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WO1998035090A1 - Procede continu de production de pate avec impregnation de liqueur residuaire - Google Patents

Procede continu de production de pate avec impregnation de liqueur residuaire Download PDF

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Publication number
WO1998035090A1
WO1998035090A1 PCT/SE1997/000192 SE9700192W WO9835090A1 WO 1998035090 A1 WO1998035090 A1 WO 1998035090A1 SE 9700192 W SE9700192 W SE 9700192W WO 9835090 A1 WO9835090 A1 WO 9835090A1
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WO
WIPO (PCT)
Prior art keywords
zone
liquor
cooking
digester
con
Prior art date
Application number
PCT/SE1997/000192
Other languages
English (en)
Inventor
Johan ENGSTRÖM
Vidar Snekkenes
Krister Olsson
Sören GUSTAVSSON
Christofer Lindgren
Mikael Lindström
Original Assignee
Kvaerner Pulping Ab
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
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=20405502&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=WO1998035090(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Kvaerner Pulping Ab filed Critical Kvaerner Pulping Ab
Priority to PCT/SE1997/000192 priority Critical patent/WO1998035090A1/fr
Priority to AU21836/97A priority patent/AU2183697A/en
Priority to ZA98936A priority patent/ZA98936B/xx
Priority to DE69800767T priority patent/DE69800767T2/de
Priority to ES98903344T priority patent/ES2159175T3/es
Priority to CA002279283A priority patent/CA2279283C/fr
Priority to AT98903344T priority patent/ATE201064T1/de
Priority to EP98903344A priority patent/EP0909353B1/fr
Publication of WO1998035090A1 publication Critical patent/WO1998035090A1/fr

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Classifications

    • 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
    • D21C3/00—Pulping cellulose-containing materials
    • D21C3/22—Other features of pulping processes
    • 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
    • D21C3/00—Pulping cellulose-containing materials
    • D21C3/02—Pulping cellulose-containing materials with inorganic bases or alkaline reacting compounds, e.g. sulfate processes
    • 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
    • D21C3/00—Pulping cellulose-containing materials
    • D21C3/22—Other features of pulping processes
    • D21C3/24—Continuous processes

Definitions

  • the present invention relates to a novel method for producing pulp, preferably sulphate cellulose, with the aid of a continuous cooking process.
  • the method is preferably directed towards exploiting, in both steam/liquid-phase digesters and hydraulic digesters, the advantages associated with impregnating the chips with the aid of hot black liquor.
  • ITCTM One recent brake through within the field of cooking is ITCTM, which was developed by us in 1992-1993.
  • ITCTM is described in WO-9411566, which shows that very good results concerning pulp quality could be achieved when using ITCTM, which mainly is based on using almost the same temperature (relatively low compared to prior art) in all cooking zones in combination with moderate alkaline levels.
  • the ITC ⁇ -concept does not merely relate to the equalisation of temperatures between different cooking zones, but a considerable contribution of the ITC ⁇ -concept relates to enabling an equalised alkaline profile also in the lower part of the counter-current cooking zone.
  • Figure 1 shows a preferred embodiment of a continuous two vessel steam/liquid-phase digester arrangement according to the invention
  • Figure 2 shows a preferred top separator to be used in a steam/vapour-phase digester according to the invention
  • Figure 3 shows a preferred top separator to be used in an hydraulic digester according to the invention
  • Figure 4 shows a preferred embodiment of a an hydraulic digester according to the invention
  • Figure 5 shows a diagram presenting the advantages related to the H-factor when using the invention
  • Figure 6 shows which conditions were used in the laboratory for one of the ITC-references and one of the cooks according to the invention (so called modified ITC) .
  • FIG. 1 shows a preferred embodiment of a two vessel steam/liquid-phase digester for producing chemical pulp according to the invention.
  • the main components of the digesting system consist of an impregnation vessel 1 and a steam/liquid-phase digester 6.
  • the impregnation vessel 1 which normally is totally liquid filled, possesses a feeding-in device 2 at the top, which feeding-in device is of a conventional type, i.e. a top separator with screw-feed device which feeds the chips in a downward direction at the same time as transport liquid is drawn off.
  • the impregnation vessel possesses a feeding-out device 3 comprising a bottom scraper.
  • the black liquor is preferably supplied at the top of the impregnation vessel.
  • no draw-off screen is located on the impregnation vessel.
  • the chips are fed from the chip bin 20A, through the steaming vessel 2OB and the chip chute 20C.
  • a feeding device preferably a high-pressure feeder 19, feeds the chips via a conduit
  • a conduit 21 for transporting chips leads from the bottom of the impregnation vessel 1 up to the top 5 of the digester 6 having a steam space, wherein the liquid level being indicated by means of a broken line.
  • a supply line for steam at the top provides for heating of the steam space.
  • Conduit 21 opens out at the bottom of a top separator 7 which feeds by means of a screw in an upwardly moving direction.
  • the screen of the separator is used to draw off the liquid D (which is then returned in line 15) together with which the chips are transported up to the top.
  • an integrated annular ring 23 At the upper edge of the screen (over which edge the chips tumble out) , there is arranged an integrated annular ring 23.
  • the annular ring 23 is connected to a conduit 24 which (preferably via a heat-exchanger 13A) leads to a white-liquor container (not shown) .
  • a screen girdle section 8 is arranged in conjunction with a step-out approximately in the middle of the digester 6. Draw-off from this screen girdle section 8 can be conducted directly via conduit 17 to the impregnation vessel 1. Preferably, however, the black liquor is drawn off via conduit 28 to a first flash cyclone 9.
  • "cold- blow” is carried out, the temperature of the pulp being cooled down at the bottom of the digester with the aid of relatively cold (preferably 70-80 °C) liquid ( wash liquid) which is added by means of the scraping element 22 and/or other liquid-adding devices 25 (appropriately annular pipes) at the bottom, and then subsequently conducted upwards in counter-current.
  • relatively cold (preferably 70-80 °C) liquid ( wash liquid) which is added by means of the scraping element 22 and/or other liquid-adding devices 25 (appropriately annular pipes) at the bottom, and then subsequently conducted upwards in counter-current.
  • This lower circulation consists of a screen girdle sections 12 (in the shown embodiment consisting of three rows) which is arranged at sufficient height above the lower liquid-addition point 22 and/or 25 to permit the attainment of a desired flow from the latter liquid-addition point towards the screen section 12.
  • the draw-off from the said screen girdles 12, is recirculated (for displacing black liquor in counter-current to the draw-off screen 8) into the digester with the aid of a central pipe 14 (or alternately a stand pipe from the bottom of the digester) which opens out approximately on a level with the said screen girdle section 12.
  • a heat exchanger 13 for temperature regulation (raising the temperature of the re-introduced liquid) and a pump are also located in the conduit 11 which connects the screen girdle 12 with the pipe 14.
  • the recirculation loop 11 is also connected via a branch conduit 27 to the white liquor supply so that fresh alkali can be supplied and, in the form of counter-current cooking, further reducing the kappa number.
  • the digester construction described is notable for the lack of a plurality of central pipes arranged from above and hanging downwards, as well as of feed pipes connected to them and of other necessary parts for the circulations.
  • a preferred installation according to the invention functions as follows.
  • the chips are fed in a conventional manner into a chip bin 20A, subsequently steamed 2OB and thereafter into a chute 20C.
  • a high- pressure feeder 19 (which in a known manner is supplied with a minor amount of white liquor ( ⁇ 5% of the total amount) in order to lubricate it) , with the aid of which the chips are fed into conduit 18 together with transport liquid.
  • the slurry of chips and liquid which is fed to the top of the impregnation vessel in this way have a temperature of about 110 - 120 °C on entry to the impregnation vessel (excluding recirculated transport liquor) .
  • the wood moisture In addition to the actual fibres in the wood, the latter also conveys its own moisture (the wood moisture) , which normally constitutes about 50 % of the ⁇
  • the chips which are fed out from the bottom of the top screen 2 then move slowly downwards in a plug flow through the impregnation vessel 1 in a liquid/wood ratio between 2/1-10/1 preferably between 3/1-8/1, more preferred of about 4/1-6/1.
  • Hot black liquor which is drawn off from the first flash 9, is added, via conduit 17, in the top of the impregnation vessel 1.
  • the high temperature of the black liquor (100 - 160 °C) , preferably exceeding 130 °C, more preferred between 130 - 160 °C, ensures rapid heating of the chips.
  • the relatively high pH, exceeding pH 10 of the black liquor neutralises acidic groups in the wood and also any acidic condensate accompanying the chips, thereby, i.a.
  • the black liquor supplied into the impregnation vessel has a high content of rest alkali, (EA as NaOH) , at least 13g/l, preferably about or above 16g/l and more preferred between 13 - 30g/l in the top of the impregnation vessel.
  • This alkali mainly comes from the black liquor due to the high amount of alkali in the con-current zone of the digester.
  • the strength properties of the fibres are positively affected by the impregnation because the high amount of sulphides.
  • the major portion of black liquor is directly (or via one flash) fed to the impregnation vessel 1.
  • a minor amount of the black liquor may be used for transferring the chips from the HP-feeder to the inlet of the impregnation vessel. This minor flow then has to be cooled (not shown) before it is entered into the feeder.
  • the two flows of black liquor are preferably used to regulate the temperature within the impregnation zone, which never must exceed 140 °C.
  • the total supply of black liquor to the impregnation vessel exceeds 80% of the amount drawn off from the draw-off strainers 8, preferably more than 90% and optimally about 100% of the total flow, which normally is about 8 - 12 m 3 /ADT.
  • the chips which have been thoroughly impregnated and partially delignified in the impregnation vessel, are fed to the top of the digester 6 and conveyed into the upwardly-feeding top separator 7.
  • the chips are thus fed upwards through the screen, meanwhile free transport liquid is withdrawn outwardly through the screen and finally the chips fall out over the edge of the screen down through the steam space.
  • the chips pieces are drained with cooking liquor which is supplied by means of the top separator 7.
  • the white liquor is preferably heated by means of a heat exchanger 13A which preferably is supplied with heat steam from flash tank 9.
  • the quantity of white liquor which is added here depends on how much white liquor possibly is added else where, but the total amount corresponds to the quantity of white liquor which is required for achieving desired delignification of the wood.
  • a major part of it is added here, i.e. more than 60%, which also improves the diffusion velocity, since it increases in relation to the concentration difference (chip-surrounding liquid) .
  • the thoroughly impregnated chips extra rapidly assimilate the active cooking chemicals by diffusion, since the concentration of alkali (EA as NaOH) is relatively high, at least 20g/l, preferably between 30g/l and 50g/l and more preferred about 40g/l.
  • the chips then move down in the con-current through the digester 6 at a relatively low cooking temperature, i.e. between 130 - 160 °C, preferably about 140 - 150 °C.
  • the major part of the delignification takes place in the first con-current cooking zone.
  • the retention time in this first cooking zone should be at least 20 minutes, preferably at least 30 minutes and more preferred at least 40 minutes.
  • the liquid-wood ratio should be at lest 2/1 and should be below 7/1, preferably in the range of 3/1 - 5.5/1, more preferred between 3.5/1 and 5/1. (The liquid wood-ratio in the counter-current cooking zone should be about the same as in the con-current cooking zone.)
  • the cooking liquid mingled with released lignins, etc., is drawn off at the draw-off screen 8.
  • liquid finally is also supplied in the lower part of the digester which moves in counter- current. It can be describes as the pipe 14 displacing it from the wood upwards towards the draw-off screen 8. This results, consequently, in the delignification being prolonged in the digester 6.
  • the temperature in this lower zone C is preferably higher than in the con-current zone B, i.e. preferably exceeding 140 °C, preferably about 145 - 165 °C, in order to dissolve remaining lignin.
  • the alkali content in the lowermost part of the counter-current cooking zone should preferably be lower than in the beginning of the concurrent zone, above 5g/l, but below 40g/l. Preferably less than 30g/l and more preferred between 10 - 20g/l.
  • the aim is to have a temperature difference of about 10 °C between the cooking zones.
  • the lower circulation 11, 12, 13, 14 is charged with about 5 - 20%, preferably 10 - 15%, white liquor.
  • the temperature of the liquid which is recirculated via the pipe 14 is regulated with the aid of a heat exchanger 13 so that the desired cooking temperature is obtained at the lowermost part of the counter-current cooking zone.
  • washing liquid having a low temperature, preferably about 70 - 80 °C, is added in a known manner using the scraping element and an outer annular conduit 25 arranged at the bottom. This liquid consequently displaces the boiling hot liquor in the pulp upwards in counter-current and thereby imparts a temperature to the remaining pulp which can be cold-blown, i.e. depressurised and disintegrated without any real loss of strength.
  • FIG 2 there is shown a preferred embodiment of a separator to be used in connection with a steam/vapour phase digester, as described in figure 1.
  • the separator comprises a screen basket (61) in which a screw feeder (62) is positioned.
  • the screw feeder is fixedly attached to a shaft (63) which at its upper end is fixedly attached to a drive unit (64) .
  • the drive unit (64) is attached to a plate (65) which is attached to the digester shell (6) .
  • Circumjacent the screen basket (61) there is arranged a liquid collecting space (67), which is connected to the return pipe circulation (15) .
  • a liquid supply space (23) which is connected to a supply line (24) .
  • annular space (70) which opens up down into the upper part of the digester (6) .
  • the functioning of the top separator is as follows. The thoroughly heated and impregnated chips are transferred by means of the supply line (21) into the bottom portion of the screen basket (61) .
  • the screw feeder (62) moves the chips upwardly at the same time as liquid is separated from the chips, by being withdrawn outwardly through the screen basket (61) and further out of the digester through return line (15) .
  • FIG 3 there is shown a preferred embodiment of a separator to be used together with a hydraulic digester. Only a part of the top of the digester (6) is shown.
  • the slurred fibre material pre- impregnated or not
  • the screw- feeder (31) is attached to a shaft (32) connected to a drive-unit (33) which is attached to a mounting-plate (34) on the top of the digester shell (6) .
  • the drive- shaft (32) is rotated in a direction so as to force the screw to feed in a down-ward direction.
  • a cylindrical screen-basket (35) surrounds the screw-feeder (31) .
  • the screen-basket (35) is arranged within the digester shell (6) so as to form a liquid collecting space (36) between the digester shell and the outer surface of the screen-basket (35) .
  • the liquid collecting space (36) which preferably is annular, communicates with a conduit (17) for withdrawing liquid from the liquid collecting space (36), which in turn is replenished by liquid from the slurry within the screen basket (35) .
  • the major part of the free liquid within the slurry entering the screen basket is withdrawn into the liquid collecting space (36) , but a small portion of free liquid, at least about 0.5 m 3 /ADT should not be withdrawn from the slurry.
  • a liquid supply device (37) Adjacent the outlet end of the screen basket (35) there is arranged a liquid supply device (37), preferably comprising an annular distribution ring which opens up into the chips pile for supply of liquid into the fibre material moving down into the digester (6) .
  • the liquid supply device (37) is replenished by means of line 38 wherein a desired liquid is supplied. If it is a two-vessel hydraulic digester system the liquid supplied through the liquid supply device (37) would be hot cooking liquor having a relatively high amount of effective alkaline, in order to provide for the possibility of establishing a con-current cooking zone (B) having a desired temperature of about 145 - 150 °C, and a desired content of effective alkaline, e.g. about 45g/l.
  • the invention is also applicable in connection with one vessel digesters of both kinds, as will be exemplified below.
  • a major advantage with both kinds of the shown separation devices is that they provide for establishing a distinguished change of zones (they enable almost a total exchange of free liquid at this point) , which means that for a two vessel system the desired conditions in the beginning of the con-current zone (B) can easily be established.
  • Figure 4 it is shown a preferred embodiment for applying the invention to a one-vessel hydraulic digester.
  • the same kind of basic equipment before and in connection with the HP-feeder as shown in fig. 1 is used, which therefore is not described in detail.
  • the basically same kind of top separator arrangement as described in figure 3 is mounted at the top of the digester 6.
  • withdrawal strainers (8) are arranged.
  • the lowermost part of the digester is in principle similar to the one shown in figure 1, with a supply line (25) for wash liquid and a blow line (26) for the digested pulp.
  • a strainer arrangement (12) for withdrawing liquid, which is heated and to which some white liquor, preferably about 10% of the total amount, is added before it is recirculated by means of a stand pipe (39) , which opens up at about the same level as the lowermost strainer girdle (12) .
  • a stand pipe (39) which opens up at about the same level as the lowermost strainer girdle (12) .
  • the upper strainer (40) is arranged for withdrawing liquid which has passed the impregnation zone (A) . Some of the withdrawn liquid D is taken out via line 46 to a flash tank 47.
  • the other part of the withdrawn liquid is recirculated for re-introducing liquid withdrawn by means of a central pipe (42A) which opens up at a level adjacent the strainer (40) .
  • a central pipe (42A) which opens up at a level adjacent the strainer (40) .
  • white liquor can be added thereto by means of a supply-line (43A) and thereafter the liquid is heated to the desired temperature by means of a heat exchanger (44A) .
  • the digesting process within a digester shown in Figure 4 is as follows.
  • the slurry of chips and transport liquid is transferred, e.g. by means of high pressure feeder, within the feeding line (21) to the top of the digester where it is introduced into the top of the screen basket (35) of the separator, wherein the major part of transport liquid is separated from the chips.
  • impregnation liquor E is supplied by means of line 38.
  • the impregnation liquor is hot black liquor which is taken from the withdrawal screen (8) via a flash tank 9 by means of the supply conduit (38) . If all the desired amount cannot be withdrawn via line 46 to flash tank 47 there is provided for the possibility to also withdraw from the outlet of the first flash tank 9 via line 45.
  • a minor amount of the black liquor withdrawn from flash tank 9 may be used for transferring the chips from the HP-feeder to the inlet of the digester 6. This minor flow then has to be cooled in a cooler 80 before it is entered into the feeder.
  • the two flows of black liquor are preferably used to regulate the temperature within the impregnation zone, which never must exceed 140 °C.
  • the amount of effective alkaline in the supplied black liquor E is relatively high, at least 13g/l, preferably about 20g/l, which provides for the impregnation zone (A) to be established without any substantial additional supply of white liquor at this position.
  • the chips is then impregnated and heated when moving down towards the upper screen (40), where spent liquor (D) is withdrawn and transferred by means of a conduit (46) to a flash tank (47) .
  • the chips are heated and alkali is introduced by means of the above described cooking circulations (40,42A,43A,44A;41,42B,43B,44B) in order to obtain desired cooking conditions.
  • the temperature at the beginning of the con-current zone is about 145 - 160 °C for soft wood and about 140 - 155 °C for hard wood and an alkaline content of about 30 - 50g/l. Thanks to the exothermic reaction of the chemicals the temperature is slightly further increased when the fibre material is moving downwardly in the con-current cooking zone (B) .
  • Liquid having a relatively high content of effective alkaline is withdrawn at the strainers (8) positioned adjacent the middle.
  • the alkaline content of this withdrawn spent liquor (E) would normally exceed 15g/l.
  • pulp produced in this manner will have higher quality and better bleachability then pulp produced with known methods.
  • lab-scale tests we have found that about 10 kg of active chlorine can be saved for reaching full brightness (about 90% ISO) , compared to a conventionally cooked pulp.
  • FIG 5 there is shown a diagram comparing the H-factor for pulp produced according to conventional ITC ⁇ -cooking and the invention.
  • the H- factor is a function of time and temperature in relation to the delignification process (degree of delignification) during cooking.
  • the H-factor is used to control the delignification process of a digester, i.e. maintaining a certain H-factor principally leads to the same Kappa number of the produced pulp (remaining lignin content of the fibre material) independent of temperature variations during the cooking.
  • the H-factor for pulp produced according to the invention is extremely much lower (about 40 - 50% lower) compared to pulp produced according to ITCTM.
  • the lower H-factor demand is achieved by a high alkali concentration and a low cooking temperature in the concurrent cooking zone, which is shown in fig. 6 which presents one reference ITC-cook (ITC 1770) and one cook according to the invention (modified ITC* 1763) .
  • ITC 1770 one reference ITC-cook
  • ITC* 1763 modified ITC* 1763
  • the temperature in the counter-current cooking zone is higher than in the con-current zone but still lower than the temperature in the counter-current zone in the ITC-reference.
  • new on-line measuring systems for example using NIR-spectroscopy
  • new on-line measuring systems provide for the possibility of exactly measuring specific contents of the fibre material and the liquids entering the digesting system, which will make it feasible to more precisely determine and control the supply/addition of specific fluids/chemicals and also their withdrawal in order to establish optimised conditions.
  • Different kind of additives can be very beneficial to use, especially for example poly-sulphide which has a better effect in a low temperature environment than in high temperatures.
  • AQ Anthraquinone
  • a centrally arranged inlet as described in WO-having a spreading device can be contrived, which device, in a known way, provides a mushroom-like film of liquid, as can a centrally arranged showering element or an annular pipe with slots, etc.
  • the invention can be used in digesters not having a distinguished counter-current cooking zone. For example in some retrofits of digesters it may be advantageous to position the withdrawal strainers close to the bottom. Also in connection with heavily overloaded digesters that can not be provided with a sufficient supply of wash liquor enabling a sufficient up-flow for counter-current cooking, the invention can be used by supplying wash liquid, as customary, in the bottom and preferably also by means of central pipe displacing liquid radially to a screen section.

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  • Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Paper (AREA)
  • General Preparation And Processing Of Foods (AREA)

Abstract

L'invention concerne un procédé de cuisson continue, nouveau et amélioré, de la matière fibreuse. Selon ce procédé, les températures et les niveaux alcalins sont régulés pour être maintenus dans des limites spécifiques dans différentes zones du processus de lessivage afin d'optimiser la consommation chimique et l'économie de chaleur tout en assurant d'excellentes propriétés à la pâte. La matière fibreuse est chauffée et imprégnée à l'aide de liqueur noire d'une température inférieure à 140 °C puis passée dans le sens du courant dans une zone d'imprégnation (A). La matière fibreuse chauffée et imprégnée est cédée à une zone de cuisson (B) située dans le sens du courant dans la partie supérieure d'un lessiveur (6). Au moins 60 % de la quantité de liqueur (F) exigée pour la réaction de cuisson sont amenés au niveau de l'extrémité amont de la zone de cuisson (B) située dans le sens du courant afin d'obtenir un niveau d'alcali effectif excédant 35 g/l. La température de cuisson dans la zone (B) située dans le sens du courant est inférieure à 160 °C. La liqueur résiduaire (E), contenant une quantité d'alcali effectif d'au moins 13 g/l, est retirée de l'enveloppe de tamisage (8) et une quantité importante de cette liqueur est envoyée à la zone d'imprégnation.
PCT/SE1997/000192 1997-02-09 1997-02-09 Procede continu de production de pate avec impregnation de liqueur residuaire WO1998035090A1 (fr)

Priority Applications (8)

Application Number Priority Date Filing Date Title
PCT/SE1997/000192 WO1998035090A1 (fr) 1997-02-09 1997-02-09 Procede continu de production de pate avec impregnation de liqueur residuaire
AU21836/97A AU2183697A (en) 1997-02-09 1997-02-09 Continuous method for producing pulp with spent liquor impregnation
ZA98936A ZA98936B (en) 1997-02-09 1998-02-05 Method and device for the continuous cooking of pulp
DE69800767T DE69800767T2 (de) 1997-02-09 1998-02-09 Verfahren und vorrichtung zur kontinuierlichen zellstoffkochung
ES98903344T ES2159175T3 (es) 1997-02-09 1998-02-09 Metodo y dispositivo para la coccion continua de pasta papelera.
CA002279283A CA2279283C (fr) 1997-02-09 1998-02-09 Procede et dispositif de cuisson continue de pate
AT98903344T ATE201064T1 (de) 1997-02-09 1998-02-09 Verfahren und vorrichtung zur kontinuierlichen zellstoffkochung
EP98903344A EP0909353B1 (fr) 1997-02-09 1998-02-09 Procede et dispositif de cuisson continue de pate

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/SE1997/000192 WO1998035090A1 (fr) 1997-02-09 1997-02-09 Procede continu de production de pate avec impregnation de liqueur residuaire

Publications (1)

Publication Number Publication Date
WO1998035090A1 true WO1998035090A1 (fr) 1998-08-13

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Application Number Title Priority Date Filing Date
PCT/SE1997/000192 WO1998035090A1 (fr) 1997-02-09 1997-02-09 Procede continu de production de pate avec impregnation de liqueur residuaire

Country Status (8)

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EP (1) EP0909353B1 (fr)
AT (1) ATE201064T1 (fr)
AU (1) AU2183697A (fr)
CA (1) CA2279283C (fr)
DE (1) DE69800767T2 (fr)
ES (1) ES2159175T3 (fr)
WO (1) WO1998035090A1 (fr)
ZA (1) ZA98936B (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1561856A1 (fr) * 2004-02-09 2005-08-10 Kvaerner Pulping Ab Procédé continu pour la cuisson de pâte cellulose
CN1318688C (zh) * 2003-08-26 2007-05-30 山东泉林纸业有限责任公司 一种烧碱法制浆所用原料的浸渍预处理工艺
CN103215834A (zh) * 2013-04-17 2013-07-24 岳阳林纸股份有限公司 一种节能环保型连续蒸煮工艺

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SE533670C2 (sv) * 2009-04-01 2010-11-30 Metso Fiber Karlstad Ab System och metod för reglering av en kontinuerlig ångfaskokare
RU2670855C1 (ru) * 2017-06-26 2018-10-25 Федеральное государственное бюджетное образовательное учреждение высшего образования "Санкт-Петербургский государственный университет промышленных технологий и дизайна" Способ варки технологической щепы в производстве целлюлозы

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2639987A (en) * 1947-07-09 1953-05-26 Ass Pulp & Paper Mills Two-stage pulping process
US5089086A (en) * 1989-04-27 1992-02-18 Jaakko Poyry Oy Process for continuous cooking of cellulose
WO1995018261A1 (fr) * 1993-12-29 1995-07-06 Kvaerner Pulping Technologies Ab Procede et dispositif pour la cuisson continue de la pate a papier
WO1996007786A1 (fr) * 1994-09-02 1996-03-14 Kamyr, Inc. Procede de cuisson continue de pate kraft avec pretraitement de la liqueur noire
US5635026A (en) * 1995-11-13 1997-06-03 Ahlstrom Machinery Inc. Cooking cellulose material with high alkali concentrations and/or high pH

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2639987A (en) * 1947-07-09 1953-05-26 Ass Pulp & Paper Mills Two-stage pulping process
US5089086A (en) * 1989-04-27 1992-02-18 Jaakko Poyry Oy Process for continuous cooking of cellulose
WO1995018261A1 (fr) * 1993-12-29 1995-07-06 Kvaerner Pulping Technologies Ab Procede et dispositif pour la cuisson continue de la pate a papier
WO1996007786A1 (fr) * 1994-09-02 1996-03-14 Kamyr, Inc. Procede de cuisson continue de pate kraft avec pretraitement de la liqueur noire
US5635026A (en) * 1995-11-13 1997-06-03 Ahlstrom Machinery Inc. Cooking cellulose material with high alkali concentrations and/or high pH

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1318688C (zh) * 2003-08-26 2007-05-30 山东泉林纸业有限责任公司 一种烧碱法制浆所用原料的浸渍预处理工艺
EP1561856A1 (fr) * 2004-02-09 2005-08-10 Kvaerner Pulping Ab Procédé continu pour la cuisson de pâte cellulose
JP2005220510A (ja) * 2004-02-09 2005-08-18 Kvaerner Pulping Ab 連続蒸煮方法
CN103215834A (zh) * 2013-04-17 2013-07-24 岳阳林纸股份有限公司 一种节能环保型连续蒸煮工艺
CN103215834B (zh) * 2013-04-17 2015-01-07 岳阳林纸股份有限公司 一种节能环保型连续蒸煮工艺

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CA2279283C (fr) 2008-08-26
CA2279283A1 (fr) 1998-08-13
EP0909353B1 (fr) 2001-05-09
ATE201064T1 (de) 2001-05-15
ZA98936B (en) 1998-09-23
DE69800767D1 (de) 2001-06-13
ES2159175T3 (es) 2001-09-16
AU2183697A (en) 1998-08-26
EP0909353A1 (fr) 1999-04-21
DE69800767T2 (de) 2001-11-29

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