EP1932967B1 - Procédé de production de pâte de cellulose dans un digesteur continu d'une manière à efficacité énergétique - Google Patents

Procédé de production de pâte de cellulose dans un digesteur continu d'une manière à efficacité énergétique Download PDF

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Publication number
EP1932967B1
EP1932967B1 EP07446011A EP07446011A EP1932967B1 EP 1932967 B1 EP1932967 B1 EP 1932967B1 EP 07446011 A EP07446011 A EP 07446011A EP 07446011 A EP07446011 A EP 07446011A EP 1932967 B1 EP1932967 B1 EP 1932967B1
Authority
EP
European Patent Office
Prior art keywords
liquid
top separator
withdrawal
chips
added
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.)
Not-in-force
Application number
EP07446011A
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German (de)
English (en)
Other versions
EP1932967A2 (fr
EP1932967A3 (fr
Inventor
Vidar Snekkenes
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.)
Metso Fiber Karlstad AB
Original Assignee
Metso Fiber Karlstad 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
Application filed by Metso Fiber Karlstad AB filed Critical Metso Fiber Karlstad AB
Publication of EP1932967A2 publication Critical patent/EP1932967A2/fr
Publication of EP1932967A3 publication Critical patent/EP1932967A3/fr
Application granted granted Critical
Publication of EP1932967B1 publication Critical patent/EP1932967B1/fr
Not-in-force legal-status Critical Current
Anticipated expiration legal-status Critical

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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
    • 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
    • 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
    • D21C1/00—Pretreatment of the finely-divided materials before digesting
    • 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
    • D21C7/00—Digesters
    • 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
    • D21C7/00—Digesters
    • D21C7/06—Feeding devices
    • 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
    • D21C7/00—Digesters
    • D21C7/14—Means for circulating the lye

Definitions

  • the present invention concerns a method for producing cellulose pulp in a continuous digester in an energy-efficient manner, as described in the preamble of patent claim 1.
  • chips are impregnated with impregnation liquid in an impregnation vessel.
  • the impregnated chips are subsequently cooked in a digester, whereby the impregnation vessel and the digester are coupled to each other by means of a transfer circulation.
  • the transfer circulation consists not only of a transfer line that feeds the chips from the outlet end of the impregnation vessel to the top of the digester for the separation of free liquid in a top separator, but also of a return line that feeds separated liquid from the top of the digester to the outlet end of the impregnation vessel in order to be used as transfer liquid for the impregnated chips.
  • SE 518 957 reveals an invention in which one of the aims is to reduce the requirement for the supply of steam to the top of the digester.
  • a fraction of the black liquor (14) withdrawn from the digester (2) is added at the beginning of the transfer flow at what is essentially the withdrawal temperature Tav, which the liquor has retained, with the aim of raising the temperature of the chips mixture in the transfer circulation.
  • a fraction of the withdrawn liquid from the top separator of the digester is returned to the impregnation vessel such that it there can act as impregnation liquid.
  • a heating of the chips is obtained with this invention, which ensures that the consumption of steam at the top of the digester can be reduced, and the steam can therefore be used for another purpose.
  • One limitation of this method is that the temperature of the black liquor that is added should not be too high, since this would then introduce the risk of steam implosion.
  • SE 511 850 reveals a way of simplifying the digestion plant with respect to the withdrawal of liquid from the digestion system before the initial phase of the cooking, such that the design of the impregnation vessel can be simplified.
  • cooking liquid is added to the top separator after the separation of liquid in order to be mixed with the fibre material that has a low liquid content under the influence of a screw in the top separator that feeds material in an upward direction.
  • the top separator of the invention has a rotating screw 29 that is arranged vertically.
  • the top separator has also a lower sieve section 31 that is surrounded by a wall 34 in order to form an intermediate liquid chamber 35 for the collection of liquid, which liquid is pressed out through the sieve section 31 under the influence of the screw.
  • a ring-shaped supply pipe 36 is arranged around the screw 29. Holes 37 are arranged in the ring-shaped supply pipe for the supply of white liquor and possibly also other liquid to the chips.
  • the return line 26 is connected to the liquid chamber 35. Steam at intermediate pressure is added through line 39 to the upper steam space of the digester at the top of the digester 4 in connection with the top separator 28 in order to heat the chips that are fed in by the screw 29 and that fall down over the edge 33. There is no connection between the withdrawal space 35 and the ring-shaped supply line.
  • a first aim of the invention is to reduce the requirement of heating with steam at the top of the digester.
  • a second aim of the invention is to be able to heat the chips before the cooking process using a temperature of the hot liquid that is higher than that which is possible when the heating is carried out at the transfer flow.
  • a third aim of the invention is to avoid clogging at the top separator in a steam phase digester.
  • the concept of the invention is to achieve a method for producing cellulose pulp in a continuous digester system that is efficient in its use of energy.
  • chips are fed continuously in a transfer liquid to a top separator arranged at the top of a digester.
  • the invention is characterised in that a hot additive liquid is added to the withdrawal space of the top separator.
  • the temperature of the hot additive liquid that is added to the withdrawal space is greater than the temperature of the withdrawn liquid in the free liquid in the return line.
  • Figures 1 and 4 show a first preferred embodiment of a method for producing cellulose pulp in a continuous digester system in an energy-efficient manner.
  • Cellulose chips are fed continuously to an impregnation vessel 10 in order to be impregnated in an impregnation liquid in the impregnation vessel 10 .
  • the impregnated chips are fed with a transfer liquid in a transfer line 11 to a top separator 20 arranged at the top of a digester 30 , for the separation of free liquid from the cellulose chips, where the digester 30 is a steam phase digester.
  • the transfer line 11 is connected to the bottom of the top separator 20 and the chips are thus fed upwards through the top separator.
  • the top separator 20 has a rotating upwardly feeding screw 22 that is arranged vertically.
  • the top separator 20 has also a screening surface 23 , which is surrounded by an impenetrable wall 24 for the formation of an intermediate withdrawal space 21 , for the collection of free liquid that is pressed out through the screening surface 23 under the influence of the screw 22 .
  • the withdrawal space 21 extends over at least 50%, preferably at least 75%, of the threaded height of the screw 22 .
  • At least a fraction of the free liquid that has separated is led in a return line 32 from the withdrawal space of the top separator to the outlet end of the impregnation vessel in order to be used as transfer liquid.
  • the return line 22 is connected to the lower part of the withdrawal space 21 and the temperature of the withdrawn liquid in the return line 32 is T ut .
  • a means 35 of creating pressure, preferably in the form of a pump, is arranged in the return line 22 .
  • At least one pressurised withdrawal of black liquor is carried out in the digester 30 essentially at the cooking temperature of at least 135 °C. A fraction of this pressurised withdrawal of black liquor can be led to the bottom of the impregnation vessel along a black liquor line 34 .
  • An additive liquid with a temperature T in is added through an addition line 33 connected to the upper part of the withdrawal space, where this additive liquid consists of at least part of the black liquor withdrawal.
  • the additive liquid is mixed with the chips under the influence of the screw 22 that feeds material upwards.
  • the relationship between the temperature of the black liquor withdrawal that is added to the withdrawal space and the temperature of the free liquid withdrawn from the withdrawal space is such that T in >T ut .
  • the additive liquid that is led in the addition line 33 is added to the withdrawal space 21 downstream of the return line 32 , when seen in the direction of motion of the chips.
  • the liquid/wood ratio in the transfer line 11 is ⁇ 7, the remaining liquid in the chips after they have passed the top separator lies at a liquid/wood ratio of ⁇ 3 and the amount of additive liquid in the addition line 33 that is added to the withdrawal space 21 lies at a liquid/wood ratio ⁇ 1.
  • the level of COD (Chemical Oxygen Demand) in the additive liquid that is added at the top separator 20 may be either lower or higher than that of the free liquid that is withdrawn at the top separator 20 in the return line 32 .
  • FIG. 2 shows a second preferred embodiment according to the method according to the invention.
  • the pressurised black liquor withdrawal as additive liquid
  • at least a part of the free liquid that is withdrawn at the withdrawal space 21 is here used.
  • This withdrawal is heated in a heat exchanger 40 , before it is led in the addition line 33 to the withdrawal space 21 as additive liquid, where the temperature of the additive liquid T in is higher than T ut .
  • the heating agent with which the additive liquid exchanges liquid in the heat exchanger 40 may be constituted of the pressurised black liquor withdrawal.
  • Other types of heating are possible instead of that of exchanging heat with liquids, such as, for example, heating by steam.
  • This embodiment otherwise is identical with the first preferred embodiment.
  • Figure 3 shows a third preferred embodiment according to the method according to the invention.
  • the additive liquid in this embodiment is constituted by two liquids: partly the pressurised black liquor withdrawal according to the first preferred embodiment, and partly the heated free liquid that is withdrawn at the withdrawal space according to the second preferred embodiment.
  • This embodiment otherwise is identical with the first preferred embodiment.
  • the chips be impregnated in an impregnation vessel before they are fed in the transfer liquid up to the top separator.
  • the chips instead can be subject to steam pre-treatment in a steam pre-treatment vessel, or they may be treated by some other method.
  • the additive liquid can, as in the third preferred embodiment, be constituted by two liquids, and it can also be constituted by more than two liquids.
  • the only point that is important for the innovative concept of the invention is that the temperature of the additive liquid is higher than the temperature of the withdrawal that is drawn in the return line.

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  • Paper (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)

Claims (14)

  1. Procédé de production d'une pâte de cellulose dans un système de digestion continue d'une manière énergétiquement efficace, où le procédé comprend les étapes suivantes :
    a) des copeaux de cellulose sont alimentés en continu avec un liquide de transfert dans un circuit de transfert (11) vers un séparateur supérieur (20) disposé au sommet d'un digesteur (30), pour la séparation du liquide libre des copeaux de cellulose, le séparateur supérieur comportant un espace libre (21) dans lequel le liquide libre s'accumule ;
    b) au moins une partie du liquide libre qui est séparé, à une température Tut, est dirigée dans une conduite de renvoi (32) à partir de l'espace libre du séparateur supérieur vers une position à utiliser comme liquide de transfert ;
    c) au moins un retrait sous pression de la liqueur noire est réalisé dans le digesteur (30) essentiellement à la température de cuisson d'au moins 135 °C ; caractérisé en ce qu'un additif liquide à une température Tin est ajouté à l'espace libre (21) du séparateur supérieur, où Tin > Tut.
  2. Procédé selon la revendication 1, caractérisé en ce que les copeaux ont été imprégnés d'un liquide d'imprégnation dans un imprégnateur (10), avant que les copeaux de cellulose soient alimentés dans le liquide de transfert vers le séparateur supérieur (20).
  3. Procédé selon la revendication 2, caractérisé en ce que le liquide libre qui s'est séparé est dirigé dans une conduite de renvoi (32) à partir de l'espace libre du séparateur supérieur vers la sortie de l'imprégnateur afin d'être utilisé comme liquide de transfert.
  4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que l'additif liquide est ajouté en aval de l'espace libre de la conduite de renvoi, observé dans la direction du mouvement des copeaux.
  5. Procédé selon l'une quelconque des revendications 1 à 4, caractérisé en ce que l'additif liquide est mélangé à des copeaux sous l'influence d'une vis qui alimente le matériau vers le haut au niveau du séparateur supérieur, et où le digesteur est un digesteur en phase vapeur.
  6. Procédé selon l'une quelconque des revendications 1 à 5, caractérisé en ce que l'additif liquide est constitué d'un liquide qui a été chauffé.
  7. Procédé selon la revendication 6, caractérisé en ce que le liquide qui a été chauffé est constitué au moins en partie du liquide retiré du séparateur supérieur.
  8. Procédé selon l'une quelconque des revendications 1 à 5, caractérisé en ce que l'additif liquide est constitué d'au moins une partie du retrait de la liqueur noire sous pression.
  9. Procédé selon l'une quelconque des revendications 1 à 5, caractérisé en ce que l'additif liquide est constitué d'au moins une partie du retrait de liqueur noire pressurisé et d'au moins une partie du retrait du séparateur supérieur qui a été chauffé.
  10. Procédé selon l'une quelconque des revendications 1 à 9, caractérisé en ce que le rapport liquide/bois dans la conduite de transfert est ≥ 7, et
    en ce que le liquide résiduel dans les copeaux après le séparateur supérieur se situe à un rapport liquide/bois ≥ 3, où la quantité d'additif liquide qui est ajoutée se situe à un rapport liquide/bois ≥ 1.
  11. Procédé selon l'une quelconque des revendications 1 à 10, caractérisé en ce que l'espace libre (21) s'étend sur au moins 50 %, de préférence au moins 75 %, de la hauteur filetée de la vis.
  12. Procédé selon l'une quelconque des revendications 1 à 11, caractérisé en ce que l'additif liquide qui est ajouté au séparateur supérieur montre un niveau de COD inférieur à celui du liquide qui est retiré du séparateur supérieur.
  13. Procédé selon l'une quelconque des revendications 1 à 11, caractérisé en ce que l'additif liquide qui est ajouté au séparateur supérieur possède un niveau de COD supérieur à celui du liquide qui est retiré du séparateur supérieur.
  14. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que l'additif liquide est ajouté à la partie supérieure de l'espace libre par une conduite d'ajout (33), et en ce que la conduite de renvoi (32) est reliée à la partie inférieure de l'espace libre (21).
EP07446011A 2006-12-13 2007-12-07 Procédé de production de pâte de cellulose dans un digesteur continu d'une manière à efficacité énergétique Not-in-force EP1932967B1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
SE0602675A SE529573C2 (sv) 2006-12-13 2006-12-13 Metod för att energieffektivt producera cellulosamassa i ett kontinuerligt kokeri

Publications (3)

Publication Number Publication Date
EP1932967A2 EP1932967A2 (fr) 2008-06-18
EP1932967A3 EP1932967A3 (fr) 2009-07-15
EP1932967B1 true EP1932967B1 (fr) 2010-03-10

Family

ID=38476375

Family Applications (1)

Application Number Title Priority Date Filing Date
EP07446011A Not-in-force EP1932967B1 (fr) 2006-12-13 2007-12-07 Procédé de production de pâte de cellulose dans un digesteur continu d'une manière à efficacité énergétique

Country Status (7)

Country Link
US (1) US20080210392A1 (fr)
EP (1) EP1932967B1 (fr)
JP (1) JP5140405B2 (fr)
AT (1) ATE460533T1 (fr)
BR (1) BRPI0704676A (fr)
DE (1) DE602007005206D1 (fr)
SE (1) SE529573C2 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SE526704C2 (sv) * 2003-12-30 2005-10-25 Kvaerner Pulping Tech Matning av cellulosaflis från en lågtrycksdel till en högtrycksdel med en slussmatare
US9644317B2 (en) * 2014-11-26 2017-05-09 International Paper Company Continuous digester and feeding system

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ATE125010T1 (de) * 1990-09-20 1995-07-15 Kvaerner Pulping Tech Tränkung mit schwarzlauge vor der zufuhr der weisslauge.
US5213662A (en) * 1991-08-14 1993-05-25 Kamyr, Inc. Treatment of chips with high temperature black liquor to reduce black liquor viscosity
SE469078B (sv) * 1991-08-23 1993-05-10 Kamyr Ab Saett vid kontinuerlig kokning av cellulosahaltigt fibermaterial
US5413677A (en) * 1993-04-05 1995-05-09 Kamyr, Inc. Method for producing chemical pulp from hardwood chips
US5824187A (en) * 1993-12-29 1998-10-20 Kvaerner Pulping Ab Method for the continuous cooking of pulp
SE511850C2 (sv) * 1997-02-10 1999-12-06 Kvaerner Pulping Tech Sätt och anläggning för kontinuerlig kokning av fibermaterial
CA2277931C (fr) * 1997-02-10 2006-11-07 Kvaerner Pulping Aktiebolag Procede et dispositif de cuisson continue de pate chimique
US6203662B1 (en) * 1997-08-07 2001-03-20 Kvaerner Pulping Ab Method for the continuous cooking of pulp in a digester system having a top separator
SE522877C2 (sv) * 1998-11-17 2004-03-16 Andritz Inc Förfarande för drift av en kontinuerlig cellulosamassakokare och en kokare
SE518957C2 (sv) 2002-01-24 2002-12-10 Kvaerner Pulping Tech Förfarande för att öka värmeekonomin i kokarsystemet vid kontinuerlig kokning
JP2005336668A (ja) * 2004-05-28 2005-12-08 Oji Paper Co Ltd リグノセルロース物質の蒸解方法
SE0401870D0 (sv) * 2004-07-15 2004-07-15 Kvaerner Pulping Tech Förfarande för impregnering av flis

Also Published As

Publication number Publication date
JP2008174892A (ja) 2008-07-31
ATE460533T1 (de) 2010-03-15
JP5140405B2 (ja) 2013-02-06
SE0602675L (sv) 2007-09-18
EP1932967A2 (fr) 2008-06-18
DE602007005206D1 (de) 2010-04-22
EP1932967A3 (fr) 2009-07-15
SE529573C2 (sv) 2007-09-18
US20080210392A1 (en) 2008-09-04
BRPI0704676A (pt) 2008-07-29

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