EP3380667B1 - Procédé et système de délignification à l'oxygène de pâte cellulosique - Google Patents

Procédé et système de délignification à l'oxygène de pâte cellulosique Download PDF

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EP3380667B1
EP3380667B1 EP16868982.6A EP16868982A EP3380667B1 EP 3380667 B1 EP3380667 B1 EP 3380667B1 EP 16868982 A EP16868982 A EP 16868982A EP 3380667 B1 EP3380667 B1 EP 3380667B1
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Prior art keywords
phase
pulp
oxygen
delignification
zone
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German (de)
English (en)
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EP3380667A4 (fr
EP3380667A1 (fr
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Håkan DAHLLÖF
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Valmet Technologies Oy
Valmet AB
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Valmet Oy
Valmet AB
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    • 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
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/10—Bleaching ; Apparatus therefor
    • D21C9/147—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications
    • 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
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/10—Bleaching ; Apparatus therefor
    • D21C9/1005—Pretreatment of the pulp, e.g. degassing the pulp

Definitions

  • the present invention relates to a method and system for oxygen delignification.
  • US 5217575 presented an improved system for the oxygen bleaching of pulp of medium consistency where this temperature profiling surprisingly showed that a lower temperature in a first phase may result in better delignification.
  • US 5217575 was shown that if an optimized single stage operated at 105°C was preceded by a phase operated at 20-40°C lower temperature, a better delignification could be obtained at higher selectivity.
  • US6221206 disclosed an alternative for temperature profiling where the difference in temperature should be kept between 0°C and 15°C. The aim was to obtain an improved yield and an improved viscosity, while retaining the same dwell time, in connection with industrial implementation.
  • SE-C 505 147 presents an alternative with instead a high pulp concentration, in the range of 25-40%, in a first phase and a lower concentration of 8-16% in a second phase, at the same time as the temperature in the second phase is to be higher than, or the same as, the temperature in the first phase.
  • the advantages of the solution in accordance with SE-C 505 147 are stated to be the possibility of admixing more oxygen in the first high-consistency phase without the risk of channeling. Here were unused quantities of oxygen bled off after the first phase for further admixture in a second mixer prior to the second phase.
  • a high-pressure alternative has been disclosed in SE526843 , where the initial pressure in first reactor is established above 15 bar, and where the pressure was maintained at high level throughout all phases of the oxygen delignification stage.
  • the idea is to increase the amount of oxygen dissolved in the liquid phase per liter liquid, and thus being able to react with the pulp.
  • the amount of inert gases produced increases throughout the phases, the net amount of oxygen dissolved may in fact decrease as the total pressure in the system is only the sum of the partial pressures from each gas present (CO, CO 2 , O 2 , etc.).
  • a method which comprises the steps of: cooking comminuted cellulosic fibrous material to produce brown stock having shives, washing the brown stock to produce chemical pulp at a consistency of between about 6-18 %, oxygen delignifying the chemical pulp and separating gas from the pulp during the oxygen delignification step, screening the oxygen delignified pulp to produce an accept fraction and a shive-containing reject fraction (where all the steps above are practiced in a main fiber line), further treating the accept fraction, and directly transporting the shive-containing reject fraction back to the main fiber line before the oxygen delignification step.
  • the disclosed method is, however, not directed to improvement of the oxygen delignification step itself, and is, for example, silent about the pressures that prevail in the oxygen delignification step.
  • EP1061173 relates to a method for treating lignocellulosic pulp, which method comprises the steps of: mixing the lignocellulosic pulp with alkali in a pulp soaking stage to create a mixture, mixing said mixture with both oxygen and steam to form a combined steam, and feeding said combined steam to a pressurized oxygen delignification stage to enable a reaction between the oxygen and the lignin in the lignocellulosic pulp, to remove colored materials from the lignocellulosic pulp.
  • the disclosed method is directed to reduction of capital equipment by obviating one stage of a two-stage oxygen delignification plant, which is achieved by the extra addition of alkali before the oxygen delignification step. Apart from the investments costs, the general advantages of a two-stage process are, however, acknowledged also in this document.
  • CA2190573 relates to a method for delignifying chemical pulp, comprising the steps of: feeding cooked pulp having a temperature above 70 °C from the brown stock washing to the delignification stage, adding alkali and oxygen and mixing the alkali and oxygen into the pulp, where at least part of the alkali is unoxidized white or green liquor.
  • the claimed process is said to preferably be carried out in at least two delignification steps and appears in practice to require an extra gas separating step between two delignification steps. In reality, on a pulp mill scale, there is, however, still a question how much the use of unoxidized white liquor impact the kappa reduction in the oxygen delignification stage.
  • high kappa pulp with kappa numbers after cook in the range 40-120, where a kappa number above 20 may be considered high for hardwood, is to be delignified, large amounts of oxygen is needed for delignification that may result in channeling in the stages. With high kappa number in pulp is also a large part of the oxygen charge consumed during delignification of the high kappa pulp.
  • a stage i.e. an oxygen delignification stage in this case, is the treatment done between two wash positions. What is done in said stage may also be divided into phases, with some changes effectively brought into next phase in aspects of chemical charges, heating and/or venting. Also, each phase may in turn be divided into zones where a first and a second zone of one phase may differ as to changes of chemical charges, heating and/or venting.
  • an oxygen delignification stage between 2 wash positions may be divided into phases, and each phase may in turn be divided into zones. This nomenclature is used throughout the description even if some prior art documents describe 2-phase delignification systems as 2 stage systems.
  • the wash positions may be performed in a number of ways, for example;
  • LC pulp low, medium and high consistency of pulp used to define the amount of liquid in the pulp suspension.
  • Low consistency (LC) in pulp is typically in the range 2-8%
  • medium consistency (MC) in the range 8-18%
  • high consistency (HC) typically above 30%.
  • LC pulp is so diluted that it behaves like water and the pulp suspension may be readily pumped by conventional liquid pumps.
  • MC is an intermediate range that is pumpable but requires special MC-pumps that fluidize the suspension, while high consistency pulp is not pumpable by conventional pumps and instead require transport screws etc. for feeding and transport.
  • One common aim of the invention is to improve oxygen delignification further and optimizing the order of oxygen dissolved in the pulp suspension such that the oxygen may react with the cellulose to a far greater extent than previously possible and make the oxygen delignification better suitable to high kappa cooking. While the shift to high kappa cooking and increased delignification order in oxygen stages has been known for many years to be beneficial for pulp strength from laboratory trials, mill implementations has been less frequent due to difficulties adding the necessary amounts of oxygen in a reactive phase after high kappa cooking.
  • the inert gases especially CO and CO 2
  • the inert gases acts parasitically on the solubility of oxygen in the liquid phase, and more or less substitutes the amount of dissolved oxygen.
  • the oxygen to the greatest extent possible is dissolved in the liquid phase such that the liquid may penetrate the cellulose fiber network and get in contact with the oxidizable material, i.e. lignin, in the cellulose fiber matrix.
  • Another aim is enable almost a total withdrawal of all inert gases that are formed and dissolved in the pulp suspension after a first phase of the oxygen delignification stage, where the oxidation process is fastest and produces most of the inert gases.
  • By dropping the pressure of the entire pulp suspension to a pressure close to atmospheric pressure could both the content of non-dissolved gases be removed, but also a large part of gases being dissolved in the liquid at higher pressure. A flashing effect is thus obtained.
  • venting away the inert gases before charging a fresh charge of oxygen to the pulp suspension could also the amount of oxygen being dissolved in the liquid phase be increased considerably as competing gas content has been reduced to a large extent.
  • the method according the invention is related to oxygen delignification of a medium consistency cellulose pulp suspension having a kappa number exceeding 18, and said pulp suspension passing through a first and a second oxygen delignification phases located between 2 wash positions (W 1 , W 2 ) for the pulp where said phases are separated by heating the pulp at least 5°C using steam after the first phase and ahead of the second phase, and both phases includes charge of alkali and oxygen to each of said first and second phase.
  • the inventive features of the method are that both the first and second phase is pressurized to an initial pressure exceeding 5 bar, and after the first phase is the pulp depressurized to an excess pressure below 0.5 bar, preferably depressurized to atmospheric pressure, i.e.
  • the method is further distinguished in that more than 90% of the inert gases, such as carbon monoxide and carbon dioxide, formed during the oxidation process in the first phase, are vented away by the depressurization, and wherein the pulp suspension for the depressurization effect is fed to an upper part of a standpipe and exposed to pressure in the range 0-0.5 bar in the upper part of the standpipe having a height exceeding 3 meter.
  • This venting principle applied here reduce the pressure of the pulp suspension to such a level that the solubility all gases decreases, i.e. follows Henry's law, and enable efficient degasification in the stand pipe volume. It is specifically the inert gases formed during the first phase of delignification that needs to be removed. Even if some residual oxygen may be lost in this venting is the parasitic effect on oxygen solubility by the competing inert gases more dominant, and by proper dosing of the oxygen charge to the first phase could most of the oxygen charged by consumed in the first phase.
  • the inert gases such as carbon monoxide and carbon
  • This division of the first phases into multiple zones, i.e. at least 2 zones, enable a full utilization of the reaction kinetics of oxygen delignification, as most of the reactions in an oxygen delignification stage occurs during the first half of the total retention time of the oxygen delignification stage, and the bulk volume of inert gases are formed in this first half.
  • the retention time for the pulp suspension in the first phase shorter than the retention time in the second phase, and that the retention time of the first zone in the first phase is shorter than the retention time of the second zone in the first phase.
  • This sizing of reactors may enable an equal amount of oxygen charged to each phase, near the charge volume possible to mix into the pulp suspension with the mixers used, said charge being further optimized such that more than 90% is consumed in each phase and is not wasted in the following degassing step.
  • the medium consistency cellulose pulp suspension fed to the first phase obtained from a preceding thickening process producing a high consistency cellulose pulp at a consistency above 30% is the medium consistency cellulose pulp suspension fed to the first phase obtained from a preceding thickening process producing a high consistency cellulose pulp at a consistency above 30%, and that the medium consistency cellulose pulp suspension is produced by mixing the high consistency cellulose pulp from the thickening process with oxidized filtrate.
  • oxidized filtrate for forming the medium consistency pulp avoids adding oxidizable matter into the pulp suspension, which oxidizable matter produce hydroxyl radicals during the oxygen stage and in presence of cellulose pulp reduce the viscosity of the pulp.
  • a final embodiment of the inventive method is the pulp suspension after the first zone in the first phase depressurized to an excess pressure below 0.5 bar, preferably depressurized to atmospheric pressure, i.e. within a pressure interval between 0 to 0.5 bar, and residual gases released from the pulp during depressurization are vented away before the start of the second zone of the first phase, and wherein a charge of oxygen to the second zone in the first phase is charged to the pulp after the residual gases has been vented away, and wherein the charge of oxygen to the second zone of the first phase is distributed into the pulp using a mixer, thus establishing increased partial pressure of the oxygen in the pulp.
  • This repeated venting of inert gases formed initially in the oxygen stage is especially suitable for oxygen delignification of high kappa pulps and when the filtrate added contains high concentration of COD, which in total introduce huge amounts of oxidizable material to the oxygen stage, and thus generates extreme amounts of inert gases during the oxygen delignification.
  • the invention comprises a system for oxygen delignification of a medium consistency cellulose pulp suspension having a kappa number exceeding 18, and where said system is located between 2 wash positions, said medium consistency pulp suspension first pressurized by a first pump passing the pulp to at least a first oxygen mixer and directly thereafter to at least a first oxygen delignification reactor in a first delignification phase.
  • the first delignification phase is the pulp suspension heated in a steam mixer ahead of a second phase in a second oxygen delignification reactor such that said phases are separated by heating the pulp at least 5°C using steam after the first phase and ahead of the second phase, and both phases include charge of alkali and oxygen to each of said first and second phase.
  • the system is further distinguished in that both the first and second phase is pressurized by said pumps to an initial pressure exceeding 5 bar in each of the oxygen delignification reactors, and after the first phase is the pulp depressurized to an excess pressure below 0.5 bar over a valve located in an outlet from the first oxygen delignification reactor, preferably depressurized to atmospheric pressure, i.e. within a pressure interval between 0 to 0.5 bar, in a vented standpipe.
  • Residual gases released from the pulp during depressurization are vented away in a degassing line connected to the standpipe before the start of the second phase, and wherein the charge of oxygen to the second phase is charged to a second oxygen mixer to the pulp after the residual gases has been vented away, and wherein the charge of oxygen to the second phase is distributed into the pulp using the second mixer, thus establishing increased partial pressure of the oxygen in the pulp in a second oxygen delignification reactor.
  • the system is designed in such a way that more than 90% of the inert gases, such as carbon monoxide and carbon dioxide, formed during the oxidation process in the first phase, are vented away by the depressurization over the valve located in the outlet from the first oxygen delignification reactor.
  • the pulp suspension for the depressurization effect is fed from the valve and to an upper part of a standpipe and exposed to pressure in the range 0-0.5 bar in the upper part of the standpipe having a height exceeding 3 meters.
  • a stand pipe connected to atmosphere and with this height enable a sufficient practical volume for establishing a retention time in this stand pipe that may allow inert gases to separate over time.
  • the system is designed such that the first phase is divided into at least 2 zones, with reactors in each zone and both zones includes charge of oxygen to each of said first and second zones of the first phase using mixers ahead of each zone.
  • this staging of zones enables maximal charges of oxygen to each phase and zones, without causing losses of oxygen in subsequent degassing and minimum risks for gas channeling in the system.
  • This kind of staging is also preferably designed such that the retention time for the pulp suspension in the first phase is shorter than the retention time in the second phase, and that the retention time of the first zone in the first phase is shorter than the retention time of the second zone in the first phase, said retention times established by increasing storage volume in reactors of each phase or zone.
  • the medium consistency cellulose pulp suspension fed to the first phase obtained from a preceding thickening process producing a high consistency cellulose pulp at a consistency above 30% is produced by mixing the high consistency cellulose pulp from the thickening process with oxidized filtrate obtained from a filtrate tank in a wash arranged after the last phase and having passed through an oxidizing reactor (RE).
  • RE oxidizing reactor
  • reactors indicated to be hydraulically filled with the pulp suspension and in the same manner is the retention volume of the pulp suspension in the stand pipes indicated in the same way.
  • FIG 1 a first embodiment of the inventive oxygen delignification stage located between 2 wash positions W 1 and W 2 in a fiberline producing bleached qualities of cellulose pulp.
  • the pulp may be obtained from any kind of continuous or batch chemical pulping process and even mechanical pulp, but most preferably the pulp is obtained from a continuous kraft pulping process.
  • the oxygen delignification system is typically located directly after a pulp screening stage or immediately preceding said pulp screening stage.
  • oxygen delignification including chlorine dioxide delignification and/or bleaching, alkali extraction, peroxide bleaching, ozone bleaching, hot acid treatment, chelating stages, etc.
  • Pulp is fed to the oxygen delignification stage from a wash position W 1 .
  • a wash press where the pulp fed to a standpipe 10 has a high consistency and the wash filtrate sent to a filtrate tank FT 1 .
  • the pulp is diluted to medium consistency in the standpipe by adding filtrate from the filtrate tank FT 2 that is obtained from the second wash press W 2 , together with the bulk charge of alkali necessary for establishing the alkaline conditions for the oxygen stage.
  • the alkali charge is typically in the order of 25 kg/ADT pulp and the consistency about 12%.
  • a protector in form of a minor charge of MgSO4 is also charged.
  • the temperature of the pulp suspension in this stage is typically around 85-95°C.
  • the pulp suspension is initially pressurized by a first pump P 1 to a pressure above 5 bar(e), and preferably about 10 bar, and this pump also bring about a mixing effect of the added liquid charges (alkali, in form of sodium hydroxide oxidized white liquor or white liquor, and filtrate).
  • the conditions are now set for starting the oxygen delignification which starts with passing the medium consistency cellulose pulp through a mixer M 2 dedicated for mixing oxygen into the pulp suspension.
  • the pulp suspension is fed to an upflow tower, i.e. an oxygen delignification reactor O2 1B , wherein the oxygen delignification process proceeds.
  • the standpipe is sufficiently high, typically more than 5 meter, and enable also inert gases dissolved in the liquid phase to release over time. In the bottom of the standpipe 11 will most of the inert gases formed in first phase have been released and vented to atmosphere.
  • Next pump P 2 pressurize the pulp suspension again to a pressure above 5 bar(e), and preferably about 10 bar, and this pump also bring about a mixing effect of the added liquid charges (alkali).
  • the conditions are now set for starting a second phase of the oxygen delignification which starts with passing the medium consistency cellulose pulp through a second mixer M 3 dedicated for mixing a second fresh charge oxygen into the pulp suspension.
  • This second mixer M 3 is preferably also used to mix in steam.
  • the amount of steam added is typically in the order that an increase of about 5°C is obtained in the pulp suspension, reaching a temperature of about 100-105°C. The order of temperature increase is dependent on the amount of exothermic heating in previous stages.
  • the pulp suspension is fed to a second or final upflow tower, i.e. an oxygen delignification reactor O2 2 , wherein the oxygen delignification process proceeds in a second phase.
  • the consumption of alkali and oxygen is moderate and the amount of inert gases such as CO and CO 2 formed are produced at a far lower rate and at less volume.
  • the standpipe is sufficiently high, typically more than 5 meter, and enable also inert gases dissolved in the liquid phase to release over time. In the bottom of the standpipe 12 will most of the inert gases formed in first phase have been released and vented to atmosphere.
  • the vented pulp suspension is fed to a final wash press W 2 , conventionally called the oxygen wash position, that ends the oxygen delignification stage.
  • the wash filtrate obtained from this final wash press W 2 is collected in a second filtrate tank FT 2 , and used as dilution liquid in the first standpipe 10.
  • This wash filtrate is also normally used as washing/displacement liquid in the first wash press W 1 .
  • the embodiment shown in figure 1 is preferably used for oxygen delignification of low kappa pulp and with filtrate having low content of COD.
  • FIG 2 a second embodiment of the inventive oxygen delignification stage located between 2 wash positions W 1 and W 2 in a fiberline producing bleached qualities of cellulose pulp.
  • This second embodiment differs from the first embodiment by an additional pre-reactor O2 1A forming a first zone in the first phase.
  • This additional pre-reactor adds yet an oxygen delignification with an additional mixer M 1 ahead of this additional pre-reactor O2 1A , and may suitably be designed as a vertical pipe loop, or using two standard standpipes together with an upper bend connecting the standpipes.
  • the second zone of the first phase may follow directly in reactor O2 1B .
  • the embodiment shown in figure 2 is preferably used for oxygen delignification of medium kappa pulp or with filtrate having medium concentration of COD, where a slightly larger order of oxidation takes place in first phase.
  • FIG 3 a third embodiment of the inventive oxygen delignification stage located between 2 wash positions W 1 and W 2 in a fiberline producing bleached qualities of cellulose pulp.
  • This third embodiment differs from the first embodiment by an additional pre-reactor O2 1A forming a first zone in the first phase, and a subsequent standpipe 14.
  • This additional standpipe 14 adds yet a position for venting of inert gases from the pulp suspension.
  • this embodiment is also degassing MC-pumps used in all MC pumps P 1A , P 1B , P 2 and P 3 , enabling venting of inert gases ahead of all oxygen mixers M 1 , M 2 and M 3 , as well as ahead of the final wash W 2 .
  • the embodiment shown in figure 3 is preferably used for oxygen delignification of medium kappa pulp and with filtrate having medium concentration of COD, where a slightly larger order of oxidation takes place in first phase.
  • FIG 4 is disclosed a fourth embodiment of the inventive oxygen delignification stage located between 2 wash positions W 1 and W 2 in a fiberline producing bleached qualities of cellulose pulp.
  • This fourth embodiment differs from the third embodiment by an additional oxidation reactor RE for the filtrate pumped by pump P 4 from the filtrate tank FT 2 and to standpipe 10.
  • Both oxygen and alkali may be added to the oxidation reactor RE, as well as additional oxidation chemicals such as peroxide (H 2 O 2 ).
  • the oxidant added to the pulp suspension may most of the oxidant added to the pulp suspension be used for delignification of the lignin content of the pulp, and almost no oxidation of dissolved lignin or other organic content in the liquid phase of the pulp suspension takes place in presence of pulp, avoiding viscosity losses in the pulp due to formation of hydroxyl radicals when oxidizing COD content in the liquid phase.
  • the embodiment shown in figure 4 is preferably used for oxygen delignification of high kappa pulp and with filtrate having high concentration of COD, where the largest order of oxidation takes place in first phase.
  • the residence time in reactors O2 1A , O2 1B and O2 2 should be continuously increasing.
  • the residence time in a pre-reactor like O2 1A may be in the range 1-10 minutes
  • the residence time in a second reactor like O2 1B in the second zone of the first phase may be in the range 20-60 minutes
  • the residence time in a reactor like O2 2 in the second or final phase may be in the range 40-180 minutes.
  • the residence time of the first phase may be shorter than 20 minutes, and preferably in the range 5-60 minutes in total, followed by a residence time in the range 40-180 minutes for the second phase.
  • inert gases formed during a first phase of the oxygen delignification stage vented away ahead of the final phase in the oxygen delignification stage, such that the oxygen charge added to the final phase may obtain highest possible level of oxygen solved in the liquid phase of the pulp suspension.
  • the oxidation produces more inert gases, with higher kappa number and/or higher COD content in filtrate, may additional venting be implemented also after a first zone in the first phase.
  • What embodiment of the invention is to be chosen depends on the rate and amount of oxidation that occurs in first phase, which order of oxidation may be controlled by measuring the temperature profile of the pulp suspension. If the temperature increase due to the exothermic reactions are modest and slow it may be fully sufficient with a 2-reactor system, with venting in between, and further costs for a third reactor and additional mixer could likely not be motivated by the smaller improvement in selectivity. If the temperature increase is very rapid in the first phase it is fair to assume that the filtrate contains high COD content, as this COD content is much easier to oxidize than the organic matter bound to the cellulose, and hence the motivation to invest in a filtrate oxidation reactor RE may be fully motivated by the improvement in selectivity.

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Claims (11)

  1. Procédé de délignification à l'oxygène d'une suspension de pâte de cellulose de consistance moyenne ayant un indice kappa dépassant 18,
    ladite suspension de pâte passant par une première et une seconde phases de délignification à l'oxygène situées entre 2 positions de lavage (W1, W2) pour la pâte, où lesdites phases sont séparées en chauffant la pâte à au moins 5 °C en utilisant de la vapeur après la première phase et avant la seconde phase, et les deux phases comportent une charge d'oxygène pour chacune desdites première et seconde phases ; caractérisé en ce que
    à la fois les première et seconde phases sont pressurisées à une pression initiale dépassant 5 bar,
    et, après la première phase, la pâte est dépressurisée à une surpression en-dessous de 0,5 bar, dépressurisée de préférence à la pression atmosphérique, c'est-à-dire, dans un intervalle de pression entre 0 et 0,5 bar,
    et les gaz résiduels libérés de la pâte durant la dépressurisation, sont évacués à l'atmosphère avant le début de la seconde phase,
    et dans lequel la charge d'oxygène pour la seconde charge est introduite dans la pâte après que les gaz résiduels ont été évacués à l'atmosphère, et dans lequel la charge d'oxygène pour la seconde phase est dispersée dans la pâte en utilisant un mélangeur, instaurant ainsi une pression partielle augmentée de l'oxygène dans la suspension de pâte.
  2. Procédé selon la revendication 1, caractérisé en ce que plus de 90 % des gaz inertes, tel que du monoxyde de carbone et du dioxyde de carbone, formés durant le processus d'oxydation dans la première phase, sont évacués à l'atmosphère par la dépressurisation, et dans lequel la suspension de pâte, pour l'effet de dépressurisation, est introduite dans une partie supérieure d'une colonne montante et exposée à une pression dans la plage de 0 à 0,5 bar dans la partie supérieure de la colonne montante ayant une hauteur dépassant 3 mètres.
  3. Procédé selon la revendication 1, caractérisé en ce que la première phase est divisée en au moins 2 zones, et les deux zones comportent une charge d'oxygène pour chacune desdites première et seconde zones de la première phase.
  4. Procédé selon la revendication 3, caractérisé en ce que le temps de rétention pour la suspension de pâte dans la première phase est plus court que le temps de rétention dans la seconde phase, et que le temps de rétention de la première zone dans la première phase est plus court que le temps de rétention de la seconde zone dans la première phase.
  5. Procédé selon la revendication 1, caractérisé en ce que la suspension de pâte de consistance moyenne alimentée dans la première phase est obtenue à partir d'un processus d'épaississement précédent produisant une pâte de cellulose de consistance élevée à une consistance au-dessus de 30 %, et que la suspension de pâte de cellulose de consistance moyenne est produite en mélangeant la pâte de cellulose de consistance élevée provenant du processus d'épaississement avec du filtrat oxydé.
  6. Procédé selon la revendication 3, caractérisé en ce que, dans et après la première zone dans la première phase, la pâte est dépressurisée jusqu'à une surpression en-dessous de 0,5 bar, de préférence, dépressurisée à la pression atmosphérique, c'est-à-dire dans un intervalle de pression entre 0 et 0,5 bar
    et les gaz résiduels libérés de la pâte durant la dépressurisation sont évacués à l'atmosphère avant le début de la seconde zone de la première phase,
    et dans lequel une charge d'oxygène vers la seconde zone dans la première phase est introduite dans la pâte après que les gaz résiduels ont été évacués à l'atmosphère, et dans lequel la charge d'oxygène dans la seconde zone de la première phase est dispersée dans la pâte en utilisant un mélangeur, établissant ainsi une pression partielle augmentée de l'oxygène dans la pâte.
  7. Système de délignification à l'oxygène d'une suspension de pâte de cellulose de consistance moyenne ayant un indice kappa dépassant 18, et où ledit système est situé entre 2 positions de lavage (W1, W2)
    ladite suspension de pâte de consistance moyenne étant pressurisée une première fois par une première pompe (P1A) passant la pâte vers au moins un premier mélangeur à oxygène (M2) et directement après, vers au moins un premier réacteur de délignification à l'oxygène (021B) dans une première phase de délignification, et, après la première phase de délignification, la suspension de pâte est chauffée dans un mélangeur à vapeur (M3) avant une seconde phase dans un second réacteur de délignification à l'oxygène (022) de sorte que lesdites phases sont séparées en chauffant la pâte d'au moins 5 °C en utilisant de la vapeur après la première phase et avant la seconde phase, et les deux phases comportent une charge d'oxygène vers chacune desdites première et seconde phases ; et une charge d'alcali vers l'au moins une première phase, caractérisé en ce que
    les deux première et seconde phases sont pressurisées par lesdites pompes à une pression initiale dépassant 5 bar dans chacun des réacteurs de délignification à l'oxygène,
    et après la première phase, la pâte est dépressurisée à une surpression en-dessous de 0,5 bar par une vanne (V2) située à une sortie à partir du premier réacteur de délignification à l'oxygène, dépressurisée de préférence à la pression atmosphérique, c'est-à-dire, dans un intervalle de pression entre 0 et 0,5 bar, dans une colonne montante (11) ventilée,
    les gaz résiduels libérés à partir de la pâte durant la dépressurisation sont évacués à l'atmosphère dans une conduite de dégazage (DG1) reliée à la colonne montante avant le début de la seconde phase,
    et dans lequel la charge d'oxygène vers la seconde phase est introduite dans un second mélangeur à oxygène (M3) dans la pâte après que les gaz résiduels ont été évacués à l'atmosphère, et dans lequel la charge d'oxygène introduite dans la seconde phase est dispersée dans la pâte en utilisant un second mélangeur, établissant ainsi une pression partielle augmentée de l'oxygène dans la pâte dans un second réacteur de délignification à l'oxygène (022).
  8. Système selon la revendication 7, caractérisé en ce que plus de 90 % des gaz inertes, tel que du monoxyde de carbone et du dioxyde de carbone, formés durant le processus d'oxydation dans la première phase, sont évacués à l'atmosphère par la dépressurisation par la vanne (V2) située dans la sortie du premier réacteur de délignification à l'oxygène (O21B) et dans lequel la suspension de pâte destinée à l'effet de dépressurisation est alimentée à partir de la vanne et dans une partie supérieure d'une colonne montante et exposée à une pression dans la plage de 0 à 0,5 bar dans la partie supérieure de la colonne montante ayant une hauteur dépassant 3 mètres.
  9. Système selon la revendication 7, caractérisé en ce que la première phase est divisée en au moins 2 zones, avec des réacteurs dans chaque zone et les deux zones comportent une charge d'oxygène pour chacune desdites première et seconde zones de la première phase en utilisant des mélangeurs avant chaque zone.
  10. Système selon la revendication 9, caractérisé en ce que le temps de rétention de la suspension de pâte dans la première phase est plus court que le temps de rétention dans la seconde phase, et que le temps de rétention de la première zone dans la première phase est plus court que le temps de rétention de la seconde zone dans la première phase, lesdits temps de rétention étant établis en augmentant le volume de stockage dans les réacteurs de chaque phase ou zone.
  11. Système selon la revendication 9, caractérisé en ce que la suspension de pâte de cellulose de consistance moyenne alimentée dans la première phase est obtenue à partir d'un processus d'épaississement (W1) précédent produisant une pâte de cellulose de consistance élevée à une consistance au-dessus de 30 %, et que la suspension de pâte de cellulose de consistance moyenne est produite en mélangeant la pâte de cellulose de consistance élevée provenant du processus d'épaississement avec un filtrat oxydé obtenu à partir d'un réservoir de filtrat dans un lavage agencé après la dernière phase et ayant passé à travers le réacteur d'oxydation (RE).
EP16868982.6A 2015-11-27 2016-11-16 Procédé et système de délignification à l'oxygène de pâte cellulosique Active EP3380667B1 (fr)

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SE1551539A SE540043C2 (en) 2015-11-27 2015-11-27 Method and system for oxygen delignification of cellulose pulp
PCT/SE2016/051128 WO2017091129A1 (fr) 2015-11-27 2016-11-16 Procédé et système de délignification à l'oxygène de pâte cellulosique

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DE102020002445A1 (de) 2020-04-23 2021-10-28 Messer Austria Gmbh Verfahren und Vorrichtung zur Herstellung von gebleichtem Zellstoff
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US4946555A (en) * 1989-01-19 1990-08-07 Canadian Liquid Air Ltd./Air Liquide Canada Apparatus and method for measuring vent gas flow rates and parameters in pulp and paper processing
US6514380B1 (en) * 1995-03-08 2003-02-04 Andritz Oy Treatment of chemical pulp
SE505147C2 (sv) * 1995-10-19 1997-06-30 Sunds Defibrator Ind Ab Syrgasdelignifiering av massa i ett första HC-steg och ett andra MC-steg
FI955519L (fi) * 1995-11-16 1997-05-17 Ahlstrom Machinery Oy Menetelmä ja laitteisto kemiallisen massan delignifioimiseksi
CN1203643A (zh) * 1995-12-07 1998-12-30 贝洛特工艺技术公司 中等稠度纸浆的氧化去木质作用
US20010050152A1 (en) * 1996-03-26 2001-12-13 Kjell Forslund Oxygen delignification of pulp in two stages
US6221207B1 (en) * 1996-03-26 2001-04-24 Valmet Fibertech Aktiebolag Oxygen delignification of pulp in two stages with low pressure steam heating between stages
EP1061173A1 (fr) * 1999-06-14 2000-12-20 Praxair Technology, Inc. Délignification de matériaux lignocellulosiques avec de l'oxygène
SE522593C2 (sv) * 1999-07-06 2004-02-24 Kvaerner Pulping Tech System och förfarande för syragasdelignifiering av massa av lignocellulosahaltigt material
SE525773C2 (sv) * 2003-09-24 2005-04-26 Kvaerner Pulping Tech Metod och arrangemang för syrgasdelignifiering av cellulosamassa med pH-reglering i slutfasen
SE0403202L (sv) * 2004-12-30 2005-10-25 Kvaerner Pulping Tech Metod för syrgasdelignifiering av cellulosamassa med inmixning av kemikalier vid högt tryck
SE0403222L (sv) * 2004-12-30 2005-11-08 Kvaerner Pulping Tech Metod för syrgasdelignifiering av cellulosamassa vid högt tryck i flera steg

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WO2017091129A1 (fr) 2017-06-01
SE1551539A1 (en) 2017-05-28
BR112018005525A2 (pt) 2018-10-09
SE540043C2 (en) 2018-03-06
EP3380667A4 (fr) 2019-04-17
BR112018005525B1 (pt) 2022-03-29
EP3380667A1 (fr) 2018-10-03

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