 14) geführt werden kann.

6. Vorrichtung nach Anspruch 5, dadurch gekennzeichnet, dass ein Entlüftungskanal (13) in Verbindung mit der Pülpeschütte 3 oberhalb der Düsen (11, 14) angeordnet ist.

7. Verfahren zum Verdünnen celluloser Pülpe mit einer Konsistenz von zwischen 20 und 45 %, wobei Verdünnungsflüssigkeit der cellulosen Pülpe in einer Pülpeschütte zugegeben wird, wobei die Verdünnung bis zu einer Konsistenz im Bereich von 16-18 % erfolgt, wenn sich die cellulose Pülpe im freien Fall oberhalb eines Niveaus der am Boden der Pülpeschütte ruhenden, verdünnten Pülpe befindet, dadurch gekennzeichnet, dass Verdünnungsflüssigkeit im Zentrum der Pülpeschütte zugeführt wird.

8. Verfahren nach Anspruch 7, dadurch gekennzeichnet, dass die Verdünnungsflüssigkeit aus einigen Düsen zugeführt wird, die im Wesentlichen gleichmäßig über der Breite der Pülpeschütte verteilt sind.

9. Verfahren nach Anspruch 7 oder 8, dadurch gekennzeichnet, dass die Verdünnungsflüssigkeit auch von der Innenwand (3A) der Pülpeschütte zugeführt wird.

10. Verfahren nach Anspruch 9, dadurch gekennzeichnet, dass verschiedene Verdünnungsflüssigkeiten im Zentrum und in der Peripherie der Pülpeschütte zugegeben werden, wobei die Verdünnungsflüssigkeit, die im Zentrum der Pülpeschütte zugegeben wird, vorzugsweise stärker konzentriert ist, als die Verdünnungsflüssigkeit die an der Peripherie der Pülpeschütte zugegeben wird.

11. Verfahren nach einem der Ansprüche 7-10, dadurch gekennzeichnet, dass zumindest 25 % der Verdünnungsflüssigkeit im Zentrum der Pülpeschütte zugegeben werden.

Revendications

1. Dispositif (1) destiné à la dilution d'une pâte de cellulose d'une consistance comprise entre 20 et 45%, lequel dispositif comprend une goulotte d'écoulement de pâte (3) par laquelle la pâte de cellulose est agencée en vue de tomber sous l'addition d'un liquide de dilution , dans lequel la dilution est effectuée jusqu'à une consistance se situant dans une plage de 6 à 18%, et dans lequel l'addition du liquide de dilution est réalisée sur la pâte lors de sa chute au-dessus d'un niveau (6) de pâte diluée établie dans le fond de la goulotte d'écoulement de la pâte (3), caractérisé par le fait d'un dispositif central de distribution pourvu d'une buse (11) disposée au centre de la goulotte d'écoulement de pâte (3) en vue de l'addition du liquide de dilution à la pâte qui tombe dans le centre de la goulotte d'écoulement de pâte (3) et au-dessus du niveau (6) de la pâte diluée établie dans le fond de la goulotte d'écoulement de la pâte, dans lequel la buse (11) est alimentée en liquide de dilution par l'intermédiaire d'un tuyau (15) qui est disposé, au moins partiellement, à travers la goulotte d'écoulement de la pâte.

2. Dispositif selon la revendication 1, caractérisé en ce que le dispositif central de distribution comporte plusieurs buses (11) qui sont réparties régulièrement sur la largeur de la goulotte d'écoulement de la pâte.

3. Dispositif selon la revendication 1 ou 2, caractérisé en ce qu'un dispositif périphérique de distribution doté de buses périphériques (14) est agencé pour ajouter du liquide de dilution à partir de la paroi interne (3A) de la goulotte d'écoulement de la pâte.

4. Dispositif selon la revendication 3, caractérisé en ce que le dispositif central de distribution est agencé sous les buses (14) du dispositif périphérique de distribution.

5. Dispositif selon la revendication 3 ou 4, caractérisé en ce que l'alimentation des buses (11) du dispositif central de distribution est séparée de l'alimentation des buses (14) du dispositif périphérique de distribution, dans lequel un liquide de dilution provenant de sources différentes peut être fourni à des buses différentes (11 et 14, respectivement).

6. Dispositif selon la revendication 5, caractérisé en ce que le canal de désaération (13) est agencé en liaison avec la goulotte d'écoulement de la pâte (3) au-dessus des buses (11, 14).

7. Procédé permettant la dilution d'une pâte de cellulose présentant une consistance comprise entre 20 et 45%, dans lequel un liquide de dilution est ajouté à la pâte de cellulose dans une goulotte d'écoulement de la pâte, laquelle dilution est réalisée jusqu'à une consistance se situant dans la plage de 6 à 18% lorsque la pâte de cellulose est en chute libre au-dessus d'un niveau établi de pâte de cellulose diluée au niveau du fond de la goulotte d'écoulement de pâte, caractérisé en ce que le liquide de dilution est ajouté au centre de la goulotte d'écoulement de la pâte.

8. Procédé selon la revendication 7, caractérisé en ce que le liquide de dilution est ajouté à partir de plusieurs buses qui sont essentiellement réparties de façon régulière sur la largeur de la goulotte d'écoulement de la pâte.

9. Procédé selon la revendication 7 ou 8, caractérisé en ce que le liquide de dilution est également ajouté à partir de la paroi interne (3A) de la goulotte d'écoulement de la pâte.

10. Procédé selon la revendication 9, caractérisé en ce que des liquides de dilution différents sont ajoutés au centre et à la périphérie de la goulotte d'écoulement de la pâte, dans lequel le liquide de dilution ajouté au centre de la goulotte d'écoulement de la pâte est, de préférence, plus concentré que le liquide de dilution ajouté à la périphérie de la goulotte d'écoulement de la pâte.

11. Procédé selon l'une quelconque des revendications 7 à 10, caractérisé en ce qu'au moins 25% du liquide de dilution est ajouté au centre de la goulotte d'écoulement de la pâte.

Drawing