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WO2015010179A1 - Procédé de réduction de concentrations d'ions chlorure et potassium dans un système de récupération chimique de moulin à pâte - Google Patents

Procédé de réduction de concentrations d'ions chlorure et potassium dans un système de récupération chimique de moulin à pâte Download PDF

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Publication number
WO2015010179A1
WO2015010179A1 PCT/CA2013/050579 CA2013050579W WO2015010179A1 WO 2015010179 A1 WO2015010179 A1 WO 2015010179A1 CA 2013050579 W CA2013050579 W CA 2013050579W WO 2015010179 A1 WO2015010179 A1 WO 2015010179A1
Authority
WO
WIPO (PCT)
Prior art keywords
chloride
potassium
process stream
producing
cation exchange
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.)
Ceased
Application number
PCT/CA2013/050579
Other languages
English (en)
Inventor
Christopher W. CHAN
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.)
Noram Engineering and Constructors Ltd
Original Assignee
Noram Engineering and Constructors Ltd
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 Noram Engineering and Constructors Ltd filed Critical Noram Engineering and Constructors Ltd
Priority to PCT/CA2013/050579 priority Critical patent/WO2015010179A1/fr
Publication of WO2015010179A1 publication Critical patent/WO2015010179A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

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
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/0035—Introduction of compounds, e.g. sodium sulfate, into the cycle in order to compensate for the losses of pulping agents
    • 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
    • D21C11/0007—Recovery of by-products, i.e. compounds other than those necessary for pulping, for multiple uses or not otherwise provided for
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C02F2001/422—Treatment of water, waste water, or sewage by ion-exchange using anionic exchangers
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C02F2001/425—Treatment of water, waste water, or sewage by ion-exchange using cation exchangers
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/26—Nature of the water, waste water, sewage or sludge to be treated from the processing of plants or parts thereof
    • C02F2103/28—Nature of the water, waste water, sewage or sludge to be treated from the processing of plants or parts thereof from the paper or cellulose industry
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/40—Production or processing of lime, e.g. limestone regeneration of lime in pulp and sugar mills

Definitions

  • This invention pertains to the production of bleached or unbleached cellulosic fibrous pulp.
  • the invention is concerned more particularly with a method by which chloride and potassium can be removed from the pulping chemicals used in the pulp production process. Chloride and potassium are common
  • pulping liquor used in a Kraft mill is known as white liquor, and comprises sodium sulfide (Na 2 S), sodium hydroxide (NaOH), sodium carbonate (Na 2 C0 3 ), and impurities.
  • APMP alkaline peroxide mechanical pulp
  • the spent pulping chemicals are recovered in the pulp mill chemical recovery cycle.
  • the first step in the chemical recovery cycle is evaporation, where spent liquor is concentrated by a multi-stage evaporation and concentration process.
  • the concentrated liquor is then burned in a recovery boiler.
  • the recovery boiler has two purposes:
  • Spent chemicals are recovered by dissolving the smelt from the recovery boiler.
  • the solution comprises mainly dissolved sodium sulfide and sodium carbonate and is known as green liquor, while in zero-effluent APMP mills it is mostly sodium carbonate.
  • Sodium carbonate is converted to sodium hydroxide in a recausticizing plant.
  • the sodium carbonate reacts with calcium oxide (CaO) in a causticizing reactor to form sodium hydroxide.
  • the calcium oxide is converted to calcium carbonate (CaC0 3 ) which is separated from the slurry by
  • the clarified slurry is reused as pulping chemical.
  • Typical methods of removing potassium and chloride are to dispose of a portion of the recovery boiler electrostatic precipitator (ESP) catch (ash) or to process the ESP catch in a separation system which separates the chloride and potassium from sulfate and carbonate pulping chemicals.
  • ESP recovery boiler electrostatic precipitator
  • Amphoteric resins used for chloride separation systems are only capable of selectively removing chloride, while cation exchange resins used for the separation of potassium suffer from poor potassium removal unless large quantities of chemicals are used to regenerate the resin. It is well known that chloride and potassium become enriched relative to sodium sulfate in the flue gas dust retained by the electrostatic precipitator in the recovery boiler. Several prior art processes have taken advantage of this enrichment to facilitate removal of chloride impurities from the chemical recovery cycle by treating the precipitator catch to separate potassium and chloride from Na 2 S0 4 and Na 2 C0 3 . Examples in the patent literature include US 4,007,082 (Fuller), US 5,567,293 (Paleologou et al.), US 5,91 1 ,854
  • Leaching, evaporation-crystallization and freeze crystallization capitalize on the solubility differences of potassium chloride and sodium sulfate.
  • the potassium chloride remains in solution while the sodium sulfate precipitates out.
  • the solid precipitate is separated from the solution and returned to the recovery cycle while the solution is sewered.
  • Sulfate and carbonate losses from these systems are typically 15-35%.
  • Chloride and potassium removal effectiveness of these systems are typically 70-90%, with greater removal effectiveness corresponding to greater chemical losses.
  • the conventional method to reduce the carbonate concentration in the ash is to add sulfuric acid to neutralize the sodium carbonate and form sodium sulfate.
  • the drawback of adding sulfuric acid is that the addition of a sulfur-containing compound upsets a mill sodium sulfur balance, causing an unwanted rise in liquor sulfidity or a need to purge streams that are enriched in sulfur (i.e. C10 2 generator salt cake, precipitator catch and/or product). Some mills are thus incapable of adding sulfuric acid and must operate chloride and potassium removal systems with reduced efficiencies.
  • amphoteric resin used for the removal of chloride does not have any selectivity of potassium over sodium, limiting potassium removal.
  • Cation exchange resin technology used for the removal of potassium requires large quantities of regenerant chemical to achieve a high level of potassium removal due to the very low potassium to sodium ratio that is typically present in the ash feed. The low potassium to sodium ratio is especially prevalent in newer boilers where low potassium levels in the ash are required to minimize superheater corrosion concerns.
  • a method of reducing chloride and potassium ion concentrations in a pulp mill chemical recovery cycle in which electrostatic precipitator ash is produced in a recovery boiler. At least a portion of the ash is mixed with water to form a mixture that is treated in a chloride and potassium removal system to separate chloride and potassium from sodium sulfate and sodium carbonate based on the solubility differences between potassium chloride and sodium sulfate, producing a first process stream enriched in chloride and potassium and a second process stream having reduced chloride and potassium.
  • the first stream is adjusted in temperature and/or diluted with water, if required.
  • this first stream is treated in an amphoteric resin bed to remove chloride, producing a third process stream having reduced chloride.
  • This third stream is treated in a cation exchange resin bed to remove potassium, producing a fourth process stream having reduced potassium.
  • the amphoteric resin is regenerated by flowing a fluid comprising water through the resin bed and producing a fifth process stream enriched in chloride.
  • the cation exchange resin is regenerated by flowing a fluid through the cation exchange resin bed and producing a sixth process stream enriched in potassium.
  • the positions of the amphoteric resin bed and the cation exchange resin bed are reversed, such that the first stream is treated first in the cation exchange resin bed.
  • an apparatus for reducing chloride and potassium ion concentration in a pulp mill recovery cycle has means for mixing electrostatic precipitator ash with water to produce a mixture and a chloride and potassium removal system for receiving the mixture and separating chloride and potassium from sodium sulfate and sodium carbonate, based on solubility differences between sodium chloride and sodium sulfate, to produce a first process stream enriched in chloride and potassium and a second process stream having reduced chloride and potassium.
  • the apparatus includes an amphoteric resin bed for receiving the first process stream and removing chloride to produce a third process stream having reduced chloride.
  • the apparatus includes means for regenerating the amphoteric resin and producing a fifth process stream enriched in chloride, and means for regenerating the cation exchange resin and producing a sixth process stream enriched in potassium.
  • the positions of the amphoteric resin bed and the cation exchange resin bed are reversed.
  • Figure 1 is a schematic diagram of an embodiment of the process and apparatus of the invention.
  • Figure 2 is a schematic diagram of a leaching system according to Example 1.
  • Figure 3 is a schematic diagram of an ion exchange system according to Example 1.
  • Figure 4 is a schematic diagram of the process of the invention, according to Example 1.
  • Figure 5 is a schematic diagram of a further embodiment of the process and apparatus of the invention, in which the positions of the amphoteric resin bed and the cation exchange resin bed are reversed.
  • the ash (catch) 10 from the electrostatic precipitator of a recovery boiler is first treated in a primary separation system 15 of a type that separates potassium chloride from sodium sulfate based on solubility differences between these salts.
  • the separation system 15 is a leaching system comprising a leaching tank 14 and a centrifuge 18.
  • the precipitator ash 10 is mixed with water 12 in the leaching tank to form an ash slurry 16.
  • the slurry 16 passes to the centrifuge 18, in which the solids, primarily sulfate, is separated from the leachate, rich in chloride and potassium.
  • the primary separation system may comprise an evaporation-crystallization system, or a freeze crystallization system.
  • evaporation-crystallization system or a freeze crystallization system.
  • the primary separation system 15 produces a first process stream 20 enriched in chloride and potassium, and a second process stream 22 having reduced chloride and potassium, enriched in sodium sulfate.
  • a portion of the first process stream 20 may be recycled (stream 27) as make-up water to minimize chemical losses of the leaching system and reduce the size of the ion- exchange equipment required.
  • the second process stream 22 may optionally be returned to the recovery cycle (stream 23) by dissolving in black or green liquor, or optionally be further processed to achieve greater removal of chloride and potassium (stream 25), for example by dissolving the stream in water and treating it in by ion exchange.
  • the first process stream 20, enriched in chloride and potassium, is adjusted in temperature and/or diluted with water 24, if required, to ensure the stream is within allowable operating temperatures of the ion exchange resin and below the solubility limit.
  • the solubility limit is the concentration at which salts begin precipitating. If temperature adjustment is required, this is done by passing the first process stream 20 through a heat exchanger 29.
  • This first process stream which may be a diluted and/or temperature-adjusted stream 26, is passed to an amphoteric resin bed 28 for treatment to selectively remove chloride.
  • An example of a suitable amphoteric resin is marketed by Mitsubishi Chemical Products as the DIAIONTM AMP series, which contains a quaternary ammonium group and a carboxyl group incorporated on a cross-linked polystyrene frame.
  • the process stream 30 exiting the amphoteric resin bed 28 constitutes a third process stream comprising a solution principally of sodium, potassium, sulfate and carbonate.
  • This third process stream 30 is passed to a cation exchange resin bed 32, in which potassium ions are adsorbed by the sodium-based cation exchange resin.
  • An example of a suitable sodium-based cation exchange resin is a strong acid cation resin marketed by Mitsubishi Chemical Products as the DIAIONTM SK series, which contains a sulfonic acid group in a cross-linked styrene frame.
  • the fourth process stream 34 enriched in sodium sulfate and sodium carbonate, is optionally sent to the evaporator set of the chemical recovery cycle (stream 36); or optionally it may be returned to the primary separation system 15 for the purpose of improving the overall removal of chloride and potassium (stream 38).
  • the resin in the amphoteric resin bed 28 is regenerated by flowing water
  • stream 40 through the bed.
  • Amphoteric resin has a slight preference to remove sodium relative to potassium, so the stream 42 is enriched in both sodium and chloride. This may be sewered (stream 43).
  • the resin in the cation exchange resin bed 32 is regenerated by a sodium-based regenerant. This elutes the potassium from the bed in a sixth process stream 46, 48.
  • the regenerant may comprise one or more of a sodium chloride brine solution (stream 44), a sodium hydroxide solution (stream 50), and the effluent stream 42 from regeneration of the amphoteric resin bed 28, with water (stream 49).
  • the amphoteric resin effluent stream 42 and/or sodium hydroxide 50 are preferentially used to regenerate the cation exchange resin, with the sodium and potassium hydroxide regenerant stream 48 used subsequently in the bleach plant. If greater potassium removal is required, sodium chloride (stream 44) may also be used as an additional regenerant chemical.
  • the amphoteric resin effluent stream 42 and/or sodium chloride (stream 44) are preferentially used to regenerate the resin.
  • the effluent stream 46 may be sewered.
  • the positions of the amphoteric resin bed and the cation exchange resin bed are reversed.
  • the system is the same as discussed above in respect of Figure 1 up to the point of treatment of the first process stream 20.
  • this first process stream 20 which may be a diluted and/or temperature-adjusted stream 26, is passed to the cation exchange resin bed 32, in which potassium ions are adsorbed by the sodium-based cation exchange resin.
  • This third process stream 52 is passed to the amphoteric resin bed 28 for treatment to selectively remove chloride.
  • the process stream 54 exiting the amphoteric resin bed constitutes a fourth process stream, enriched in sodium sulfate and sodium carbonate. It is optionally sent to the evaporator set of the chemical recovery cycle (stream 56); or it may optionally be returned to the primary separation system 15 for the purpose of improving the overall removal of chloride and potassium (stream 38).
  • the regeneration of the resins in the amphoteric resin bed 28 and the cation exchange resin bed 32, and the use or disposition of the effluents, are done in the same manner as described above for the embodiment of Figure 1.
  • Examples compare the results of treatment of ESP ash by the process of the invention versus treatment by leaching alone and by ion exchange alone, with respect to chloride and potassium removal and the loss of sulfate and carbonate.
  • Example 1 A representative ESP ash composition typical for modern pulp mills is the following: potassium - 2 wt%; chloride - 2 wt%; sodium - 35 wt%; carbonate - 20 wt%; sulfate - 41 wt%.
  • FIG. 2 shows the results of the treatment of 200 tons/day of ash by a leaching system.
  • the treatment removes 65 wt% of the potassium, 65 wt% of the chloride, and resulted in a loss of 25 wt% of sulfate and 40 wt% loss of carbonate. This would be the expected performance of a single stage leaching system treating high carbonate ash, based on known data from operating plants.
  • the ash is dissolved in water in a dissolving tank 52, and the ash slurry 54 is passed to an amphoteric resin bed 28.
  • the effluent from that bed passes to a cation exchange resin bed 32 ( Figure 3).
  • the demand for caustic in the bleach plant is 30 tons/day NaOH, the caustic used for
  • regeneration of the cation exchange resin is not sufficient to remove a substantial amount of potassium.
  • Performance of the amphoteric resin is based on known data from operating plants, while an equilibrium-based calculation routine was used to calculate the potassium removal efficiency. The results of the treatment are shown in the process flow diagram of Figure 3. If additional potassium removal were desired, additional brine or other chemicals would be required, which would have an associated cost and environmental impact.
  • the ion exchange system is used to treat the leach effluent rather than to treat the ash directly.
  • a marked improvement is seen in the overall potassium removal.
  • an equilibrium-based calculation routine was used to calculation potassium removal efficiency.
  • the calculation routine determined what would be expected, that a marked improvement in removal is seen when the potassium to sodium ratio in the feed increases. In this case, the overall removal of potassium and chloride is close to that of the initial leaching system, but the chemical losses are greatly reduced.
  • the results of the treatment are shown in the process flow diagram of Figure 4.
  • chloride removal would be:
  • the chemical losses from the use of the present invention are lower than those of either leaching alone or ion exchange alone.
  • the potassium removal by the present invention is greater than that by the ion exchange alone due to the enrichment of the potassium relative to sodium that occurs in the primary leach treatment.
  • the size of the ion exchange equipment required when treating the leach waste is much smaller than when ion exchange equipment is used to treat the entire ash stream.
  • a second representative ESP ash composition typical for modern pulp mills is the following: potassium - 2 wt%; chloride - 2 wt%; sodium - 32 wt%;
  • the chemical losses of the present invention are the lowest when compared to leaching alone and to ion exchange alone.
  • the potassium removal of the present invention is greater than removal by the ion exchange alone due to the enrichment of the potassium relative to sodium that occurs in the primary leach treatment.

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Abstract

L'invention porte sur un procédé de réduction de concentration d'ions chlorure et potassium dans un cycle de récupération chimique de moulin à pâte, dans lequel procédé une cendre de précipitateur électrostatique est produite dans une chaudière de récupération. Un mélange (16) de la cendre (10) et d'eau (12) est séparé en un premier courant de traitement (20) enrichi en chlorure et en potassium et un second courant de traitement (22) ayant une teneur en chlorure et en potassium réduite, à l'aide d'un système de retrait de chlorure et de potassium primaire (15) qui sépare le chlorure et le potassium à partir de sulfate de sodium et de carbonate de sodium sur la base de différences de solubilité. Le premier courant de traitement (20) est traité dans un lit de résine amphotère (28) pour retirer le chlorure, produisant un troisième courant de traitement (30) ayant une teneur en chlorure réduite. Le troisième courant de traitement est traité dans un lit de résine d'échange de cations (32) pour retirer le potassium, produisant un quatrième courant de traitement (34) ayant une teneur en potassium réduite. La résine amphotère est régénérée par circulation d'eau (40) à travers le lit de résine amphotère (28) et la production d'un cinquième courant de traitement (42) enrichi en chlorure. La résine d'échange de cations est régénérée par l'écoulement d'un fluide à travers le lit de résine d'échange de cations (32) et la production d'un sixième courant de traitement (46, 48) enrichi en potassium. Dans un autre mode de réalisation, les positions des lits de résine amphotère et d'échange de cations sont inversées.
PCT/CA2013/050579 2013-07-25 2013-07-25 Procédé de réduction de concentrations d'ions chlorure et potassium dans un système de récupération chimique de moulin à pâte Ceased WO2015010179A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/CA2013/050579 WO2015010179A1 (fr) 2013-07-25 2013-07-25 Procédé de réduction de concentrations d'ions chlorure et potassium dans un système de récupération chimique de moulin à pâte

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PCT/CA2013/050579 WO2015010179A1 (fr) 2013-07-25 2013-07-25 Procédé de réduction de concentrations d'ions chlorure et potassium dans un système de récupération chimique de moulin à pâte

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2017089656A1 (fr) * 2015-11-27 2017-06-01 Andritz Oy Procédé de traitement de cendres de chaudière de récupération
US9834114B2 (en) 2014-08-27 2017-12-05 Quantumscape Corporation Battery thermal management system and methods of use
WO2020165504A1 (fr) * 2019-02-13 2020-08-20 Metsä Fibre Oy Procédé de remplacement de pertes de sodium dans une usine de pâte à papier, procédé de production de pâte cellulosique blanchie, et système
US10889205B2 (en) 2014-01-03 2021-01-12 Quantumscape Corporation Thermal management system for vehicles with an electric powertrain
US11011783B2 (en) 2013-10-25 2021-05-18 Quantumscape Battery, Inc. Thermal and electrical management of battery packs
WO2024151589A1 (fr) * 2023-01-10 2024-07-18 Veolia Water Technologies, Inc. Système et procédé de réduction de pertes chimiques dans le traitement de cendres produites dans une chaudière de récupération d'un procédé de réduction en pâte de bois

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2225927A1 (fr) * 1997-01-03 1998-07-03 Eka Chemicals Ab Processus de recuperation dans une usine de pate
US5922171A (en) * 1997-01-24 1999-07-13 Eco-Tec Limited Method and apparatus for removing sodium chloride from pulping chemicals using an amphoteric ion-exchange resin
CA2504303A1 (fr) * 2002-11-05 2004-05-21 Nippon Rensui Co. Procede de production de pate kraft

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2225927A1 (fr) * 1997-01-03 1998-07-03 Eka Chemicals Ab Processus de recuperation dans une usine de pate
US5922171A (en) * 1997-01-24 1999-07-13 Eco-Tec Limited Method and apparatus for removing sodium chloride from pulping chemicals using an amphoteric ion-exchange resin
CA2504303A1 (fr) * 2002-11-05 2004-05-21 Nippon Rensui Co. Procede de production de pate kraft

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11777153B2 (en) 2013-10-25 2023-10-03 Quantumscape Battery, Inc. Thermal and electrical management of battery packs
US11011783B2 (en) 2013-10-25 2021-05-18 Quantumscape Battery, Inc. Thermal and electrical management of battery packs
US11577626B2 (en) 2014-01-03 2023-02-14 Quantumscape Battery, Inc. Thermal management system for vehicles with an electric powertrain
US12311805B2 (en) 2014-01-03 2025-05-27 Quantumscape Battery, Inc. Thermal management system for vehicles with an electric powertrain
US11884183B2 (en) 2014-01-03 2024-01-30 Quantumscape Battery, Inc. Thermal management system for vehicles with an electric powertrain
US10889205B2 (en) 2014-01-03 2021-01-12 Quantumscape Corporation Thermal management system for vehicles with an electric powertrain
US11040635B2 (en) 2014-08-27 2021-06-22 Quantumscape Battery, Inc. Battery thermal management system and methods of use
US11673486B2 (en) 2014-08-27 2023-06-13 Quantumscape Battery, Inc. Battery thermal management system and methods of use
US10369899B2 (en) 2014-08-27 2019-08-06 Quantumscape Corporation Battery thermal management system and methods of use
US9834114B2 (en) 2014-08-27 2017-12-05 Quantumscape Corporation Battery thermal management system and methods of use
US12311804B2 (en) 2014-08-27 2025-05-27 Quantumscape Battery, Inc. Battery thermal management system and methods of use
WO2017089656A1 (fr) * 2015-11-27 2017-06-01 Andritz Oy Procédé de traitement de cendres de chaudière de récupération
WO2020165504A1 (fr) * 2019-02-13 2020-08-20 Metsä Fibre Oy Procédé de remplacement de pertes de sodium dans une usine de pâte à papier, procédé de production de pâte cellulosique blanchie, et système
US12331460B2 (en) 2019-02-13 2025-06-17 Metsä Fibre Oy Method of replacing sodium losses in a pulp mill, a method of producing bleached cellulosic pulp, and a system
WO2024151589A1 (fr) * 2023-01-10 2024-07-18 Veolia Water Technologies, Inc. Système et procédé de réduction de pertes chimiques dans le traitement de cendres produites dans une chaudière de récupération d'un procédé de réduction en pâte de bois

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