EP2427598A1 - Procédé de lixiviation améliorée de cendres de filtre électrostatique en provenance d'une chaudière de récupération - Google Patents

Procédé de lixiviation améliorée de cendres de filtre électrostatique en provenance d'une chaudière de récupération

Info

Publication number
EP2427598A1
EP2427598A1 EP09846901A EP09846901A EP2427598A1 EP 2427598 A1 EP2427598 A1 EP 2427598A1 EP 09846901 A EP09846901 A EP 09846901A EP 09846901 A EP09846901 A EP 09846901A EP 2427598 A1 EP2427598 A1 EP 2427598A1
Authority
EP
European Patent Office
Prior art keywords
centrifugal separation
leaching
electrostatic precipitator
separation stage
stage
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.)
Granted
Application number
EP09846901A
Other languages
German (de)
English (en)
Other versions
EP2427598B1 (fr
EP2427598A4 (fr
Inventor
Martin Wimby
Joana Nunes
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.)
Valmet AB
Original Assignee
Metso Power 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 Power AB filed Critical Metso Power AB
Publication of EP2427598A1 publication Critical patent/EP2427598A1/fr
Publication of EP2427598A4 publication Critical patent/EP2427598A4/fr
Application granted granted Critical
Publication of EP2427598B1 publication Critical patent/EP2427598B1/fr
Active legal-status Critical Current
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Links

Classifications

    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
    • D21H13/00—Pulp or paper, comprising synthetic cellulose or non-cellulose fibres or web-forming material
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/06—Treatment of pulp gases; Recovery of the heat content of the gases; Treatment of gases arising from various sources in pulp and paper mills; Regeneration of gaseous SO2, e.g. arising from liquors containing sulfur compounds

Definitions

  • the invention relates to a process for leaching electrostatic precipitator ash from a recovery boiler in accordance with the preamble of Patent Claim 1 .
  • Chlorides are also supplied to the pulp process by way of make-up chemicals and water.
  • the wood also has a content of chloride, even if this content is normally low.
  • Potassium is another non-process element which is principally supplied by way of the wood. Even low contents of the non-process elements such as potassium and chlorides in the flows entering the pulp process contribute to high contents in the pulp process since the process is becoming increasingly closed.
  • Potassium and chlorides contribute to major corrosion problems throughout the pulp mill, and especially to clogging of the recovery boiler and to corrosion of heating surfaces.
  • electrostatic precipitator ash which is separated off from the flue gases from the recovery boiler principally contains Na 2 SO 4 , it also contains, due to the process being closed, the highest concentrations of potassium and chlorides within the pulp mill.
  • One way of decreasing the content of potassium and chloride in the liquor stock in the pulp mill is to separate off part of the electrostatic precipitator ash from the chemical cycle in the mill.
  • the separation can take place by the ash being dumped or by the ash being dissolved in water and then conducted to the water purification in the mill. These types of separation result in the heavy metals which are present in the electrostatic precipitator ash polluting the effluent.
  • SE, C, 504374 discloses a process in which the electrostatic precipitator ash is treated in a pressurized filter, in which process filtration and washing of the filter cake, and any possible leaching, take place in one and the same vessel. This process affords a good result as long as the filter can be kept free from clogging. Methods for cleaning the filter, with the cleaning taking place either during operation or in association with occasional interruptions in the filtration process, are required.
  • US, A, 3833462 discloses another process in which leaching takes place at pH 3-6 and 40- 80 9 C, followed by filtration in a filter.
  • SE, A, 9504281 discloses another method which includes cooling.
  • the leaching is to take place at a pH of less than 10 and at a temperature greater than 20 9 C, typically at 30 °C, after which the total quantity of slurried material undergoes cooling down to a temperature of less than 20 9 C.
  • This process involves a need for cooling, with an attendant consumption of energy.
  • SE, A, 9603972 also discloses another method for leaching the electrostatic precipitator ash in which the latter firstly undergoes a leaching at least 32 °C, preferably in the vicinity of the boiling point of the aqueous solution, and in which a first substance which has crystallized out is returned, after separation, to the black liquor.
  • the leachate which is obtained from the process then also undergoes cooling down to approximately 10-15 9 C, after which a second substance which has crystallized out is likewise returned to the black liquor. While this system affords good leaching, it demands a high requirement of energy for the cooling even if the cooling is only required for the relatively small quantities constituted by the leachate.
  • SE, C, 517587 discloses another method patented by Metso Power AB which includes gentle leaching of the electrostatic precipitator ash, followed by a centrifugal stage. In this process the order of separation of chlorides and potassium has been reaching as high level as over 80-85% when maximizing the recovery efficiency of sodium sulphate. The losses are still high, amounting to losses in the order of 25-30% for sodium sulphate.
  • the object of the invention is to obtain an improved process for recovering the useful chemicals, principally Na 2 SO 4 , in the electrostatic precipitator ash, which process does not suffer from the disadvantages of the prior art. While the improvement is first and foremost aimed at an increased recovery of useful chemicals in the pulping process, it is also aimed at an improved degree of recovery of these useful chemicals without these chemicals being accompanied by a high proportion of chlorides, in particular, but also potassium.
  • This objective is met by a process wherein the ashes are leached in a first leaching tank and thereafter sent to centrifugal separation comprising at least two centrifugal separation stages in series, and where at least a part of the first liquid fraction from the first centrifugal separation stage containing chlorides and potassium is bled out from the process.
  • the first dry matter substance obtained from the first centrifugal separation stage is further led to a second leaching tank where preferably similar conditions as in the first leaching tank is established as of pH and dry substance level.
  • the total dwell time in this second leaching tank is not as important as of further crystallization of sodium sulphate, as most
  • a dwell time in the second leaching tank could preferably be in the order of at least 40-80% of the dwell time in the first leaching tank, as further crystallization of sodium sulphate could take place at the larger particles of sodium sulphate already formed.
  • the reslurried and leached first dry matter substance from the first centrifugal separation stage is thereafter fed to a second centrifugal separation stage from which a second liquid fraction is obtained that is led back to at least one preceding leaching tank, and a second dry matter substance which thereafter is mixed into black liquor before the black liquor is being sent to the recovery process.
  • the difference between a one-stage leaching process and the two-stage leaching process according to the invention is the solubility equilibrium between the first and second leaching tanks.
  • leaching out chlorides and potassium after the first leaching step is crystallization of sodium sulphate favored in the second leach tank, reaching a higher sodium sulphate content of the final dry matter content, as well as high concentrations of chlorides and potassium in the first liquid phase bled out after first leaching stage.
  • Another object is to adapt and optimize the stages for the specific process function of the specific stage, such that the first centrifugal separation stage takes place in a high rotational speed centrifuge optimized for obtaining a clean first liquid fraction and a first dry matter substance, and that the second centrifugal separation stage takes place in a low rotational speed centrifuge optimized for obtaining a second dry matter substance at o dry matter concentration being at least 15% higher than that of the first dry matter substance.
  • the first centrifugal separation stage preferably takes place at a rotational speed above 3500 rpm, and the second centrifugal separation stage takes place at a rotational speed below 3500 rpm. while the difference in rotational speed between first and second centrifugal separation stages is at least 2000 rpm.
  • the more aggressive separation in the first stage could thus obtain a cleaner filtrate, while not optimizing the dry matter concentration, as this dry matter concentration is subject to a following leaching stage and anyway needs dilution for that stage.
  • the first centrifugal separation stage is taking place in a nozzle bowl separator centrifuge, which has proven its capability of obtaining clean filtrates from these kinds of slurries, but not necessarily as high concentration in the separated dry matter phase.
  • the nozzle bowl separator is also less expensive than a decanter centrifuge for the same capacity, which latter decanter centrifuge is more than 2.5 times more expensive than a nozzle bowl separator.
  • the second centrifugal separation stage is taking place in a decanter centrifuge, which has proven its capability of obtaining a high concentration in the separated dry matter phase (i.e. the sodium sulphate), with a clean filtrate in the separated liquid phase.
  • a decanter centrifuge which has proven its capability of obtaining a high concentration in the separated dry matter phase (i.e. the sodium sulphate), with a clean filtrate in the separated liquid phase.
  • the leaching process in at least one leaching tank preferably established at a temperature in the interval 65-105 9 C, and preferably below boiling temperature below 95 °C and most preferred at about 80 9 C which provides a safe margin towards boiling.
  • the slurried electrostatic precipitator ash having a dry substance level in the interval 15-40% by weight being obtained.
  • the leaching process in at least one leaching tank is further preferably established such that the slurried electrostatic precipitator ash passing through, and being treated in, the leaching tank in at least two agitation zones, in which agitation zones the slurried electrostatic precipitator ash undergoes repeated gentle agitation in the leaching tank.
  • Fig. 1 shows a prior art one-stage leaching and centrifugal process
  • Fig. 2 shows the principal system set up and flow routing in a two-stage leaching and centrifugal process according to the invention
  • Fig. 3 shows a nozzle bowl separator preferably used in the first centrifugal stage of the two- stage process shown in figure 2.
  • Figure 1 show an apparatus set-up which is used in a prior art one-stage leaching and centrifugal process for leaching electrostatic precipitator ash.
  • the electrostatic precipitator ash, from electrostatic precipitator 19, and liquids for leaching are supplied to a first leaching tank 1.
  • a part of the liquid for leaching can expediently be fabrication water from the bleaching department or the pulp drying machine, evaporation condensate, scrubber condensate or tap-water.
  • H 2 SO 4 or other suitable acidic conditioner for establishment of correct pH can be supplied when the electrostatic precipitator ash contains high contents of Na 2 CO 3 .
  • the amount supplied is typically around 0.1 kg per 1 .0 kg of electrostatic precipitator ash, i. e. in proportions of approx. 5-15% by weight.
  • the electrostatic precipitator ash can typically have a composition corresponding to the following;
  • the ash which is supplied to the leaching tank contains chloride ions and potassium ions.
  • the chloride content in the slurry is typically 2.0-7.0 % by weight.
  • a pH in the interval pH 8-13, preferably around pH 9, is established in the leaching tank.
  • the mixture in the leaching tank should preferably not exceed 1600 kg/m 3 , which thus sets an upper limit to the leaching process. If the consistency becomes too high, something which already begins to become apparent at 1570 kg/m 3 , the mixture then becomes increasingly difficult to pump and agitate with the stirrers. In particular, the initial admixing with the electrostatic precipitator ash using the first stirrer 1 1 is rendered more difficult at these concentrations.
  • a suitable lower concentration level corresponds to a mixture at 1450-1550 kg/m 3 .
  • the temperature should preferably be kept within the interval 65-105 9 C, with a relatively high temperature within the interval 80-105 9 C being most favorable for the leaching process.
  • An optimum temperature both from the point of view of the process and the point of view of the apparatus is around 80 9 C.
  • leaching takes place under these process conditions (pH, concentration and temperature) for a relatively long time, within the interval 1 -5 hours, preferably 2 hours, and while agitating gently, favorable process conditions are created for crystal growth of, in particular, a solid phase of Na 2 SO 4 . It has been found that the crystals which are formed are distributed normally around a particle size of about 200 ⁇ m, which is a surprisingly good result which should be compared with what can be obtained using the energy-intensive cooling technique, where a crystal formation with particles normally distributed around 300 ⁇ m can be achieved under optimum conditions.
  • the leaching tank is shaped such that repeated gentle agitation is obtained over the whole volume.
  • An initial agitation preferably takes place using a first stirrer 1 1 in connection with the electrostatic precipitator ash being supplied. After that, the mixture passes through at least one additional agitation zone and preferably two agitation zones. This can be achieved by installing at least one double bottom 13 in the middle of the leaching tank. An intermediate-stage stirrer 12a is arranged in an outlet from this double bottom 13, and a final-stage stirrer 12b is arranged in connection with the outlet from the leaching tank.
  • the dwell time in the leaching tank, between agitations, when the mixture is not subjected to direct agitation, should amount to at least 30% of the total dwell time in the leaching tank.
  • the intermediate-stage stirrer consequently acts on the slurried electrostatic precipitator ash when the latter has had a dwell time in the region of 30-70% of the total dwell time in the leaching tank, and the slurried electrostatic precipitator ash is subjected to a final-stage stirrer in a lower part of the leaching tank in connection with the outlet from the leaching tank.
  • the agitation should preferably be gentle in order to ensure that particles which have already crystallized out are not broken, and a mechanical blade-equipped stirrer of the propeller type can expediently be used, in each respective position, for the intermediate-stage and final- stage stirrers, with both the stirrers being driven by the same shaft, which latter is driven at a moderate rotational speed in the region of 50-200 rpm, preferably around 80 rpm.
  • the slurry which is obtained in this way is pumped onwards, via the pump 4, to a centrifugation stage, in this present case a decanter centrifuge 2, where particles which have been formed, i. e. solid phase containing Na 2 SO 4 , are separated out as a dry fraction.
  • a centrifugation stage in this present case a decanter centrifuge 2, where particles which have been formed, i. e. solid phase containing Na 2 SO 4 , are separated out as a dry fraction.
  • the decanter centrifuge affords a continuous process which does not require to be interrupted for regenerating the equipment (due to clogging, etc.).
  • the decanter centrifuge comprises, in a known manner, a rotating screw body 20, on which a worm 21 has been formed.
  • a casing 22, which also rotates, is arranged around the screw body 20.
  • the slurry is fed into the decanter centrifuge via the inlet 23 and, due to the rotation of the casing 22, the leached liquid is flung against the inside of the casing, where the heavier solid-particle fraction forms the outer layer 28, due to the centrifugal effect, and the liquid fraction forms the inner layer 29.
  • the liquid fraction leaves the decanter centrifuge via the spillway 25, while the screw feeds the solid fraction out towards the outlet 24. Due to the spillway 25 for the liquid fraction being located at a shorter distance from the axis of rotation than the outlet 24, it will be mainly the solid fraction which is transported by the worm 21 towards the outlet 24 via the conformed outlet of the casing.
  • the solid fraction which is obtained in this way, and which consists of enriched Na 2 SO 4 , is given, by the decanter centrifuge, a relatively high dry substance content, in the dry substance fraction, which is in the interval 58-97%, and is then fed to a slurrying vessel 3, where it is admixed with black liquor/BL, for example, for forwarding to recovery, either via evaporation (not shown) or directly to the recovery boiler 18.
  • the liquid fraction with its content of chloride ions and potassium ions, can in part be returned to the leaching tank 1 or in part, 26, forwarded to the effluent for external purification or further working up.
  • a washing zone can optionally be arranged in the decanter centrifuge. This is shown in the figure by means of a distribution ring 27 for washing liquid, which ring opens up radially inwards towards the layer 28 of the solid fraction which is passing by.
  • the washing liquid which is preferably pressurized, can expediently be the condensate (cond. ) which is otherwise added to the top of the leaching tank in connection with the initial slurrying of the electrostatic precipitator ash.
  • the washing liquid is advantageously added at a position in the decanter centrifuge at which a separating effect is exerted on the liquid even after the position at which the washing liquid is added.
  • figure 2 is the system set up according to the invention shown.
  • the leaching tank and associated leaching process is preferably similar to the one described in figure 1 , and similar components and flows have same reference numbers.
  • the slurry which is obtained in this way is pumped onwards, via a pump 4a, to a first centrifugation stage 2a.
  • a centrifugation stage In this centrifugation stage is a first liquid fraction LF1 as well as a first dry matter substance DM1 obtained.
  • the first liquid fraction LF1 contains high levels of chlorides and potassium and a part of this fraction is bled off from the process via 26. The remaining part of this first liquid fraction could be returned back to the first leaching tank 1 a.
  • acidic liquids such as Na 2 SO 4 and/or H 2 SO 4 be added in a dedicated supply conduit connected to the first leaching tank 1 a as shown in figure 2.
  • This pH correction is needed if the carbonate content of the ash is typically higher than 5 weight-%, and thus dependent on the specific overall mill process.
  • the first dry matter substance DM1 obtained contains high levels of sodium sulphate, and is sent to a second leaching tank 1 b, where the crystallization of sodium sulphate is taken even further on the particles already formed.
  • the crystallization process is improved as large parts of the chlorides and potassium has been bled off in the first centrifugal stage 2a.
  • the leaching process in the second leaching tank 1 b is essentially at the similar conditions as in the first leaching tank as of pH and dry substance level, excluding the bled off part of the chlorides and potassium.
  • the leached slurry which is obtained in this way is pumped onwards, via a pump 4b, to a second centrifugation stage 2b.
  • a second centrifugation stage 2b In this centrifugation stage is a second liquid fraction LF2 as well as a second dry matter substance DM2 obtained.
  • the second liquid fraction LF2 contains some residual levels of sodium sulphate and a part of this fraction is returned back to the first leaching tank 1 a while the remaining part of this second liquid fraction could be returned back to the second leaching tank 1 b.
  • the final dry matter substance DM2 is similarly to figure 1 led via outlet 24 to any appropriate mixing tank where this dry matter substance DM2 is mixed with black liquor before sending it further to the recovery process via the evaporation train of directly to the recovery boiler.
  • the first centrifugal separation stage 2a taking place in a high rotational speed centrifuge optimized for obtaining a clean first liquid fraction
  • the second centrifugal separation stage takes place in a low rotational speed centrifuge optimized for obtaining a second dry matter substance DM2 with a dry matter concentration being at least 15% higher than that of the first dry matter substance.
  • the first centrifugal separation stage takes preferably place at a rotational speed above 3500 rpm, and the second centrifugal separation stage takes place at a rotational speed below 3500 rpm, while the difference in rotational speed between first and second centrifugal separation stages is at least 2000 rpm.
  • the first centrifugal separation stage takes place in a nozzle bowl separator centrifuge which is shown in figure 3.
  • the nozzle centrifuge consists basically of a stationary housing 50 and a bowl 51 rotating inside of the housing at high rotational speed.
  • the slurry is fed from 1 a via a feed inlet pipe into the inlet chamber 52 at the lower end of the rotating bowl 51 , and passes thereafter around a lower edge of a conical wall to a disc stack 53 with conical discs where the main separation takes place. Separation takes place under the influence of high centrifugal force.
  • the narrow conical discs establish interspaces which split the total liquid flow into several thin layers.
  • the solid particles are flung and settle on the underside of the disc above and slide down into the outer separation chamber 54 for the denser solid particles.
  • the separated solid particles i.e. Na 2 SO 4 crystals
  • the clarified liquid LF1 is conveyed to the centre of the bowl from where it is pumped by a centripetal pump 56 to the outlet 58.
  • This type of centrifuge could also preferably be equipped with a washing stage, where washing liquid (Kond.) may be added via a central pipe 60 to the lowermost part of the inlet chamber 52.
  • washing liquid Kond.
  • the second centrifugal separation stage 2b preferably takes place in a decanter centrifuge, also used in the prior art one-stage leaching and centrifugal process as shown in figure 1 .
  • the leaching process in at least one leaching tank 1 a/1 b is established at a temperature in the interval 65-105 9 C, preferably around 80 9 C with a slurried electrostatic precipitator ash having a dry substance level in the interval 15-40% by weight being obtained.
  • the leaching process in at least one leaching tank 1 a/1 b is preferably also established such that the slurried electrostatic precipitator ash passing through, and being treated in, the leaching tank in at least two agitation zones, in which agitation zones the slurried electrostatic precipitator ash undergoes repeated gentle agitation in the leaching tank.
  • the chlorides and potassium are bled out via the liquid fraction from the first centrifugal separation stage, with at least 0.5-2.0 ton of liquid fraction per ton of electrostatic precipitator ash being forwarded to effluent or further working-up.
  • the 2-stage process it was found possible to separate over 85% of its chloride and potassium content from the electrostatic precipitator ash.

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  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un procédé de purification de cendres de filtre électrostatique de chaudière de récupération (via 19) pour en enlever les chlorures (Cl) et le potassium (K), afin de récupérer les produits de dépulpage utiles tels que le sulfate de sodium (Na2SO4). Le procédé fait appel à deux étapes de séparation centrifuge (2a, 2b) en série comportant une étape de lixiviation (1a et 1b) en amont de chaque étape centrifuge. Les chlorures et le potassium sont exsudés (26) avec la première fraction liquide (LF1) provenant de la première étape de séparation centrifuge, et la seconde substance finale formée de matière sèche (DM2) présentant une teneur enrichie en sulfate de sodium et provenant de la seconde étape de séparation centrifuge est dirigée (24) vers le cycle de récupération de liqueur, mélangée dans de la liqueur noire avant que la liqueur noire ne soit dirigée vers le procédé de récupération en vue d'une réutilisation du sulfate de sodium dans le procédé de dépulpage. Grâce au procédé selon l'invention, les pertes de sulfate de sodium ont pu être considérablement réduites par rapport à un procédé de lixiviation et centrifugation en une seule étape.
EP09846901.8A 2009-05-06 2009-05-06 Procédé de lixiviation améliorée de cendres de filtre électrostatique en provenance d'une chaudière de récupération Active EP2427598B1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/SE2009/050493 WO2011002354A1 (fr) 2009-05-06 2009-05-06 Procédé de lixiviation améliorée de cendres de filtre électrostatique en provenance d'une chaudière de récupération

Publications (3)

Publication Number Publication Date
EP2427598A1 true EP2427598A1 (fr) 2012-03-14
EP2427598A4 EP2427598A4 (fr) 2014-04-02
EP2427598B1 EP2427598B1 (fr) 2016-01-06

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EP09846901.8A Active EP2427598B1 (fr) 2009-05-06 2009-05-06 Procédé de lixiviation améliorée de cendres de filtre électrostatique en provenance d'une chaudière de récupération

Country Status (4)

Country Link
EP (1) EP2427598B1 (fr)
CN (1) CN102421961B (fr)
BR (1) BRPI0924612B1 (fr)
WO (1) WO2011002354A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11725341B2 (en) 2017-04-28 2023-08-15 Andritz Oy Method of treating fly ash of a recovery boiler

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8721837B2 (en) * 2012-07-26 2014-05-13 Veolia Water Solutions & Technologies North America, Inc. Method for recovering pulping chemicals and reducing the concentration of potassium and chloride therein
US9333468B2 (en) 2012-09-24 2016-05-10 Abengoa Bioenergy New Technologies, Llc Soak vessels and methods for impregnating biomass with liquid
FI126767B (en) 2012-11-16 2017-05-15 Andritz Oy Method for extracting the ash from a recovery boiler
CN104631181B (zh) * 2013-11-12 2018-09-25 王子控股株式会社 回收锅炉收集灰的处理方法及处理装置
SE538684C2 (sv) * 2014-12-10 2016-10-18 Göran Hofstedt Anders Förfarande och anläggning för tvättning av råtallsåpa
FI127615B (en) 2015-11-27 2018-10-31 Andritz Oy Procedure for treating ash by a recovery boiler
FR3072396B1 (fr) * 2017-10-12 2019-11-08 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Methode de traitement des cendres d'electrofiltres de la chaudiere de recuperation dans un procede kraft

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WO2003016616A1 (fr) * 2001-08-14 2003-02-27 Kvaerner Power Ab Procede de lixiviation des cendres de filtres electriques dans une chaudiere de recuperation

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SE504374C2 (sv) * 1994-10-20 1997-01-20 Kvaerner Pulping Tech Lakning av elfilteraska
JPH08170288A (ja) * 1994-12-15 1996-07-02 Mitsubishi Heavy Ind Ltd ソーダ回収ボイラの捕集灰からの食塩及びカリウム塩の除去方法
SE526435C2 (sv) * 2001-09-28 2005-09-13 Skogsind Tekn Foskningsinst Metod för återvinnande av massakemikalier i ett alkaliskt sulfitmassaförfarande och för framställning av ånga
JP3683870B2 (ja) * 2002-07-15 2005-08-17 太平洋セメント株式会社 ダスト水洗システム及びダスト水洗方法
EP1798297A1 (fr) * 2005-12-16 2007-06-20 CTU - Conzepte Technik Umwelt AG Procédé pour le traitement de poussières contenant des métaux lourds

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WO2003016616A1 (fr) * 2001-08-14 2003-02-27 Kvaerner Power Ab Procede de lixiviation des cendres de filtres electriques dans une chaudiere de recuperation

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11725341B2 (en) 2017-04-28 2023-08-15 Andritz Oy Method of treating fly ash of a recovery boiler

Also Published As

Publication number Publication date
EP2427598B1 (fr) 2016-01-06
BRPI0924612B1 (pt) 2018-08-07
CN102421961B (zh) 2013-09-18
BRPI0924612A2 (pt) 2016-08-30
WO2011002354A1 (fr) 2011-01-06
EP2427598A4 (fr) 2014-04-02
CN102421961A (zh) 2012-04-18

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