US20070131363A1 - Fiberline systems, processes and methods - Google Patents

Fiberline systems, processes and methods Download PDF

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Publication number
US20070131363A1
US20070131363A1 US11/548,911 US54891106A US2007131363A1 US 20070131363 A1 US20070131363 A1 US 20070131363A1 US 54891106 A US54891106 A US 54891106A US 2007131363 A1 US2007131363 A1 US 2007131363A1
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Prior art keywords
black liquor
steam
flashing
digester
evaporator
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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.)
Abandoned
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US11/548,911
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English (en)
Inventor
Auvo Kettunen
Jarmo Kaila
Bertil Stromberg
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Andritz Inc
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Andritz Inc
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Publication date
Application filed by Andritz Inc filed Critical Andritz Inc
Priority to US11/548,911 priority Critical patent/US20070131363A1/en
Priority to JP2006284495A priority patent/JP4878982B2/ja
Priority to FI20060928A priority patent/FI123103B/fi
Priority to CA2565358A priority patent/CA2565358C/fr
Priority to RU2006137408/12A priority patent/RU2404316C2/ru
Priority to SE0602249A priority patent/SE532462C2/sv
Priority to BRPI0604341-0A priority patent/BRPI0604341B1/pt
Assigned to ANDRITZ INC. reassignment ANDRITZ INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: KAILA, JARMO, KETTUNEN, AUVO, STROMBERG, BERTIL C.
Publication of US20070131363A1 publication Critical patent/US20070131363A1/en
Priority to US13/096,923 priority patent/US20110198049A1/en
Abandoned legal-status Critical Current

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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
    • 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

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  • the manner of handling the extracted black liquor from the digester is to pass the black liquor to a pre-evaporation system comprising two flash tanks and a series of exchangers and then to pass the resulting liquor to other equipment in an evaporation/recovery phase. See, e.g., FIG. 1 .
  • one embodiment of a continuous cooking and recovery system, process and method utilizes one or more streams of black liquor extracted from the cooking system (i.e., the cooking system, which is also known as the digester system or digester plant, includes the chip bin through the digester—and optionally including an impregnation vessel) in an evaporation/recovery system after any pre-heater (if applicable) and without any pre-evaporation system (i.e., pre-evaporation equipment being equipment such as flash tanks, reboilers and exchangers where steam is generated as the black liquor is cooled prior to sending the black liquor to the evaporation system in the recovery area).
  • pre-evaporation equipment being equipment such as flash tanks, reboilers and exchangers where steam is generated as the black liquor is cooled prior to sending the black liquor to the evaporation system in the recovery area.
  • black liquor from the digester is sent to a flash tank and then to the evaporation/recovery system without using any flashing steam condenser.
  • the embodiments of the invention result in the improvement of the steam economy of the fiberline system, improved recovery of the various ingredients used in the system, reduction of foul condensate and malodorous gases, and/or reduced equipment and system requirements.
  • FIG. 1 is a schematic view illustrating a conventional fiberline system.
  • FIG. 2 is a schematic view illustrating a pre-evaporation and evaporation portion of a conventional fiberline system.
  • FIG. 3 is a schematic view illustrating an evaporation portion of a fiberline system according to an embodiment the present invention.
  • FIG. 4 is a schematic view illustrating an evaporation portion of a fiberline system according to an embodiment the present invention.
  • FIG. 5 is a schematic view illustrating a portion of a conventional fiberline system.
  • FIG. 6 is a schematic view like that of FIG. 5 , but illustrating an embodiment the present invention.
  • FIG. 7 is a schematic view like that of FIG. 5 , but illustrating another embodiment the present invention.
  • FIG. 12 . 2 (simplified as FIG. 1 herein) is an example of the current state of the art with regard to pre-evaporation and evaporation systems, including the following technology terms:
  • Pre-heaters in FIG. 1 , see the exchangers identified as “Pre-Heaters” in the extraction line from the digester whose purpose is to use some of the heat in the extracted black liquor to “pre-heat” white liquor, other black liquor streams or other liquid streams being sent to the digester or feed system.
  • Evaporator System in FIG. 1 , see the circled section identified as “EVAP.”
  • EVAP Evaporator System
  • I through N The effects are numbered I through N, with I operating at the highest temperature and N operating at the lowest temperature.
  • the current state of the art utilizes a fiberline system with a chip bin 100 where steaming of wood chips or other cellulose material may or may not be occurring, liquid is added to form a slurry, followed by pressurization of the slurry (this section is also referred to as the feed system), fed to a treatment vessel or vessels (could be an impregnation vessel, a pre-hydrolysis process or other vessels), followed by a digester 5 (this section is also referred to as the cooking system).
  • a black liquor stream typically at a temperature of 110-150° C.
  • the extracted black liquor stream or streams are used as a source of heat to “pre-heat” white liquor, other black liquor streams, and/or other liquid streams being sent to the feed and cooking systems.
  • the extracted black liquor stream (or streams) is then sent to the pre-evaporation system, e.g., two or more flash tanks 10 , 20 and/or reboilers where steam is produced from the hot black liquor as the liquor is cooled, typically to temperatures of about 95-110° C. At this point, the black liquor is sent to the evaporator system “EVAP” in the recovery area.
  • the “cool” black liquor entering the recovery area is stored in a “weak black liquor”(WBL) tank 30 until fed to the evaporator system.
  • the evaporator system consists of a series of effects (numbered I to VI in FIG. 2 ) each operating at different temperatures and/or conditions to allow for the production of steam while cooling and concentrating the WBL.
  • the concentration of the black liquor leaving effect I i.e., the highest temperature effect, is about 75% solids, and is sent to a recovery boiler (not shown) to be burned while the liquid stream out of the last effect VI is condensate at the lowest temperature (65° C. in FIG. 2 ) of the various effects and is used throughout the mill.
  • the WBL is introduced into the evaporator system at the effect which is most appropriate (e.g., effect IV in FIG. 2 ), that means the effect where the temperature of the WBL will allow flashing to produce steam, typically the third or fourth effect.
  • effect IV the effect where the temperature of the WBL will allow flashing to produce steam
  • the black liquor flow is split, going in either direction (some black liquor goes to hotter effects, which allows for the evaporation of the liquid and concentration of solids, other black liquor goes to lower temperature effects and is heated and then sent to higher temperature effects for concentration).
  • the solids content in the black liquor from the first effect is set (solids content such as 75% in FIG. 2 ).
  • One of the embodiments of the subject invention eliminates the pre-evaporator system. See FIGS. 3 and 4 .
  • the temperature of the WBL when sent to the recovery area is higher, thereby allowing for the WBL introduction into the evaporator system at an effect that will allow for a greater production of steam.
  • the steam produced in this inventive evaporator system is cleaner than that produced in a pre-evaporator system at the digester area.
  • the cleaner steam is suitable for use as steam for the chip bin 100 and can be drawn off the evaporator system between effects so that the steam going to the chip bin 100 has a temperature suitable for this use and thereby eliminates a steaming vessel, thus allowing for more efficient use of the steam produced in the mill.
  • An advantage of this inventive process is the reduction of contaminates introduced into the chip bin in the steam, which, in turn, reduces contaminates in the gas vented out of the chip bin.
  • the cleaner steam produced in the evaporation system and used in the chip bin 100 reduces adverse emissions from the mill.
  • This inventive process also allows for the elimination of the WBL storage tank external to the train of the evaporator system.
  • the WBL storage tank can become part of the evaporator system train, not external to the training, thereby saving costs.
  • the exemplary evaporator system shown in FIGS. 3 and 4 has other improvements over the conventional systems of FIGS. 1 and 2 .
  • the black liquor stream coming from the digester 5 to the evaporator system is higher in temperature. This stream can be sent directly to the appropriate effect in the evaporation system to improve the steam efficiency of the mill.
  • a pressurized fiber filter 40 can be located in the line between the digester and the evaporator system to allow the removal of fiber from the black liquor stream to a level of about 40 ppm leaving the filter.
  • the fiber material removed from the filter would be in the form of a slurry to be returned to the digester 5 or feed system.
  • the temperature of the stream entering the filter is too low (95-130° C.); thus, this stream material must be returned to the feed system to be reheated to cooking temperature prior to further treatment.
  • the higher temperature of the black liquor stream from the digester to the evaporator system means the filtered material is at a higher temperature. This higher temperature material is closer to the cooking temperature and therefore can be returned to the top of the digester, reducing the overall need for heat addition.
  • a small portion of the stream from the digester could be sent through a cooler 50 and to a smaller tank 30 and to the evaporator system at the appropriate effect.
  • the inventive system has never been contemplated or used before because it has never been considered to “connect” the digester/cooking area and the recovery area because of the distance between the two areas in the mill and other factors. Another reason is the reliability of the separation of each area. It is undesirable to have one of these areas “upset” that would cause a shutdown in the other area. Particularly detrimental are upsets at the recovery area that would cause the digester to be shut down. In short, loosing one area could cause extreme problems in the other area. The inventive process overcomes these problems.
  • a chemical pulping system, method and process utilizes a flashing tank.
  • the prior art is first described, followed by the inventive embodiments.
  • cooking liquor at a high temperature is discharged from a continuous digester.
  • the discharged amount is 8-12 m 3 /ADMT and the temperature on average is about 130-170° C.
  • the cooking liquor discharged from the digester i.e., black liquor
  • flows to an evaporation plant containing pre-evaporation and evaporation systems
  • almost all the water present in the black liquor is removed in several evaporation effects connected in series prior to black liquor combustion.
  • Various black liquor evaporation effects use fresh steam and flashing steam obtained from effects having a higher temperature and pressure.
  • the black liquor is led into a non-pressurized storage tank prior to the actual evaporation.
  • the temperature of the black liquor Prior to the storage tank, the temperature of the black liquor is decreased below 100° C. for preventing boiling in the tank. Between the digester and the storage tank of the evaporation plant, a very large amount of heat—1-4 GJ/ADMT—is removed from the black liquor.
  • the amount of water flashing i.e., vaporizing
  • the temperature of the black liquor in the flashing tank decreases at best to a level of about 110° C., whereby the amount of water being vaporized is between 0.3-1.3 m 3 /ADMT.
  • Final cooling below 100° C. is typically performed indirectly in a heat exchanger, simultaneously providing hot water for pulp washing.
  • the amount of heat transferred into the flashing steam is typically utilized in chip steaming.
  • chip steaming the chips are heated and the air contained therein is removed by means of steam, whereby significant advantages are achieved for the digesting process.
  • steam is consumed during chip steaming, depending on the chip properties and the steaming method, in the amount of about 0.5-2 GJ/ADMT. As the above calculations indicate, the situation often is such that flashing steam is available in excess of steaming purposes.
  • this excess flashing steam is led to a separate flashing steam condenser, where water vapor is condensed and simultaneously hot water is obtained.
  • the flashing steam contains compounds referred to as non-condensable gases (methanol, turpentine, various sulfur compounds etc.), which are removed from the condenser in gaseous form and at high concentration. These gases are called concentrated malodorous gases.
  • a chemical pulp mill also produces so-called weak malodorous gases, wherein the content of malodorous compounds is maintained under explosive concentration.
  • Condensed flashing steam contains other compounds in addition to water, and it is called foul condensate.
  • the non-condensable gases generated in the flashing steam condenser and the foul condensate are led into other plants of the mill for further treatment, because if released into the atmosphere they would cause a significant emission problem.
  • the concentrated malodorous gases and foul condensate are toxic and explosive, the treatment thereof is dangerous and requires particular care.
  • FIG. 5 illustrates a typical system for utilizing the heat of black liquor exiting the digester in a modern pulp mill.
  • Black liquor from the digester enters the flashing tank 1 via pipe 4 .
  • black liquor may be discharged to pipe 4 from more than one zone.
  • flashing steam is separated from the black liquor, which steam is led via pipe 5 into an atmospheric steaming phase and, depending on the situation, via pipe 6 to the flashing steam condenser 2 .
  • More than one condenser may be used for condensing the flashing steam.
  • the flashing steam condenser receives cold (about 0-30° C.) or warm (about 40-60° C.) water via pipe 11 .
  • the temperature of this water increases and it discharges as hot water (about 65-90° C. ) via pipe 12 into the hot water system of the mill.
  • Condensed steam exits as foul condensate via pipe 10 typically into the foul condensate system of the digester plant and therefrom further to a foul condensate container of the evaporation plant.
  • the non-condensable gases i.e. concentrated malodorous gases, exit via pipe 9 into the concentrated gases collection and treatment system.
  • the black liquor flashed and cooled in the flashing tank exits via pipe 7 to black liquor cooler 3 . There the temperature of the black liquor decreases further and it is discharged to the black liquor storage tank of the evaporation plant via pipe 8 .
  • the water used for black liquor cooling enters the cooler via pipe 13 and exits into the hot water system via pipe 14 .
  • the objective of this embodiment of the invention is to utilize the excess flashing steam in a simple way, and simultaneously prevent the generation of concentrated malodorous gases and foul condensates in the digesting plant.
  • the solution according to this embodiment of the invention does not use a flashing steam condenser, but the excess flashing steam is led directly to a suitable evaporation stage of the evaporation plant, where it partly replaces fresh steam and thus improves the steam economy of the evaporation plant. Simultaneously, generation of foul condensate and concentrated malodorous gases in the area of the digester plant is prevented and the treatment thereof can to that extent be restricted to the evaporation plant, where they are inevitably treated anyway.
  • a process devoid of a flashing steam condenser and treatment of concentrated malodorous gases and foul condensate is naturally smaller than a conventional process, including a favorable decrease in investment costs.
  • FIG. 6 illustrates a solution according to this embodiment of the invention for flashing black liquor and utilizing flashing steam.
  • Black liquor from the digester enters the flashing tank 1 via pipe 4 .
  • black liquor may be discharged to pipe 4 from more than one zone.
  • flashing steam is separated from the black liquor and led via pipe 5 to a steaming phase operating at atmospheric pressure and via pipe 15 to the evaporation plant into a suitable condenser or other preferable location. No flashing steam condenser is used. As a result, the generation of foul condensate and concentrated malodorous gases in the digester plant may be prevented.
  • the black liquor flashed and cooled in the flashing tank exits via pipe 7 to black liquor cooler 3 .
  • the temperature of the black liquor decreases further and it is discharged to the evaporation plant via pipe 8 (for example, into a black liquor storage tank).
  • the water used for black liquor cooling enters the cooler via pipe 13 and exits into the hot water system via pipe 14 .
  • FIG. 7 illustrates another embodiment where the flashing steam is led to chip steaming only, and there is no flashing steam condenser.
  • the black liquor from the digester enters the flashing tank 1 via pipe 4 .
  • black liquor may be removed from more than one zone.
  • flashing steam is separated from the black liquor, and flashing steam is led via pipe 5 only into an atmospheric steaming phase. Because no flashing steam condenser is used, generation of foul condensate and concentrated malodorous gases in the digesting plant may be prevented.
  • the black liquor flashed and cooled in the flashing tank exits via pipe 7 to a black liquor cooler 3 .
  • the temperature of the black liquor decreases further and it is discharged to the evaporation plant via pipe 8 (e.g., into a black liquor storage tank).
  • the water used for cooling black liquor enters the cooler via pipe 13 and exits into a hot water system via pipe 14 .
  • this embodiment is a novel and good solution and prevents generation of concentrated malodorous gases and foul condensate in the digester plant, it may have some drawbacks that can be addressed as follows. If flashing steam is available in greater amounts than needed for steaming, there is no way of utilizing this excess steam. Another disadvantage becomes obvious during shutdowns of the plant, whereby the flashing steam may not be led to steaming and no flashing of black liquor takes place. For this reason, the constructional pressure of the flashing tank should be significantly higher than normal in order to resist the high pressure resulting from the high temperature. Further, the cooling capacity of the black liquor cooler has to be much higher than normal, so that the black liquor may be cooled under 100° C. even in this situation.
  • flashing steam in evaporation has also been practiced in connection with various pre-evaporation solutions.
  • black liquor is flashed in several stages and flashing steam from a preceding stage is used for flashing of black liquor in the following stage.
  • the flashing steam used in chip steaming is typically obtained from some pre-evaporator, and not directly from the flashing tank.
  • the mill also has a normal evaporation plant, where the dry solids content of the black liquor is increased to a level high enough for combustion.
  • the pre-evaporation plant solutions have often been complicated processes and prone to black liquor foaming. For these reasons, pre-evaporation plants are undesireable.
  • Another challenging situation might occur if the evaporation plant is not in operation while the digester plant is operating. This situation is very rare and short-term because the black liquor storage tank between the digester plant and the evaporation plant fills quickly and would not permit the digester plant to operate without the operation of the evaporation plant.
  • the previously presented solution may be utilized, where flashing steam is used for chip steaming only.
  • the sizing of the flashing tank and the black liquor cooler should be engineered for a situation where no flashing steam is removed from the black liquor.
  • Another solution is to lead the excess flashing steam to a condenser in the evaporation plant.
  • Possible condensers include, e.g., a surface condenser following the evaporation plant or a condenser for a stripper used in cleaning foul condensates from the evaporation plant. During short-term disturbances in the evaporation plant, these condensers can preferably receive steam. In case of a longer-term shutdown of the evaporation plant, there is no reason to operate the digester plant.
  • the flashing steam from the flashing tank 1 may led into any of the evaporation stages in the evaporation plant, where the pressure is low enough. Because the typical operational pressure in the flashing tank is about 0.2-0.5 bar overpressure, the evaporation stages operating at atmospheric or lower pressure are suitable. The most preferable solution, however, is to lead the steam into an evaporation unit having the highest possible pressure, because that provides the largest possible saving of fresh steam. In a typical modern 7-stage evaporation plant, it would be most advantageous to lead the flashing steam to the third evaporator stage. In that case, the flashing steam would be present and working in five evaporation stages and allow for saving fresh steam in a proportion of 5:7. In other words, one kilogram of flashing steam would decrease the consumption of fresh steam by 5/7 kilos.
  • the use of flashing steam in the evaporation plant is most advantageous when the evaporation plant has at least six evaporation stages.
  • the principles of the invention may also be applied in situations where there is more than one flashing tank and also a pressurized steaming phase is used.
  • higher-pressure fractions may be separated from the total amount of flashing steam available, and the higher-pressure fractions may be used for various purposes.
  • the use of several flashing stages gives only a marginal benefit compared to the simple solution based on a single flashing stage according to the invention because, with the solution utilizing one flashing tank, all the flashing steam generated can be efficiently utilized in steaming and in the evaporation plant.
  • “Efficient use” of flashing steam means that it replaces fresh steam usage with high efficiency. For this reason, the solution according to the invention is most advantageous when using one flashing tank.

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US11/548,911 2005-10-24 2006-10-12 Fiberline systems, processes and methods Abandoned US20070131363A1 (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
US11/548,911 US20070131363A1 (en) 2005-10-24 2006-10-12 Fiberline systems, processes and methods
JP2006284495A JP4878982B2 (ja) 2005-10-24 2006-10-19 改良されたファイバーラインのシステム、プロセスおよび方法
FI20060928A FI123103B (fi) 2005-10-24 2006-10-23 Menetelmä ja järjestelmä mustalipeän paisuntahöyryn käyttämiseksi
CA2565358A CA2565358C (fr) 2005-10-24 2006-10-23 Systeme et procede fiberline utilisant de la vapeur de vaporisation a liqueur noire
RU2006137408/12A RU2404316C2 (ru) 2005-10-24 2006-10-23 Усовершенствованные системы линии для производства волокнистой массы, процессы и способы
SE0602249A SE532462C2 (sv) 2005-10-24 2006-10-24 Förfarande och system för avspänning av svartlut i indunstningssystem samt användning av därvid alstrad ånga
BRPI0604341-0A BRPI0604341B1 (pt) 2005-10-24 2006-10-24 Method for using black liquor volatilization vapor of a digester system for a chemical pulp and a chemical powder mill system
US13/096,923 US20110198049A1 (en) 2005-10-24 2011-04-28 Fiberline systems, processes and methods

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US72923905P 2005-10-24 2005-10-24
US11/548,911 US20070131363A1 (en) 2005-10-24 2006-10-12 Fiberline systems, processes and methods

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US13/096,923 Division US20110198049A1 (en) 2005-10-24 2011-04-28 Fiberline systems, processes and methods

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US20070131363A1 true US20070131363A1 (en) 2007-06-14

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US11/548,911 Abandoned US20070131363A1 (en) 2005-10-24 2006-10-12 Fiberline systems, processes and methods
US13/096,923 Abandoned US20110198049A1 (en) 2005-10-24 2011-04-28 Fiberline systems, processes and methods

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US13/096,923 Abandoned US20110198049A1 (en) 2005-10-24 2011-04-28 Fiberline systems, processes and methods

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US (2) US20070131363A1 (fr)
JP (1) JP4878982B2 (fr)
CN (1) CN101046073A (fr)
BR (1) BRPI0604341B1 (fr)
CA (1) CA2565358C (fr)
FI (1) FI123103B (fr)
RU (1) RU2404316C2 (fr)
SE (1) SE532462C2 (fr)

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JPS6094227A (ja) * 1983-10-26 1985-05-27 Daiichi Denko Kk ワイヤカツト放電加工用電極線
US20050115691A1 (en) * 2002-01-24 2005-06-02 Lindstroem Mikael Cooking of cellulose pulp in a cooking liquor containing preevaporated black liquor
CN100439267C (zh) * 2007-10-29 2008-12-03 山东泉林纸业有限责任公司 一种碱法和亚铵法混合草浆黑液、碱法和亚铵法混合浓缩草浆黑液及其制备方法
WO2009142681A3 (fr) * 2008-05-22 2010-01-14 Flsmidth A/S Procédé et appareil de traitement de la liqueur verte
US20100224335A1 (en) * 2009-03-05 2010-09-09 Andritz Inc. Heat recovery from spent cooking liquor in a digester plant of a chemical pulp mill
CN102134002A (zh) * 2011-01-21 2011-07-27 济南碧云天环保科技有限公司 一种物料加工线
US8709204B1 (en) * 2013-03-14 2014-04-29 Veolia Water Solutions & Technologies North America Inc. System and process for recovering heat from weak black liquor in a wood pulping process
CN105088847A (zh) * 2015-09-07 2015-11-25 武汉凯比思电力设备有限公司 一种由造纸黑液提取分离木质素的装置及方法
WO2016038247A1 (fr) * 2014-09-08 2016-03-17 Andritz Oy Procédé de génération de vapeur à une installation de lessiveur d'une usine de pâte chimique
EP3458643A4 (fr) * 2016-05-17 2019-12-11 Valmet Aktiebolag Procédé de génération de vapeur propre dans un système de digesteur continu

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FI121967B (fi) * 2009-11-19 2011-06-30 Metso Paper Inc KUITURAINAKONEEN KUIVATUSOSAN HöYRY- JA LAUHDEJARJESTELMA
CN102226319B (zh) * 2011-06-03 2013-04-10 长沙理工大学 一种间歇蒸煮冷喷放装置及冷喷放方法
US9644317B2 (en) 2014-11-26 2017-05-09 International Paper Company Continuous digester and feeding system
SE542991C2 (en) * 2019-03-29 2020-09-22 Valmet Oy A method and a system for extracting hydrolyzate in a continuous cooking process for producing pulp

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US20030164227A1 (en) * 1999-12-29 2003-09-04 Paivi Uusitalo Method for improved turpentine recovery from modern cooking plants

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JPS6094227A (ja) * 1983-10-26 1985-05-27 Daiichi Denko Kk ワイヤカツト放電加工用電極線
US20050115691A1 (en) * 2002-01-24 2005-06-02 Lindstroem Mikael Cooking of cellulose pulp in a cooking liquor containing preevaporated black liquor
US7351306B2 (en) * 2002-01-24 2008-04-01 Metso Fiber Karlstad Ab Cooking of cellulose pulp in a cooking liquor containing pre-evaporated black liquor
CN100439267C (zh) * 2007-10-29 2008-12-03 山东泉林纸业有限责任公司 一种碱法和亚铵法混合草浆黑液、碱法和亚铵法混合浓缩草浆黑液及其制备方法
WO2009142681A3 (fr) * 2008-05-22 2010-01-14 Flsmidth A/S Procédé et appareil de traitement de la liqueur verte
RU2532568C2 (ru) * 2009-03-05 2014-11-10 Андритц Инк. Рекуперация тепла из отработанной варочной жидкости в варочном котле на целлюлозно-бумажном предприятии
US8808498B2 (en) 2009-03-05 2014-08-19 Andritz Inc. Heat recovery from spent cooking liquor in a digester plant of a chemical pulp mill
US20100224335A1 (en) * 2009-03-05 2010-09-09 Andritz Inc. Heat recovery from spent cooking liquor in a digester plant of a chemical pulp mill
CN102134002A (zh) * 2011-01-21 2011-07-27 济南碧云天环保科技有限公司 一种物料加工线
US8709204B1 (en) * 2013-03-14 2014-04-29 Veolia Water Solutions & Technologies North America Inc. System and process for recovering heat from weak black liquor in a wood pulping process
JP2016501993A (ja) * 2013-03-14 2016-01-21 ヴェオリア ウォーター テクノロジーズ インコーポレイテッド 木材パルプ化プロセスにおいて弱黒液から熱を回収するシステム及び方法
WO2016038247A1 (fr) * 2014-09-08 2016-03-17 Andritz Oy Procédé de génération de vapeur à une installation de lessiveur d'une usine de pâte chimique
CN105088847A (zh) * 2015-09-07 2015-11-25 武汉凯比思电力设备有限公司 一种由造纸黑液提取分离木质素的装置及方法
EP3458643A4 (fr) * 2016-05-17 2019-12-11 Valmet Aktiebolag Procédé de génération de vapeur propre dans un système de digesteur continu

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CA2565358A1 (fr) 2007-04-24
FI20060928A (fi) 2007-04-25
CA2565358C (fr) 2014-01-14
US20110198049A1 (en) 2011-08-18
RU2006137408A (ru) 2008-05-10
SE532462C2 (sv) 2010-01-26
FI123103B (fi) 2012-11-15
JP4878982B2 (ja) 2012-02-15
CN101046073A (zh) 2007-10-03
FI20060928A0 (fi) 2006-10-23
BRPI0604341A (pt) 2007-08-21
SE0602249L (sv) 2007-04-25
BRPI0604341B1 (pt) 2017-12-26
JP2007119995A (ja) 2007-05-17

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