CA2565358C - Fiberline system and method using black liquor flashed steam - Google Patents
Fiberline system and method using black liquor flashed steam Download PDFInfo
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- CA2565358C CA2565358C CA2565358A CA2565358A CA2565358C CA 2565358 C CA2565358 C CA 2565358C CA 2565358 A CA2565358 A CA 2565358A CA 2565358 A CA2565358 A CA 2565358A CA 2565358 C CA2565358 C CA 2565358C
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- black liquor
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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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Abstract
A chemical pulp mill system and method of using black liquor flashing steam from a digester system comprises generating black liquor in the digester system, sending the black liquor to an evaporator system without using any pre-evaporator system, flashing the black liquor in the evaporator system to yield steam, and using at least some of the steam for chip steaming in a chip bin and/or for supplying in-direct heat exchangers in the digester system for pre-heating white liquor and/or filtrates for use in the digester system. In other embodiments, a chemical pulp mill system and method for utilizing black liquor flashing steam from a digester system comprises generating black liquor from the digester system, flashing the black liquor in one stage to yield steam prior to leading the black liquor into an evaporation system storage tank, using the steam to steam chips and/or evaporate black liquor in the evaporation system, and preventing formation of concentrated non-condensable gases and foul condensate in the digester system by using the digester system without any condenser for the black liquor flashing steam.
Description
FIBERLINE SYSTEM AND METHOD USING BLACK LIQUOR FLASHED
STEAM
BACKGROUND AND SUMMARY OF THE INVENTION
In conventional facilities producing chemical pulp utilizing continuous digesters, 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., Figure 1.
According to the present invention, 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).
According to another embodiment of the invention, 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.
BRIEF DESCRIPTION OF THE DRAWINGS
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.
DETAILED DESCRIPTION OF THE INVENTIVE
EMBODIMENTS AND DRAWINGS
To assist in an understanding of the technology in the field and area of the invention, attention is directed to the attached documents, U.S. Patent Nos.
6,346,166, 6,176,971, 6,132,555, 4,789,428 and 4,897,157, patent document nos. W096/32531 and W096/12848, and pages 183-184 of the book entitled Present and Future Developments of Continuous Cooking and its Figure 12.2.
Figure 12.2 (simplified as Figure 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-evaporation ¨ in Figure 1, see the dash-line box around flash tanks and 20 and the series of exchangers near the top of the figure and identified as "PRE-EVAP."
= Pre-heaters ¨ in Figure 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 Figure 1, see the circled section identified as "EVAP." In this area, there are a series of exchangers that are referred to as effects. Each effect produces steam from the black liquor that enters the effect. 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 8-0(this section is also referred to as the cooking system). Currently, at least one black liquor stream (typically at a temperature of 110-150 C) is withdrawn from the cooking system. 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 82, 84 and/or reboilers where steam is produced from the hot black liquor as the liquor is cooled, typically to temperatures of about 110 C. At this point, the black liquor is sent to the evaporator system "EVAP"
in the recovery area.
Once in the recovery area (Figure 2), 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 Figure 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 Figure 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 Figure 2), that means the effect where the temperature of the WBL will allow flashing to produce steam, typically the third or fourth effect. From this point of entry, 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 Figure 2).
One of the embodiments of the subject invention eliminates the pre-evaporator system. See Figures 3 and 4. In this inventive process, 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.
It has also been discovered that 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 Figures 3 and 4 has other improvements over the conventional systems of Figures 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.
Optionally, 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 40ppm 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.
In current systems that may arguably have a filter somewhat like this, 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. However, in the inventive process, 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. Depending on the temperature of the material, 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.
STEAM
BACKGROUND AND SUMMARY OF THE INVENTION
In conventional facilities producing chemical pulp utilizing continuous digesters, 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., Figure 1.
According to the present invention, 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).
According to another embodiment of the invention, 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.
BRIEF DESCRIPTION OF THE DRAWINGS
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.
DETAILED DESCRIPTION OF THE INVENTIVE
EMBODIMENTS AND DRAWINGS
To assist in an understanding of the technology in the field and area of the invention, attention is directed to the attached documents, U.S. Patent Nos.
6,346,166, 6,176,971, 6,132,555, 4,789,428 and 4,897,157, patent document nos. W096/32531 and W096/12848, and pages 183-184 of the book entitled Present and Future Developments of Continuous Cooking and its Figure 12.2.
Figure 12.2 (simplified as Figure 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-evaporation ¨ in Figure 1, see the dash-line box around flash tanks and 20 and the series of exchangers near the top of the figure and identified as "PRE-EVAP."
= Pre-heaters ¨ in Figure 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 Figure 1, see the circled section identified as "EVAP." In this area, there are a series of exchangers that are referred to as effects. Each effect produces steam from the black liquor that enters the effect. 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 8-0(this section is also referred to as the cooking system). Currently, at least one black liquor stream (typically at a temperature of 110-150 C) is withdrawn from the cooking system. 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 82, 84 and/or reboilers where steam is produced from the hot black liquor as the liquor is cooled, typically to temperatures of about 110 C. At this point, the black liquor is sent to the evaporator system "EVAP"
in the recovery area.
Once in the recovery area (Figure 2), 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 Figure 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 Figure 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 Figure 2), that means the effect where the temperature of the WBL will allow flashing to produce steam, typically the third or fourth effect. From this point of entry, 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 Figure 2).
One of the embodiments of the subject invention eliminates the pre-evaporator system. See Figures 3 and 4. In this inventive process, 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.
It has also been discovered that 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 Figures 3 and 4 has other improvements over the conventional systems of Figures 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.
Optionally, 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 40ppm 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.
In current systems that may arguably have a filter somewhat like this, 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. However, in the inventive process, 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. Depending on the temperature of the material, 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.
In another embodiment of the invention, a chemical pulping system, method and process utilizes a flashing tank. The prior art is first described, followed by the inventive embodiments.
In chemical pulping, cooking liquor at a high temperature is discharged from a continuous digester. Typically, the discharged amount is 8 ¨ 12 m3/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), where, among other things, 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. In the evaporation plant, the black liquor is led into a non-pressurized storage tank prior to the actual evaporation. 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.
Typically, several flashing tanks are used for removing heat from the black liquor, wherein part of the hot black liquor converts into flashing steam.
If it was possible to remove by flashing the total amount of heat mentioned above, the amount of water flashing, i.e., vaporizing, would be 0.5 ¨ 1.7 m3/ADMT. In practice, 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 m3/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. In the 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. Typically, 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.
Typically, 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. As the concentrated malodorous gases and foul condensate are toxic and explosive, the treatment thereof is dangerous and requires particular care.
It often happens, e.g., due to low capacity of the flashing steam condenser, that the black liquor is not flashed to the maximum level of about 110 C, but the black liquor exits the flashing tank at a higher temperature.
In that case, the flashing steam removal from the black liquor is below maximum and the need for evaporation in the evaporation plant increases. In view of the overall energy efficiency of the mill, it is advantageous to remove as much flashing steam from the black liquor as possible, provided that sensible objects of use are found, where it can be used to replace fresh steam with high efficiency.
Various techniques have been used for chip steaming. Conventionally, in addition to atmospheric steaming, a short-term pressurized steaming has been performed in a so-called steaming vessel or chip chute. Pressurized steaming is usually performed at a pressure of 1.0 ¨ 1.5 bar. Pressurized steaming consumes a great amount of steam. Therefore, in connection with pressurized steaming, also the black liquor steaming is performed in two stages so that from the first stage the flashing steam is led into a steaming vessel and from the second stage into an atmospheric chip bin with a remarkably longer steaming retention time. In modern pulp mills, steaming in the chip bin is so efficient that pressurized steaming has been omitted and typically only one black liquor flashing phase is used. This way, the process is simpler and the investment costs are lower.
Figure 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. From the digesters, black liquor may be discharged to pipe 4 from more than one zone. As the pressure decreases, 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.
As the steam condenses, 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.
In modern fiberlines, the amount of hot water used in pulp washing has significantly decreased and often there is no reasonable use for the whole amount of hot water generated in the flashing steam condenser and the black liquor cooler, but the hot water has to be recooled and removed from the plant. Thus, part of the heat amount of the black liquor is lost. 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.
Figure 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. From the digester (or digesters), black liquor may be discharged to pipe 4 from more than one zone.
As the pressure decreases in the flashing tank 1, 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. In the 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.
Figure 7 illustrates another embodiment where the flashing steam is led to chip steaming only, and there is no flashing steam condenser. In this embodiment, the black liquor from the digester enters the flashing tank 1 via pipe 4. From the digester(s), black liquor may be removed from more than one zone. As the pressure decreases in the flashing tank 1, 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. There, 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.
Although 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. There is a further risk that in a situation where the flashing steam is not discharged from the flashing tank, concentrated malodorous gases are enriched in the flashing tank. When flashing steam is taken into use again, a large amount of concentrated malodorous gases may erupt. This forceful and sudden eruption of concentrated malodorous gases may cause dangerous situations in the steaming area or devices connected thereto. In this embodiment according to the invention, no enrichment would take place because flashing steam is continuously discharged to the evaporation plant.
The use of flashing steam in evaporation has also been practiced in connection with various pre-evaporation solutions. In these 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. In addition to the pre-evaporation plant, 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. In practice, the pre-evaporation plant solutions have often been complicated processes and prone to black liquor foaming. For these reasons, pre-evaporation plants are undesireable.
When using the inventive systems, processes and methods of the invention, some may argue that the operation of the digester plant and the evaporation plant are more dependent on each other than normal. For example, if the amount of flashing steam led into the evaporation plant varies significantly, it may result in an irregular operation of the evaporation plant.
This problem may be easily solved by stabilizing the steam flow going to the evaporation plant by means of an optional flow controller 16 and allowing the amount of steam for steaming to change in various fault situations of the digester plant. The amount of steam required for steaming may easily be compensated for in various fault situations by means of fresh steam without any practical negative effect on the overall steam economy.
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. In this situation, the previously presented solution may be utilized, where flashing steam is used for chip steaming only. However, 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.
In principle, 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. When several flashing tanks are 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. Nevertheless, 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.
Thus, a number of preferred embodiments have been fully described above with reference to the drawing figures. The scope of the claims should not be limited by the preferred embodiments and examples, but should be given the broadest interpretation consistent with the description as a whole.
In chemical pulping, cooking liquor at a high temperature is discharged from a continuous digester. Typically, the discharged amount is 8 ¨ 12 m3/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), where, among other things, 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. In the evaporation plant, the black liquor is led into a non-pressurized storage tank prior to the actual evaporation. 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.
Typically, several flashing tanks are used for removing heat from the black liquor, wherein part of the hot black liquor converts into flashing steam.
If it was possible to remove by flashing the total amount of heat mentioned above, the amount of water flashing, i.e., vaporizing, would be 0.5 ¨ 1.7 m3/ADMT. In practice, 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 m3/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. In the 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. Typically, 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.
Typically, 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. As the concentrated malodorous gases and foul condensate are toxic and explosive, the treatment thereof is dangerous and requires particular care.
It often happens, e.g., due to low capacity of the flashing steam condenser, that the black liquor is not flashed to the maximum level of about 110 C, but the black liquor exits the flashing tank at a higher temperature.
In that case, the flashing steam removal from the black liquor is below maximum and the need for evaporation in the evaporation plant increases. In view of the overall energy efficiency of the mill, it is advantageous to remove as much flashing steam from the black liquor as possible, provided that sensible objects of use are found, where it can be used to replace fresh steam with high efficiency.
Various techniques have been used for chip steaming. Conventionally, in addition to atmospheric steaming, a short-term pressurized steaming has been performed in a so-called steaming vessel or chip chute. Pressurized steaming is usually performed at a pressure of 1.0 ¨ 1.5 bar. Pressurized steaming consumes a great amount of steam. Therefore, in connection with pressurized steaming, also the black liquor steaming is performed in two stages so that from the first stage the flashing steam is led into a steaming vessel and from the second stage into an atmospheric chip bin with a remarkably longer steaming retention time. In modern pulp mills, steaming in the chip bin is so efficient that pressurized steaming has been omitted and typically only one black liquor flashing phase is used. This way, the process is simpler and the investment costs are lower.
Figure 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. From the digesters, black liquor may be discharged to pipe 4 from more than one zone. As the pressure decreases, 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.
As the steam condenses, 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.
In modern fiberlines, the amount of hot water used in pulp washing has significantly decreased and often there is no reasonable use for the whole amount of hot water generated in the flashing steam condenser and the black liquor cooler, but the hot water has to be recooled and removed from the plant. Thus, part of the heat amount of the black liquor is lost. 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.
Figure 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. From the digester (or digesters), black liquor may be discharged to pipe 4 from more than one zone.
As the pressure decreases in the flashing tank 1, 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. In the 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.
Figure 7 illustrates another embodiment where the flashing steam is led to chip steaming only, and there is no flashing steam condenser. In this embodiment, the black liquor from the digester enters the flashing tank 1 via pipe 4. From the digester(s), black liquor may be removed from more than one zone. As the pressure decreases in the flashing tank 1, 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. There, 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.
Although 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. There is a further risk that in a situation where the flashing steam is not discharged from the flashing tank, concentrated malodorous gases are enriched in the flashing tank. When flashing steam is taken into use again, a large amount of concentrated malodorous gases may erupt. This forceful and sudden eruption of concentrated malodorous gases may cause dangerous situations in the steaming area or devices connected thereto. In this embodiment according to the invention, no enrichment would take place because flashing steam is continuously discharged to the evaporation plant.
The use of flashing steam in evaporation has also been practiced in connection with various pre-evaporation solutions. In these 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. In addition to the pre-evaporation plant, 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. In practice, the pre-evaporation plant solutions have often been complicated processes and prone to black liquor foaming. For these reasons, pre-evaporation plants are undesireable.
When using the inventive systems, processes and methods of the invention, some may argue that the operation of the digester plant and the evaporation plant are more dependent on each other than normal. For example, if the amount of flashing steam led into the evaporation plant varies significantly, it may result in an irregular operation of the evaporation plant.
This problem may be easily solved by stabilizing the steam flow going to the evaporation plant by means of an optional flow controller 16 and allowing the amount of steam for steaming to change in various fault situations of the digester plant. The amount of steam required for steaming may easily be compensated for in various fault situations by means of fresh steam without any practical negative effect on the overall steam economy.
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. In this situation, the previously presented solution may be utilized, where flashing steam is used for chip steaming only. However, 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.
In principle, 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. When several flashing tanks are 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. Nevertheless, 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.
Thus, a number of preferred embodiments have been fully described above with reference to the drawing figures. The scope of the claims should not be limited by the preferred embodiments and examples, but should be given the broadest interpretation consistent with the description as a whole.
=
Claims (11)
1. A method of using black liquor flashing steam from a digester system of a chemical pulp mill, said method comprising:
(a) generating black liquor in the digester system, (b) sending the black liquor to an evaporator system, the evaporator system including a multi-effect evaporator having at least six effects, without using any pre-evaporator system, wherein the temperature of the black liquor sent to the evaporator system is about 130°C or greater, and the black liquor is sent to a desired evaporator effect based on the temperature of the black liquor, (c) flashing the black liquor in the evaporator system to yield steam, and wherein at least some of the steam is used for chip steaming in a chip bin and/or for supplying in-direct heat exchangers in the digester system for pre-heating white liquor and/or filtrates for use in the digester system.
(a) generating black liquor in the digester system, (b) sending the black liquor to an evaporator system, the evaporator system including a multi-effect evaporator having at least six effects, without using any pre-evaporator system, wherein the temperature of the black liquor sent to the evaporator system is about 130°C or greater, and the black liquor is sent to a desired evaporator effect based on the temperature of the black liquor, (c) flashing the black liquor in the evaporator system to yield steam, and wherein at least some of the steam is used for chip steaming in a chip bin and/or for supplying in-direct heat exchangers in the digester system for pre-heating white liquor and/or filtrates for use in the digester system.
2. A method according to claim 1 wherein the temperature of said black liquor at the introduction in said evaporator system is about 130°C to about 170°C.
3. A method according to claim 1 or 2 wherein the temperature of the black liquor sent to the evaporator system is about 130°C to about 150°C.
4. A method according to anyone of claims 1 to 3 wherein the temperature of the black liquor sent to an effect in the evaporator system is about 130°C or greater.
5. A method according to anyone of claims 1 to 4 wherein the temperature of the black liquor sent to an effect in the evaporator system is about 130°C to about 150°C.
6. A method according to anyone of claims 1 to 5, further utilizing a pressurized fiber filter between the digester system and the evaporator system.
7. A method according to claim 6 wherein the filter allows the removal of fiber from the black liquor stream to a level of about 40 ppm leaving the filter.
8. A chemical pulp mill system comprising:
(a) a digester system that can generate black liquor, (b) an evaporator system, comprising a multi-effect evaporator having at least six effects, wherein the chemical pulp mill system has no pre-evaporator system, and wherein at least a portion of the black liquor is provided to the evaporator system as a liquid and is flashed in one of the at least six effects of the evaporator system to yield steam, and at least some of the steam can be used for chip steaming in a chip bin and/or for supplying in-direct heat exchangers in the digester system for preheating white liquor and/or filtrates for use in the digester system.
(a) a digester system that can generate black liquor, (b) an evaporator system, comprising a multi-effect evaporator having at least six effects, wherein the chemical pulp mill system has no pre-evaporator system, and wherein at least a portion of the black liquor is provided to the evaporator system as a liquid and is flashed in one of the at least six effects of the evaporator system to yield steam, and at least some of the steam can be used for chip steaming in a chip bin and/or for supplying in-direct heat exchangers in the digester system for preheating white liquor and/or filtrates for use in the digester system.
9. A system according to claim 8 further comprising a pressurized fiber filter between the digester system and the evaporator system.
10. A system according to claim 9 wherein the filter can allow the removal of fiber from a black liquor stream to a level of about 40 ppm leaving the filter.
11. A system according to claim 8 comprising two or more digesters.
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| US11/548,911 | 2006-10-12 | ||
| US11/548,911 US20070131363A1 (en) | 2005-10-24 | 2006-10-12 | Fiberline systems, processes and methods |
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| CA2565358A1 CA2565358A1 (en) | 2007-04-24 |
| CA2565358C true CA2565358C (en) | 2014-01-14 |
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| CA2565358A Expired - Fee Related CA2565358C (en) | 2005-10-24 | 2006-10-23 | Fiberline system and method using black liquor flashed steam |
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| JP (1) | JP4878982B2 (en) |
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| JPS6094227A (en) * | 1983-10-26 | 1985-05-27 | Daiichi Denko Kk | Electrode wire for wire cut electric discharge machining |
| SE518993E (en) * | 2002-01-24 | 2013-04-23 | Metso Paper Sweden Ab | Preparation of cellulose pulp by boiling with a boiling liquid containing evaporated black liquor |
| CN100439267C (en) * | 2007-10-29 | 2008-12-03 | 山东泉林纸业有限责任公司 | Alkali digester and sulammonium process mixed straw pulping black liquor, alkali digester and sulammonium process mixed compression straw pulping black liquor, and preparation method thereof |
| US20090288790A1 (en) * | 2008-05-22 | 2009-11-26 | Flanagan Peter J | Process and apparatus for treating green liquor |
| FI20090079A (en) * | 2009-03-05 | 2010-09-06 | Andritz Inc | Heat recovery from waste cooking liquor at a pulp mill digester |
| FI121967B (en) * | 2009-11-19 | 2011-06-30 | Metso Paper Inc | Steam and condensate systems for the dryer section of a fiber web machine |
| CN102134002B (en) * | 2011-01-21 | 2012-08-01 | 济南碧云天环保科技有限公司 | Material processing line |
| CN102226319B (en) * | 2011-06-03 | 2013-04-10 | 长沙理工大学 | Batch cooking cold blow device and cold blow method |
| 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 |
| FI20145784A (en) * | 2014-09-08 | 2016-03-09 | Andritz Oy | Water vapor development at the pulp mill digester |
| US9644317B2 (en) | 2014-11-26 | 2017-05-09 | International Paper Company | Continuous digester and feeding system |
| CN105088847B (en) * | 2015-09-07 | 2018-02-13 | 武汉凯比思电力设备有限公司 | A kind of device and method that separating lignin is extracted by black liquid |
| SE539572C2 (en) * | 2016-05-17 | 2017-10-17 | Valmet Oy | Method for generation of clean steam in a continuous digester system |
| SE1950386A1 (en) * | 2019-03-29 | 2020-09-22 | Valmet Oy | A method and a system for extracting hydrolysate in a continuous cooking process for producing pulp |
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| US3176971A (en) * | 1962-10-08 | 1965-04-06 | Kirk And Blum Mfg Company | Metal scarfing apparatus |
| SE454895B (en) * | 1985-07-11 | 1988-06-06 | Ahlstroem Foeretagen | SET AND DEVICE FOR DISPOSAL OF DISPOSAL |
| US4897157A (en) * | 1986-07-08 | 1990-01-30 | Kamyr, Inc. | Make-up liquor and black liquor evaporating processing during pulp production |
| SE463316B (en) * | 1988-01-14 | 1990-11-05 | Ahlstroem Foeretagen | PROCEDURE AND DEVICE FOR EVAPORATION OF WASTE IN CONNECTION WITH COOKING CELLULOUS FIBER MATERIAL IN A CONTINUOUS COOKER |
| FI85515C (en) * | 1990-07-09 | 1996-04-10 | Ahlstroem Oy | Process for controlling the sulphidity of a sulphate cellulose plant |
| US5527427A (en) * | 1995-03-21 | 1996-06-18 | Optima Specialty Chemicals & Technology Inc. | High solids black liquor of reduced viscosity and viscosity reduction method for high solids black liquor |
| US6306252B1 (en) * | 1995-04-10 | 2001-10-23 | Andritz-Ahlstrom Inc. | Heat recovery from spent digester cooking liquor |
| FI118131B (en) * | 1996-11-01 | 2007-07-13 | Kvaerner Power Oy | Process and arrangement for increasing the evaporation capacity of the residual liquor in a multi-evaporation cellulosic plant consisting of several evaporation stages |
| US6174411B1 (en) * | 1997-02-10 | 2001-01-16 | Andritz-Ahlstrom Inc. | Continuous digester with inverted top separator |
| FI122655B (en) * | 1998-11-06 | 2012-05-15 | Ovivo Luxembourg Sarl | Batch-making process for mass production |
| US6176971B1 (en) * | 1998-11-18 | 2001-01-23 | Andritz-Ahlstrom Inc. | Heat economy enhancements for the recovery and use of energy obtained from spent cooking liquors |
| US6346166B1 (en) * | 1999-06-14 | 2002-02-12 | Andritz-Ahlstrom Inc. | Flash tank steam economy improvement |
| FI121384B (en) * | 1999-12-29 | 2010-10-29 | Metso Paper Inc | Improved process for the preparation of cell pulp with turpentine recovery |
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| JP4878982B2 (en) | 2012-02-15 |
| US20070131363A1 (en) | 2007-06-14 |
| SE0602249L (en) | 2007-04-25 |
| BRPI0604341A (en) | 2007-08-21 |
| CA2565358A1 (en) | 2007-04-24 |
| CN101046073A (en) | 2007-10-03 |
| RU2404316C2 (en) | 2010-11-20 |
| FI123103B (en) | 2012-11-15 |
| SE532462C2 (en) | 2010-01-26 |
| FI20060928A (en) | 2007-04-25 |
| US20110198049A1 (en) | 2011-08-18 |
| JP2007119995A (en) | 2007-05-17 |
| FI20060928A0 (en) | 2006-10-23 |
| BRPI0604341B1 (en) | 2017-12-26 |
| RU2006137408A (en) | 2008-05-10 |
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