CA2530704A1 - Batch process for preparing pulp - Google Patents
Batch process for preparing pulp Download PDFInfo
- Publication number
- CA2530704A1 CA2530704A1 CA002530704A CA2530704A CA2530704A1 CA 2530704 A1 CA2530704 A1 CA 2530704A1 CA 002530704 A CA002530704 A CA 002530704A CA 2530704 A CA2530704 A CA 2530704A CA 2530704 A1 CA2530704 A1 CA 2530704A1
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- Prior art keywords
- liquor
- cooking
- impregnation
- polysulfide
- hot
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Classifications
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C1/00—Pretreatment of the finely-divided materials before digesting
- D21C1/06—Pretreatment of the finely-divided materials before digesting with alkaline reacting compounds
-
- 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
- D21C11/0021—Introduction of various effluents, e.g. waste waters, into the pulping, recovery and regeneration cycle (closed-cycle)
-
- 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
- D21C3/00—Pulping cellulose-containing materials
- D21C3/02—Pulping cellulose-containing materials with inorganic bases or alkaline reacting compounds, e.g. sulfate processes
-
- 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
- D21C3/00—Pulping cellulose-containing materials
- D21C3/22—Other features of pulping processes
- D21C3/222—Use of compounds accelerating the pulping processes
-
- 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
- D21C3/00—Pulping cellulose-containing materials
- D21C3/22—Other features of pulping processes
- D21C3/26—Multistage processes
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- Paper (AREA)
- Polysaccharides And Polysaccharide Derivatives (AREA)
Abstract
According to the invention, polysulfide is used in the manufacture of kraft pulp in the initial stage of a displacement batch process in order to improve the yield. Polysulfide-containing white liquor is added intermixed with the first liquor charged to the digester, or as a separate charge before the impregnation liquor is introduced. Preferably, a cooking catalyst, e.g.
antraquinone, is added to the white liquor charge as the cooking stage commences.
antraquinone, is added to the white liquor charge as the cooking stage commences.
Description
BATCH PROCESS FOR PREPARING PULP
FIELD OF THE INVENTION
The present invention relates to a process for preparing kraal pulp in which lignocellulosic material is treated with recycled process liquors, polysulfide and fresh re-causticized white liquor for removing lignin therefrom. More particularly, the present invention relates to the use of polysulfide white liquor (or another polysulfide source) in the early stages ofmodern displacement kraft batch cooking, and the advantage thereof in terms of improved pulp yield.
BACKGROUND OF THE INVENTION
In the various kraft pulping processes, lignocellulosic material, most commonly wood chips, is generally treated at elevated temperatures with alkaline cooking liquor containing sodium hydroxide and sodium hydrogen sulfide, called white liquor. In these processes a significant part of the cellulosic material, especially hemicelluloses, are partly lost due to reactions with the white liquor. In kraft pulping conditions hemicelluloses undergo alkaline peeling reactions, de polymerization, in which the hemicelluloses are dissolved as organic acids into the cooking liquor. A known fact is that by a polysulfide treatment, hemicelluloses are stabilized and are thereafter more resistant to cooking liquor in kraft cooking conditions, which leads to higher yield from the processes lignocellulosic substance input.
In kraft pulping processes, fresh cooking liquor is obtained from the recovery furnace's inorganic smelt, which is dissolved in water and causticized to produce white liquor.
Polysulfide-containing white liquor is obtained from causticized white liquor by various processes, which partially oxidize the liquor's sodium sulfide into polysulfide. These processes typically use oxidation catalysts to polymerize the white liquor's hydrogen sulfide.. Also, polysulfide can be produced directly by elemental sulfur addition into white liquor. Polysulfide-containing white liquor is called polysulfide white liquor or orange liquor.
The use of polysulfide white liquor has been quite straightforward in conventional kraft cooking operations. The normal white liquor has been converted to polysulfide white liquor, and that liquor has been used in the same manner as normal white liquor. Aver the impregnation into the wood chips in the digester and during the temperature rise to above 100 °C, the polysulfide has reacted with the carbohydrates making them less vulnerable to alkaline degradation. Later during the cook, when temperature has risen over 140 °C, the rest of the polysulfide has rapidly broken down through thermal decomposition.
As all the conventional cooking systems have used cooking liquors having initial temperatures well below 100 °C and the temperature in the digester has been elevated slowly or in steps, the polysulfide has had the possibility to react and facilitate higher pulp yield.
However, the development of the batch cooleing systems has caused a major deviation from the conventional cooking technology: White liquor is introduced into the digester as "hot 1 S white liquor", which has been heated up using the heat of the previously generated spent liquor, and steam. For the purpose ofthis disclosure, "hot" is meant to designate a liquor having a temperature above its boiling point at ambient pressure, i.e. a liquor that must be stored in a pressurized vessel.
The hot white liquor temperature in typical displacement batch cooking is 140 -180 °C.
From the displacement batch process point of view, polysulfide has been an impossible chemical. Polysulfide is unstable at higher temperatures, for instance at those used in kraft cooking; the chemical begins to break down at temperatures above 100°C, and it degrades completely in a few minutes at 150 °C. Thus at the typical process temperature ofthe hot white liquor, polysulfide white liquor is not stable at all. This fact has disabled the use of polysulfide in the modern displacement kraft pulping processes developed for higher energy and chemical economy and improved pulp quality.
During the early 80's, new energy efficient kraft batch processes using various liquor displacements emerged. Characteristic for the displacement kraft batch process is to recover hot black liquor from the end of the cooking by displacement and then re-use the energy in the subsequent batches. Partly this is done by using the hot spent cooking liquor as such, and partly by heating the white liquor with the heat of the hot spent liquor leaving the digester system or collected for re-use at low temperature. This process arrangement leads to high temperatures in the input liquor accumulators. A low temperature white liquor, typically at 80 °C in the storage tank after re-causticization, cannot be used anymore, and the environment for stable polysulfide in the white liquor does not exist anymore.
Good examples of the development of displacement batch processes are given in, e. g., Fagerlund, U.S. Pat 4,578,149 and Ostman, U.S. Pat 4,764,251. A fixrther characteristic feature of a modern displacement batch process is to combine energy efficiency and efficient use of residual and fresh cooking chemicals to achieve, in addition to energy efficiency, high pulp strength and good delignification through hydroxyl and hydrosulfide concentration and temperature profiling at different stages of the cooking cycle (Hiljanen, Tikka, EP-B 520 452, Tikka, U.S. Pat 5,183,535).
The strive for higher pulp yield is easy to understand. It is always more profitable to produce more pulp from a certain wood amount. The pulping industry has faced increasing environmental pressure to radically cut down environment-polluting effluents.
Reduction of the organic effluents from pulp bleaching requires kraft cooking to be extended to yield much lower residual lignin concentration in the pulp than before. Extended cooking means more carbohydrate losses. In order to enable extended cooking while improving energy economy and pulp quality, one popular option for the industry has been to use modern displacement batch cooking technology. In spite of all the advantages of this technology, it has not been possible to take the pulp yield advantage by using polysulfide white liquor.
The present invention overcomes these problems and enables an efficient use ofpolysulfide by a novel displacement batch cooking process.
The use of anthraquinone (A~) as a cooking catalyst is well known. It acts by reducing carbohydrate end groups, stabilising them against alkaline peeling and producing anthrahydroquinone, which is alkali soluble. Anthrahydroquinone reduces lignin, making it more reactive. In this process, anthraquinone is formed again and may react with carbohydrates.
During operation of displacement batch cooking processes, it has been observed that the properties of the black liquor originating from the early stages of the cook differ from those of black liquor from a traditional cook. Recycled black liquor originating from the early stages of the cooking sequence may complicate the evaporation of black liquor.
A
particular problem is fouling of the surfaces of heat exchangers in the evaporation plant, leading to a decrease in heat transfer. These evaporator fouling problems are typically related to calcium. In the early stage of alkaline cooking, calcium-containing material dissolves into the black liquor from the lignocellulosic material. In a traditional cook, the cook proceeds with heating, the temperature increases and no essential liquor exchange occurs. Then, a major part of the dissolved calcium-containing material in the cooking liquor is broken down, calcium carbonate is formed and as a result, a major part of the calcium is resorbed onto the lignocellulosic material in the digester.
Following such a cooking process, evaporation of the black liquor can normally be carried out without problems caused by precipitation of calcium. In contrast, the evaporation problems with black liquors originating from the early stages of cooking are typically related to calcium-containing material dissolved in the early stages of a cook. The dissolved calcium-containing material has not been degraded, and the amount of calcium bound to the dissolved material in the black liquor is high. As disclosed in publication EP
1242 674, this problem may be solved by re-introducing liquor having a high calcium precipitating potential into the digester as a displacement liquor at the end of a cook. At this point, the digester temperature is suiEciently high to cause calcium liberation. The calcium is then removed together with the pulp, and does not enter the evaporation and regeneration cycle.
SUNIl~~IARY OF THE INVENTION
In accordance with the present invention, a method for producing pulp using polysulfide white liquor has been provided. The method involves a kraft batch process which comprises the addition ofpolysulfide white liquor in the impregnation and pretreatment in the very 'front-end' of the cooking process, and a finalizing delignification stage with white liquor and optional cooking catalyst addition, which is facilitated by the modified 'front-end' process chemistry resulting in improved pulp yield. A volume of polysulfide white liquor is added as the first portion of liquor to enter the digester, or admixed with the impregnation liquor prior to this being pumped into the digester. For the purpose ofthis disclosure, "impregnation liquor" means a liquor stored at a temperature below its atmospheric boiling point, used for a first immersion of the lignocellulosic raw material in a batch pulping process.
In the present invention, lignocellulosic material entering a displacement batch process is thus pretreated with polysulfide- containing process liquors in conditions favourable for pre-treatment and polysulfide stability. A set of displacement batch process arrangements, capable of taking advantage of the polysulfide white liquor, are presented.
The required dose of fresh polysulfide white liquor is introduced in the initial stage of the process. The impregnation stage provides for both impregnation and polysulflde pre-treatment reactions.
An impregnation liquor circulation collects the displaced impregnation liquor which is re-used to fill and pressurize the digester after the first fresh liquor fill. As a result, the polysulfide concentration and dosage remain at a high level, and only the liquor balance excess is left over to be sent to chemicals recovery or re-use later in the cooking sequence.
The displacement cooking process sequence then continues with hot fills of black and white liquors, cooking and final displacement.
;:An optional feature in the present invention is a new way to use a cooking catalyst, such as anthraquinone (AQ). As the generation of polysulfide white liquor decreases the concentration ofhydrosulfide ions, the delignification rate is slower, reducing cooking capacity. The cooking catalyst can be used to maintain a normal kraft cooking rate and produci~on level. In the present invention, the catalyst may be introduced into the digester together with the hot white liquor. By this means it will not escape due to displacements, and on the other hand, it an~ives in the hot cooking stage where it is most needed. As a result, the technical and economical benefits of the displacement batch cooking are retained, while the advantages of polysulfide and cooking catalyst can be fully exploited.
BRIEF DESCRIPTION OF THE FIGURES
Figure 1 shows a block diagram of a kraft displacement batch cooking system according to the invention. The top of the figure defines the required tanks, leaving or entering streams denoted by letters. The cooking stage sequence is displayed therebelow, chronologically starting from the top and the vertically indicated streams representing the liquors passing through the digester during the various stages. The letters denoting the various entering and leaving streams correspond to the source or destination in the tank scheme.
Figure 2 shows a further embodiment of a kra,ft displacement batch cooking system according to the invention.
DISCLOSURE OF THE INVENTION
In the following, the method ofthe invention is disclosed in detail with reference to the attached Figure 1. It is understood, that liquor is charged from the digester bottom and displaced gases and liquor leave from the top.
The kraft batch cook is started by charging the digester with wood chips, or with another lignocellulosic material. Ail:er the lignocellulosic material charge, the digester is filled in a stepwise sequence using a volume of fresh polysulfide white liquor Xl from polysulfide white liquor tank 6, and impregnation liquor A1 from tank 4, topping the digester full of liquor. The volume ofpolysulfide white liquor may be added as a separate first portion, forming a raising pad of liquor as further liquor is pumped in from below.
Alternatively, the polysulfide white liquor is mixed into the impregnation liquor.
An overflow, A2, conducted to the impregnation liquor tank 4, is preferred in order to remove air and the diluted first front of liquor. Ailer the flow A2 is stopped, the digester is pressurized and impregnation is completed during an appropriate period oftime.
The cooking process is then continued by pumping in a volume of hot black liquor B
1 from hot black liquor accumulator 1. The cooler impregnation liquor A3, displaced by hot black liquor, is conducted to impregnation liquor tank 4 to be ro-used in subsequent batches.
Pumping a volume C of hot white liquor from tank 3 into the digester then continues the cooking sequence. Together with white liquor C, an amount of cooking catalyst may be dosed into the digester. The liquor D1, displaced by hot liquor above about the atmospheric boiling point, in conducted to hot black liquor accumulator 2.
At the end of the sequence described above, the digester is close to the final cooking temperature. The final heating-up is carried out using direct or indirect steam heating and digester re-circulation. After the desired cooking time when the delignification has proceeded to the desired final reaction degree, the spent liquor is ready to be displaced with wash filtrate E1 from tank 5. A volume A4 from impregnation liquor tank 4 may be used as a first portion of displacement liquor in order to deactivate the potential scale-forming calcium therein, as disclosed in EP 1242 674.
In the final displacement, the f rst displaced volume B2 displaced by wash filtrate is conducted to black liquor accumulator 1. The second portion D2 of displaced black liquor, which is diluted by the wash filtrate but is still above atmospheric boiling point, is conducted to the hot black liquor accumulator 2. After completed final displacement, the digester contents are discharged for further processing of the pulp. The above cooking sequence may then be repeated The hot black liquor from accumulator 2 is conducted to the evaporation plant, first being used to heat white liquor due for tank 3, and/or water, by means ofheat exchange.
Tank 6 is~provided for storage of polysulfide white liquor, supplied from a plant for polysulfide generation.
DESCRIPTION OF PREFERABLE EMBODIMENTS
In the following, reference is made to the figure described in the preceding section.
In the process of the present invention, a volume of polysulfide white liquor, corresponding to 25-90 % of the total active alkali dosage and resulting in 0,5% to 5%
polysulfide dosage on abs. dry wood is added into the digester before the impregnation fill is completed.
Impregnation is carried out using temperature ofbetween 70 °C and 120 °C, preferably between 85 - 95 °C, and a time ofbetween about 20 to about 120 minutes, preferably between about 30 to about 60 minutes, more preferably between about 25 to about 40 minutes.
In a preferable embodiment, the polysulfide white liquor is added as a separate portion before the introduction of further liquor.
In a preferable embodiment, the volume ofpolysulfide white liquor corresponds to 50-75 of the total active alkali dosage for the relevant batch.
In accordance with a particular embodiment of the process of the present invention, a cooking catalyst is used. Preferable catalysts are anthraquinone, anthraquinone sulfonate, and hydroanthraquinone. Any other appropriate redox-catalyst as anticipated by those skilled in the art may be used.
In accordance with an alternative embodiment of the process ofthe present invention, the following fractions displaced from the digester:
- hot cooking spent liquor fraction B2 and - fractions Dl and D2, which are of lower temperature and poorer in chemicals, are collected in a single accumulator to be used in the hot black liquor pretreatment stage.
In this configuration, hot black liquor accumulators 1 and 2 of Figure 1 are combined. The black liquor flow to the evaporation plant is drawn from the single hot black liquor accumulator, the stream being used to heat, by means of heat exchange, white liquor heading for white liquor accumulator 3, and/or water, as shown for tank 2 in Fig 1.
Ifhigh dosages ofpolysulfide white liquor are used in the impregnation stage ofthe process, longer impregnation times than in the prior art and/or a two accumulator system and/or impregnation liquor transfer to hot black liquor tank 1 may be used in order to avoid too high a residual alkali concentration in the feed of the evaporation plant.
Thus, in accordance with a further embodiment of the process of the present invention, shown in Figure 2, a volume of impregnation liquor from impregnation lank 4 is conducted to hot black liquor tank 1 to be used in hot black liquor treatment, B 1. The stream from impregnation liquor tank 4 to hot black liquor tank 1 may be heated by means of heat exchange with the stream from hot black liquor accumulator 2 to the evaporation plant.
In addition to the white liquor charge prior to the cooking stage, one or more additional white liquor charges may be carried out during the cook.
The principal advantage of the process of the present invention is that the 'front-end' of the kraft displacement batch cooking system is rendered more effective from a chemical point of view, and in regard to process arrangements. The polysulfide charge used reflects the improvement in pulp yield from the digested lignocellulosic material.
The following examples are illustrative of the invention. The following abbreviations are used:
WBL Warm impregnation black liquor DWBL Displaced WBL (from the digester) HBL Hot black liquor RHBL Displaced HBL (from the digester) DCBL Displaced cooking black liquor WF Wash filtrate PSWL Polysulfide white liquor Production of a normal 'reference' pine kraft pulp using the displacement kraft batch technique:
4,0 kg pine (Pious sylvesfris) chips {oven dry basis) were metered into a chip basket positioned in a 20-litre jacketed displacement batch digester. The lid of the digester was closed. Impregnation black liquor, consisting of wash filtrate and white liquor (WBL, 80-90°C, 25 gEA/1) was pumped in during app. 10 minutes followed by impregnation at 90°C
under 2,5 bar overpressure. The duration of the impregnation stage was 40 minutes (WBL-fill and impregnation in toi:al). Alter impregnation, a hot black liquor pre-treatment stage was commenced by introducing hot black liquor (HBL 1, 150°C, app. 20 gEAll) to the bottom of the digester, displacing the spent impregnation liquor (DWBL) out from the top of the digester. The hot black liquor pre-treatment stage duration was 30 minutes. After hot black liquor pre-treatment stage, hot white liquor (121 gEA {NaOI~/l, sulfidity 37%) charge was introduced into the digester bottom displacing the corresponding volume of spent hot black liquor (RI-IBL) out of the digester. A 45 minute heat up sequence with cooking liquor circulation raised the temperature from 150°C to the cooking temperature of 167°C. At 250 H-factors, a white liquor charge was introduced into the digester bottom 5 displacing the corresponding volume of spent hot black liquor out of the digester (DCBL
1). After the cooking time fulfilled the target H-factor, terminal displacement was started by introducing cool DWBL and wash filtrate (WF) in a sequence into the digester bottom displacing the hot spent black liquor out of the digester top {DCBL 2). The first displaced portion the hot black liquor with the hot black liquor displaced earlier during the cooking 10 sequence (DCBL 2 + DCBL 1) covered the volume needed for the next cook's hot black liquor (HBL 1 ). The terminal displacement stage duration was approximately 40 minutes.
After the terminal displacement, the pulp was disintegrated, washed with deionised water, screened and analysed. The cooking procedure was repeated and thus equilibrium in the cooking process was obtained and the cooks si;arted to repeat themselves corresponding to the industrial batch cooking system.
The experimental set up to produce pulp according to the invention is described below.
,. 4,0 kg pine (Panes sylvesfris) chips (oven dry basis) were.metered into a chip basket positioned in a 20-litre jacketed displacement batch digester. The lid of the digester was closed. The chips were steamed until the digester temperature was 100°C, approximately 5 minutes. Impregnation liquors were introduced as sequence as follows:
initially polysulfide white liquor black liquor (PSWL, volume according to the charge, app. 4,5-51);
subsequently re-circulated spent impregnation liquor (DWBL) to hydraulically fill the digester. The impregnation fill sequence took app. 11-13 minutes and was followed by impregnation at 90°C under 2,5 bar overpressure. The duration of the impregnation stage was 40 minutes (fill sequence and impregnation in total). After impregnation, a hot black liquor pre-treatment stage was carried out by introducing hot black liquor (ILL l, 150°C, app. 20 gEA/1) to the bottom of the digester of the digester, displacing the spent impregnation liquor from the top of the digester (DWBL). The hot black liquor pre-treatment stage duration was 30 minutes. Ailer the hot black liquor pre-treatment stage, hot white liquor {l21 gEA (NaOH)!1, sulfidity 37%) charge was introduced, displacing the corresponding volume of spent hot black liquor from the digester (RHBL).
Together with the WL, a cooking catalyst was charged mixed with a small volume of hot black liquor. A
45 minute heat-up sequence with cooking liquor circulation raised the temperature from 150°C to the cooking temperature of 167 °C. At 250 H-factors, a further white liquor charge was introduced into the digester bottom displacing the corresponding volume of spent hot black liquor from the digester (DCBL 1). After the cooking time fulfilled the target H-factor, terminal displacement was started by introducing a volume of cool DWBL
and wash filtrate (WF) in a sequence into the digester bottom displacing the hot spent black liquor out of the digester top (DCBL 2). The first displaced portion of hot black liquor together with the hot black liquor displaced earlier during the cooking sequence (DCBL 2 +
DCBL 1) covered the 171 volume needed for the next cook's hot black liquor (HBL 1).
After the terminal displacement, the pulp was disintegrated, washed with deionised water, screened and analysed. The cooking procedure was repeated, equilibrium in the cooking process was reached and the cooks started to repeat themselves corresponding to the industrial batch cooking system.
Example 1. Demonstration of yield improvement using polysulfide white liquor addition The reference cook follows the same addition and temperature sequences as the cooks according to the invention. All cooks were digested to the same target kappa number. A
clear yield improvement correlating with polysulfide addition can be observed PS-charge, % Total yield, % Rejects, % on Cooking model on wood Kappa number on wood wood Reference Nil 25,9 44,0 0,26 SB-PSAQ 1,21 25,9 45,8 0,36 SB-PSAQ 1,58 25,8 46,8 0,24 Example 2. The effect of anthraquinone to preserve the rate of delignification during cooking It is seen, that the reference cook requires a significantly higher H-factor to reach the target kappa number.
PSWL Reject, in imp,PS, % Yield,%
% on Method % on wood H-factorEoC, Kappa#on wood g/1 wood Reference - - 1285 16 26,9 43,6 1,01 PS pad, AQ 70 % 1,45 1106 19,1 27,1 44,3 0,15 0%
PS pad, AQ 70 % 1,45 1030 19,9 26,7 44,5 0,16 0,05%
PS pad, AQ 70 % 1,45 1096 18,1 27,3 45,8 0,1 0,1%
FIELD OF THE INVENTION
The present invention relates to a process for preparing kraal pulp in which lignocellulosic material is treated with recycled process liquors, polysulfide and fresh re-causticized white liquor for removing lignin therefrom. More particularly, the present invention relates to the use of polysulfide white liquor (or another polysulfide source) in the early stages ofmodern displacement kraft batch cooking, and the advantage thereof in terms of improved pulp yield.
BACKGROUND OF THE INVENTION
In the various kraft pulping processes, lignocellulosic material, most commonly wood chips, is generally treated at elevated temperatures with alkaline cooking liquor containing sodium hydroxide and sodium hydrogen sulfide, called white liquor. In these processes a significant part of the cellulosic material, especially hemicelluloses, are partly lost due to reactions with the white liquor. In kraft pulping conditions hemicelluloses undergo alkaline peeling reactions, de polymerization, in which the hemicelluloses are dissolved as organic acids into the cooking liquor. A known fact is that by a polysulfide treatment, hemicelluloses are stabilized and are thereafter more resistant to cooking liquor in kraft cooking conditions, which leads to higher yield from the processes lignocellulosic substance input.
In kraft pulping processes, fresh cooking liquor is obtained from the recovery furnace's inorganic smelt, which is dissolved in water and causticized to produce white liquor.
Polysulfide-containing white liquor is obtained from causticized white liquor by various processes, which partially oxidize the liquor's sodium sulfide into polysulfide. These processes typically use oxidation catalysts to polymerize the white liquor's hydrogen sulfide.. Also, polysulfide can be produced directly by elemental sulfur addition into white liquor. Polysulfide-containing white liquor is called polysulfide white liquor or orange liquor.
The use of polysulfide white liquor has been quite straightforward in conventional kraft cooking operations. The normal white liquor has been converted to polysulfide white liquor, and that liquor has been used in the same manner as normal white liquor. Aver the impregnation into the wood chips in the digester and during the temperature rise to above 100 °C, the polysulfide has reacted with the carbohydrates making them less vulnerable to alkaline degradation. Later during the cook, when temperature has risen over 140 °C, the rest of the polysulfide has rapidly broken down through thermal decomposition.
As all the conventional cooking systems have used cooking liquors having initial temperatures well below 100 °C and the temperature in the digester has been elevated slowly or in steps, the polysulfide has had the possibility to react and facilitate higher pulp yield.
However, the development of the batch cooleing systems has caused a major deviation from the conventional cooking technology: White liquor is introduced into the digester as "hot 1 S white liquor", which has been heated up using the heat of the previously generated spent liquor, and steam. For the purpose ofthis disclosure, "hot" is meant to designate a liquor having a temperature above its boiling point at ambient pressure, i.e. a liquor that must be stored in a pressurized vessel.
The hot white liquor temperature in typical displacement batch cooking is 140 -180 °C.
From the displacement batch process point of view, polysulfide has been an impossible chemical. Polysulfide is unstable at higher temperatures, for instance at those used in kraft cooking; the chemical begins to break down at temperatures above 100°C, and it degrades completely in a few minutes at 150 °C. Thus at the typical process temperature ofthe hot white liquor, polysulfide white liquor is not stable at all. This fact has disabled the use of polysulfide in the modern displacement kraft pulping processes developed for higher energy and chemical economy and improved pulp quality.
During the early 80's, new energy efficient kraft batch processes using various liquor displacements emerged. Characteristic for the displacement kraft batch process is to recover hot black liquor from the end of the cooking by displacement and then re-use the energy in the subsequent batches. Partly this is done by using the hot spent cooking liquor as such, and partly by heating the white liquor with the heat of the hot spent liquor leaving the digester system or collected for re-use at low temperature. This process arrangement leads to high temperatures in the input liquor accumulators. A low temperature white liquor, typically at 80 °C in the storage tank after re-causticization, cannot be used anymore, and the environment for stable polysulfide in the white liquor does not exist anymore.
Good examples of the development of displacement batch processes are given in, e. g., Fagerlund, U.S. Pat 4,578,149 and Ostman, U.S. Pat 4,764,251. A fixrther characteristic feature of a modern displacement batch process is to combine energy efficiency and efficient use of residual and fresh cooking chemicals to achieve, in addition to energy efficiency, high pulp strength and good delignification through hydroxyl and hydrosulfide concentration and temperature profiling at different stages of the cooking cycle (Hiljanen, Tikka, EP-B 520 452, Tikka, U.S. Pat 5,183,535).
The strive for higher pulp yield is easy to understand. It is always more profitable to produce more pulp from a certain wood amount. The pulping industry has faced increasing environmental pressure to radically cut down environment-polluting effluents.
Reduction of the organic effluents from pulp bleaching requires kraft cooking to be extended to yield much lower residual lignin concentration in the pulp than before. Extended cooking means more carbohydrate losses. In order to enable extended cooking while improving energy economy and pulp quality, one popular option for the industry has been to use modern displacement batch cooking technology. In spite of all the advantages of this technology, it has not been possible to take the pulp yield advantage by using polysulfide white liquor.
The present invention overcomes these problems and enables an efficient use ofpolysulfide by a novel displacement batch cooking process.
The use of anthraquinone (A~) as a cooking catalyst is well known. It acts by reducing carbohydrate end groups, stabilising them against alkaline peeling and producing anthrahydroquinone, which is alkali soluble. Anthrahydroquinone reduces lignin, making it more reactive. In this process, anthraquinone is formed again and may react with carbohydrates.
During operation of displacement batch cooking processes, it has been observed that the properties of the black liquor originating from the early stages of the cook differ from those of black liquor from a traditional cook. Recycled black liquor originating from the early stages of the cooking sequence may complicate the evaporation of black liquor.
A
particular problem is fouling of the surfaces of heat exchangers in the evaporation plant, leading to a decrease in heat transfer. These evaporator fouling problems are typically related to calcium. In the early stage of alkaline cooking, calcium-containing material dissolves into the black liquor from the lignocellulosic material. In a traditional cook, the cook proceeds with heating, the temperature increases and no essential liquor exchange occurs. Then, a major part of the dissolved calcium-containing material in the cooking liquor is broken down, calcium carbonate is formed and as a result, a major part of the calcium is resorbed onto the lignocellulosic material in the digester.
Following such a cooking process, evaporation of the black liquor can normally be carried out without problems caused by precipitation of calcium. In contrast, the evaporation problems with black liquors originating from the early stages of cooking are typically related to calcium-containing material dissolved in the early stages of a cook. The dissolved calcium-containing material has not been degraded, and the amount of calcium bound to the dissolved material in the black liquor is high. As disclosed in publication EP
1242 674, this problem may be solved by re-introducing liquor having a high calcium precipitating potential into the digester as a displacement liquor at the end of a cook. At this point, the digester temperature is suiEciently high to cause calcium liberation. The calcium is then removed together with the pulp, and does not enter the evaporation and regeneration cycle.
SUNIl~~IARY OF THE INVENTION
In accordance with the present invention, a method for producing pulp using polysulfide white liquor has been provided. The method involves a kraft batch process which comprises the addition ofpolysulfide white liquor in the impregnation and pretreatment in the very 'front-end' of the cooking process, and a finalizing delignification stage with white liquor and optional cooking catalyst addition, which is facilitated by the modified 'front-end' process chemistry resulting in improved pulp yield. A volume of polysulfide white liquor is added as the first portion of liquor to enter the digester, or admixed with the impregnation liquor prior to this being pumped into the digester. For the purpose ofthis disclosure, "impregnation liquor" means a liquor stored at a temperature below its atmospheric boiling point, used for a first immersion of the lignocellulosic raw material in a batch pulping process.
In the present invention, lignocellulosic material entering a displacement batch process is thus pretreated with polysulfide- containing process liquors in conditions favourable for pre-treatment and polysulfide stability. A set of displacement batch process arrangements, capable of taking advantage of the polysulfide white liquor, are presented.
The required dose of fresh polysulfide white liquor is introduced in the initial stage of the process. The impregnation stage provides for both impregnation and polysulflde pre-treatment reactions.
An impregnation liquor circulation collects the displaced impregnation liquor which is re-used to fill and pressurize the digester after the first fresh liquor fill. As a result, the polysulfide concentration and dosage remain at a high level, and only the liquor balance excess is left over to be sent to chemicals recovery or re-use later in the cooking sequence.
The displacement cooking process sequence then continues with hot fills of black and white liquors, cooking and final displacement.
;:An optional feature in the present invention is a new way to use a cooking catalyst, such as anthraquinone (AQ). As the generation of polysulfide white liquor decreases the concentration ofhydrosulfide ions, the delignification rate is slower, reducing cooking capacity. The cooking catalyst can be used to maintain a normal kraft cooking rate and produci~on level. In the present invention, the catalyst may be introduced into the digester together with the hot white liquor. By this means it will not escape due to displacements, and on the other hand, it an~ives in the hot cooking stage where it is most needed. As a result, the technical and economical benefits of the displacement batch cooking are retained, while the advantages of polysulfide and cooking catalyst can be fully exploited.
BRIEF DESCRIPTION OF THE FIGURES
Figure 1 shows a block diagram of a kraft displacement batch cooking system according to the invention. The top of the figure defines the required tanks, leaving or entering streams denoted by letters. The cooking stage sequence is displayed therebelow, chronologically starting from the top and the vertically indicated streams representing the liquors passing through the digester during the various stages. The letters denoting the various entering and leaving streams correspond to the source or destination in the tank scheme.
Figure 2 shows a further embodiment of a kra,ft displacement batch cooking system according to the invention.
DISCLOSURE OF THE INVENTION
In the following, the method ofthe invention is disclosed in detail with reference to the attached Figure 1. It is understood, that liquor is charged from the digester bottom and displaced gases and liquor leave from the top.
The kraft batch cook is started by charging the digester with wood chips, or with another lignocellulosic material. Ail:er the lignocellulosic material charge, the digester is filled in a stepwise sequence using a volume of fresh polysulfide white liquor Xl from polysulfide white liquor tank 6, and impregnation liquor A1 from tank 4, topping the digester full of liquor. The volume ofpolysulfide white liquor may be added as a separate first portion, forming a raising pad of liquor as further liquor is pumped in from below.
Alternatively, the polysulfide white liquor is mixed into the impregnation liquor.
An overflow, A2, conducted to the impregnation liquor tank 4, is preferred in order to remove air and the diluted first front of liquor. Ailer the flow A2 is stopped, the digester is pressurized and impregnation is completed during an appropriate period oftime.
The cooking process is then continued by pumping in a volume of hot black liquor B
1 from hot black liquor accumulator 1. The cooler impregnation liquor A3, displaced by hot black liquor, is conducted to impregnation liquor tank 4 to be ro-used in subsequent batches.
Pumping a volume C of hot white liquor from tank 3 into the digester then continues the cooking sequence. Together with white liquor C, an amount of cooking catalyst may be dosed into the digester. The liquor D1, displaced by hot liquor above about the atmospheric boiling point, in conducted to hot black liquor accumulator 2.
At the end of the sequence described above, the digester is close to the final cooking temperature. The final heating-up is carried out using direct or indirect steam heating and digester re-circulation. After the desired cooking time when the delignification has proceeded to the desired final reaction degree, the spent liquor is ready to be displaced with wash filtrate E1 from tank 5. A volume A4 from impregnation liquor tank 4 may be used as a first portion of displacement liquor in order to deactivate the potential scale-forming calcium therein, as disclosed in EP 1242 674.
In the final displacement, the f rst displaced volume B2 displaced by wash filtrate is conducted to black liquor accumulator 1. The second portion D2 of displaced black liquor, which is diluted by the wash filtrate but is still above atmospheric boiling point, is conducted to the hot black liquor accumulator 2. After completed final displacement, the digester contents are discharged for further processing of the pulp. The above cooking sequence may then be repeated The hot black liquor from accumulator 2 is conducted to the evaporation plant, first being used to heat white liquor due for tank 3, and/or water, by means ofheat exchange.
Tank 6 is~provided for storage of polysulfide white liquor, supplied from a plant for polysulfide generation.
DESCRIPTION OF PREFERABLE EMBODIMENTS
In the following, reference is made to the figure described in the preceding section.
In the process of the present invention, a volume of polysulfide white liquor, corresponding to 25-90 % of the total active alkali dosage and resulting in 0,5% to 5%
polysulfide dosage on abs. dry wood is added into the digester before the impregnation fill is completed.
Impregnation is carried out using temperature ofbetween 70 °C and 120 °C, preferably between 85 - 95 °C, and a time ofbetween about 20 to about 120 minutes, preferably between about 30 to about 60 minutes, more preferably between about 25 to about 40 minutes.
In a preferable embodiment, the polysulfide white liquor is added as a separate portion before the introduction of further liquor.
In a preferable embodiment, the volume ofpolysulfide white liquor corresponds to 50-75 of the total active alkali dosage for the relevant batch.
In accordance with a particular embodiment of the process of the present invention, a cooking catalyst is used. Preferable catalysts are anthraquinone, anthraquinone sulfonate, and hydroanthraquinone. Any other appropriate redox-catalyst as anticipated by those skilled in the art may be used.
In accordance with an alternative embodiment of the process ofthe present invention, the following fractions displaced from the digester:
- hot cooking spent liquor fraction B2 and - fractions Dl and D2, which are of lower temperature and poorer in chemicals, are collected in a single accumulator to be used in the hot black liquor pretreatment stage.
In this configuration, hot black liquor accumulators 1 and 2 of Figure 1 are combined. The black liquor flow to the evaporation plant is drawn from the single hot black liquor accumulator, the stream being used to heat, by means of heat exchange, white liquor heading for white liquor accumulator 3, and/or water, as shown for tank 2 in Fig 1.
Ifhigh dosages ofpolysulfide white liquor are used in the impregnation stage ofthe process, longer impregnation times than in the prior art and/or a two accumulator system and/or impregnation liquor transfer to hot black liquor tank 1 may be used in order to avoid too high a residual alkali concentration in the feed of the evaporation plant.
Thus, in accordance with a further embodiment of the process of the present invention, shown in Figure 2, a volume of impregnation liquor from impregnation lank 4 is conducted to hot black liquor tank 1 to be used in hot black liquor treatment, B 1. The stream from impregnation liquor tank 4 to hot black liquor tank 1 may be heated by means of heat exchange with the stream from hot black liquor accumulator 2 to the evaporation plant.
In addition to the white liquor charge prior to the cooking stage, one or more additional white liquor charges may be carried out during the cook.
The principal advantage of the process of the present invention is that the 'front-end' of the kraft displacement batch cooking system is rendered more effective from a chemical point of view, and in regard to process arrangements. The polysulfide charge used reflects the improvement in pulp yield from the digested lignocellulosic material.
The following examples are illustrative of the invention. The following abbreviations are used:
WBL Warm impregnation black liquor DWBL Displaced WBL (from the digester) HBL Hot black liquor RHBL Displaced HBL (from the digester) DCBL Displaced cooking black liquor WF Wash filtrate PSWL Polysulfide white liquor Production of a normal 'reference' pine kraft pulp using the displacement kraft batch technique:
4,0 kg pine (Pious sylvesfris) chips {oven dry basis) were metered into a chip basket positioned in a 20-litre jacketed displacement batch digester. The lid of the digester was closed. Impregnation black liquor, consisting of wash filtrate and white liquor (WBL, 80-90°C, 25 gEA/1) was pumped in during app. 10 minutes followed by impregnation at 90°C
under 2,5 bar overpressure. The duration of the impregnation stage was 40 minutes (WBL-fill and impregnation in toi:al). Alter impregnation, a hot black liquor pre-treatment stage was commenced by introducing hot black liquor (HBL 1, 150°C, app. 20 gEAll) to the bottom of the digester, displacing the spent impregnation liquor (DWBL) out from the top of the digester. The hot black liquor pre-treatment stage duration was 30 minutes. After hot black liquor pre-treatment stage, hot white liquor (121 gEA {NaOI~/l, sulfidity 37%) charge was introduced into the digester bottom displacing the corresponding volume of spent hot black liquor (RI-IBL) out of the digester. A 45 minute heat up sequence with cooking liquor circulation raised the temperature from 150°C to the cooking temperature of 167°C. At 250 H-factors, a white liquor charge was introduced into the digester bottom 5 displacing the corresponding volume of spent hot black liquor out of the digester (DCBL
1). After the cooking time fulfilled the target H-factor, terminal displacement was started by introducing cool DWBL and wash filtrate (WF) in a sequence into the digester bottom displacing the hot spent black liquor out of the digester top {DCBL 2). The first displaced portion the hot black liquor with the hot black liquor displaced earlier during the cooking 10 sequence (DCBL 2 + DCBL 1) covered the volume needed for the next cook's hot black liquor (HBL 1 ). The terminal displacement stage duration was approximately 40 minutes.
After the terminal displacement, the pulp was disintegrated, washed with deionised water, screened and analysed. The cooking procedure was repeated and thus equilibrium in the cooking process was obtained and the cooks si;arted to repeat themselves corresponding to the industrial batch cooking system.
The experimental set up to produce pulp according to the invention is described below.
,. 4,0 kg pine (Panes sylvesfris) chips (oven dry basis) were.metered into a chip basket positioned in a 20-litre jacketed displacement batch digester. The lid of the digester was closed. The chips were steamed until the digester temperature was 100°C, approximately 5 minutes. Impregnation liquors were introduced as sequence as follows:
initially polysulfide white liquor black liquor (PSWL, volume according to the charge, app. 4,5-51);
subsequently re-circulated spent impregnation liquor (DWBL) to hydraulically fill the digester. The impregnation fill sequence took app. 11-13 minutes and was followed by impregnation at 90°C under 2,5 bar overpressure. The duration of the impregnation stage was 40 minutes (fill sequence and impregnation in total). After impregnation, a hot black liquor pre-treatment stage was carried out by introducing hot black liquor (ILL l, 150°C, app. 20 gEA/1) to the bottom of the digester of the digester, displacing the spent impregnation liquor from the top of the digester (DWBL). The hot black liquor pre-treatment stage duration was 30 minutes. Ailer the hot black liquor pre-treatment stage, hot white liquor {l21 gEA (NaOH)!1, sulfidity 37%) charge was introduced, displacing the corresponding volume of spent hot black liquor from the digester (RHBL).
Together with the WL, a cooking catalyst was charged mixed with a small volume of hot black liquor. A
45 minute heat-up sequence with cooking liquor circulation raised the temperature from 150°C to the cooking temperature of 167 °C. At 250 H-factors, a further white liquor charge was introduced into the digester bottom displacing the corresponding volume of spent hot black liquor from the digester (DCBL 1). After the cooking time fulfilled the target H-factor, terminal displacement was started by introducing a volume of cool DWBL
and wash filtrate (WF) in a sequence into the digester bottom displacing the hot spent black liquor out of the digester top (DCBL 2). The first displaced portion of hot black liquor together with the hot black liquor displaced earlier during the cooking sequence (DCBL 2 +
DCBL 1) covered the 171 volume needed for the next cook's hot black liquor (HBL 1).
After the terminal displacement, the pulp was disintegrated, washed with deionised water, screened and analysed. The cooking procedure was repeated, equilibrium in the cooking process was reached and the cooks started to repeat themselves corresponding to the industrial batch cooking system.
Example 1. Demonstration of yield improvement using polysulfide white liquor addition The reference cook follows the same addition and temperature sequences as the cooks according to the invention. All cooks were digested to the same target kappa number. A
clear yield improvement correlating with polysulfide addition can be observed PS-charge, % Total yield, % Rejects, % on Cooking model on wood Kappa number on wood wood Reference Nil 25,9 44,0 0,26 SB-PSAQ 1,21 25,9 45,8 0,36 SB-PSAQ 1,58 25,8 46,8 0,24 Example 2. The effect of anthraquinone to preserve the rate of delignification during cooking It is seen, that the reference cook requires a significantly higher H-factor to reach the target kappa number.
PSWL Reject, in imp,PS, % Yield,%
% on Method % on wood H-factorEoC, Kappa#on wood g/1 wood Reference - - 1285 16 26,9 43,6 1,01 PS pad, AQ 70 % 1,45 1106 19,1 27,1 44,3 0,15 0%
PS pad, AQ 70 % 1,45 1030 19,9 26,7 44,5 0,16 0,05%
PS pad, AQ 70 % 1,45 1096 18,1 27,3 45,8 0,1 0,1%
Claims (11)
1. A batch process for the preparation of kraft pulp with improved yield from lignin-containing cellulosic material, comprising the steps of - filling and pressurizing said vessel with impregnation liquor collected from a previous batch, said impregnation liquor admixed with, or preceded by an addition of, a volume of polysulfide white liquor;
- impregnating the cellulosic material with the resulting mixture of impregnation liquor;
- displacing the impregnation liquor with hot spent cooking liquor;
- reacting the impregnated cellulosic material with said hot spent liquor;
- displacing hot spent cooking liquor With a volume of hot white liquor and cooking the cellulosic material with said white liquor to a desired degree of delignification;
- displacing the liquor used for cooking.
- impregnating the cellulosic material with the resulting mixture of impregnation liquor;
- displacing the impregnation liquor with hot spent cooking liquor;
- reacting the impregnated cellulosic material with said hot spent liquor;
- displacing hot spent cooking liquor With a volume of hot white liquor and cooking the cellulosic material with said white liquor to a desired degree of delignification;
- displacing the liquor used for cooking.
2. The process of claim 1, wherein the amount of polysulfide white liquor added corresponds to 25 - 90 % of the total active alkali dosage for the batch.
3. The process of claim 1, wherein the amount of polysulfide white liquor added corresponds to 50 - 75 % of the total active alkali dosage for the batch.
4. The process of claim 1, wherein the polysulfide dosage corresponds to 0,5 -
5 % relative to abs. dry wood.
5. The process of claim 1, wherein the volume of polysulfide white liquor is added separately to the digester before the impregnation liquor.
5. The process of claim 1, wherein the volume of polysulfide white liquor is added separately to the digester before the impregnation liquor.
6. The process of claim 1, wherein an amount of cooking catalyst is added to the hot white liquor.
7. The process of claim 6, wherein the cooking catalyst is anthraquinone, anthraquinone sulfonate, hydroantraquinone or a redox-catalyst derivative thereof
8. The process of claim 1, wherein hot spent liquor displaced from the digester is collected in a single hot liquor tank.
9. The process of claim l, wherein after the cook is finished, a volume of impregnation liquor is introduced into the digester as the first volume of displacement liquor.
10. The process of claim 1, wherein a volume of impregnation liquor is transferred from an impregnation liquor tank to a hot spent cooking liquor tank.
11. The process of claim 10, wherein the digester system comprises two hot spent liquor tanks.
1. A batch process for the preparation of kraft pulp with improved yield from lignin-containing cellulosic material, comprising the steps of - filling and pressurizing a vessel containing cellulosic material with impregnation liquor collected from a previous batch, said impregnation liquor admixed with, or preceded by an addition of, a volume of polysulfide white liquor;
- impregnating the cellulosic material with the resulting mixture of impregnation liquor;
- displacing the impregnation liquor with hot spent cooking liquor;
- reacting the impregnated cellulosic material with said hot spent liquor;
- displacing hot spent cooking liquor with a volume of hot white liquor and cooking the cellulosic material with said white liquor to a desired degree of delignification;
- displacing the liquor used for cooking.
2. The process of claim 1, wherein the amount of polysulfide white liquor added corresponds to 25 - 90 % of the total active alkali dosage for the batch.
3. The process of claim 1, wherein the amount of polysulfide white liquor added corresponds to 50 - 75 % of the total active alkali dosage for the batch.
4. The process of claim 1, wherein the polysulfide dosage corresponds to 0,5 -relative to abs. dry wood.
5. The process of claim 1, wherein the volume of polysulfide white liquor is added separately to the digester before the impregnation liquor.
6. The process of claim 1, wherein an amount of cooking catalyst is added to the hot white liquor.
7. The process of claim 6, wherein the cooking catalyst is anthraquinone, anthraquinone sulfonate, hydroantraquinone or a redox-catalyst derivative thereof.
8. The process of claim 1, wherein hot spent liquor displaced from the digester is collected in a single hot liquor tank.
9. The process of claim 1, wherein after the cook is finished, a volume of impregnation liquor is introduced into the digester as the first volume of displacement liquor.
10. The process of claim 1, wherein a volume of impregnation liquor is transferred from an impregnation liquor tank to a hot spent cooking liquor tank.
11. The process of claim 10, wherein the digester system comprises two hot spent liquor tanks.
1. A batch process for the preparation of kraft pulp with improved yield from lignin-containing cellulosic material, comprising the steps of - filling and pressurizing a vessel containing cellulosic material with impregnation liquor collected from a previous batch, said impregnation liquor admixed with, or preceded by an addition of, a volume of polysulfide white liquor;
- impregnating the cellulosic material with the resulting mixture of impregnation liquor;
- displacing the impregnation liquor with hot spent cooking liquor;
- reacting the impregnated cellulosic material with said hot spent liquor;
- displacing hot spent cooking liquor with a volume of hot white liquor and cooking the cellulosic material with said white liquor to a desired degree of delignification;
- displacing the liquor used for cooking.
2. The process of claim 1, wherein the amount of polysulfide white liquor added corresponds to 25 - 90 % of the total active alkali dosage for the batch.
3. The process of claim 1, wherein the amount of polysulfide white liquor added corresponds to 50 - 75 % of the total active alkali dosage for the batch.
4. The process of claim 1, wherein the polysulfide dosage corresponds to 0,5 -relative to abs. dry wood.
5. The process of claim 1, wherein the volume of polysulfide white liquor is added separately to the digester before the impregnation liquor.
6. The process of claim 1, wherein an amount of cooking catalyst is added to the hot white liquor.
7. The process of claim 6, wherein the cooking catalyst is anthraquinone, anthraquinone sulfonate, hydroantraquinone or a redox-catalyst derivative thereof.
8. The process of claim 1, wherein hot spent liquor displaced from the digester is collected in a single hot liquor tank.
9. The process of claim 1, wherein after the cook is finished, a volume of impregnation liquor is introduced into the digester as the first volume of displacement liquor.
10. The process of claim 1, wherein a volume of impregnation liquor is transferred from an impregnation liquor tank to a hot spent cooking liquor tank.
11. The process of claim 10, wherein the digester system comprises two hot spent liquor tanks.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI20031929A FI120361B (en) | 2003-12-31 | 2003-12-31 | Batch cooking process for the production of kraft pulp |
| FI20031929 | 2003-12-31 | ||
| PCT/FI2004/050196 WO2005064075A1 (en) | 2003-12-31 | 2004-12-22 | Batch process for preparing pulp |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2530704A1 true CA2530704A1 (en) | 2005-07-14 |
Family
ID=29763617
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002530704A Abandoned CA2530704A1 (en) | 2003-12-31 | 2004-12-22 | Batch process for preparing pulp |
Country Status (7)
| Country | Link |
|---|---|
| US (1) | US20060175029A1 (en) |
| EP (1) | EP1702101B1 (en) |
| AT (1) | ATE423866T1 (en) |
| CA (1) | CA2530704A1 (en) |
| DE (1) | DE602004019689D1 (en) |
| FI (1) | FI120361B (en) |
| WO (1) | WO2005064075A1 (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7828930B2 (en) | 2007-11-20 | 2010-11-09 | International Paper Company | Use of polysulfide in modified cooking |
| AU2010202496B2 (en) * | 2010-05-04 | 2015-04-16 | Bahia Specialty Cellulose Sa | Method and system for high alpha dissolving pulp production |
| KR20110123184A (en) | 2010-05-06 | 2011-11-14 | 바히아 스페셜티 셀룰로스 에스에이 | Method and system for high alpha dissolving pulp production |
| CN103003487B (en) * | 2010-05-04 | 2016-04-27 | 巴伊亚特种纤维素公司 | The method and system that high α dissolving pulp is produced |
| FI127420B (en) | 2011-06-23 | 2018-05-31 | Andritz Oy | Process for producing cellulose pulp |
| FI129362B (en) | 2017-05-16 | 2021-12-31 | Andritz Oy | Method for producing chemical pulp |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4578149A (en) * | 1981-03-05 | 1986-03-25 | Fagerlund Bertil K E | Process for digesting cellulosic material with heat recovery |
| FI71176C (en) * | 1983-11-30 | 1991-12-03 | Ekono Oy | Process for preparing cellulose with batch boiling |
| US5183535B1 (en) * | 1990-02-09 | 1996-02-06 | Sunds Defibrator Rauma Oy | Process for preparing kraft pulp using black liquor pretreatment reaction |
| FI92224C (en) * | 1991-06-28 | 1994-10-10 | Sunds Defibrator Rauma Oy | Batch process for the production of cogeneration |
| FI105929B (en) * | 1996-05-30 | 2000-10-31 | Sunds Defibrator Pori Oy | An improved batch process for the preparation of sulphate cellulose |
| FI970254A (en) * | 1997-01-22 | 1998-07-23 | Ahlstrom Machinery Oy | Method and apparatus for cooking pulp |
| SE9703365D0 (en) * | 1997-09-18 | 1997-09-18 | Kvaerner Pulping Tech | Method in connection with impregnation and digestion of lignocelulosic material |
| WO1999014423A1 (en) * | 1997-09-18 | 1999-03-25 | Kvaerner Pulping Ab | Polysulfide pulping process |
| FI110327B (en) * | 1999-10-04 | 2002-12-31 | Metso Chemical Pulping Oy | Process for the production of pulp |
-
2003
- 2003-12-31 FI FI20031929A patent/FI120361B/en not_active IP Right Cessation
-
2004
- 2004-12-22 EP EP04805227A patent/EP1702101B1/en not_active Not-in-force
- 2004-12-22 US US10/564,373 patent/US20060175029A1/en not_active Abandoned
- 2004-12-22 CA CA002530704A patent/CA2530704A1/en not_active Abandoned
- 2004-12-22 AT AT04805227T patent/ATE423866T1/en active
- 2004-12-22 DE DE602004019689T patent/DE602004019689D1/en not_active Expired - Fee Related
- 2004-12-22 WO PCT/FI2004/050196 patent/WO2005064075A1/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| EP1702101A1 (en) | 2006-09-20 |
| US20060175029A1 (en) | 2006-08-10 |
| FI120361B (en) | 2009-09-30 |
| FI20031929A0 (en) | 2003-12-31 |
| EP1702101B1 (en) | 2009-02-25 |
| FI20031929A (en) | 2005-07-01 |
| WO2005064075A1 (en) | 2005-07-14 |
| ATE423866T1 (en) | 2009-03-15 |
| DE602004019689D1 (en) | 2009-04-09 |
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